CN101825370A - Backheating type double-effect and multi-effect second-class absorption heat pump - Google Patents

Backheating type double-effect and multi-effect second-class absorption heat pump Download PDF

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CN101825370A
CN101825370A CN200910019105A CN200910019105A CN101825370A CN 101825370 A CN101825370 A CN 101825370A CN 200910019105 A CN200910019105 A CN 200910019105A CN 200910019105 A CN200910019105 A CN 200910019105A CN 101825370 A CN101825370 A CN 101825370A
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solution
heat exchanger
newly
evaporimeter
absorber
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李华玉
尹志青
巩秀云
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A30/00—Adapting or protecting infrastructure or their operation
    • Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
    • Y02A30/274—Relating to heating, ventilation or air conditioning [HVAC] technologies using waste energy, e.g. from internal combustion engine
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/52—Heat recovery pumps, i.e. heat pump based systems or units able to transfer the thermal energy from one area of the premises or part of the facilities to a different one, improving the overall efficiency
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/62—Absorption based systems
    • Y02B30/625—Absorption based systems combined with heat or power generation [CHP], e.g. trigeneration

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Abstract

The invention relates to a backheating type double-effect and multi-effect second-class absorption heat pump which belongs to the technical filed of heating pumps. Aiming at a double-effect and multi-effect second-class absorption heat pump, a newly added absorption-evaporator, a newly added throttle valve or a newly added refrigerant fluid pump, a newly added solution heat exchanger and/or a newly added solution pump are introduced; the newly added absorption-evaporator is added between an absorber and an evaporator or between two different generators; a refrigerant steam pipeline is added from the evaporator to communicate with the newly added absorption-evaporator; or the newly added absorption-evaporator and the absorber are communicated in sequence by the newly added refrigerant fluid pump from the evaporator; or the newly added absorption-evaporator and the absorber are communicated in sequence by the newly added refrigerant fluid pump from a condenser, and a refrigerant liquid pipe communicated with the evaporator is changed to communicate with the evaporator via the newly added throttle valve at the same time; a solution entering the newly added absorption-evaporator from the absorber or the generators absorbs refrigerant steam from the evaporator, heats refrigerant fluid into refrigerant steam, and supplies the refrigerant steam for the absorber to obtain a backheating type triple-effect or double-effect second-class absorption heat pump; and then a re-added absorber is mainly added to obtain a backheating type triple-effect or double-effect second-class absorption heat pump with an added low-temperature heat supply end.

Description

Backheating type double-effect and multi-effect second-class absorption heat pump
Technical field:
The invention belongs to low temperature exhaust heat utilization and technical field of heat pumps.
Background technology:
For second class absorption heat pump, triple effect is compared with economic benefits and social benefits, the performance index height of triple effect second class absorption heat pump---utilization rate of waste heat height---and heat supply temperature is low, but the heat supply temperature aspect that embodies the performance index of utilization rate of waste heat between the two and embody heat capacity all has than big difference; Similarly, also be like this between economic benefits and social benefits and the single-action.Indicating between triple effect and the economic benefits and social benefits or existing the centre second class absorption heat pump unit between economic benefits and social benefits and the single-action than the existence of large span with intermediate heat mechanical property and parameter.
From the thermodynamic principles angle, backheat can improve the forward circulation thermal efficiency, then corresponding the performance index that reduces reverse circulation; And the reduction of reverse circulation performance index then is accompanied by the raising of its heat supply temperature.Like this, adopt rational backheat technological means, can obtain thermodynamic effects between the second class absorption heat pump unit between triple effect and the economic benefits and social benefits or between economic benefits and social benefits and the single-action---Here it is back-heating type triple-effect (being multiple-effect) second class absorption heat pump and backheating type double-effect second class absorption heat pump.
In addition, lower for the heated medium initial temperature---be suitable for triple effect or double-effect process---and the occasion that finishing temperature is higher---being suitable for back-heating type triple-effect or double-effect process---, single flow process then can't realize the maximization of residual heat resources utilization rate.At this moment, take the suitable technique means, in back-heating type triple-effect second class absorption heat pump, add the low-temperature heat supply terminal of triple effect flow process, obtain back-heating type triple-effect second class absorption heat pump of additional low-temperature heat supply terminal; Or at the low-temperature heat supply terminal of the additional double-effect process of backheating type double-effect second class absorption heat pump, the backheating type double-effect that obtains additional low-temperature heat supply terminal is imitated second class absorption heat pump, then can realize obtaining the raising of residual heat resources utilization rate and simplifying the structure of heat pump assembly.
Summary of the invention:
Main purpose of the present invention is back-heating type triple-effect second class absorption heat pump that backheating type double-effect second class absorption heat pump, back-heating type triple-effect second class absorption heat pump and the additional low-temperature heat supply terminal of backheating type double-effect second class absorption heat pump, additional low-temperature heat supply terminal will be provided.Concrete summary of the invention comprises:
1. one of backheating type double-effect second class absorption heat pump on the solution series circulation economic benefits and social benefits basis, be in solution series circulation economic benefits and social benefits second class absorption heat pump of forming by high pressure generator, low pressure generator, condenser, evaporimeter, absorber, solution pump, cryogen liquid pump, choke valve, solution heat exchanger and second solution heat exchanger, increase newly-increased choke valve or newly-increased cryogen liquid pump, newly-increased absorption-evaporimeter and newly-increased solution heat exchanger; Or low pressure generator (b1) there is the concentrated solution pipeline through solution pump (f1), second solution heat exchanger (j1) is communicated with absorber (e1) with solution heat exchanger (i1), absorber (e1) has the weak solution pipeline to change low pressure generator (b1) into through solution heat exchanger (i1) connection high pressure generator (a1) again and the concentrated solution pipeline is arranged through solution pump (f1), second solution heat exchanger (j1), solution heat exchanger (i1) is communicated with absorber (e1) with newly-increased solution heat exchanger (3), absorber (e1) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with high pressure generator (a1) through solution heat exchanger (i1) more again, or low pressure generator (b1) is had the concentrated solution pipeline through solution pump (f1), second solution heat exchanger (j1) connection solution heat exchanger (i1) changes low pressure generator (b1) into has the concentrated solution pipeline through solution pump (f1), second solution heat exchanger (j1) is communicated with solution heat exchanger (i1) and has the concentrated solution pipeline to change high pressure generator (a1) into through second solution heat exchanger (j1) connection low pressure generator (b1) high pressure generator (a1) with newly-increased solution heat exchanger (3) have concentrated solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) the weak solution pipeline to be arranged again through second solution heat exchanger (j1) connection low pressure generator (b1); Or set up the cryogen liquid pipeline by evaporimeter (d1) and be communicated with the newly-increased absorptions-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back through newly-increased cryogen liquid pump (4) refrigerant vapour pipeline connection absorber (e1) is arranged again, or have the cryogen liquid pipeline to be communicated with evaporimeter (d1) condenser (c1) to change condenser (c1) into and have the cryogen liquid pipeline behind cryogen liquid pump (g1), to be divided into two-way through cryogen liquid pump (g1)---the one tunnel again warp increase choke valve (2) connection evaporimeter (d1) newly, another road directly is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back refrigerant vapour pipeline connection absorber (e1) again; Set up the newly-increased absorption-evaporimeter (1) of refrigerant vapour pipeline connection by evaporimeter (d1); Absorber (e1) or high pressure generator (a1) provide solution to newly-increased absorption-evaporimeter (1), evaporimeter (d1) provides refrigerant vapour to newly-increased absorption-evaporimeter (1), newly-increased absorption-evaporimeter (1) heating becomes refrigerant vapour to provide to absorber (e1) from the cryogen liquid of condenser (c1) or evaporimeter (d1), obtains backheating type double-effect second class absorption heat pump on the solution series circulation economic benefits and social benefits basis.
2. in backheating type double-effect second class absorption heat pump on aforementioned solution series circulation economic benefits and social benefits basis, or increase increases absorber and resolubilization liquid heat exchanger again, between the concentrated solution pipeline of the newly-increased solution heat exchanger (3) of solution heat exchanger (i1) connection, draw a concentrated solution pipeline through resolubilization liquid heat exchanger (6) connection increasing again absorber (5), set up the refrigerant vapour pipeline connection by evaporimeter (d1) and increase absorber (5) again, increasing absorber (5) more also has the weak solution pipeline to be communicated with high pressure generator (a1) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (6) respectively; Or increase increases absorber again, resolubilization liquid heat exchanger and resolubilization liquid control valve, low pressure generator (b1) there is the concentrated solution pipeline through solution pump (f1), second solution heat exchanger (j1), solution heat exchanger (i1), newly-increased solution heat exchanger (3) connection absorber (e1) changes low pressure generator (b1) into has the concentrated solution pipeline through solution pump (f1), second solution heat exchanger (j1), solution heat exchanger (i1), the resolubilization liquid heat exchanger is divided into two-way after (6)---and one the tunnel is communicated with absorber (e1) through newly-increased solution heat exchanger (3) again, another Lu Zaijing resolubilization liquid control valve (7) connection increasing again absorber (5), set up the refrigerant vapour pipeline connection by evaporimeter (d1) and increase absorber (5) again, increase absorber (5) again and also have the weak solution pipeline to be communicated with high pressure generator (a1) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (6); Increase absorber (5) and absorber (e1) more respectively to the heated medium heat supply, obtain on the solution series circulation economic benefits and social benefits basis and backheating type double-effect second class absorption heat pump of additional low-temperature heat supply terminal.
3. two of backheating type double-effect second class absorption heat pump on the solution series circulation economic benefits and social benefits basis, be in solution series circulation economic benefits and social benefits second class absorption heat pump of forming by high pressure generator, low pressure generator, condenser, evaporimeter, absorber, solution pump, cryogen liquid pump, choke valve, solution heat exchanger and second solution pump, increase newly-increased choke valve or newly-increased cryogen liquid pump, newly-increased absorption-evaporimeter and newly-increased solution heat exchanger; Or there is the concentrated solution pipeline to be communicated with absorber (e1) with solution heat exchanger (i 1) high pressure generator (a1) through solution pump (f1), absorber (e1) has the weak solution pipeline to change high pressure generator (a1) into through solution heat exchanger (i1) connection low pressure generator (b1) again and the concentrated solution pipeline is arranged through solution pump (f1), solution heat exchanger (i1) is communicated with absorber (e1) with newly-increased solution heat exchanger (3), absorber (e1) has the weak solution pipeline to be communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back through newly-increased solution heat exchanger (3) again and the weak solution pipeline is arranged through solution heat exchanger (i1) connection low pressure generator (b1) again, or has the concentrated solution pipeline to change low pressure generator (b1) into through second solution pump (k1) connection high pressure generator (a1) low pressure generator (b1) the concentrated solution pipeline to be arranged through second solution pump (k1), newly-increased solution heat exchanger (3) is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back has the weak solution pipeline to be communicated with high pressure generator (a1) through newly-increased solution heat exchanger (3) again; Or set up the cryogen liquid pipeline by evaporimeter (d1) and be communicated with the newly-increased absorptions-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back through newly-increased cryogen liquid pump (4) refrigerant vapour pipeline connection absorber (e1) is arranged again, or have the cryogen liquid pipeline to be communicated with evaporimeter (d1) condenser (c1) to change condenser (c1) into and have the cryogen liquid pipeline behind cryogen liquid pump (g1), to be divided into two-way through cryogen liquid pump (g1)---the one tunnel again warp increase choke valve (2) connection evaporimeter (d1) newly, another road directly is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back refrigerant vapour pipeline connection absorber (e1) again; Set up the newly-increased absorption-evaporimeter (1) of refrigerant vapour pipeline connection by evaporimeter (d1); Absorber (e1) or low pressure generator (b1) provide solution to newly-increased absorption-evaporimeter (1), evaporimeter (d1) provides refrigerant vapour to newly-increased absorption-evaporimeter (1), newly-increased absorption-evaporimeter (1) heating becomes refrigerant vapour to provide to absorber (e1) from the cryogen liquid of condenser (c1) or evaporimeter (d1), obtains backheating type double-effect second class absorption heat pump on the solution series circulation economic benefits and social benefits basis.
4. in backheating type double-effect second class absorption heat pump on aforementioned solution series circulation economic benefits and social benefits basis, or increase increases absorber and resolubilization liquid heat exchanger again, or increase increases absorber again, resolubilization liquid heat exchanger and resolubilization liquid control valve, obtain comprising backheating type double-effect second class absorption heat pump of economic benefits and social benefits low-temperature heat supply terminal---1. in backheating type double-effect second class absorption heat pump on the solution series circulation economic benefits and social benefits basis of claim 1, or increase increases absorber and resolubilization liquid heat exchanger again, between the concentrated solution pipeline of the newly-increased solution heat exchanger (3) of solution heat exchanger (i1) connection, draw a concentrated solution pipeline through resolubilization liquid heat exchanger (6) connection increasing again absorber (5), set up the refrigerant vapour pipeline connection by evaporimeter (d1) and increase absorber (5) again, increasing absorber (5) more also has the weak solution pipeline to be communicated with low pressure generator (b1) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (6) respectively; Or increase increases absorber again, resolubilization liquid heat exchanger and resolubilization liquid control valve, high pressure generator (a1) there is the concentrated solution pipeline through solution pump (f1), solution heat exchanger (i1), newly-increased solution heat exchanger (3) connection absorber (e1) changes high pressure generator (a1) into has the concentrated solution pipeline through solution pump (f1), solution heat exchanger (i1), the resolubilization liquid heat exchanger is divided into two-way after (6)---and one the tunnel is communicated with absorber (e1) through newly-increased solution heat exchanger (3) again, another Lu Zaijing resolubilization liquid control valve (7) connection increasing again absorber (5), set up the refrigerant vapour pipeline connection by evaporimeter (d1) and increase absorber (5) again, increasing absorber (5) more also has the weak solution pipeline to be communicated with low pressure generator (b1) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (6) respectively; Increase absorber (5) and absorber (e1) more respectively to the heated medium heat supply, obtain on the solution series circulation economic benefits and social benefits basis and backheating type double-effect second class absorption heat pump of additional low-temperature heat supply terminal.
5. backheating type double-effect second class absorption heat pump on the solution circulation economic benefits and social benefits in parallel basis, be in the solution of forming by high pressure generator, low pressure generator, condenser, evaporimeter, absorber, solution pump, second solution pump, cryogen liquid pump, choke valve, solution heat exchanger and second solution heat exchanger circulation economic benefits and social benefits in parallel second class absorption heat pump, increase newly-increased choke valve or newly-increased cryogen liquid pump, newly-increased absorption-evaporimeter and newly-increased solution heat exchanger; Or there is the concentrated solution pipeline to have the concentrated solution pipeline to be communicated with absorber (e1) respectively with second solution heat exchanger (j1) high pressure generator (a1) through second solution pump (k1) through solution pump (f1) and solution heat exchanger (i1) and low pressure generator (b1), absorber (e1) have again the weak solution pipeline respectively through solution heat exchanger (i1) be communicated with high pressure generator (a1) and through second solution heat exchanger (j1) be communicated with low pressure generator (b1) change into high pressure generator (a1) have the concentrated solution pipeline through solution pump (f1) and solution heat exchanger (i1) and low pressure generator (b1) have the concentrated solution pipeline through second solution pump (k1) with after second solution heat exchanger (j1) two tunnel merges into one the tunnel jointly again warp increase solution heat exchanger (3) newly and be communicated with absorber (e1), absorber (e1) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with high pressure generator (a1) and to be communicated with low pressure generator (b1) through second solution heat exchanger (j1) through solution heat exchanger (i1) respectively more again, or there is the concentrated solution pipeline to be communicated with absorber (e1) with second solution heat exchanger (j1) low pressure generator (b1) through second solution pump (k1), absorber (e1) has the weak solution pipeline to change low pressure generator (b1) into through second solution heat exchanger (j1) connection low pressure generator (b1) again and the concentrated solution pipeline is arranged through second solution pump (k1), second solution heat exchanger (j1) is communicated with absorber (e1) with newly-increased solution heat exchanger (3), absorber (e1) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with low pressure generator (b1) through second solution heat exchanger (j1) again, or has the concentrated solution pipeline to be communicated with absorber (e1) through solution pump (f1) with solution heat exchanger (i1) high pressure generator (a1), absorber (e1) has the weak solution pipeline to change high pressure generator (a1) into through solution heat exchanger (i1) connection high pressure generator (b1) again and the concentrated solution pipeline is arranged through solution pump (f1), solution heat exchanger (i1) is communicated with absorber (e1) with newly-increased solution heat exchanger (3), absorber (e1) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with low pressure generator (b1) through solution heat exchanger (i1) more again; Or set up the cryogen liquid pipeline by evaporimeter (d1) and be communicated with the newly-increased absorptions-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back through newly-increased cryogen liquid pump (4) refrigerant vapour pipeline connection absorber (e1) is arranged again, or have the cryogen liquid pipeline to be communicated with evaporimeter (d1) condenser (c1) to change condenser (c1) into and have the cryogen liquid pipeline behind cryogen liquid pump (g1), to be divided into two-way through cryogen liquid pump (g1)---the one tunnel again warp increase choke valve (2) connection evaporimeter (d1) newly, another road directly is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back refrigerant vapour pipeline connection absorber (e1) again; Evaporimeter (d1) is also set up the newly-increased absorption-evaporimeter (1) of refrigerant vapour pipeline connection; Absorber (e1) provides solution to newly-increased absorption-evaporimeter (1), evaporimeter (d1) provides refrigerant vapour to newly-increased absorption-evaporimeter (1), newly-increased absorption-evaporimeter (1) heating becomes refrigerant vapour to provide to absorber (e1) from the cryogen liquid of condenser (c1) or evaporimeter (d1), obtains backheating type double-effect second class absorption heat pump on the solution circulation economic benefits and social benefits in parallel basis.
6. in backheating type double-effect second class absorption heat pump on aforementioned solution circulation economic benefits and social benefits in parallel basis, or increase increases absorber and resolubilization liquid heat exchanger again, at high pressure generator (a1) through solution pump (f1), solution heat exchanger (i1) and low pressure generator (b1) are through second solution pump (k1), draw the solution pipeline after second solution heat exchanger (j1) converges between the solution pipeline of the newly-increased solution heat exchanger (3) of connection and increase absorber (5) again, increase absorber (5) again and also have the weak solution pipeline behind resolubilization liquid heat exchanger (6), to be communicated with high pressure generator (a1) and low pressure generator (b1) respectively through resolubilization liquid heat exchanger (6) connection; Or increase increases absorber again, resolubilization liquid heat exchanger and resolubilization liquid control valve, with high pressure generator (a1) concentrated solution pipeline through solution pump (f1), solution heat exchanger (i1) and low pressure generator (b1) concentrated solution pipeline are through second solution pump (k1), second solution heat exchanger (j1) converges the newly-increased solution heat exchanger (3) of back connection and changes high pressure generator (a1) concentrated solution pipeline into through solution pump (f1), solution heat exchanger (i1) and low pressure generator (b1) concentrated solution pipeline are through second solution pump (k1), second solution heat exchanger (j1) converges after resolubilization liquid heat exchanger (6) is divided into two-way---and one the tunnel is communicated with newly-increased solution heat exchanger (3), another Lu Zaijing resolubilization liquid control valve (7) connection increasing again absorber (5); Set up the refrigerant vapour pipeline connection by evaporimeter (d1) and increase absorber (5) again, increase absorber (5) again and also have heated medium pipeline and external communications; Increase absorber (5) and absorber (e1) more respectively to the heated medium heat supply, obtain on the solution circulation economic benefits and social benefits in parallel basis and backheating type double-effect second class absorption heat pump of additional low-temperature heat supply terminal.
7. one of back-heating type triple-effect second class absorption heat pump on the solution series circulation three-effect basis, be in solution series circulation three-effect second class absorption heat pump of forming by high pressure generator, middle pressure generator, low pressure generator, condenser, evaporimeter, absorber, solution pump, cryogen liquid pump, choke valve, second choke valve, solution heat exchanger, second solution heat exchanger and the 3rd solution heat exchanger, increase newly-increased choke valve or newly-increased cryogen liquid pump, newly-increased absorption-evaporimeter and newly-increased solution heat exchanger; Or low pressure generator (c2) there is the concentrated solution pipeline through the 3rd solution heat exchanger (m2), second solution heat exchanger (l2) is communicated with absorber (f2) with solution heat exchanger (k2), absorber (f2) has the weak solution pipeline to change low pressure generator (c2) into through solution heat exchanger (k2) connection high pressure generator (a2) again and the concentrated solution pipeline is arranged through the 3rd solution heat exchanger (m2), second solution heat exchanger (l2), solution heat exchanger (k2) is communicated with absorber (f2) with newly-increased solution heat exchanger (3), absorber (f2) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with high pressure generator (a2) through solution heat exchanger (k2) more again, or low pressure generator (c2) there is the concentrated solution pipeline through the 3rd solution heat exchanger (m2), being communicated with solution heat exchanger (k2) behind second solution heat exchanger (l2) again changes low pressure generator (c2) into and the concentrated solution pipeline is arranged through the 3rd solution heat exchanger (m2), second solution heat exchanger (l2), being communicated with solution heat exchanger (k2) again behind the newly-increased solution heat exchanger (3) and simultaneously high pressure generator (a2) being had the concentrated solution pipeline to press generator (b2) to change high pressure generator (a2) in second solution heat exchanger (l2) is communicated with has the concentrated solution pipeline to increase absorption-evaporimeter (1) newly after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to press generator (b2) again in second solution heat exchanger (l2) connection, or has the concentrated solution pipeline to be communicated with second solution heat exchanger (l2) again behind the 3rd solution heat exchanger (m2) low pressure generator (c2) to change low pressure generator (c2) into and the concentrated solution pipeline is arranged through the 3rd solution heat exchanger (m2), being communicated with second solution heat exchanger (l2) again behind the newly-increased solution heat exchanger 3 and simultaneously middle pressure generator (b2) being had the concentrated solution pipeline to press generator (b2) to have the concentrated solution pipeline to increase absorption-evaporimeter (1) newly after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) in the 3rd solution heat exchanger (m2) connection low pressure generator (c2) changes into has the weak solution pipeline to be communicated with low pressure generator (c2) through the 3rd solution heat exchanger (m2) again; Or set up the cryogen liquid pipeline by evaporimeter (e2) and be communicated with the newly-increased absorptions-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back through newly-increased cryogen liquid pump (4) refrigerant vapour pipeline connection absorber (f2) is arranged again, or have the cryogen liquid pipeline to be communicated with evaporimeter (e2) condenser (d2) to change condenser (d2) into and have the cryogen liquid pipeline behind cryogen liquid pump (h2), to be divided into two-way through cryogen liquid pump (h2)---the one tunnel again warp increase choke valve (2) connection evaporimeter (e2) newly, another road directly is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back refrigerant vapour pipeline connection absorber (f2) again; Evaporimeter (e2) is also set up the newly-increased absorption-evaporimeter (1) of refrigerant vapour pipeline connection; Absorber (f2) or high pressure generator (a2) or middle pressure generator (b2) provide solution to newly-increased absorption-evaporimeter (1), evaporimeter (e2) provides refrigerant vapour to newly-increased absorption-evaporimeter (1), newly-increased absorption-evaporimeter (1) heating becomes refrigerant vapour to provide to absorber (f2) from the cryogen liquid of condenser (d2) or evaporimeter (e2), obtains back-heating type triple-effect second class absorption heat pump on the solution series circulation three-effect basis.
8. in back-heating type triple-effect second class absorption heat pump on aforementioned solution series circulation three-effect basis, or increase increases absorber and resolubilization liquid heat exchanger again, between the concentrated solution pipeline of solution heat exchanger (k2) connection absorber (f2) or the newly-increased solution heat exchanger (3) of connection, draw a concentrated solution pipeline through resolubilization liquid heat exchanger (6) connection increasing again absorber (5), set up the refrigerant vapour pipeline connection by evaporimeter (e2) and increase absorber (5) again, increasing absorber (5) more also has the weak solution pipeline to be communicated with high pressure generator (a2) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (6) respectively; Or increase increases absorber again, resolubilization liquid heat exchanger and resolubilization liquid control valve, low pressure generator (c2) there is the concentrated solution pipeline through solution pump (g2), the 3rd solution heat exchanger (m2), second solution heat exchanger (l2), solution heat exchanger (k2) is communicated with absorber (f2) or changes low pressure generator (c2) into through newly-increased solution heat exchanger (3) connection absorber (f2) again has the concentrated solution pipeline through solution pump (g2), the 3rd solution heat exchanger (m2), second solution heat exchanger (l2), solution heat exchanger (k2) or be divided into two-way again behind resolubilization liquid heat exchanger (6)---the one tunnel is communicated with absorber (f2) through newly-increased solution heat exchanger (3) again, another Lu Zaijing resolubilization liquid control valve (7) connection increasing again absorber (5), set up the refrigerant vapour pipeline connection by evaporimeter (e2) and increase absorber (5) again, increase absorber (5) again and also have the weak solution pipeline to be communicated with high pressure generator (a2) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (6); Increase absorber (5) and absorber (e1) more respectively to the heated medium heat supply, obtain on the solution series circulation three-effect basis and back-heating type triple-effect second class absorption heat pump of additional low-temperature heat supply terminal.
9. two of back-heating type triple-effect second class absorption heat pump on the solution series circulation three-effect basis, be in solution series circulation three-effect second class absorption heat pump of forming by high pressure generator, middle pressure generator, low pressure generator, condenser, evaporimeter, absorber, solution pump, second solution pump, the 3rd solution pump, cryogen liquid pump, choke valve, second choke valve and solution heat exchanger, increase newly-increased choke valve or newly-increased cryogen liquid pump, newly-increased absorption-evaporimeter and newly-increased solution heat exchanger; Or there is the concentrated solution pipeline to be communicated with absorber (f2) high pressure generator (a2) through solution heat exchanger (k2), absorber (f2) has the weak solution pipeline to change high pressure generator (a2) into through solution heat exchanger (k2) connection low pressure generator (c2) again has the concentrated solution pipeline to be communicated with absorber (f2) through solution heat exchanger (k2) with newly-increased solution heat exchanger (3), absorber (f2) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with low pressure generator c2 through solution heat exchanger (k2) more again, or have the concentrated solution pipeline in the 3rd solution pump (o2) is communicated with, to press generator (b2) to change low pressure generator (c2) into low pressure generator (c2) the concentrated solution pipeline to be arranged through the 3rd solution pump (o2), newly-increased absorption-evaporimeter (1) had the weak solution pipeline to press generator (b2) again in newly-increased solution heat exchanger (3) is communicated with after newly-increased solution heat exchanger (3) was communicated with newly-increased absorption-evaporimeter (1), or had the concentrated solution pipeline to press generator (b2) the concentrated solution pipeline to be arranged through second solution pump (n2) in second solution pump (n2) connection high pressure generator (a2) changes in middle pressure generator (b2), newly-increased solution heat exchanger (3) is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back has the weak solution pipeline to be communicated with high pressure generator (a2) through newly-increased solution heat exchanger (3) again; Or set up the cryogen liquid pipeline by evaporimeter (e2) and be communicated with the newly-increased absorptions-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back through newly-increased cryogen liquid pump (4) refrigerant vapour pipeline connection absorber (f2) is arranged again, or have the cryogen liquid pipeline to be communicated with evaporimeter (e2) condenser (d2) to change condenser (d2) into and have the cryogen liquid pipeline behind cryogen liquid pump (h2), to be divided into two-way through cryogen liquid pump (h2)---the one tunnel again warp increase choke valve (2) connection evaporimeter (e2) newly, another road directly is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back refrigerant vapour pipeline connection absorber (f2) again; Evaporimeter (e2) is also set up the newly-increased absorption-evaporimeter (1) of refrigerant vapour pipeline connection; Absorber (f2) or low pressure generator (c2) or middle pressure generator (b2) provide solution to newly-increased absorption-evaporimeter (1), evaporimeter (e2) provides refrigerant vapour to newly-increased absorption-evaporimeter (1), newly-increased absorption-evaporimeter (1) heating becomes refrigerant vapour to provide to absorber (f2) from the cryogen liquid of condenser (d2) or evaporimeter (e2), obtains back-heating type triple-effect second class absorption heat pump on the solution series circulation three-effect basis.
10. in back-heating type triple-effect second class absorption heat pump on aforementioned solution series circulation three-effect basis, or increase increases absorber and resolubilization liquid heat exchanger again, between the concentrated solution pipeline of solution heat exchanger (k2) connection absorber (f2) or the newly-increased solution heat exchanger (3) of connection, draw the concentrated solution pipeline through resolubilization liquid heat exchanger (6) connection increasing again absorber (5), set up the refrigerant vapour pipeline connection by evaporimeter (e2) and increase absorber (5) again, increasing absorber (5) more also has the weak solution pipeline to be communicated with low pressure generator (c2) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (6) respectively; Or increase increases absorber again, resolubilization liquid heat exchanger and resolubilization liquid control valve, high pressure generator (a2) there is the concentrated solution pipeline through solution pump (g2), solution heat exchanger (k2) is communicated with absorber (f2) or changes high pressure generator (a2) into through newly-increased solution heat exchanger (3) connection absorber (f2) again has the concentrated solution pipeline through solution pump (g2), solution heat exchanger (k2) or be divided into two-way again behind resolubilization liquid heat exchanger (6)---the one tunnel is communicated with absorber (f2) through newly-increased solution heat exchanger (3) again, another Lu Zaijing resolubilization liquid control valve (7) connection increasing again absorber (5), set up the refrigerant vapour pipeline connection by evaporimeter (e2) and increase absorber (5) again, increasing absorber (5) more also has the weak solution pipeline to be communicated with low pressure generator (c2) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (6) respectively; Increase absorber (5) and absorber (f2) more respectively to the heated medium heat supply, obtain on the solution series circulation three-effect basis and back-heating type triple-effect second class absorption heat pump of additional low-temperature heat supply terminal.
11. back-heating type triple-effect second class absorption heat pump on the solution circulation three-effect in parallel basis, be in solution series circulation three-effect second class absorption heat pump of forming by high pressure generator, middle pressure generator, low pressure generator, condenser, evaporimeter, absorber, solution pump, second solution pump, the 3rd solution pump, cryogen liquid pump, choke valve, second choke valve, solution heat exchanger, second solution heat exchanger and the 3rd solution heat exchanger, increase newly-increased choke valve or newly-increased cryogen liquid pump, newly-increased absorption-evaporimeter and newly-increased solution heat exchanger; Or high pressure generator (a2) there is the concentrated solution pipeline through solution pump (g2) and solution heat exchanger (k2), the middle generator (b2) of pressing has the concentrated solution pipeline to have the concentrated solution pipeline to be communicated with absorber (f2) through the 3rd solution pump (o2) respectively with the 3rd solution heat exchanger (m2) through second solution pump (n2) and second solution heat exchanger (l2) and low pressure generator (c2), absorber (f2) has the weak solution pipeline to be communicated with high pressure generator (a2) through solution heat exchanger (k2) respectively again, in second solution heat exchanger (l2) is communicated with, press generator (b2) and change high pressure generator (a2) into and the concentrated solution pipeline is arranged through solution pump (g2) and solution heat exchanger (k2) through the 3rd solution heat exchanger (m2) connection low pressure generator (c2), in press generator (b2) have the concentrated solution pipeline through second solution pump (n2) and second solution heat exchanger (l2) and low pressure generator (c2) have the concentrated solution pipeline through the 3rd solution pump (o2) with after the 3rd solution heat exchanger (m2) three tunnel merges into one the tunnel jointly again warp increase solution heat exchanger (3) newly and be communicated with absorber (f2), absorber (f2) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with high pressure generator (a1) through solution heat exchanger (k2) respectively more again, in second solution heat exchanger (l2) is communicated with, press generator (b2) and be communicated with low pressure generator (c2) through the 3rd solution heat exchanger (m2), or high pressure generator (a2) there is the concentrated solution pipeline through solution pump (g2) and solution heat exchanger (k2), the middle generator (b2) of pressing has the concentrated solution pipeline to have the concentrated solution pipeline to be communicated with absorber (f2) through the 3rd solution pump (o2) respectively with the 3rd solution heat exchanger (m2) through second solution pump (n2) and second solution heat exchanger (l2) and low pressure generator (c2), absorber (f2) has the weak solution pipeline to be communicated with high pressure generator (a2) through solution heat exchanger (k2) respectively again, in second solution heat exchanger (l2) is communicated with, press generator (b2) and change high pressure generator (a2) into and the concentrated solution pipeline is arranged through solution pump (g2) and solution heat exchanger (k2) through the 3rd solution heat exchanger (m2) connection low pressure generator (c2), in press generator (b2) have the concentrated solution pipeline through second solution pump (n2) and second solution heat exchanger (l2) and low pressure generator (c2) have the concentrated solution pipeline through the 3rd solution pump (o2) with after the 3rd solution heat exchanger (m2) three tunnel merges into one the tunnel jointly again warp increase solution heat exchanger (3) newly and be communicated with absorber (f2), absorber (f2) has the weak solution pipeline to be divided into two-way behind newly-increased solution heat exchanger (3)---and one the tunnel through solution heat exchanger (k2) connection high pressure generator (a1), another road is communicated with the newly-increased absorptions-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back has the weak solution pipeline to press generator (b2) respectively and through the 3rd solution heat exchanger (m2) connection low pressure generator (c2) in second solution heat exchanger (l2) connection again, or there is the concentrated solution pipeline to have the concentrated solution pipeline to be communicated with absorber (f2) respectively with the 3rd solution heat exchanger (m2) the middle pressure generator (b2) through the 3rd solution pump (o2) through second solution pump (n2) and second solution heat exchanger (l2) and low pressure generator (c2), absorber (f2) have again the weak solution pipeline in second solution heat exchanger (l2) is communicated with, press respectively generator (b2) and through the 3rd solution heat exchanger (m2) be communicated with low pressure generator (c2) press in changing into generator (b2) have the concentrated solution pipeline through second solution pump (n2) and second solution heat exchanger (l2) and low pressure generator (c2) have the concentrated solution pipeline through the 3rd solution pump (o2) with after the 3rd solution heat exchanger (m2) two tunnel merges into one the tunnel jointly again warp increase solution heat exchanger (3) newly and be communicated with absorber (f2), absorber (f2) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to press generator (b2) respectively again in second solution heat exchanger (l2) is communicated with and is communicated with low pressure generator (c2) through the 3rd solution heat exchanger (m2), or there is the concentrated solution pipeline to be communicated with absorber (f2) with the 3rd solution heat exchanger (m2) low pressure generator (c2) through the 3rd solution pump (o2), absorber (f2) has the weak solution pipeline to change low pressure generator (c2) into through the 3rd solution heat exchanger (m2) connection low pressure generator (c2) again and the concentrated solution pipeline is arranged through the 3rd solution pump (o2), the 3rd solution heat exchanger (m2) is communicated with absorber (f2) with newly-increased solution heat exchanger (3), absorber (f2) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with low pressure generator (c2) through the 3rd solution heat exchanger (m2) again, or there is the concentrated solution pipeline to be communicated with absorber (f2) with second solution heat exchanger (l2) the middle pressure generator (b2) through second solution pump (n2), absorber (f2) has the weak solution pipeline to press generator (b2) to change the middle generator (b2) of pressing in second solution heat exchanger (l2) is communicated with again and the concentrated solution pipeline is arranged through second solution pump (n2), second solution heat exchanger (l2) is communicated with absorber (f2) with newly-increased solution heat exchanger (3), absorber (f2) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to press generator (b2) again in second solution heat exchanger (l2) is communicated with again, or has the concentrated solution pipeline to be communicated with absorber (f2) through solution pump (g2) with solution heat exchanger (k2) high pressure generator (a2), absorber (f2) has the weak solution pipeline to change high pressure generator (a2) into through solution heat exchanger (k2) connection high pressure generator (a2) respectively again and the concentrated solution pipeline is arranged through solution pump (g2), solution heat exchanger (k2) is communicated with absorber (f2) with newly-increased solution heat exchanger (3), absorber (f2) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with high pressure generator (a1) through solution heat exchanger (k2) more again; Or set up the cryogen liquid pipeline by evaporimeter (e2) and be communicated with the newly-increased absorptions-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back through newly-increased cryogen liquid pump (4) refrigerant vapour pipeline connection absorber (f2) is arranged again, or have the cryogen liquid pipeline to be communicated with evaporimeter (e2) condenser (d2) to change condenser (d2) into and have the cryogen liquid pipeline behind cryogen liquid pump (h2), to be divided into two-way through cryogen liquid pump (h2)---the one tunnel again warp increase choke valve (2) connection evaporimeter (e2) newly, another road directly is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back refrigerant vapour pipeline connection absorber (f2) again; Evaporimeter (e2) is also set up the newly-increased absorption-evaporimeter (1) of refrigerant vapour pipeline connection; Absorber (f2) provides solution to newly-increased absorption-evaporimeter (1), evaporimeter (e2) provides refrigerant vapour to newly-increased absorption-evaporimeter (1), newly-increased absorption-evaporimeter (1) heating becomes refrigerant vapour to provide to absorber (f2) from the cryogen liquid of condenser (d2) or evaporimeter (e2), obtains back-heating type triple-effect second class absorption heat pump on the solution circulation three-effect in parallel basis.
12. in back-heating type triple-effect second class absorption heat pump on aforementioned solution circulation three-effect in parallel basis, or increase increases absorber and resolubilization liquid heat exchanger again, at high pressure generator (a2) through solution pump (g2) and solution heat exchanger (k2), in press generator (b2) to draw a solution pipeline between the solution pipeline that increases solution heat exchanger (3) newly and increase absorber (5) again with being communicated with again after the 3rd solution heat exchanger (m2) converges through the 3rd solution pump (o2) through resolubilization liquid heat exchanger (6) connection through second solution pump (n2) and second solution heat exchanger (i2) and low pressure generator (c2), increase again absorber (5) in addition the weak solution pipeline behind resolubilization liquid heat exchanger (6), be communicated with high pressure generator (a2) respectively, middle generator (b2) and the low pressure generator (c2) of pressing; Or increase increases absorber again, resolubilization liquid heat exchanger and resolubilization liquid control valve, with high pressure generator (a2) through solution pump (g2) and solution heat exchanger (k2), in press generator (b2) to increase solution heat exchanger (3) newly and change high pressure generator (a2) into being communicated with again after the 3rd solution heat exchanger (m2) converges through the 3rd solution pump (o2) through solution pump (g2) and solution heat exchanger (k2) through second solution pump (n2) and second solution heat exchanger (i2) and low pressure generator (c2), the middle generator (b2) of pressing converges with the 3rd solution heat exchanger (m2) after resolubilization liquid heat exchanger (6) is divided into two-way through the 3rd solution pump (o2) with second solution heat exchanger (i2) and low pressure generator (c2) through second solution pump (n2)---and one the tunnel is communicated with newly-increased solution heat exchanger (3), another Lu Zaijing resolubilization liquid control valve (7) connection increasing again absorber (5); Set up the refrigerant vapour pipeline connection by evaporimeter (e2) and increase absorber (5) again, increase absorber (5) again and also have heated medium pipeline and external communications; Increase absorber (5) and absorber (f2) more respectively to the heated medium heat supply, obtain on the solution circulation three-effect in parallel basis and back-heating type triple-effect second class absorption heat pump of additional low-temperature heat supply terminal.
Description of drawings:
At first be noted that, in the description of drawings below, back-heating type second class absorption heat pump of same names has adopted numercal different layout, same names and the difference of different digital layout shows three aspects: the 1. position difference of newly-increased absorption-evaporimeter; 2. the connected mode difference between condenser, evaporimeter and the newly-increased absorption-evaporimeter; 3. have any different on the solution flow process.
Fig. 1 be provided by the invention, based on the 1st backheating type double-effect second class absorption heat pump structure and the schematic flow sheet of solution series circulation economic benefits and social benefits.
Fig. 2 be provided by the invention, based on the 2nd backheating type double-effect second class absorption heat pump structure and the schematic flow sheet of solution series circulation economic benefits and social benefits.
Fig. 3 be provided by the invention, based on the 3rd backheating type double-effect second class absorption heat pump structure and the schematic flow sheet of solution series circulation economic benefits and social benefits.
Fig. 4 be provided by the invention, based on the 4th backheating type double-effect second class absorption heat pump structure and the schematic flow sheet of solution series circulation economic benefits and social benefits.
Fig. 5 be provided by the invention, based on the 1st backheating type double-effect second class absorption heat pump structure and the schematic flow sheet of solution circulation economic benefits and social benefits in parallel.
Fig. 6 be provided by the invention, based on the 2nd backheating type double-effect second class absorption heat pump structure and the schematic flow sheet of solution circulation economic benefits and social benefits in parallel.
Fig. 7 be provided by the invention, based on the 3rd backheating type double-effect second class absorption heat pump structure and the schematic flow sheet of solution circulation economic benefits and social benefits in parallel.
Fig. 8 be provided by the invention, based on the 1st back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of solution series circulation three-effect.
Fig. 9 be provided by the invention, based on the 2nd back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of solution series circulation three-effect.
Figure 10 be provided by the invention, based on the 3rd back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of solution series circulation three-effect.
Figure 11 be provided by the invention, based on the 4th back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of solution series circulation three-effect.。
Figure 12 be provided by the invention, based on the 5th back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of solution series circulation three-effect.。
Figure 13 be provided by the invention, based on the 6th back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of solution series circulation three-effect.
Figure 14 be provided by the invention, based on the 1st back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of solution circulation three-effect in parallel.
Figure 15 be provided by the invention, based on the 2nd back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of solution circulation three-effect in parallel.
Figure 16 be provided by the invention, based on the 3rd back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of solution circulation three-effect in parallel.
Figure 17 be provided by the invention, based on the 4th back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of solution circulation three-effect in parallel.
Figure 18 be provided by the invention, based on the 5th back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of solution circulation three-effect in parallel.
Figure 19 be provided by the invention, based on the 6th back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of solution circulation three-effect in parallel.
Figure 20 be provided by the invention, based on the backheating type double-effect second class absorption heat pump structure and the schematic flow sheet of the 1st additional low-temperature heat supply terminal of solution series circulation economic benefits and social benefits.
Figure 21 be provided by the invention, based on the backheating type double-effect second class absorption heat pump structure and the schematic flow sheet of the 2nd additional low-temperature heat supply terminal of solution series circulation economic benefits and social benefits.
Figure 22 be provided by the invention, based on the backheating type double-effect second class absorption heat pump structure and the schematic flow sheet of the 3rd additional low-temperature heat supply terminal of solution series circulation economic benefits and social benefits.
Figure 23 be provided by the invention, based on the backheating type double-effect second class absorption heat pump structure and the schematic flow sheet of the 1st additional low-temperature heat supply terminal of solution circulation economic benefits and social benefits in parallel.
Figure 24 be provided by the invention, based on the backheating type double-effect second class absorption heat pump structure and the schematic flow sheet of the 2nd additional low-temperature heat supply terminal of solution circulation economic benefits and social benefits in parallel.
Figure 25 be provided by the invention, based on the back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of the 1st additional low-temperature heat supply terminal of solution series circulation three-effect.
Figure 26 be provided by the invention, based on the back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of the 2nd additional low-temperature heat supply terminal of solution series circulation three-effect.
Figure 27 be provided by the invention, based on the back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of the 3rd additional low-temperature heat supply terminal of solution series circulation three-effect.
Figure 28 be provided by the invention, based on the back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of the 4th additional low-temperature heat supply terminal of solution series circulation three-effect.
Figure 29 be provided by the invention, based on the back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of the 1st additional low-temperature heat supply terminal of solution circulation three-effect in parallel.
Figure 30 be provided by the invention, based on the back-heating type triple-effect second class absorption heat pump structure and the schematic flow sheet of the 2nd additional low-temperature heat supply terminal of solution circulation three-effect in parallel.
Figure 31 is solution series circulation economic benefits and social benefits second class absorption heat pump structure and the schematic flow sheets.
Figure 32 also is solution series circulation economic benefits and social benefits second class absorption heat pump structure and the schematic flow sheets.
Figure 33 is solution series circulation economic benefits and social benefits second class absorption heat pump structure and the schematic flow sheets.
Figure 34 also is solution series circulation economic benefits and social benefits second class absorption heat pump structure and the schematic flow sheets.
Figure 35 is solution circulation economic benefits and social benefits in parallel second class absorption heat pump structure and the schematic flow sheets.
Providing Figure 27-existing economic benefits and social benefits second class absorption heat pump shown in Figure 29, is in order to make the present invention more clear aspect the content description; They also are the references of triple effect second class absorption heat pump in addition.
Among the figure, 1-increases absorption-evaporimeter newly, and 2-increases choke valve newly, and 3-increases solution heat exchanger newly, and 4-increases the cryogen liquid pump newly, and 5-increases absorber again, 6-resolubilization liquid heat exchanger, 7-resolubilization liquid control valve.
Among Fig. 1-Fig. 6, Figure 17-Figure 21, Figure 27-Figure 29, a1-high pressure generator, b1-low pressure generator, c1-condenser, the d1-evaporimeter, e1-absorber, f1-solution pump, g1-cryogen liquid pump, the h1-choke valve, i1-solution heat exchanger, j1-second solution heat exchanger, k1-second solution pump.
Among Fig. 7-Figure 16, Figure 22-Figure 26, a2-condenser, b2-high pressure generator, the c2-low pressure generator, d2-condenser, e2-evaporimeter, the f2-absorber, g2-solution pump, h2-cryogen liquid pump, the i2-choke valve, j2-second choke valve, k2-solution heat exchanger, l2-second solution heat exchanger, m2-the 3rd solution heat exchanger, n2-second solution pump, o2-the 3rd solution pump.
The specific embodiment:
Describe the present invention in detail below in conjunction with accompanying drawing and example.
Shown in Figure 1, obtain like this based on backheating type double-effect second class absorption heat pump of solution series circulation economic benefits and social benefits:
With shown in Figure 31 by high pressure generator a1, low pressure generator b1, condenser c1, evaporimeter d1, absorber e1, solution pump f1, cryogen liquid pump g1, choke valve h1, in solution series circulation economic benefits and social benefits second class absorption heat pump that the solution heat exchanger i1 and the second solution heat exchanger j1 form, increase newly-increased absorption-evaporimeter 1, newly-increased choke valve 2 and newly-increased solution heat exchanger 3, low pressure generator b1 there is the concentrated solution pipeline through solution pump f1, the second solution heat exchanger j1 is communicated with absorber e1 with solution heat exchanger i1, absorber e1 has the weak solution pipeline to change low pressure generator b1 into through solution heat exchanger i1 connection high pressure generator a1 again and the concentrated solution pipeline is arranged through solution pump f1, the second solution heat exchanger j1, solution heat exchanger i1 is communicated with absorber e1 with newly-increased solution heat exchanger 3, absorber e1 has weak solution pipeline newly-increased absorption-evaporimeter 1 after newly-increased solution heat exchanger 3 is communicated with newly-increased absorption-evaporimeter 1 to have the weak solution pipeline to be communicated with high pressure generator a1 through solution heat exchanger i1 more again, set up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection by evaporimeter d1, having the cryogen liquid pipeline to change condenser c1 into through cryogen liquid pump g1 connection evaporimeter d1 condenser c1 has the cryogen liquid pipeline to be divided into two-way behind cryogen liquid pump g1---and one the tunnel is communicated with evaporimeter d1 through newly-increased choke valve 2 again, another road directly is communicated with the newly-increased absorption-evaporimeter 1 in newly-increased absorption-evaporimeter 1 back refrigerant vapour pipeline connection absorber e1 again; The weak solution of absorber e1 enters newly-increased absorption-evaporimeter 1 through newly-increased absorption-evaporimeter 3, absorb refrigerant vapour and the heat release of flash-pot d1 to increase the cryogen liquid of absorption-evaporimeter 1 newly in flowing through, the weak solution of newly-increased absorption-evaporimeter 1 enters high pressure generator a1 through solution heat exchanger i1, the cryogen liquid of the condenser c1 newly-increased absorption-evaporimeter 1 of flowing through after cryogen liquid pump g1 pressurization absorbs heat into refrigerant vapour and enters absorber e1, being absorbed also by the concentrated solution from low pressure generator b1, heat release obtains backheating type double-effect second class absorption heat pump on the solution series circulation economic benefits and social benefits basis in heated medium.
In above-mentioned flow process, the solution that enters newly-increased absorptions-evaporimeter 1 absorb the refrigerant vapour of flash-pot d1 and heat release in the cryogen liquid of the newly-increased absorptions-evaporimeter 1 of flowing through, belong to the backheat technology---utilize the heat release (coming the liquefaction of the refrigerant vapour of flash-pot d1) of working medium in circulating to satisfy the heat absorption of working medium (vaporization of the cryogen liquid that increases absorption-evaporimeter 1 newly of flowing through).
Shown in Figure 2, also can obtain like this based on backheating type double-effect second class absorption heat pump of solution series circulation economic benefits and social benefits:
With shown in Figure 31 by high pressure generator a1, low pressure generator b1, condenser c1, evaporimeter d1, absorber e1, solution pump f1, cryogen liquid pump g1, choke valve h1, in solution series circulation economic benefits and social benefits second class absorption heat pump that the solution heat exchanger i1 and the second solution heat exchanger j1 form, increase newly-increased absorption-evaporimeter 1, newly-increased solution heat exchanger 3 and newly-increased cryogen liquid pump 4, low pressure generator b1 there is the concentrated solution pipeline through solution pump f1, second solution heat exchanger j1 connection solution heat exchanger i1 changes low pressure generator b1 into has the concentrated solution pipeline through solution pump f1, the second solution heat exchanger j1 is communicated with solution heat exchanger i1 with newly-increased solution heat exchanger 3, having the concentrated solution pipeline to change high pressure generator a1 into through the second solution heat exchanger j1 connection low pressure generator b1 high pressure generator a1 has concentrated solution pipeline newly-increased absorption-evaporimeter 1 after newly-increased solution heat exchanger 3 is communicated with newly-increased absorption-evaporimeter 1 the weak solution pipeline to be arranged again through second solution heat exchanger j1 connection low pressure generator b1, set up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection by evaporimeter d1, setting up cryogen liquid pipeline newly-increased absorption-evaporimeter 1 after newly-increased cryogen liquid pump 4 is communicated with newly-increased absorption-evaporimeter 1 again by evaporimeter d1 has refrigerant vapour pipeline connection absorber e1 again; The concentrated solution of high pressure generator a1 enters newly-increased absorption-evaporimeter 1 through newly-increased absorption-evaporimeter 3, absorb refrigerant vapour and the heat release of flash-pot d1 to increase the cryogen liquid of absorption-evaporimeter 1 newly in flowing through, the weak solution of newly-increased absorption-evaporimeter 1 enters low pressure generator b1 through the second solution heat exchanger j 1, the cryogen liquid of the evaporimeter d1 newly-increased absorption-evaporimeter 1 of flowing through after newly-increased cryogen liquid pump 4 pressurizations absorbs heat into refrigerant vapour and enters absorber e1, being absorbed also by the concentrated solution from high pressure generator a1, heat release obtains backheating type double-effect second class absorption heat pump on the solution series circulation economic benefits and social benefits basis in heated medium.
Shown in Figure 3, can obtain so again based on backheating type double-effect second class absorption heat pump of solution series circulation economic benefits and social benefits:
With shown in Figure 32 by high pressure generator a1, low pressure generator b1, condenser c1, evaporimeter d1, absorber e1, solution pump f1, cryogen liquid pump g1, choke valve h1, in solution series circulation economic benefits and social benefits second class absorption heat pump that the solution heat exchanger i1 and the second solution pump k1 form, newly-increased absorption-evaporimeter 1, increase newly-increased choke valve 2 and newly-increased solution heat exchanger 3, there is the concentrated solution pipeline to be communicated with absorber e1 with solution heat exchanger i1 high pressure generator a1 through solution pump f1, absorber e1 has the weak solution pipeline to change high pressure generator a1 into through solution heat exchanger i1 connection low pressure generator b1 again and the concentrated solution pipeline is arranged through solution pump f1, solution heat exchanger i1 is communicated with absorber e1 with newly-increased solution heat exchanger 3, absorber e1 has weak solution pipeline newly-increased absorption-evaporimeter 1 after newly-increased solution heat exchanger 3 is communicated with newly-increased absorption-evaporimeter 1 to have the weak solution pipeline to be communicated with low pressure generator b1 through solution heat exchanger i1 more again, having the cryogen liquid pipeline to change condenser c1 into through cryogen liquid pump g1 connection evaporimeter d1 condenser c1 has the cryogen liquid pipeline to be divided into two-way behind cryogen liquid pump g1---and one the tunnel is communicated with evaporimeter d1 through newly-increased choke valve 2 again, another road directly is communicated with the newly-increased absorption-evaporimeter 1 in newly-increased absorption-evaporimeter 1 back refrigerant vapour pipeline connection absorber e1 again, sets up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection by evaporimeter d1; The weak solution of absorber e1 enters newly-increased absorption-evaporimeter 1 through newly-increased absorption-evaporimeter 3, absorb refrigerant vapour and the heat release of flash-pot d1 to increase the cryogen liquid of absorption-evaporimeter 1 newly in flowing through, the weak solution of newly-increased absorption-evaporimeter 1 enters low pressure generator b1 through solution heat exchanger i1, the cryogen liquid of the condenser c1 newly-increased absorption-evaporimeter 1 of flowing through after cryogen liquid pump g1 pressurization absorbs heat into refrigerant vapour and enters absorber e1, being absorbed also by the concentrated solution from high pressure generator a1, heat release obtains backheating type double-effect second class absorption heat pump on the solution series circulation economic benefits and social benefits basis in heated medium.
Shown in Figure 4, also can obtain like this based on backheating type double-effect second class absorption heat pump of solution series circulation economic benefits and social benefits:
With shown in Figure 32 by high pressure generator a1, low pressure generator b1, condenser c1, evaporimeter d1, absorber e1, solution pump f1, cryogen liquid pump g1, choke valve h1, in solution series circulation economic benefits and social benefits second class absorption heat pump that the solution heat exchanger i1 and the second solution pump k1 form, newly-increased absorption-evaporimeter 1, increase newly-increased choke valve 2 and newly-increased solution heat exchanger 3, there is the concentrated solution pipeline to change low pressure generator b1 into low pressure generator b1 and the concentrated solution pipeline arranged through the second solution pump k1 through second solution pump k1 connection high pressure generator a1, newly-increased solution heat exchanger 3 is communicated with the newly-increased absorption-evaporimeter 1 in newly-increased absorption-evaporimeter 1 back has the weak solution pipeline to be communicated with high pressure generator a1 through newly-increased solution heat exchanger 3 again, setting up cryogen liquid pipeline newly-increased absorption-evaporimeter 1 after newly-increased cryogen liquid pump 4 is communicated with newly-increased absorption-evaporimeter 1 by evaporimeter d1 has refrigerant vapour pipeline connection absorber e1 again, sets up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection by evaporimeter d1; The concentrated solution of low pressure generator a1 enters newly-increased absorption-evaporimeter 1 through the second solution pump k1 and newly-increased solution heat exchanger 3, absorb refrigerant vapour and the heat release of flash-pot d1 to increase the cryogen liquid of absorption-evaporimeter 1 newly in flowing through, the weak solution of newly-increased absorption-evaporimeter 1 enters high pressure generator a1 through newly-increased solution heat exchanger 3, the cryogen liquid of the evaporimeter d1 newly-increased absorption-evaporimeter 1 of flowing through after newly-increased cryogen liquid pump 4 pressurizations absorbs heat into refrigerant vapour and enters absorber e1, being absorbed also by the concentrated solution from high pressure generator a1, heat release obtains backheating type double-effect second class absorption heat pump on the solution series circulation economic benefits and social benefits basis in heated medium.
Shown in Figure 5, obtain like this based on backheating type double-effect second class absorption heat pump of solution circulation economic benefits and social benefits in parallel:
With shown in Figure 33 by high pressure generator a1, low pressure generator b1, condenser c1, evaporimeter d1, absorber e1, solution pump f1, the second solution pump k1, cryogen liquid pump g1, choke valve h1, in the solution that the solution heat exchanger i1 and the second solution heat exchanger j1 form circulation economic benefits and social benefits in parallel second class absorption heat pump, newly-increased absorption-evaporimeter 1, increase newly-increased choke valve 2 and newly-increased solution heat exchanger 3, there is the concentrated solution pipeline to have the concentrated solution pipeline to be communicated with absorber e1 respectively with the second solution heat exchanger j1 high pressure generator a1 through the second solution pump k1 through solution pump f1 and solution heat exchanger i1 and low pressure generator b1, absorber e1 have again the weak solution pipeline respectively through solution heat exchanger i1 be communicated with high pressure generator a1 and through the second solution heat exchanger j1 be communicated with low pressure generator b1 change into high pressure generator a1 have the concentrated solution pipeline through solution pump f1 and solution heat exchanger i1 and low pressure generator b1 have the concentrated solution pipeline through the second solution pump k1 with after the second solution heat exchanger j1 two tunnel merges into one the tunnel jointly again warp increase solution heat exchanger 3 newly and be communicated with absorber e1, absorber e1 has weak solution pipeline newly-increased absorption-evaporimeter 1 after newly-increased solution heat exchanger 3 is communicated with newly-increased absorption-evaporimeter 1 to have the weak solution pipeline to be communicated with high pressure generator a1 and to be communicated with low pressure generator b1 through the second solution heat exchanger j1 through solution heat exchanger i1 respectively more again, having the cryogen liquid pipeline to change condenser c1 into through cryogen liquid pump g1 connection evaporimeter d1 condenser c1 has the cryogen liquid pipeline to be divided into two-way behind cryogen liquid pump g1---and one the tunnel is communicated with evaporimeter d1 through newly-increased choke valve 2 again, another road directly is communicated with the newly-increased absorption-evaporimeter 1 in newly-increased absorption-evaporimeter 1 back refrigerant vapour pipeline connection absorber e1 again, sets up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection by evaporimeter d1; The weak solution of absorber e1 enters newly-increased absorption-evaporimeter 1 through newly-increased absorption-evaporimeter 3, absorb refrigerant vapour and the heat release of flash-pot d1 to increase the cryogen liquid of absorption-evaporimeter 1 newly in flowing through, the weak solution of newly-increased absorption-evaporimeter 1 enters high pressure generator a1 and enters low pressure generator b1 through the second solution heat exchanger j1 through solution heat exchanger i1 respectively, the cryogen liquid of the condenser c1 newly-increased absorption-evaporimeter 1 of flowing through after cryogen liquid pump g1 pressurization absorbs heat into refrigerant vapour and enters absorber e1, absorbed also heat release in heated medium by concentrated solution, obtain backheating type double-effect second class absorption heat pump on the solution circulation economic benefits and social benefits in parallel basis from high pressure generator a1 and low pressure generator b1.
Shown in Figure 6, also can obtain like this based on backheating type double-effect second class absorption heat pump of solution circulation economic benefits and social benefits in parallel:
With shown in Figure 33 by high pressure generator a1, low pressure generator b1, condenser c1, evaporimeter d1, absorber e1, solution pump f1, the second solution pump k1, cryogen liquid pump g1, choke valve h1, in the solution that the solution heat exchanger i1 and the second solution heat exchanger j1 form circulation economic benefits and social benefits in parallel second class absorption heat pump, increase newly-increased absorption-evaporimeter 1, newly-increased solution heat exchanger 3 and newly-increased cryogen liquid pump 4, there is the concentrated solution pipeline to be communicated with absorber e1 with the second solution heat exchanger j1 low pressure generator b1 through the second solution pump k1, absorber e1 has the weak solution pipeline to change low pressure generator b1 into through second solution heat exchanger j1 connection low pressure generator b1 again and the concentrated solution pipeline is arranged through the second solution pump k1, the second solution heat exchanger j1 is communicated with absorber e1 with newly-increased solution heat exchanger 3, absorber e1 has weak solution pipeline newly-increased absorption-evaporimeter 1 after newly-increased solution heat exchanger 3 is communicated with newly-increased absorption-evaporimeter 1 to have the weak solution pipeline to be communicated with low pressure generator b1 through the second solution heat exchanger j 1 more again, setting up cryogen liquid pipeline newly-increased absorption-evaporimeter 1 after newly-increased cryogen liquid pump 4 is communicated with newly-increased absorption-evaporimeter 1 by evaporimeter d1 has refrigerant vapour pipeline connection absorber e1 again, and evaporimeter d1 also sets up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection; A part of weak solution of absorber e1 enters newly-increased absorption-evaporimeter 1 through newly-increased absorption-evaporimeter 3, absorb refrigerant vapour and the heat release of flash-pot d1 to increase the cryogen liquid of absorption-evaporimeter 1 newly in flowing through, the weak solution of newly-increased absorption-evaporimeter 1 enters low pressure generator b1 through the second solution heat exchanger j 1, the cryogen liquid of the evaporimeter d1 newly-increased absorption-evaporimeter 1 of flowing through after newly-increased cryogen liquid pump 4 pressurizations absorbs heat into refrigerant vapour and enters absorber e1, absorbed also heat release in heated medium by concentrated solution, obtain backheating type double-effect second class absorption heat pump on the solution circulation economic benefits and social benefits in parallel basis from high pressure generator a1 and low pressure generator b1.
Shown in Figure 7, also can obtain like this based on backheating type double-effect second class absorption heat pump of solution circulation economic benefits and social benefits in parallel:
With shown in Figure 33 by high pressure generator a1, low pressure generator b1, condenser c1, evaporimeter d1, absorber e1, solution pump f1, the second solution pump k1, cryogen liquid pump g1, choke valve h1, in the solution that the solution heat exchanger i1 and the second solution heat exchanger j1 form circulation economic benefits and social benefits in parallel second class absorption heat pump, increase newly-increased absorption-evaporimeter 1, newly-increased choke valve 2 and newly-increased solution heat exchanger 3, there is the concentrated solution pipeline to be communicated with absorber e1 with solution heat exchanger i1 high pressure generator a1 through solution pump f1, absorber e1 has the weak solution pipeline to change high pressure generator a1 into through solution heat exchanger i1 connection high pressure generator b1 again and the concentrated solution pipeline is arranged through solution pump f1, solution heat exchanger i1 is communicated with absorber e1 with newly-increased solution heat exchanger 3, absorber e 1 has weak solution pipeline newly-increased absorption-evaporimeter 1 after increasing solution heat exchanger 3 newly to be communicated with newly-increased absorption-evaporimeter 1 to have the weak solution pipeline to be communicated with low pressure generator b1 through solution heat exchanger i1 more again, and having the cryogen liquid pipeline to change condenser c1 into through cryogen liquid pump g1 connection evaporimeter d1 condenser c1 has the cryogen liquid pipeline to be divided into two-way behind cryogen liquid pump g1---and one the tunnel is communicated with evaporimeter d1 through newly-increased choke valve 2 again, another road directly is communicated with the newly-increased absorption-evaporimeter 1 in newly-increased absorption-evaporimeter 1 back refrigerant vapour pipeline connection absorber e1 again; Evaporimeter d1 also sets up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection; A part of weak solution of absorber e1 enters newly-increased absorption-evaporimeter 1 through newly-increased absorption-evaporimeter 3, absorb the refrigerant vapour of flash-pot d1 and heat to flow through and increase the cryogen liquid of absorption-evaporimeter 1 newly, the weak solution of newly-increased absorption-evaporimeter 1 enters low pressure generator b1 through solution heat exchanger i1, the cryogen liquid of the condenser c1 newly-increased absorption-evaporimeter 1 of flowing through after cryogen liquid pump g1 pressurization absorbs heat into refrigerant vapour and enters absorber e1, absorbed also heat release in heated medium by concentrated solution, obtain backheating type double-effect second class absorption heat pump on the solution circulation economic benefits and social benefits in parallel basis from high pressure generator a1 and low pressure generator b1.
Shown in Figure 8, obtain like this based on back-heating type triple-effect second class absorption heat pump of solution series circulation three-effect:
By high pressure generator a2, the middle generator b2 that presses, low pressure generator c2, condenser d2, evaporimeter e2, absorber f2, solution pump g2, cryogen liquid pump h2, choke valve i2, the second choke valve j2, solution heat exchanger k2, in solution series circulation three-effect second class absorption heat pump that the second solution heat exchanger l2 and the 3rd solution heat exchanger m2 form, increase newly-increased absorption-evaporimeter 1, newly-increased choke valve 2 and newly-increased solution heat exchanger 3, low pressure generator c2 there is the concentrated solution pipeline through the 3rd solution heat exchanger m2, the second solution heat exchanger l2 is communicated with absorber f2 with solution heat exchanger k2, absorber f2 has the weak solution pipeline to change low pressure generator c2 into through solution heat exchanger k2 connection high pressure generator a2 again and the concentrated solution pipeline is arranged through the 3rd solution heat exchanger m2, the second solution heat exchanger l2, solution heat exchanger k2 is communicated with absorber f2 with newly-increased solution heat exchanger 3, absorber f2 has weak solution pipeline newly-increased absorption-evaporimeter 1 after newly-increased solution heat exchanger 3 is communicated with newly-increased absorption-evaporimeter 1 to have the weak solution pipeline to be communicated with high pressure generator a2 through solution heat exchanger k2 more again, having the cryogen liquid pipeline to change condenser d2 into through cryogen liquid pump h2 connection evaporimeter e2 condenser d2 has the cryogen liquid pipeline to be divided into two-way behind cryogen liquid pump h2---and one the tunnel is communicated with evaporimeter e2 through newly-increased choke valve 2 again, another road directly is communicated with the newly-increased absorption-evaporimeter 1 in newly-increased absorption-evaporimeter 1 back refrigerant vapour pipeline connection absorber f2 again, and evaporimeter e2 also sets up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection; The weak solution of absorber f2 enters newly-increased absorption-evaporimeter 1 through newly-increased absorption-evaporimeter 3, absorb refrigerant vapour and the heat release of flash-pot e2 to increase the cryogen liquid of absorption-evaporimeter 1 newly in flowing through, the weak solution of newly-increased absorption-evaporimeter 1 enters high pressure generator a2 through solution heat exchanger k2, the cryogen liquid of the condenser d2 newly-increased absorption-evaporimeter 1 of flowing through after cryogen liquid pump h2 pressurization absorbs heat into refrigerant vapour and enters absorber f2, being absorbed also by the concentrated solution from low pressure generator c2, heat release obtains back-heating type triple-effect second class absorption heat pump on the solution series circulation three-effect basis in heated medium.
Shown in Figure 9, also can obtain like this based on back-heating type triple-effect second class absorption heat pump of solution series circulation three-effect:
By high pressure generator a2, the middle generator b2 that presses, low pressure generator c2, condenser d2, evaporimeter e2, absorber f2, solution pump g2, cryogen liquid pump h2, choke valve i2, the second choke valve j2, solution heat exchanger k2, in solution series circulation three-effect second class absorption heat pump that the second solution heat exchanger l2 and the 3rd solution heat exchanger m2 form, increase newly-increased absorption-evaporimeter 1, newly-increased choke valve 2 and newly-increased solution heat exchanger 3, low pressure generator c2 there is the concentrated solution pipeline through the 3rd solution heat exchanger m2, being communicated with solution heat exchanger k2 behind the second solution heat exchanger l2 again changes low pressure generator c2 into and the concentrated solution pipeline is arranged through the 3rd solution heat exchanger m2, the second solution heat exchanger l2, be communicated with solution heat exchanger k2 again behind the newly-increased solution heat exchanger 3, having the concentrated solution pipeline to press generator b2 to change high pressure generator a2 in the second solution heat exchanger l2 is communicated with high pressure generator a2 has concentrated solution pipeline newly-increased absorption-evaporimeter 1 after newly-increased solution heat exchanger 3 is communicated with newly-increased absorption-evaporimeter 1 to have the weak solution pipeline to press generator b2 again in the second solution heat exchanger l2 is communicated with, having the cryogen liquid pipeline to change condenser d2 into through cryogen liquid pump h2 connection evaporimeter e2 condenser d2 has the cryogen liquid pipeline to be divided into two-way behind cryogen liquid pump h2---and one the tunnel is communicated with evaporimeter e2 through newly-increased choke valve 2 again, another road directly is communicated with the newly-increased absorption-evaporimeter 1 in newly-increased absorption-evaporimeter 1 back refrigerant vapour pipeline connection absorber f2 again, and evaporimeter e2 also sets up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection; The concentrated solution of high pressure generator a2 enters newly-increased absorption-evaporimeter 1 through newly-increased absorption-evaporimeter 3, absorb the refrigerant vapour of flash-pot e2 and heat to flow through and increase the cryogen liquid of absorption-evaporimeter 1 newly, the weak solution of newly-increased absorption-evaporimeter 1 is pressed generator b2 in the second solution heat exchanger l2 enters, the cryogen liquid of condenser d2 absorbs heat into refrigerant vapour through cryogen liquid pump h2 pressurized stream through newly-increased absorption-evaporimeter 1 and enters absorber f2, being absorbed also by the concentrated solution from low pressure generator c2, heat release obtains back-heating type triple-effect second class absorption heat pump on the solution series circulation three-effect basis in heated medium.
Shown in Figure 10, can obtain so again based on back-heating type triple-effect second class absorption heat pump of solution series circulation three-effect:
By high pressure generator a2, the middle generator b2 that presses, low pressure generator c2, condenser d2, evaporimeter e2, absorber f2, solution pump g2, cryogen liquid pump h2, choke valve i2, the second choke valve j2, solution heat exchanger k2, in solution series circulation three-effect second class absorption heat pump that the second solution heat exchanger l2 and the 3rd solution heat exchanger m2 form, increase newly-increased absorption-evaporimeter 1, newly-increased solution heat exchanger 3 and newly-increased cryogen liquid pump 4, having the concentrated solution pipeline to be communicated with second solution heat exchanger (l2) again behind the 3rd solution heat exchanger (m2) low pressure generator (c2) changes low pressure generator (c2) into and the concentrated solution pipeline is arranged through the 3rd solution heat exchanger (m2), be communicated with second solution heat exchanger (l2) again behind the newly-increased solution heat exchanger 3 and simultaneously middle pressure generator (b2) had the concentrated solution pipeline to be communicated with low pressure generator (c2) through the 3rd solution heat exchanger (m2) and press in changing into generator (b2) to have the concentrated solution pipeline to be communicated with the newly-increased absorptions-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back through newly-increased solution heat exchanger (3) to have the weak solution pipeline to be set up the cryogen liquid pipeline by evaporimeter e2 through the 3rd solution heat exchanger (m2) connection low pressure generator (c2) again to increase absorption-evaporimeter 1 newly after 4 connections of cryogen liquid pump increase absorption-evaporimeter 1 newly refrigerant vapour pipeline connection absorber f2 is arranged again through increasing newly, evaporimeter e2 sets up the refrigerant vapour pipeline connection and increases absorption-evaporimeter 1 newly; The middle concentrated solution of generator b2 of pressing enters newly-increased absorption-evaporimeter 1 through newly-increased absorption-evaporimeter 3, absorb refrigerant vapour and the heat release of flash-pot e2 to increase the cryogen liquid of absorption-evaporimeter 1 newly in flowing through, the weak solution of newly-increased absorption-evaporimeter 1 enters low pressure generator c2 through the 3rd solution heat exchanger m2, the cryogen liquid of the evaporimeter e2 newly-increased absorption-evaporimeter 1 of flowing through after newly-increased cryogen liquid pump 4 pressurizations absorbs heat into refrigerant vapour and enters absorber f2, being absorbed also by the concentrated solution from low pressure generator c2, heat release obtains back-heating type triple-effect second class absorption heat pump on the solution series circulation three-effect basis in heated medium.
Shown in Figure 11, also can obtain like this based on back-heating type triple-effect second class absorption heat pump of solution series circulation three-effect:
By high pressure generator a2, the middle generator b2 that presses, low pressure generator c2, condenser d2, evaporimeter e2, absorber f2, solution pump g2, the second solution pump n2, the 3rd solution pump o2, cryogen liquid pump h2, choke valve i2, in solution series circulation three-effect second class absorption heat pump that the second choke valve j2 and solution heat exchanger k2 form, increase newly-increased absorption-evaporimeter 1, newly-increased choke valve 2 and newly-increased solution heat exchanger 3, there is the concentrated solution pipeline to be communicated with absorber f2 high pressure generator a2 through solution heat exchanger k2, absorber f2 has the weak solution pipeline to change high pressure generator a2 into through solution heat exchanger k2 connection low pressure generator c2 again has the concentrated solution pipeline to be communicated with absorber f2 through solution heat exchanger k2 with newly-increased solution heat exchanger 3, absorber f2 has weak solution pipeline newly-increased absorption-evaporimeter 1 after increasing solution heat exchanger 3 newly to be communicated with newly-increased absorption-evaporimeter 1 to have the weak solution pipeline to be communicated with low pressure generator c2 through solution heat exchanger k2 more again, and having the cryogen liquid pipeline to change condenser d2 into through cryogen liquid pump h2 connection evaporimeter e2 condenser d2 has the cryogen liquid pipeline to be divided into two-way behind cryogen liquid pump h2---and one the tunnel is communicated with evaporimeter e2 through newly-increased choke valve 2 again, another road directly is communicated with the newly-increased absorption-evaporimeter 1 in newly-increased absorption-evaporimeter 1 back refrigerant vapour pipeline connection absorber f2 again; Evaporimeter e2 also sets up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection; The weak solution of absorber f2 enters newly-increased absorption-evaporimeter 1 through newly-increased absorption-evaporimeter 3, absorb refrigerant vapour and the heat release of flash-pot e2 to increase the cryogen liquid of absorption-evaporimeter 1 newly in flowing through, the weak solution of newly-increased absorption-evaporimeter 1 enters low pressure generator c2 through solution heat exchanger k2, the cryogen liquid of the condenser d2 newly-increased absorption-evaporimeter 1 of flowing through after cryogen liquid pump h2 pressurization absorbs heat into refrigerant vapour and enters absorber f2, being absorbed also by the concentrated solution from high pressure generator a2, heat release obtains back-heating type triple-effect second class absorption heat pump on the solution series circulation three-effect basis in heated medium.
Shown in Figure 12, obtain like this based on back-heating type triple-effect second class absorption heat pump of solution series circulation three-effect:
By high pressure generator a2, the middle generator b2 that presses, low pressure generator c2, condenser d2, evaporimeter e2, absorber f2, solution pump g2, the second solution pump n2, the 3rd solution pump o2, cryogen liquid pump h2, choke valve i2, in solution series circulation three-effect second class absorption heat pump that the second choke valve j2 and solution heat exchanger k2 form, increase newly-increased absorption-evaporimeter 1, newly-increased choke valve 2 and newly-increased solution heat exchanger 3, there is the concentrated solution pipeline in the 3rd solution pump o2 is communicated with, to press generator b2 to change low pressure generator c2 into low pressure generator c2 and the concentrated solution pipeline arranged through the 3rd solution pump o2, newly-increased solution heat exchanger 3 is communicated with the newly-increased absorptions-evaporimeter 1 in newly-increased absorptions-evaporimeter 1 back has the weak solution pipeline to press generator b2 again in newly-increased solution heat exchanger 3 is communicated with, and has the cryogen liquid pipeline to be communicated with evaporimeter e2 through cryogen liquid pump h2 condenser d2 and changes condenser d2 into and have the cryogen liquid pipeline to be divided into two-way behind cryogen liquid pump h2---and one the tunnel again through increasing choke valve 2 connection evaporimeter e2 newly, another road directly is communicated with the newly-increased absorption-evaporimeter 1 in newly-increased absorption-evaporimeter 1 back refrigerant vapour pipeline connection absorber f2 again; Evaporimeter e2 also sets up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection; The concentrated solution of low pressure generator c2 enters newly-increased absorption-evaporimeter 1 through the 3rd solution pump o2 with newly-increased absorption-evaporimeter 3, absorb the refrigerant vapour of flash-pot e2 and heat to flow through and increase the cryogen liquid of absorption-evaporimeter 1 newly, the weak solution of newly-increased absorption-evaporimeter 1 is pressed generator b2 in newly-increased solution heat exchanger 3 enters, the cryogen liquid of the condenser d2 newly-increased absorption-evaporimeter 1 of flowing through after cryogen liquid pump h2 pressurization absorbs heat into refrigerant vapour and enters absorber f2, being absorbed also by the concentrated solution from high pressure generator a2, heat release obtains back-heating type triple-effect second class absorption heat pump on the solution series circulation three-effect basis in heated medium.
Shown in Figure 13, be achieved in that based on back-heating type triple-effect second class absorption heat pump of solution series circulation three-effect
By high pressure generator a2, the middle generator b2 that presses, low pressure generator c2, condenser d2, evaporimeter e2, absorber f2, solution pump g2, the second solution pump n2, the 3rd solution pump o2, cryogen liquid pump h2, choke valve i2, in solution series circulation three-effect second class absorption heat pump that the second choke valve j2 and solution heat exchanger k2 form, increase newly-increased absorption-evaporimeter 1, newly-increased solution heat exchanger 3 and newly-increased cryogen liquid pump 4, there is the concentrated solution pipeline in second solution pump n2 connection high pressure generator a2 changes into, to press generator b2 the concentrated solution pipeline to be arranged middle pressure generator b2 through the second solution pump n2, newly-increased solution heat exchanger 3 is communicated with the newly-increased absorption-evaporimeter 1 in newly-increased absorption-evaporimeter 1 back has the weak solution pipeline to be communicated with high pressure generator a2 through newly-increased solution heat exchanger 3 again, setting up cryogen liquid pipeline newly-increased absorption-evaporimeter 1 after newly-increased cryogen liquid pump 4 is communicated with newly-increased absorption-evaporimeter 1 by evaporimeter e2 has refrigerant vapour pipeline connection absorber f2 again, and evaporimeter e2 also sets up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection; The middle generator b2 that presses provides solution to newly-increased absorption-evaporimeter 1, evaporimeter e2 provides refrigerant vapour to newly-increased absorption-evaporimeter 1, newly-increased absorption-evaporimeter 1 heating comes the cryogen liquid of flash-pot e2 to become refrigerant vapour to provide to absorber f2, the weak solution of newly-increased absorption-evaporimeter 1 enters high pressure generator a2 through newly-increased solution heat exchanger 3, obtains back-heating type triple-effect second class absorption heat pump on the solution series circulation three-effect basis.
Shown in Figure 14, be achieved in that based on back-heating type triple-effect second class absorption heat pump of solution circulation three-effect in parallel
By high pressure generator a2, the middle generator b2 that presses, low pressure generator c2, condenser d2, evaporimeter e2, absorber f2, solution pump g2, the second solution pump n2, the 3rd solution pump o2, cryogen liquid pump h2, choke valve i2, the second choke valve j2, solution heat exchanger k2, in solution series circulation three-effect second class absorption heat pump that the second solution heat exchanger l2 and the 3rd solution heat exchanger m2 form, increase newly-increased choke valve 2, newly-increased absorption-evaporimeter 1 and newly-increased solution heat exchanger 3, high pressure generator a2 there is the concentrated solution pipeline through solution pump g2 and solution heat exchanger k2, the middle generator b2 that presses has the concentrated solution pipeline to have the concentrated solution pipeline to be communicated with absorber (f2) through the 3rd solution pump o2 respectively with the 3rd solution heat exchanger m2 through the second solution pump n2 and the second solution heat exchanger l2 and low pressure generator c2, absorber f2 has the weak solution pipeline to be communicated with high pressure generator a2 through solution heat exchanger k2 respectively again, in the second solution heat exchanger l2 is communicated with, press generator b2 and change high pressure generator a2 into and the concentrated solution pipeline is arranged through solution pump g2 and solution heat exchanger k2 through the 3rd solution heat exchanger m2 connection low pressure generator (c2), in press generator b2 have the concentrated solution pipeline through the second solution pump n2 and the second solution heat exchanger l2 and low pressure generator c2 have the concentrated solution pipeline through the 3rd solution pump o2 with after the 3rd solution heat exchanger m2 three tunnel merges into one the tunnel jointly again warp increase solution heat exchanger 3 newly and be communicated with absorber f2, absorber f2 has weak solution pipeline newly-increased absorption-evaporimeter 1 after newly-increased solution heat exchanger 3 is communicated with newly-increased absorption-evaporimeter 1 to have the weak solution pipeline to be communicated with high pressure generator a1 through solution heat exchanger k2 respectively more again, in the second solution heat exchanger l2 is communicated with, press generator b2 and be communicated with low pressure generator c2 through the 3rd solution heat exchanger m2, also set up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection by evaporimeter (e2), having the cryogen liquid pipeline to change condenser d2 into through cryogen liquid pump h2 connection evaporimeter e2 condenser d2 has the cryogen liquid pipeline to be divided into two-way behind cryogen liquid pump h2---and one the tunnel is communicated with evaporimeter e2 through newly-increased choke valve 2 again, another road directly is communicated with the newly-increased absorption-evaporimeter 1 in newly-increased absorption-evaporimeter 1 back refrigerant vapour pipeline connection absorber f2 again; The weak solution of absorber f2 enters newly-increased absorption-evaporimeter 1 through newly-increased absorption-evaporimeter 3, absorb refrigerant vapour and the heat release of flash-pot e2 to increase the cryogen liquid of absorption-evaporimeter 1 newly in flowing through, the weak solution of newly-increased absorption-evaporimeter 1 enters high pressure generator a2 through solution heat exchanger k2 respectively, in the second solution heat exchanger l2 enters, press generator b2 and enter low pressure generator c2 through the 3rd solution heat exchanger m2, the cryogen liquid of the condenser d2 newly-increased absorption-evaporimeter 1 of flowing through after cryogen liquid pump h2 pressurization absorbs heat into refrigerant vapour and enters absorber f2, quilt is from high pressure generator a2, the concentrated solution of middle generator b2 of pressure and low pressure generator c2 absorbs also heat release in heated medium, obtains back-heating type triple-effect second class absorption heat pump on the solution circulation three-effect in parallel basis.
Shown in Figure 15, also realize like this based on back-heating type triple-effect second class absorption heat pump of solution circulation three-effect in parallel:
By high pressure generator a2, the middle generator b2 that presses, low pressure generator c2, condenser d2, evaporimeter e2, absorber f2, solution pump g2, the second solution pump n2, the 3rd solution pump o2, cryogen liquid pump h2, choke valve i2, the second choke valve j2, solution heat exchanger k2, in solution series circulation three-effect second class absorption heat pump that the second solution heat exchanger l2 and the 3rd solution heat exchanger m2 form, increase newly-increased choke valve 2, newly-increased absorption-evaporimeter 1 and newly-increased solution heat exchanger 3, high pressure generator a2 there is the concentrated solution pipeline through solution pump g2 and solution heat exchanger k2, the middle generator b2 that presses has the concentrated solution pipeline to have the concentrated solution pipeline to be communicated with absorber (f2) through the 3rd solution pump o2 respectively with the 3rd solution heat exchanger m2 through the second solution pump n2 and the second solution heat exchanger l2 and low pressure generator c2, absorber f2 has the weak solution pipeline to be communicated with high pressure generator a2 through solution heat exchanger k2 respectively again, in the second solution heat exchanger l2 is communicated with, press generator b2 and change high pressure generator a2 into and the concentrated solution pipeline is arranged through solution pump g2 and solution heat exchanger k2 through the 3rd solution heat exchanger m2 connection low pressure generator c2, in press generator b2 have the concentrated solution pipeline through the second solution pump n2 and the second solution heat exchanger l2 and low pressure generator c2 have the concentrated solution pipeline through the 3rd solution pump o2 with after the 3rd solution heat exchanger m2 three tunnel merges into one the tunnel jointly again warp increase solution heat exchanger 3 newly and be communicated with absorber f2, absorber f2 has the weak solution pipeline to be divided into two-way again behind newly-increased solution heat exchanger 3---and one the tunnel through solution heat exchanger k2 connection high pressure generator a1, another road is communicated with the newly-increased absorptions-evaporimeter 1 in newly-increased absorptions-evaporimeter 1 back weak solution pipeline pressure generator b2 and through the 3rd solution heat exchanger m2 connection low pressure generator c2 in the second solution heat exchanger l2 is communicated with respectively again, also set up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection by evaporimeter (e2), having the cryogen liquid pipeline to change condenser d2 into through cryogen liquid pump h2 connection evaporimeter e2 condenser d2 has the cryogen liquid pipeline to be divided into two-way behind cryogen liquid pump h2---and one the tunnel is communicated with evaporimeter e2 through newly-increased choke valve 2 again, another road directly is communicated with the newly-increased absorption-evaporimeter 1 in newly-increased absorption-evaporimeter 1 back refrigerant vapour pipeline connection absorber f2 again; A part of weak solution of absorber f2 enters newly-increased absorption-evaporimeter 1 through newly-increased absorption-evaporimeter 3, absorb refrigerant vapour and the heat release of flash-pot e2 to increase the cryogen liquid of absorption-evaporimeter 1 newly in flowing through, the weak solution of newly-increased absorption-evaporimeter 1 is pressed generator b2 respectively and is entered low pressure generator c2 through the 3rd solution heat exchanger m2 in the second solution heat exchanger l2 enters, the cryogen liquid of the condenser d2 newly-increased absorption-evaporimeter 1 of flowing through after cryogen liquid pump h2 pressurization absorbs heat into refrigerant vapour and enters absorber f2, quilt is from high pressure generator a2, the concentrated solution of middle generator b2 of pressure and low pressure generator c2 absorbs also heat release in heated medium, obtains back-heating type triple-effect second class absorption heat pump on the solution circulation three-effect in parallel basis.
Shown in Figure 16, can realize so again based on back-heating type triple-effect second class absorption heat pump of solution circulation three-effect in parallel:
By high pressure generator a2, the middle generator b2 that presses, low pressure generator c2, condenser d2, evaporimeter e2, absorber f2, solution pump g2, the second solution pump n2, the 3rd solution pump o2, cryogen liquid pump h2, choke valve i2, the second choke valve j2, solution heat exchanger k2, in solution series circulation three-effect second class absorption heat pump that the second solution heat exchanger l2 and the 3rd solution heat exchanger m2 form, increase newly-increased choke valve 2, newly-increased absorption-evaporimeter 1 and newly-increased solution heat exchanger 3, there is the concentrated solution pipeline to have the concentrated solution pipeline to be communicated with absorber f2 respectively with the 3rd solution heat exchanger m2 middle pressure generator b2 through the 3rd solution pump o2 through the second solution pump n2 and the second solution heat exchanger l2 and low pressure generator c2, absorber f2 have again the weak solution pipeline in the second solution heat exchanger l2 is communicated with, press respectively generator b2 and through the 3rd solution heat exchanger m2 be communicated with low pressure generator c2 press in changing into generator b2 have the concentrated solution pipeline through the second solution pump n2 and the second solution heat exchanger l2 and low pressure generator c2 have the concentrated solution pipeline through the 3rd solution pump o2 with after the 3rd solution heat exchanger m2 two tunnel merges into one the tunnel jointly again warp increase solution heat exchanger 3 newly and be communicated with absorber f2, absorber f2 has weak solution pipeline newly-increased absorption-evaporimeter 1 after newly-increased solution heat exchanger 3 is communicated with newly-increased absorption-evaporimeter 1 to have the weak solution pipeline to press generator b2 respectively again in the second solution heat exchanger l2 is communicated with again and is communicated with low pressure generator c2 through the 3rd solution heat exchanger m2, also set up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection by evaporimeter (e2), having the cryogen liquid pipeline to change condenser d2 into through cryogen liquid pump h2 connection evaporimeter e2 condenser d2 has the cryogen liquid pipeline to be divided into two-way behind cryogen liquid pump h2---and one the tunnel is communicated with evaporimeter e2 through newly-increased choke valve 2 again, another road directly is communicated with the newly-increased absorption-evaporimeter 1 in newly-increased absorption-evaporimeter 1 back refrigerant vapour pipeline connection absorber f2 again; A part of weak solution of absorber f2 enters newly-increased absorption-evaporimeter 1 through newly-increased absorption-evaporimeter 3, absorb refrigerant vapour and the heat release of flash-pot e2 to increase the cryogen liquid of absorption-evaporimeter 1 newly in flowing through, the weak solution of newly-increased absorption-evaporimeter 1 is pressed generator b2 respectively and is entered low pressure generator c2 through the 3rd solution heat exchanger m2 in the second solution heat exchanger l2 enters, the cryogen liquid of the condenser d2 newly-increased absorption-evaporimeter 1 of flowing through after cryogen liquid pump h2 pressurization absorbs heat into refrigerant vapour and enters absorber f2, quilt is from high pressure generator a2, the concentrated solution of middle generator b2 of pressure and low pressure generator c2 absorbs also heat release in heated medium, obtains back-heating type triple-effect second class absorption heat pump on the solution circulation three-effect in parallel basis.
Shown in Figure 17, also obtain like this based on back-heating type triple-effect second class absorption heat pump of solution circulation three-effect in parallel:
By high pressure generator a2, the middle generator b2 that presses, low pressure generator c2, condenser d2, evaporimeter e2, absorber f2, solution pump g2, the second solution pump n2, the 3rd solution pump o2, cryogen liquid pump h2, choke valve i2, the second choke valve j2, solution heat exchanger k2, in solution series circulation three-effect second class absorption heat pump that the second solution heat exchanger l2 and the 3rd solution heat exchanger m2 form, increase newly-increased absorption-evaporimeter 1, newly-increased solution heat exchanger 3 and newly-increased cryogen liquid pump 4, there is the concentrated solution pipeline to be communicated with absorber f2 with the 3rd solution heat exchanger m2 low pressure generator c2 through the 3rd solution pump o2, absorber f2 has the weak solution pipeline to change low pressure generator c2 into through the 3rd solution heat exchanger m2 connection low pressure generator c2 again and the concentrated solution pipeline is arranged through the 3rd solution pump o2, the 3rd solution heat exchanger m2 is communicated with absorber f2 with newly-increased solution heat exchanger 3, absorber f2 has weak solution pipeline newly-increased absorption-evaporimeter 1 after newly-increased solution heat exchanger 3 is communicated with newly-increased absorption-evaporimeter 1 to have the weak solution pipeline to be communicated with low pressure generator c2 through the 3rd solution heat exchanger m2 more again, evaporimeter e2 sets up cryogen liquid pipeline newly-increased absorption-evaporimeter 1 after newly-increased cryogen liquid pump 4 is communicated with newly-increased absorption-evaporimeter 1 refrigerant vapour pipeline connection absorber f2 again, and evaporimeter e2 also sets up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection; A part of weak solution of absorber f2 enters newly-increased absorption-evaporimeter 1 through newly-increased absorption-evaporimeter 3, absorb refrigerant vapour and the heat release of flash-pot e2 to increase the cryogen liquid of absorption-evaporimeter 1 newly in flowing through, the weak solution of newly-increased absorption-evaporimeter 1 enters low pressure generator c2 through the 3rd solution heat exchanger m2, the cryogen liquid of the evaporimeter e2 newly-increased absorption-evaporimeter 1 of flowing through after newly-increased cryogen liquid pump 4 pressurizations absorbs heat into refrigerant vapour and enters absorber f2, quilt is from high pressure generator a2, the concentrated solution of middle generator b2 of pressure and low pressure generator c2 absorbs also heat release in heated medium, obtains back-heating type triple-effect second class absorption heat pump on the solution circulation three-effect in parallel basis.
Shown in Figure 180, also obtain like this based on back-heating type triple-effect second class absorption heat pump of solution circulation three-effect in parallel:
By high pressure generator a2, the middle generator b2 that presses, low pressure generator c2, condenser d2, evaporimeter e2, absorber f2, solution pump g2, the second solution pump n2, the 3rd solution pump o2, cryogen liquid pump h2, choke valve i2, the second choke valve j2, solution heat exchanger k2, in solution series circulation three-effect second class absorption heat pump that the second solution heat exchanger l2 and the 3rd solution heat exchanger m2 form, increase newly-increased absorption-evaporimeter 1, newly-increased solution heat exchanger 3 and newly-increased cryogen liquid pump 4, there is the concentrated solution pipeline to be communicated with absorber f2 with the second solution heat exchanger l2 middle pressure generator b2 through the second solution pump n2, absorber f2 has the weak solution pipeline to press generator b2 to change the middle generator b2 that presses in the second solution heat exchanger l2 is communicated with again and the concentrated solution pipeline is arranged through the second solution pump n2, the second solution heat exchanger l2 is communicated with absorber f2 with newly-increased solution heat exchanger 3, absorber f2 has weak solution pipeline newly-increased absorption-evaporimeter 1 after newly-increased solution heat exchanger 3 is communicated with newly-increased absorption-evaporimeter 1 to have the weak solution pipeline to press generator b2 again in the second solution heat exchanger l2 is communicated with again, evaporimeter e2 sets up cryogen liquid pipeline newly-increased absorption-evaporimeter 1 after newly-increased cryogen liquid pump 4 is communicated with newly-increased absorption-evaporimeter 1 refrigerant vapour pipeline connection absorber f2 again, and evaporimeter e2 also sets up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection; A part of weak solution of absorber f2 enters newly-increased absorption-evaporimeter 1 through newly-increased absorption-evaporimeter 3, absorb refrigerant vapour and the heat release of flash-pot e2 to increase the cryogen liquid of absorption-evaporimeter 1 newly in flowing through, the weak solution of newly-increased absorption-evaporimeter 1 is pressed generator b2 in the second solution heat exchanger l2 enters, the cryogen liquid of the evaporimeter e2 newly-increased absorption-evaporimeter 1 of flowing through after newly-increased cryogen liquid pump 4 pressurizations absorbs heat into refrigerant vapour and enters absorber f2, quilt is from high pressure generator a2, the concentrated solution of middle generator b2 of pressure and low pressure generator c2 absorbs also heat release in heated medium, obtains back-heating type triple-effect second class absorption heat pump on the solution circulation three-effect in parallel basis.
Shown in Figure 19, also obtain like this based on back-heating type triple-effect second class absorption heat pump of solution circulation three-effect in parallel:
By high pressure generator a2, the middle generator b2 that presses, low pressure generator c2, condenser d2, evaporimeter e2, absorber f2, solution pump g2, the second solution pump n2, the 3rd solution pump o2, cryogen liquid pump h2, choke valve i2, the second choke valve j2, solution heat exchanger k2, in solution series circulation three-effect second class absorption heat pump that the second solution heat exchanger l2 and the 3rd solution heat exchanger m2 form, increase newly-increased absorption-evaporimeter 1, newly-increased solution heat exchanger 3 and newly-increased cryogen liquid pump 4, there is the concentrated solution pipeline to be communicated with absorber f2 with solution heat exchanger k2 high pressure generator a2 through solution pump g2, absorber f2 has the weak solution pipeline to change high pressure generator a2 into through solution heat exchanger k2 connection high pressure generator a2 respectively again and the concentrated solution pipeline is arranged through solution pump g2, solution heat exchanger k2 is communicated with absorber f2 with newly-increased solution heat exchanger 3, absorber f2 has weak solution pipeline newly-increased absorption-evaporimeter 1 after newly-increased solution heat exchanger 3 is communicated with newly-increased absorption-evaporimeter 1 to have the weak solution pipeline to be communicated with high pressure generator a1 through solution heat exchanger k2 more again, evaporimeter e2 sets up cryogen liquid pipeline newly-increased absorption-evaporimeter 1 after newly-increased cryogen liquid pump 4 is communicated with newly-increased absorption-evaporimeter 1 refrigerant vapour pipeline connection absorber f2 again, and evaporimeter e2 also sets up the newly-increased absorption-evaporimeter 1 of refrigerant vapour pipeline connection; A part of weak solution of absorber f2 enters newly-increased absorption-evaporimeter 1 through newly-increased absorption-evaporimeter 3, absorb refrigerant vapour and the heat release of flash-pot e2 to increase the cryogen liquid of absorption-evaporimeter 1 newly in flowing through, the weak solution of newly-increased absorption-evaporimeter 1 enters high pressure generator a2 through solution heat exchanger k2, the cryogen liquid of the evaporimeter e2 newly-increased absorption-evaporimeter 1 of flowing through after newly-increased cryogen liquid pump 4 pressurizations absorbs heat into refrigerant vapour and enters absorber f2, quilt is from high pressure generator a2, the concentrated solution of middle generator b2 of pressure and low pressure generator c2 absorbs also heat release in heated medium, obtains back-heating type triple-effect second class absorption heat pump on the solution circulation three-effect in parallel basis.
Shown in Figure 20, be achieved in that based on backheating type double-effect second class absorption heat pump of solution series circulation economic benefits and social benefits, additional low-temperature heat supply terminal
As shown in Figure 1, in backheating type double-effect second class absorption heat pump based on solution series circulation economic benefits and social benefits, increase and increase absorber 5 and resolubilization liquid heat exchanger 6 again, between the concentrated solution pipeline of the newly-increased solution heat exchanger 3 of solution heat exchanger i1 connection, draw a concentrated solution pipeline and increase absorber 5 again through 6 connections of resolubilization liquid heat exchanger, set up the refrigerant vapour pipeline connection by evaporimeter d1 and increase absorber 5 again, increasing absorber 5 more also has the weak solution pipeline to be communicated with high pressure generator a1 and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger 6 respectively; Enter the solution that increases absorber 5 again by low pressure generator b1 through solution pump f1, the second solution heat exchanger j 1, solution heat exchanger i 1 and resolubilization liquid heat exchanger 6 and absorb the refrigerant vapour of flash-pot d1 and heat release in heated medium, the weak solution that increases absorber 5 again enters high pressure generator a1 through resolubilization liquid heat exchanger 6; Increase absorber 5 and absorber e1 more respectively to the heated medium heat supply, obtain backheating type double-effect second class absorption heat pump of solution series circulation economic benefits and social benefits for upward basic and additional low-temperature heat supply terminal.
Shown in Figure 21, also can realize like this based on backheating type double-effect second class absorption heat pump of solution series circulation economic benefits and social benefits, additional low-temperature heat supply terminal:
As shown in Figure 1, in backheating type double-effect second class absorption heat pump based on solution series circulation economic benefits and social benefits, increase and increase absorber 5 again, resolubilization liquid heat exchanger 6 and resolubilization liquid control valve 7, low pressure generator b1 there is the concentrated solution pipeline through solution pump f1, the second solution heat exchanger j1, solution heat exchanger i1 is communicated with absorber e1 and changes low pressure generator b1 into and the concentrated solution pipeline is arranged through solution pump f1 with newly-increased solution heat exchanger 3, the second solution heat exchanger j1, solution heat exchanger i1, be divided into two-way behind the resolubilization liquid heat exchanger 6---the one tunnel is communicated with absorber e1 through newly-increased solution heat exchanger 3 again, another Lu Zaijing resolubilization liquid control valve 7 connections increase absorber 5 again, set up the refrigerant vapour pipeline connection by evaporimeter d1 and increase absorber 5 again, increase absorber 5 again and also have the weak solution pipeline to be communicated with high pressure generator a1 and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger 6; Enter the solution that increases absorber 5 again by low pressure generator b1 through solution pump f1, the second solution heat exchanger j1, solution heat exchanger i1, resolubilization liquid heat exchanger 6 and solution control valve 7 and absorb the refrigerant vapour of flash-pot d1 and heat release in heated medium, the weak solution that increases absorber 5 again enters high pressure generator a1 through resolubilization liquid heat exchanger 6; Increase absorber 5 and absorber e1 more respectively to the heated medium heat supply, obtain on the solution series circulation economic benefits and social benefits basis and backheating type double-effect second class absorption heat pump of additional low-temperature heat supply terminal.
Shown in Figure 22, backheating type double-effect second class absorption heat pump that joins circulation economic benefits and social benefits, additional low-temperature heat supply terminal based on solution series is achieved in that
As shown in Figure 3, in backheating type double-effect second class absorption heat pump based on solution series circulation economic benefits and social benefits, increase and increase absorber 5 and resolubilization liquid heat exchanger 6 again, drawing a concentrated solution pipeline between solution heat exchanger i1 and concentrated solution pipeline that newly-increased solution heat exchanger 3 links to each other is communicated with through resolubilization liquid heat exchanger 6 and increases absorber 5 again, set up the refrigerant vapour pipeline connection by evaporimeter d1 and increase absorber 5 again, increasing absorber 5 more also has the weak solution pipeline to be communicated with low pressure generator b1 and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger 6 respectively; Entered through solution pump f1, solution heat exchanger i 1, resolubilization liquid heat exchanger 6 by high pressure generator a1 and to increase absorber 5 concentrated solutions again and absorb the refrigerant vapour of flash-pot d1 and heat release in heated medium, the weak solution that increases absorber 5 again enters low pressure generator b1 through resolubilization liquid heat exchanger 6; Increase absorber 5 and absorber e1 more respectively to the heated medium heat supply, obtain on the solution series circulation economic benefits and social benefits basis and backheating type double-effect second class absorption heat pump of additional low-temperature heat supply terminal.
Shown in Figure 23, be achieved in that based on solution circulation economic benefits and social benefits in parallel, backheating type double-effect second class absorption heat pump that adds low-temperature heat supply terminal
In backheating type double-effect second class absorption heat pump on the round-robin basis in parallel of solution as shown in Figure 5, increase and increase absorber 5 and resolubilization liquid heat exchanger 6 again, merge into through the second solution pump k1 and the second solution heat exchanger j1 two tunnel through solution pump f1 and solution heat exchanger i1 and low pressure generator b1 at high pressure generator a1 and to draw a solution pipeline between the solution pipeline that is communicated with newly-increased solution heat exchanger 3 after a tunnel and be communicated with through resolubilization liquid heat exchanger 6 and increase absorber 5 again, set up the refrigerant vapour pipeline connection by evaporimeter d1 and increase absorber 5 again, increase absorber 5 again and also have heated medium pipeline and external communications, increase absorber 5 again and also have the weak solution pipeline behind resolubilization liquid heat exchanger 6, to be divided into two-way to be communicated with high pressure generator a1 and low pressure generator b1 respectively; Enter through resolubilization liquid heat exchanger 6 again from the concentrated solution of high pressure generator a1 and low pressure generator b1 and to increase absorber 5, the refrigerant vapour that absorbs flash-pot d1 and heat release again in heated medium, the weak solution that increases absorber 5 again enters high pressure generator a1 and low pressure generator b1 respectively through resolubilization liquid heat exchanger 6; Increase absorber 5 and absorber e1 more respectively to the heated medium heat supply, obtain on the solution circulation economic benefits and social benefits in parallel basis and backheating type double-effect second class absorption heat pump of additional low-temperature heat supply terminal.
Shown in Figure 24, also can realize like this based on backheating type double-effect second class absorption heat pump of solution circulation economic benefits and social benefits in parallel, additional low-temperature heat supply terminal:
In backheating type double-effect second class absorption heat pump on the round-robin basis in parallel of solution as shown in Figure 5, increase and increase absorber 5 again, resolubilization liquid heat exchanger 6 and resolubilization liquid control valve 7, high pressure generator a1 there is the concentrated solution pipeline through solution pump f1, solution heat exchanger i1 and low pressure generator b1 have the concentrated solution pipeline through the second solution pump k1, the newly-increased solution heat exchanger 3 of connection changed high pressure generator a1 into after the second solution heat exchanger j 1 converged has the concentrated solution pipeline through solution pump f1, solution heat exchanger i1 and low pressure generator b1 have the concentrated solution pipeline through the second solution pump k1, the second solution heat exchanger j1 converges after resolubilization liquid heat exchanger 6 is divided into two-way---and one the tunnel is communicated with newly-increased solution heat exchanger 3, another Lu Zaijing resolubilization liquid control valve 7 connections increase absorber 5 again, set up the refrigerant vapour pipeline connection by evaporimeter d1 and increase absorber 5 again, increase absorber 5 again and also have heated medium pipeline and external communications; Increase absorber 5 and absorber e1 more respectively to the heated medium heat supply, obtain on the solution circulation economic benefits and social benefits in parallel basis and backheating type double-effect second class absorption heat pump of additional low-temperature heat supply terminal.
Shown in Figure 25, be achieved in that based on back-heating type triple-effect second class absorption heat pump of solution series circulation three-effect, additional low-temperature heat supply terminal
In back-heating type triple-effect second class absorption heat pump on solution series round-robin basis as shown in Figure 8, increase and increase absorber 5 and resolubilization liquid heat exchanger 6 again, between the concentrated solution pipeline of the newly-increased solution heat exchanger 3 of solution heat exchanger k2 connection, draw a concentrated solution pipeline and increase absorber 5 again through 6 connections of resolubilization liquid heat exchanger, set up the refrigerant vapour pipeline connection by evaporimeter e2 and increase absorber 5 again, increasing absorber 5 more also has the weak solution pipeline to be communicated with high pressure generator a2 and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger 6 respectively; Enter through resolubilization liquid heat exchanger 6 again from the concentrated solution of low pressure generator c2 and to increase absorber 5, the refrigerant vapour that absorbs flash-pot e2 and heat release again in heated medium, the weak solution that increases absorber 5 again enters high pressure generator a2 through resolubilization liquid heat exchanger 6; Increase absorber 5 and absorber e1 more respectively to the heated medium heat supply, obtain on the solution series circulation three-effect basis and back-heating type triple-effect second class absorption heat pump of additional low-temperature heat supply terminal.
Shown in Figure 26, also can realize like this based on back-heating type triple-effect second class absorption heat pump of solution series circulation three-effect, additional low-temperature heat supply terminal:
In back-heating type triple-effect second class absorption heat pump on solution series round-robin basis as shown in Figure 8, increase and increase absorber 5 again, resolubilization liquid heat exchanger 6 and resolubilization liquid control valve 7, low pressure generator c2 there is the concentrated solution pipeline through solution pump g2, the 3rd solution heat exchanger m2, the second solution heat exchanger l2, solution heat exchanger k2, newly-increased solution heat exchanger 3 connection absorber f2 change low pressure generator c2 into has the concentrated solution pipeline through solution pump g2, the 3rd solution heat exchanger m2, the second solution heat exchanger l2, solution heat exchanger k2, be divided into two-way behind the resolubilization liquid heat exchanger 6---the one tunnel is communicated with absorber f2 through newly-increased solution heat exchanger 3 again, another Lu Zaijing resolubilization liquid control valve 7 connections increase absorber 5 again, set up the refrigerant vapour pipeline connection by evaporimeter e2 and increase absorber 5 again, increase absorber 5 again and also have the weak solution pipeline to be communicated with high pressure generator a2 and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger 6; Part in the concentrated solution of resolubilization liquid heat exchanger 6 of flowing through enters through solution control valve 7 and increases absorber 5, the refrigerant vapour that absorbs flash-pot e2 and heat release again in heated medium, and the weak solution that increases absorber 5 again enters high pressure generator a2 through resolubilization liquid heat exchanger 6; Increase absorber 5 and absorber e1 more respectively to the heated medium heat supply, obtain on the solution series circulation three-effect basis and back-heating type triple-effect second class absorption heat pump of additional low-temperature heat supply terminal.
2. in back-heating type triple-effect second class absorption heat pump on the solution series circulation three-effect basis of claim 5, or increase increases absorber and resolubilization liquid heat exchanger again, between the concentrated solution pipeline of the newly-increased solution heat exchanger (3) of solution heat exchanger (k2) connection, draw the concentrated solution pipeline through resolubilization liquid heat exchanger (6) connection increasing again absorber (5), set up the refrigerant vapour pipeline connection by evaporimeter (e2) and increase absorber (5) again, increasing absorber (5) more also has the weak solution pipeline to be communicated with low pressure generator (c2) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (6) respectively; Or increase increases absorber again, resolubilization liquid heat exchanger and resolubilization liquid control valve, high pressure generator (a2) there is the concentrated solution pipeline through solution pump (g2), solution heat exchanger (k2), newly-increased solution heat exchanger (3) connection absorber (f2) changes high pressure generator (a2) into has the concentrated solution pipeline through solution pump (g2), solution heat exchanger (k2), the resolubilization liquid heat exchanger is divided into two-way after (6)---and one the tunnel is communicated with absorber (f2) through newly-increased solution heat exchanger (3) again, another Lu Zaijing resolubilization liquid control valve (7) connection increasing again absorber (5), set up the refrigerant vapour pipeline connection by evaporimeter (e2) and increase absorber (5) again, increasing absorber (5) more also has the weak solution pipeline to be communicated with low pressure generator (c2) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (6) respectively; Increase absorber (5) and absorber (f2) more respectively to the heated medium heat supply, obtain on the solution series circulation three-effect basis and back-heating type triple-effect second class absorption heat pump of additional low-temperature heat supply terminal.
The effect that the technology of the present invention can realize---backheating type double-effect and multi-effect second-class absorption heat pump proposed by the invention have following effect and advantage:
1. thermodynamic property has been enriched the concrete kind of second-kind absorption-type heat pump between between triple effect and the economic benefits and social benefits or between economic benefits and social benefits and the single-action, is conducive to improve the utilization rate of residual heat resources.
2. be the simplest second-kind absorption-type heat pump unit of structure, flow process between triple effect and the economic benefits and social benefits or between economic benefits and social benefits and the single-action, be conducive to reduce equipment manufacturing cost.
3. the backheat flow process can realize further utilizing the waste heat of lower temperature and provide the heat supply of higher temperature to the user, has enlarged the heat supply temperature scope of second-kind absorption-type heat pump.
4. behind the additional low-temperature heat supply terminal, utilize the present invention can further improve energy-saving benefit in the wide occasion of heated medium range of temperature.
In a word, backheating type double-effect provided by the invention and triple-effect second-kind absorption-type heat pump have further been realized the diversity of unit kind; Have the simplest structure and flow process, improved the unit heat capacity, and had relatively high performance index, can satisfy better user's heat demand, have good creativeness, novelty and practicality.

Claims (10)

1. one of backheating type double-effect second class absorption heat pump on the solution series circulation economic benefits and social benefits basis, be by high pressure generator, low pressure generator, condenser, evaporimeter, absorber, solution pump, the cryogen liquid pump, choke valve, in solution series circulation economic benefits and social benefits second class absorption heat pump that the solution heat exchanger and second solution heat exchanger are formed, or newly-increased choke valve of increase or newly-increased cryogen liquid pump, newly-increased absorption-evaporimeter and newly-increased solution heat exchanger have the concentrated solution pipeline through solution pump (f1) with low pressure generator (b1), second solution heat exchanger (j1) is communicated with absorber (e1) with solution heat exchanger (i1), absorber (e1) has the weak solution pipeline to change low pressure generator (b1) into through solution heat exchanger (i1) connection high pressure generator (a1) again and the concentrated solution pipeline is arranged through solution pump (f1), second solution heat exchanger (j1), solution heat exchanger (i1) is communicated with absorber (e1) with newly-increased solution heat exchanger (3), absorber (e1) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with high pressure generator (a1) through solution heat exchanger (i1) more again; Or newly-increased choke valve of increase or newly-increased cryogen liquid pump, newly-increased absorption-evaporimeter, newly-increased solution heat exchanger and newly-increased solution pump have the concentrated solution pipeline through solution pump (f1) with low pressure generator (b1), second solution heat exchanger (j1) connection solution heat exchanger (i1) changes low pressure generator (b1) into has the concentrated solution pipeline through solution pump (f1), second solution heat exchanger (j1) is communicated with solution heat exchanger (i1) and has the concentrated solution pipeline to change high pressure generator (a1) into through second solution heat exchanger (j1) connection low pressure generator (b1) high pressure generator (a1) with newly-increased solution heat exchanger (3) have the concentrated solution pipeline through newly-increased solution heat exchanger (3), newly-increased solution pump (5) is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back has the weak solution pipeline to be communicated with low pressure generator (b1) through second solution heat exchanger (j1) again; Or set up the cryogen liquid pipeline by evaporimeter (d1) and be communicated with the newly-increased absorptions-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back through newly-increased cryogen liquid pump (4) refrigerant vapour pipeline connection absorber (e1) is arranged again, or have the cryogen liquid pipeline to be communicated with evaporimeter (d1) condenser (c1) to change condenser (c1) into and have the cryogen liquid pipeline behind cryogen liquid pump (g1), to be divided into two-way through cryogen liquid pump (g1)---the one tunnel again warp increase choke valve (2) connection evaporimeter (d1) newly, another road directly is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back refrigerant vapour pipeline connection absorber (e1) again; Set up the newly-increased absorption-evaporimeter (1) of refrigerant vapour pipeline connection by evaporimeter (d1); Absorber (e1) or high pressure generator (a1) provide solution to newly-increased absorption-evaporimeter (1), evaporimeter (d1) provides refrigerant vapour to newly-increased absorption-evaporimeter (1), newly-increased absorption-evaporimeter (1) heating becomes refrigerant vapour to provide to absorber (e1) from the cryogen liquid of condenser (c1) or evaporimeter (d1), obtains backheating type double-effect second class absorption heat pump on the solution series circulation economic benefits and social benefits basis.
2. two of backheating type double-effect second class absorption heat pump on the solution series circulation economic benefits and social benefits basis, be in solution series circulation economic benefits and social benefits second class absorption heat pump of forming by high pressure generator, low pressure generator, condenser, evaporimeter, absorber, solution pump, cryogen liquid pump, choke valve, solution heat exchanger and second solution pump, increase newly-increased choke valve or newly-increased cryogen liquid pump, newly-increased absorption-evaporimeter and newly-increased solution heat exchanger; Or there is the concentrated solution pipeline to be communicated with absorber (e1) with solution heat exchanger (i1) high pressure generator (a1) through solution pump (f1), absorber (e1) has the weak solution pipeline to change high pressure generator (a1) into through solution heat exchanger (i1) connection low pressure generator (b1) again and the concentrated solution pipeline is arranged through solution pump (f1), solution heat exchanger (i1) is communicated with absorber (e1) with newly-increased solution heat exchanger (3), absorber (e1) has the weak solution pipeline to be communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back through newly-increased solution heat exchanger (3) again and the weak solution pipeline is arranged through solution heat exchanger (i1) connection low pressure generator (b1) again, or has the concentrated solution pipeline to change low pressure generator (b1) into through second solution pump (k1) connection high pressure generator (a1) low pressure generator (b1) the concentrated solution pipeline to be arranged through second solution pump (k1), newly-increased solution heat exchanger (3) is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back has the weak solution pipeline to be communicated with high pressure generator (a1) through newly-increased solution heat exchanger (3) again; Or set up the cryogen liquid pipeline by evaporimeter (d1) and be communicated with the newly-increased absorptions-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back through newly-increased cryogen liquid pump (4) refrigerant vapour pipeline connection absorber (e1) is arranged again, or have the cryogen liquid pipeline to be communicated with evaporimeter (d1) condenser (c1) to change condenser (c1) into and have the cryogen liquid pipeline behind cryogen liquid pump (g1), to be divided into two-way through cryogen liquid pump (g1)---the one tunnel again warp increase choke valve (2) connection evaporimeter (d1) newly, another road directly is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back refrigerant vapour pipeline connection absorber (e1) again; Set up the newly-increased absorption-evaporimeter (1) of refrigerant vapour pipeline connection by evaporimeter (d1); Absorber (e1) or low pressure generator (b1) provide solution to newly-increased absorption-evaporimeter (1), evaporimeter (d1) provides refrigerant vapour to newly-increased absorption-evaporimeter (1), newly-increased absorption-evaporimeter (1) heating becomes refrigerant vapour to provide to absorber (e1) from the cryogen liquid of condenser (c1) or evaporimeter (d1), obtains backheating type double-effect second class absorption heat pump on the solution series circulation economic benefits and social benefits basis.
3. backheating type double-effect second class absorption heat pump on the solution circulation economic benefits and social benefits in parallel basis, be in the solution of forming by high pressure generator, low pressure generator, condenser, evaporimeter, absorber, solution pump, second solution pump, cryogen liquid pump, choke valve, solution heat exchanger and second solution heat exchanger circulation economic benefits and social benefits in parallel second class absorption heat pump, increase newly-increased choke valve or newly-increased cryogen liquid pump, newly-increased absorption-evaporimeter and newly-increased solution heat exchanger; Or there is the concentrated solution pipeline to have the concentrated solution pipeline to be communicated with absorber (e1) respectively with second solution heat exchanger (j1) high pressure generator (a1) through second solution pump (k1) through solution pump (f1) and solution heat exchanger (i1) and low pressure generator (b1), absorber (e1) have again the weak solution pipeline respectively through solution heat exchanger (i1) be communicated with high pressure generator (a1) and through second solution heat exchanger (j1) be communicated with low pressure generator (b1) change into high pressure generator (a1) have the concentrated solution pipeline through solution pump (f1) and solution heat exchanger (i1) and low pressure generator (b1) have the concentrated solution pipeline through second solution pump (k1) with after second solution heat exchanger (j1) two tunnel merges into one the tunnel jointly again warp increase solution heat exchanger (3) newly and be communicated with absorber (e1), absorber (e1) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with high pressure generator (a1) and to be communicated with low pressure generator (b1) through second solution heat exchanger (j1) through solution heat exchanger (i1) respectively more again, or there is the concentrated solution pipeline to be communicated with absorber (e1) with second solution heat exchanger (j1) low pressure generator (b1) through second solution pump (k1), absorber (e1) has the weak solution pipeline to change low pressure generator (b1) into through second solution heat exchanger (j1) connection low pressure generator (b1) again and the concentrated solution pipeline is arranged through second solution pump (k1), second solution heat exchanger (j1) is communicated with absorber (e1) with newly-increased solution heat exchanger (3), absorber (e1) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with low pressure generator (b1) through second solution heat exchanger (j1) again, or has the concentrated solution pipeline to be communicated with absorber (e1) through solution pump (f1) with solution heat exchanger (i1) high pressure generator (a1), absorber (e1) has the weak solution pipeline to change high pressure generator (a1) into through solution heat exchanger (i1) connection high pressure generator (a1) again and the concentrated solution pipeline is arranged through solution pump (f1), solution heat exchanger (i1) is communicated with absorber (e1) with newly-increased solution heat exchanger (3), absorber (e1) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with high pressure generator (a1) through solution heat exchanger (i1) more again; Or set up the cryogen liquid pipeline by evaporimeter (d1) and be communicated with the newly-increased absorptions-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back through newly-increased cryogen liquid pump (4) refrigerant vapour pipeline connection absorber (e1) is arranged again, or have the cryogen liquid pipeline to be communicated with evaporimeter (d1) condenser (c1) to change condenser (c1) into and have the cryogen liquid pipeline behind cryogen liquid pump (g1), to be divided into two-way through cryogen liquid pump (g1)---the one tunnel again warp increase choke valve (2) connection evaporimeter (d1) newly, another road directly is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back refrigerant vapour pipeline connection absorber (e1) again; Evaporimeter (d1) is also set up the newly-increased absorption-evaporimeter (1) of refrigerant vapour pipeline connection; Absorber (e1) provides solution to newly-increased absorption-evaporimeter (1), evaporimeter (d1) provides refrigerant vapour to newly-increased absorption-evaporimeter (1), newly-increased absorption-evaporimeter (1) heating becomes refrigerant vapour to provide to absorber (e1) from the cryogen liquid of condenser (c1) or evaporimeter (d1), obtains backheating type double-effect second class absorption heat pump on the solution circulation economic benefits and social benefits in parallel basis.
4. one of back-heating type triple-effect second class absorption heat pump on the solution series circulation three-effect basis, be by high pressure generator, the middle generator of pressing, low pressure generator, condenser, evaporimeter, absorber, solution pump, the cryogen liquid pump, choke valve, second choke valve, solution heat exchanger, in solution series circulation three-effect second class absorption heat pump that second solution heat exchanger and the 3rd solution heat exchanger are formed, or newly-increased choke valve of increase or newly-increased cryogen liquid pump, newly-increased absorption-evaporimeter and newly-increased solution heat exchanger have the concentrated solution pipeline through solution pump (g2) with low pressure generator (c2), the 3rd solution heat exchanger (m2), second solution heat exchanger (l2) is communicated with absorber (f2) with solution heat exchanger (k2), absorber (f2) has the weak solution pipeline to change low pressure generator (c2) into through solution heat exchanger (k2) connection high pressure generator (a2) again and the concentrated solution pipeline is arranged through solution pump (g2), the 3rd solution heat exchanger (m2), second solution heat exchanger (l2), solution heat exchanger (k2) is communicated with absorber (f2) with newly-increased solution heat exchanger (3), absorber (f2) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with high pressure generator (a2) through solution heat exchanger (k2) more again; Or newly-increased choke valve of increase or newly-increased cryogen liquid pump, newly-increased absorption-evaporimeter, newly-increased solution heat exchanger and newly-increased solution pump, or low pressure generator (c2) there is the concentrated solution pipeline through solution pump (g2), the 3rd solution heat exchanger (m2), being communicated with solution heat exchanger (k2) behind second solution heat exchanger (l2) again changes low pressure generator (c2) into and the concentrated solution pipeline is arranged through solution pump (g2), the 3rd solution heat exchanger (m2), second solution heat exchanger (l2), be communicated with solution heat exchanger (k2) again behind the newly-increased solution heat exchanger (3) and simultaneously high pressure generator (a2) had the concentrated solution pipeline in second solution heat exchanger (l2) is communicated with, to press generator (b2) to change high pressure generator (a2) into and the concentrated solution pipeline is arranged through newly-increased solution heat exchanger (3), newly-increased solution pump (5) is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back has the weak solution pipeline to press generator (b2) again in second solution heat exchanger (l2) is communicated with, or low pressure generator (c2) is had the concentrated solution pipeline through solution pump (g2), being communicated with second solution heat exchanger (l2) behind the 3rd solution heat exchanger (m2) again changes low pressure generator (c2) into and the concentrated solution pipeline is arranged through solution pump (g2), the 3rd solution heat exchanger (m2), be communicated with second solution heat exchanger (l2) again behind the newly-increased solution heat exchanger (3) and simultaneously middle pressure generator (b2) had the concentrated solution pipeline in the 3rd solution heat exchanger (m2) connection low pressure generator (c2) changes into, to press generator (b2) the concentrated solution pipeline to be arranged through newly-increased solution heat exchanger (3), newly-increased solution pump (5) is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back has the weak solution pipeline to be communicated with low pressure generator (c2) through the 3rd solution heat exchanger (m2) again; Or set up the cryogen liquid pipeline by evaporimeter (e2) and be communicated with the newly-increased absorptions-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back through newly-increased cryogen liquid pump (4) refrigerant vapour pipeline connection absorber (f2) is arranged again, or have the cryogen liquid pipeline to be communicated with evaporimeter (e2) condenser (d2) to change condenser (d2) into and have the cryogen liquid pipeline behind cryogen liquid pump (h2), to be divided into two-way through cryogen liquid pump (h2)---the one tunnel again warp increase choke valve (2) connection evaporimeter (e2) newly, another road directly is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back refrigerant vapour pipeline connection absorber (f2) again; Evaporimeter (e2) is also set up the newly-increased absorption-evaporimeter (1) of refrigerant vapour pipeline connection; Absorber (f2) or high pressure generator (a2) or middle pressure generator (b2) provide solution to newly-increased absorption-evaporimeter (1), evaporimeter (e2) provides refrigerant vapour to newly-increased absorption-evaporimeter (1), newly-increased absorption-evaporimeter (1) heating becomes refrigerant vapour to provide to absorber (f2) from the cryogen liquid of condenser (d2) or evaporimeter (e2), obtains back-heating type triple-effect second class absorption heat pump on the solution series circulation three-effect basis.
5. two of back-heating type triple-effect second class absorption heat pump on the solution series circulation three-effect basis, be in solution series circulation three-effect second class absorption heat pump of forming by high pressure generator, middle pressure generator, low pressure generator, condenser, evaporimeter, absorber, solution pump, second solution pump, the 3rd solution pump, cryogen liquid pump, choke valve, second choke valve and solution heat exchanger, increase newly-increased choke valve or newly-increased cryogen liquid pump, newly-increased absorption-evaporimeter and newly-increased solution heat exchanger; Or high pressure generator (a2) there is the concentrated solution pipeline through solution pump (g2), solution heat exchanger (k2) is communicated with absorber (f2), absorber (f2) has the weak solution pipeline to change high pressure generator (a2) into through solution heat exchanger (k2) connection low pressure generator (c2) again and the concentrated solution pipeline is arranged through solution pump (g2), solution heat exchanger (k2) is communicated with absorber (f2) with newly-increased solution heat exchanger (3), absorber (f2) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with low pressure generator (c2) through solution heat exchanger (k2) more again, or have the concentrated solution pipeline in the 3rd solution pump (o2) is communicated with, to press generator (b2) to change low pressure generator (c2) into low pressure generator (c2) the concentrated solution pipeline to be arranged through the 3rd solution pump (o2), newly-increased absorption-evaporimeter (1) had the weak solution pipeline to press generator (b2) again in newly-increased solution heat exchanger (3) is communicated with after newly-increased solution heat exchanger (3) was communicated with newly-increased absorption-evaporimeter (1), or had the concentrated solution pipeline to press generator (b2) the concentrated solution pipeline to be arranged through second solution pump (n2) in second solution pump (n2) connection high pressure generator (a2) changes in middle pressure generator (b2), newly-increased solution heat exchanger (3) is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back has the weak solution pipeline to be communicated with high pressure generator (a2) through newly-increased solution heat exchanger (3) again; Or set up the cryogen liquid pipeline by evaporimeter (e2) and be communicated with the newly-increased absorptions-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back through newly-increased cryogen liquid pump (4) refrigerant vapour pipeline connection absorber (f2) is arranged again, or have the cryogen liquid pipeline to be communicated with evaporimeter (e2) condenser (d2) to change condenser (d2) into and have the cryogen liquid pipeline behind cryogen liquid pump (h2), to be divided into two-way through cryogen liquid pump (h2)---the one tunnel again warp increase choke valve (2) connection evaporimeter (e2) newly, another road directly is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back refrigerant vapour pipeline connection absorber (f2) again; Evaporimeter (e2) is also set up the newly-increased absorption-evaporimeter (1) of refrigerant vapour pipeline connection; Absorber (f2) or low pressure generator (c2) or middle pressure generator (b2) provide solution to newly-increased absorption-evaporimeter (1), evaporimeter (e2) provides refrigerant vapour to newly-increased absorption-evaporimeter (1), newly-increased absorption-evaporimeter (1) heating becomes refrigerant vapour to provide to absorber (f2) from the cryogen liquid of condenser (d2) or evaporimeter (e2), obtains back-heating type triple-effect second class absorption heat pump on the solution series circulation three-effect basis.
6. back-heating type triple-effect second class absorption heat pump on the solution circulation three-effect in parallel basis, be in the solution of forming by high pressure generator, middle pressure generator, low pressure generator, condenser, evaporimeter, absorber, solution pump, second solution pump, the 3rd solution pump, cryogen liquid pump, choke valve, second choke valve, solution heat exchanger, second solution heat exchanger and the 3rd solution heat exchanger circulation three-effect second class absorption heat pump in parallel, increase newly-increased choke valve or newly-increased cryogen liquid pump, newly-increased absorption-evaporimeter and newly-increased solution heat exchanger;
Or high pressure generator (a2) there is the concentrated solution pipeline through solution pump (g2) and solution heat exchanger (k2), the middle generator (b2) of pressing has the concentrated solution pipeline to have the concentrated solution pipeline to be communicated with absorber (f2) through the 3rd solution pump (o2) respectively with the 3rd solution heat exchanger (m2) through second solution pump (n2) and second solution heat exchanger (l2) and low pressure generator (c2), absorber (f2) has the weak solution pipeline to be communicated with high pressure generator (a2) through solution heat exchanger (k2) respectively again, in second solution heat exchanger (l2) is communicated with, press generator (b2) and change high pressure generator (a2) into and the concentrated solution pipeline is arranged through solution pump (g2) and solution heat exchanger (k2) through the 3rd solution heat exchanger (m2) connection low pressure generator (c2), in press generator (b2) have the concentrated solution pipeline through second solution pump (n2) and second solution heat exchanger (l2) and low pressure generator (c2) have the concentrated solution pipeline through the 3rd solution pump (o2) with after the 3rd solution heat exchanger (m2) three tunnel merges into one the tunnel jointly again warp increase solution heat exchanger (3) newly and be communicated with absorber (f2), absorber (f2) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with high pressure generator (a1) through solution heat exchanger (k2) respectively more again, in second solution heat exchanger (l2) is communicated with, press generator (b2) and be communicated with low pressure generator (c2) through the 3rd solution heat exchanger (m2)
Or high pressure generator (a2) there is the concentrated solution pipeline through solution pump (g2) and solution heat exchanger (k2), the middle generator (b2) of pressing has the concentrated solution pipeline to have the concentrated solution pipeline to be communicated with absorber (f2) through the 3rd solution pump (o2) respectively with the 3rd solution heat exchanger (m2) through second solution pump (n2) and second solution heat exchanger (l2) and low pressure generator (c2), absorber (f2) has the weak solution pipeline to be communicated with high pressure generator (a2) through solution heat exchanger (k2) respectively again, in second solution heat exchanger (l2) is communicated with, press generator (b2) and change high pressure generator (a2) into and the concentrated solution pipeline is arranged through solution pump (g2) and solution heat exchanger (k2) through the 3rd solution heat exchanger (m2) connection low pressure generator (c2), in press generator (b2) have the concentrated solution pipeline through second solution pump (n2) and second solution heat exchanger (l2) and low pressure generator (c2) have the concentrated solution pipeline through the 3rd solution pump (o2) with after the 3rd solution heat exchanger (m2) three tunnel merges into one the tunnel jointly again warp increase solution heat exchanger (3) newly and be communicated with absorber (f2), absorber (f2) has the weak solution pipeline to be divided into two-way again behind newly-increased solution heat exchanger (3)---and one the tunnel through solution heat exchanger (k2) connection high pressure generator (a1), another road is communicated with the newly-increased absorptions-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back has the weak solution pipeline to press generator (b2) respectively and through the 3rd solution heat exchanger (m2) connection low pressure generator (c2) in second solution heat exchanger (l2) connection again
( b2 ) ( n2 ) ( l2 ) ( c2 ) ( o2 ) ( m2 ) ( f2 ) 、 ( f2 ) ( l2 ) ( b2 ) ( m2 ) ( c2 ) ( b2 ) ( n2 ) ( l2 ) ( c2 ) ( o2 ) ( m2 ) ( 3 ) ( f2 ) 、 ( f2 ) ( 3 ) - ( 1 ) - ( 1 ) ( l2 ) ( b2 ) ( m2 ) ( c2 )
Or there is the concentrated solution pipeline to be communicated with absorber (f2) with the 3rd solution heat exchanger (m2) low pressure generator (c2) through the 3rd solution pump (o2), absorber (f2) has the weak solution pipeline to change low pressure generator (c2) into through the 3rd solution heat exchanger (m2) connection low pressure generator (c2) again and the concentrated solution pipeline is arranged through the 3rd solution pump (o2), the 3rd solution heat exchanger (m2) is communicated with absorber (f2) with newly-increased solution heat exchanger (3), absorber (f2) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with low pressure generator (c2) through the 3rd solution heat exchanger (m2) more again
Or there is the concentrated solution pipeline to be communicated with absorber (f2) with second solution heat exchanger (l2) the middle pressure generator (b2) through second solution pump (n2), absorber (f2) has the weak solution pipeline to press generator (b2) to change the middle generator (b2) of pressing in second solution heat exchanger (l2) is communicated with again and the concentrated solution pipeline is arranged through second solution pump (n2), second solution heat exchanger (l2) is communicated with absorber (f2) with newly-increased solution heat exchanger (3), absorber (f2) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to press generator (b2) again in second solution heat exchanger (l2) is communicated with again
Or there is the concentrated solution pipeline to be communicated with absorber (f2) with solution heat exchanger (k2) high pressure generator (a2) through solution pump (g2), absorber (f2) has the weak solution pipeline to change high pressure generator (a2) into through solution heat exchanger (k2) connection high pressure generator (a2) respectively again and the concentrated solution pipeline is arranged through solution pump (g2), solution heat exchanger (k2) is communicated with absorber (f2) with newly-increased solution heat exchanger (3), absorber (f2) has weak solution pipeline newly-increased absorption-evaporimeter (1) after newly-increased solution heat exchanger (3) is communicated with newly-increased absorption-evaporimeter (1) to have the weak solution pipeline to be communicated with high pressure generator (a2) through solution heat exchanger (k2) more again;
Or set up the cryogen liquid pipeline by evaporimeter (e2) and be communicated with the newly-increased absorptions-evaporimeter (1) in newly-increased absorptions-evaporimeter (1) back through newly-increased cryogen liquid pump (4) refrigerant vapour pipeline connection absorber (f2) is arranged again, or have the cryogen liquid pipeline to be communicated with evaporimeter (e2) condenser (d2) to change condenser (d2) into and have the cryogen liquid pipeline behind cryogen liquid pump (h2), to be divided into two-way through cryogen liquid pump (h2)---the one tunnel again warp increase choke valve (2) connection evaporimeter (e2) newly, another road directly is communicated with the newly-increased absorption-evaporimeter (1) in newly-increased absorption-evaporimeter (1) back refrigerant vapour pipeline connection absorber (f2) again; Evaporimeter (e2) is also set up the newly-increased absorption-evaporimeter (1) of refrigerant vapour pipeline connection; Absorber (f2) provides solution to newly-increased absorption-evaporimeter (1), evaporimeter (e2) provides refrigerant vapour to newly-increased absorption-evaporimeter (1), newly-increased absorption-evaporimeter (1) heating becomes refrigerant vapour to provide to absorber (f2) from the cryogen liquid of condenser (d2) or evaporimeter (e2), obtains back-heating type triple-effect second class absorption heat pump on the solution circulation three-effect in parallel basis.
7. on the solution series circulation economic benefits and social benefits basis and backheating type double-effect second class absorption heat pump of additional low-temperature heat supply terminal, be in backheating type double-effect second class absorption heat pump on claim 1 or the described solution series circulation of the claim 2 economic benefits and social benefits basis, or increase increases absorber and resolubilization liquid heat exchanger again, or increase increases absorber again, resolubilization liquid heat exchanger and resolubilization liquid control valve, obtain comprising backheating type double-effect second class absorption heat pump of economic benefits and social benefits low-temperature heat supply terminal---1. in backheating type double-effect second class absorption heat pump on the solution series circulation economic benefits and social benefits basis of claim 1, or increase increases absorber and resolubilization liquid heat exchanger again, drawing a concentrated solution pipeline between solution heat exchanger (i1) and concentrated solution pipeline that newly-increased solution heat exchanger (3) is connected is communicated with through resolubilization liquid heat exchanger (7) and increases absorber (6) again, set up the refrigerant vapour pipeline connection by evaporimeter (d1) and increase absorber (6) again, increasing absorber (6) more also has the weak solution pipeline to be communicated with high pressure generator (a1) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (7) respectively; Or increase increases absorber again, resolubilization liquid heat exchanger and resolubilization liquid control valve, between solution heat exchanger (i1) and concentrated solution pipeline that newly-increased solution heat exchanger (3) is connected, increase resolubilization liquid heat exchanger 7, low pressure generator (b1) there is the concentrated solution pipeline through solution pump (f1), second solution heat exchanger (j1), solution heat exchanger (i1), newly-increased solution heat exchanger (3) connection absorber (e1) changes low pressure generator (b1) into has the concentrated solution pipeline through solution pump (f1), second solution heat exchanger (j1), solution heat exchanger (i1), the resolubilization liquid heat exchanger is divided into two-way after (7)---and one the tunnel is communicated with absorber (e1) through newly-increased solution heat exchanger (3) again, another Lu Zaijing resolubilization liquid control valve (8) connection increasing again absorber (6), set up the refrigerant vapour pipeline connection by evaporimeter (d1) and increase absorber (6) again, increase absorber (6) again and also have the weak solution pipeline to be communicated with high pressure generator (a1) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (7); Increase absorber (6) and absorber (e1) more respectively to the heated medium heat supply, obtain on the solution series circulation economic benefits and social benefits basis and backheating type double-effect second class absorption heat pump of additional low-temperature heat supply terminal; 2. in backheating type double-effect second class absorption heat pump on the solution series circulation economic benefits and social benefits basis of claim 2, or increase increases absorber and resolubilization liquid heat exchanger again, drawing a concentrated solution pipeline between solution heat exchanger (i1) and concentrated solution pipeline that newly-increased solution heat exchanger (3) links to each other is communicated with through resolubilization liquid heat exchanger (7) and increases absorber (6) again, set up the refrigerant vapour pipeline connection by evaporimeter (d1) and increase absorber (6) again, increasing absorber (6) more also has the weak solution pipeline to be communicated with low pressure generator (b1) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (7) respectively; Or increase increases absorber again, resolubilization liquid heat exchanger and resolubilization liquid control valve, high pressure generator (a1) there is the concentrated solution pipeline through solution pump (f1), solution heat exchanger (i1), newly-increased solution heat exchanger (3) connection absorber (e1) changes high pressure generator (a1) into has the concentrated solution pipeline through solution pump (f1), solution heat exchanger (i1), the resolubilization liquid heat exchanger is divided into two-way after (7)---and one the tunnel is communicated with absorber (e1) through newly-increased solution heat exchanger (3) again, another Lu Zaijing resolubilization liquid control valve (8) connection increasing again absorber (6), set up the refrigerant vapour pipeline connection by evaporimeter (d1) and increase absorber (6) again, increasing absorber (6) more also has the weak solution pipeline to be communicated with low pressure generator (b1) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (7) respectively; Increase absorber (6) and absorber (e1) more respectively to the heated medium heat supply, obtain on the solution series circulation economic benefits and social benefits basis and backheating type double-effect second class absorption heat pump of additional low-temperature heat supply terminal.
On the solution circulation economic benefits and social benefits in parallel basis and additional low-temperature heat supply terminal backheating type double-effect second class absorption heat pump, be in backheating type double-effect second class absorption heat pump on described solution circulation economic benefits and social benefits in parallel basis with claim 3, or increase increases absorber and resolubilization liquid heat exchanger again, merge into through second solution pump (k1) and second solution heat exchanger (j1) two tunnel through solution pump (f1) and solution heat exchanger (i1) and low pressure generator (b1) at high pressure generator (a1) and to draw a solution pipeline between the solution pipeline that is communicated with newly-increased solution heat exchanger (3) after a tunnel and be communicated with through resolubilization liquid heat exchanger (7) and increase absorber (6) again, increase absorber (6) again and also have the weak solution pipeline behind resolubilization liquid heat exchanger (7), to be communicated with high pressure generator (a1) and low pressure generator (b1) respectively; Or increase increases absorber again, resolubilization liquid heat exchanger and resolubilization liquid control valve have the concentrated solution pipeline through solution pump (f1) with high pressure generator (a1), solution heat exchanger (i1) and low pressure generator (b1) have the concentrated solution pipeline through second solution pump (k1), second solution heat exchanger (j1) converges the newly-increased solution heat exchanger (3) of back connection and changes high pressure generator (a1) concentrated solution pipeline into through solution pump (f1), solution heat exchanger (i1) and low pressure generator (b1) concentrated solution pipeline are through second solution pump (k1), second solution heat exchanger (j1) converges after resolubilization liquid heat exchanger (7) is divided into two-way---and one the tunnel is communicated with newly-increased solution heat exchanger (3), another Lu Zaijing resolubilization liquid control valve (8) connection increasing again absorber (6); Set up the refrigerant vapour pipeline connection by evaporimeter (d1) and increase absorber (6) again, increase absorber (6) again and also have heated medium pipeline and external communications; Increase absorber (6) and absorber (e1) more respectively to the heated medium heat supply, obtain on the solution circulation economic benefits and social benefits in parallel basis and backheating type double-effect second class absorption heat pump of additional low-temperature heat supply terminal.
9. on the solution series circulation three-effect basis and back-heating type triple-effect second class absorption heat pump of additional low-temperature heat supply terminal, be in back-heating type triple-effect second class absorption heat pump on claim 4 or the described solution series circulation three-effect of claim 5 basis, or increase increases absorber and resolubilization liquid heat exchanger again, or increase increases absorber again, resolubilization liquid heat exchanger and resolubilization liquid control valve, obtain comprising back-heating type triple-effect second class absorption heat pump of triple effect low-temperature heat supply terminal---1. in backheating type double-effect second class absorption heat pump on the solution series circulation three-effect basis of claim 4, or increase increases absorber and resolubilization liquid heat exchanger again, at solution heat exchanger (k2) and be communicated with and draw a concentrated solution pipeline between the concentrated solution pipeline that newly-increased solution heat exchanger (3) is connected and be communicated with through resolubilization liquid heat exchanger (7) and increase absorber (6) again, set up the refrigerant vapour pipeline connection by evaporimeter (e2) and increase absorber (6) again, increasing absorber (6) more also has the weak solution pipeline to be communicated with high pressure generator (a2) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (7) respectively; Or increase increases absorber again, resolubilization liquid heat exchanger and resolubilization liquid control valve, low pressure generator (c2) there is the concentrated solution pipeline through solution pump (g2), the 3rd solution heat exchanger (m2), second solution heat exchanger (l2), solution heat exchanger (k2) be communicated with absorber (f2) through newly-increased solution heat exchanger (3) again and change low pressure generator (c2) into and the concentrated solution pipeline is arranged through solution pump (g2), the 3rd solution heat exchanger (m2), second solution heat exchanger (l2), behind resolubilization liquid heat exchanger (7), be divided into two-way again behind the solution heat exchanger (k2)---the one tunnel through newly-increased solution heat exchanger (3) connection absorber (f2), another road is through resolubilization liquid control valve (8) connection increasing again absorber (6), set up the refrigerant vapour pipeline connection by evaporimeter (e2) and increase absorber (6) again, increase absorber (6) again and also have the weak solution pipeline to be communicated with high pressure generator (a2) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (7); Increase absorber (6) and absorber (f2) more respectively to the heated medium heat supply, obtain on the solution series circulation three-effect basis and back-heating type triple-effect second class absorption heat pump of additional low-temperature heat supply terminal; 2. in back-heating type triple-effect second class absorption heat pump on the solution series circulation three-effect basis of claim 5, or increase increases absorber and resolubilization liquid heat exchanger again, drawing the concentrated solution pipeline between solution heat exchanger (k2) and concentrated solution pipeline that newly-increased solution heat exchanger (3) is connected is communicated with through resolubilization liquid heat exchanger (7) and increases absorber (6) again, set up the refrigerant vapour pipeline connection by evaporimeter (e2) and increase absorber (6) again, increasing absorber (6) more also has the weak solution pipeline to be communicated with low pressure generator (c2) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (7) respectively; Or increase increases absorber again, resolubilization liquid heat exchanger and resolubilization liquid control valve, high pressure generator (a2) there is the concentrated solution pipeline through solution pump (g2), solution heat exchanger (k2) is communicated with absorber (f2) and changes high pressure generator (a2) into and the concentrated solution pipeline is arranged through solution pump (g2) with newly-increased solution heat exchanger (3), be divided into two-way behind solution heat exchanger (k2) the back resolubilization liquid heat exchanger (7)---the one tunnel through newly-increased solution heat exchanger (3) connection absorber (f2), another road is through resolubilization liquid control valve (8) connection increasing again absorber (6), set up the refrigerant vapour pipeline connection by evaporimeter (e2) and increase absorber (6) again, increasing absorber (6) more also has the weak solution pipeline to be communicated with low pressure generator (c2) and heated medium pipeline and external communications are arranged through resolubilization liquid heat exchanger (7) respectively; Increase absorber (6) and absorber (f2) more respectively to the heated medium heat supply, obtain on the solution series circulation three-effect basis and back-heating type triple-effect second class absorption heat pump of additional low-temperature heat supply terminal.
10. on the solution circulation three-effect in parallel basis and back-heating type triple-effect second class absorption heat pump of additional low-temperature heat supply terminal, be in back-heating type triple-effect second class absorption heat pump on described solution circulation three-effect in parallel basis with claim 6, or increase increases absorber and resolubilization liquid heat exchanger again, at high pressure generator (a2) through solution pump (g2) and solution heat exchanger (k2), in press generator (b2) through second solution pump (n2) and second solution heat exchanger (l2) and low pressure generator (c2) through the 3rd solution pump (o2) with draw a solution pipeline and increase absorber (6) again after the 3rd solution heat exchanger (m2) converges with between solution pipeline that newly-increased solution heat exchanger (3) is connected through resolubilization liquid heat exchanger (7) connection, increase again absorber (6) in addition the weak solution pipeline behind resolubilization liquid heat exchanger (7), be communicated with high pressure generator (a2) respectively, middle generator (b2) and the low pressure generator (c2) of pressing; Or increase increases absorber again, resolubilization liquid heat exchanger and resolubilization liquid control valve, with high pressure generator (a2) through solution pump (g2) and solution heat exchanger (k2), in press generator (b2) to increase solution heat exchanger (3) newly and change high pressure generator (a2) into being communicated with again after the 3rd solution heat exchanger (m2) converges through the 3rd solution pump (o2) through solution pump (g2) and solution heat exchanger (k2) through second solution pump (n2) and second solution heat exchanger (l2) and low pressure generator (c2), the middle generator (b2) of pressing converges with the 3rd solution heat exchanger (m2) after resolubilization liquid heat exchanger (7) is divided into two-way through the 3rd solution pump (o2) with second solution heat exchanger (l2) and low pressure generator (c2) through second solution pump (n2)---and one the tunnel is communicated with newly-increased solution heat exchanger (3), another Lu Zaijing resolubilization liquid control valve (8) connection increasing again absorber (6); Set up the refrigerant vapour pipeline connection by evaporimeter (e2) and increase absorber (6) again, increase absorber (6) again and also have heated medium pipeline and external communications; Increase absorber (6) and absorber (f2) more respectively to the heated medium heat supply, obtain on the solution circulation three-effect in parallel basis and back-heating type triple-effect second class absorption heat pump of additional low-temperature heat supply terminal.
CN200910019105A 2009-09-19 2009-09-19 Backheating type double-effect and multi-effect second-class absorption heat pump Pending CN101825370A (en)

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CN102607209A (en) * 2012-02-27 2012-07-25 李华玉 Third type absorption heat pump with afterheat double-effect driving function
WO2012145859A1 (en) * 2011-04-25 2012-11-01 Li Huayu Recuperative double-effect and triple-effect second-type absorption heat pump
CN103175331A (en) * 2013-03-13 2013-06-26 李华玉 Second kind absorption heat pump circulating through shunt circuits

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JP4521855B2 (en) * 2003-05-14 2010-08-11 荏原冷熱システム株式会社 Absorption refrigerator
JP4287705B2 (en) * 2003-06-18 2009-07-01 東京瓦斯株式会社 Single double effect absorption refrigerator and operation control method thereof
JP2005155975A (en) * 2003-11-21 2005-06-16 Sanyo Electric Co Ltd Absorption refrigerating machine
JP4260095B2 (en) * 2004-10-25 2009-04-30 三洋電機株式会社 Single double effect absorption refrigerator

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WO2012145859A1 (en) * 2011-04-25 2012-11-01 Li Huayu Recuperative double-effect and triple-effect second-type absorption heat pump
CN102607209A (en) * 2012-02-27 2012-07-25 李华玉 Third type absorption heat pump with afterheat double-effect driving function
CN102607209B (en) * 2012-02-27 2014-07-30 李华玉 Third type absorption heat pump with afterheat double-effect driving function
CN103175331A (en) * 2013-03-13 2013-06-26 李华玉 Second kind absorption heat pump circulating through shunt circuits

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