CN102242982B - Absorption heat pump - Google Patents
Absorption heat pump Download PDFInfo
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- CN102242982B CN102242982B CN201110124518.2A CN201110124518A CN102242982B CN 102242982 B CN102242982 B CN 102242982B CN 201110124518 A CN201110124518 A CN 201110124518A CN 102242982 B CN102242982 B CN 102242982B
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 41
- 239000007788 liquid Substances 0.000 claims abstract description 497
- 239000006096 absorbing agent Substances 0.000 claims abstract description 128
- 238000001179 sorption measurement Methods 0.000 claims description 153
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 122
- 239000012530 fluid Substances 0.000 claims description 45
- 238000011144 upstream manufacturing Methods 0.000 claims description 27
- 238000001704 evaporation Methods 0.000 claims description 15
- 239000003795 chemical substances by application Substances 0.000 claims description 14
- 238000005057 refrigeration Methods 0.000 claims description 14
- 230000008020 evaporation Effects 0.000 claims description 11
- 230000008929 regeneration Effects 0.000 claims description 10
- 238000011069 regeneration method Methods 0.000 claims description 10
- 239000003507 refrigerant Substances 0.000 abstract description 139
- 239000002912 waste gas Substances 0.000 description 198
- 239000007789 gas Substances 0.000 description 103
- 238000010438 heat treatment Methods 0.000 description 32
- 239000008400 supply water Substances 0.000 description 23
- 238000001816 cooling Methods 0.000 description 18
- 238000002425 crystallisation Methods 0.000 description 16
- 230000008025 crystallization Effects 0.000 description 16
- 238000010276 construction Methods 0.000 description 15
- 230000000694 effects Effects 0.000 description 14
- 238000000034 method Methods 0.000 description 14
- 239000012141 concentrate Substances 0.000 description 13
- 235000008504 concentrate Nutrition 0.000 description 12
- 239000000498 cooling water Substances 0.000 description 12
- 230000001105 regulatory effect Effects 0.000 description 12
- 230000004087 circulation Effects 0.000 description 11
- 238000009833 condensation Methods 0.000 description 11
- 230000005494 condensation Effects 0.000 description 11
- 238000010586 diagram Methods 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 10
- 230000002411 adverse Effects 0.000 description 8
- 239000002356 single layer Substances 0.000 description 8
- 238000001514 detection method Methods 0.000 description 7
- 230000008569 process Effects 0.000 description 7
- 230000000903 blocking effect Effects 0.000 description 6
- 238000007599 discharging Methods 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 230000001276 controlling effect Effects 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 238000000280 densification Methods 0.000 description 4
- 239000011810 insulating material Substances 0.000 description 4
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 description 4
- 230000033228 biological regulation Effects 0.000 description 3
- 230000001143 conditioned effect Effects 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 239000010410 layer Substances 0.000 description 3
- 230000014759 maintenance of location Effects 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- 238000003466 welding Methods 0.000 description 3
- 230000004308 accommodation Effects 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 239000011229 interlayer Substances 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000003252 repetitive effect Effects 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- 238000005452 bending Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000004941 influx Effects 0.000 description 1
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- 235000014666 liquid concentrate Nutrition 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 230000011218 segmentation Effects 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
Classifications
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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
-
- 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
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- Sorption Type Refrigeration Machines (AREA)
Abstract
Provided is an absorption heat pump which utilizes exhaust gas as heat source for an evaporator and a regenerator. The absorption heat pump comprises an evaporator (E) which makes refrigerant (CL) to evaporate through heat source gas, an absorber (A) which absorbs evaporated refrigerant (CS) and heats heated medium (W1) with absorbed heat, a regenerator (G) which regenerates absorption liquid (Ali) through heat source gas from an absorber, and an evaporator having a plurality of vertical heat transferring pipes (51) which are arranged between upper pipe plates and lower pipe plates and has liquid refrigerant flown therein. The regenerator has having a plurality of vertical heat transferring pipes (71) which are arranged between upper pipe plates and lower pipe plates and has absorption liquid flown therein. Heat source gas flows on the external sides of the vertical heat transferring pipes which respectively form an evaporator pipe group (50) and a regenerator pipe group (70). The evaporator pipe group and a regenerator pipe group are linearly arranged relative to flow of the heat source gas.
Description
Technical field
The present invention relates to a kind of sorption type heat pump.Particularly relate to and reclaim the hot sorption type heat pump that heated medium is heated from the heat source gas that waste gas is such.In addition, the sorption type heat pump that the large temperature difference as far as possible between relating to inlet temperature utilizes.
Background technology
As shown in figure 15, thermal source employs heat drain WH to Absorption heat transformer in the past.Such as, the hot water of 85 DEG C is sent into sorption type heat pump, uses till 80 DEG C ~ about 75 DEG C, manufacture high-temperature water or the water vapour SS of more than 120 DEG C.This heat pump configurations comprises absorber AA, evaporimeter EE, the regenerator GG and condenser CC of outer shell-and-tube, and nest of tubes is divided into many paths by the regenerator GG, the evaporimeter EE that send into used heat, and heat drain WH is repeatedly turned round while flow.
In addition, at the steam that regenerator GG produces, cool and condensation at the condenser CC water WC that is cooled, and Returning evaporimeter EE.On the other hand, due to recuperation of heat, temperature can sharply reduce the less waste heat source of the thermal capacity such as waste gas, is difficult to carry out direct recuperation of heat by Absorption heat transformer.Therefore, from waste gas by recuperation of heat to hot water WH, and using the thermal source of hot water WH as heat pump.In this situation, the heat exchange from waste gas to hot water WH makes available temperature reduce, and being risen by the temperature adding hot fluid diminishes, and therefore subtend Absorption heat transformer directly imports waste gas and the mode of carrying out utilizing is inquired into.So, compared with being converted to the situation of hot water WH, more recuperation of heat can be carried out.
Patent document 1: Japanese Unexamined Patent Publication 2006-207883 publication
On the other hand, as shown in Figure 9, from the used heat that the factory of Japan discharges, the hot water used heat of the gas used heat of more than 100 DEG C and more than 40 DEG C estimates there is 1110PJ (Heisei 12 year: 2000 years) between 1 year.But the temperature of the gas be wherein less than the hot water of 100 DEG C, being less than 250 DEG C is lower, be therefore difficult to recycle in factory as energy, its amount for 914PJ/, actually occupies 82%.The situation absoluteness ground of wherein discharging with the form of waste gas is many.But the thermal capacity of the per unit volume of waste gas is less, volume flow is very large.In addition, such as carried out supplying with 200 DEG C by waste gas and carry out utilizing to 100 DEG C and obtain the steam of 180 DEG C etc. like that, the variations in temperature of waste gas is larger.
According to such exhaust gas properties, in sorption type heat pump in the past, being difficult to is the thermal source of evaporimeter and regenerator by exhaust gas utilization larger for volume flow.In addition, because flow resistance causes the pressure loss, therefore for making the power of this exhaust-gas flow become large, easily energy-saving effect is weakened.
In addition, the thermal capacity of waste gas is less, and therefore to carry out recuperation of heat as far as possible to low temperature, then the gateway temperature difference of heat reclamation device becomes very large.Such as, supplied by waste gas at 200 DEG C to sorption type heat pump, use till 100 DEG C, when obtaining the steam etc. of 180 DEG C, the variations in temperature of waste gas is 100 DEG C, is larger.If gateway temperature difference can be effectively utilized, then can realize the increase of reclaiming heat.But, because gateway temperature difference is comparatively large, so concentrate or crystallization to the surplus directly being utilized this waste gas then especially likely to produce absorbing liquid in high exhaust temperatures side by sorption type heat pump, be therefore difficult to waste gas to effectively utilize in sorption type heat pump as thermal source.Especially, have difficulties when increasing generating steam amount wanting as far as possible to carry out recuperation of heat till low temperature.
Summary of the invention
In order to solve the problem, the sorption type heat pump of first method of the present invention (first aspect of the invention) is such as shown in Fig. 1, Fig. 3, Fig. 4, sorption type heat pump possesses: evaporimeter E, is heated and make it evaporate by heat source gas GH1 to cold-producing medium CL; Absorber A, absorbs the cold-producing medium CS after above-mentioned evaporation, utilizes absorption heat to heat heated medium W1; And regenerator G, the absorbing liquid Ali by heat source gas GH3 absorption refrigeration agent CS in absorber A being reduced to concentration is heated, and this absorbing liquid Ali is regenerated; Evaporimeter E has: evaporimeter upper tube sheet 52; Evaporimeter lower tube sheet 53; And many vertical heat-transfer pipes 51, be arranged between evaporimeter upper tube sheet 52 and evaporimeter lower tube sheet 53, inner side flowing has aqueous above-mentioned cold-producing medium; Regenerator G has: regenerator upper tube sheet 72; Regenerator lower tube sheet 73; And many vertical heat-transfer pipes 71, be arranged between regenerator upper tube sheet 72 and regenerator lower tube sheet 73, inner side flowing has above-mentioned absorbing liquid ALi; Be configured to have heat source gas GH1, GH3 the outside of many vertical heat-transfer pipes 51,71 and vertical heat-transfer pipe 51,71 crossing flowings; Many vertical heat-transfer pipes 51,71 form evaporimeter nest of tubes 50 and regenerator nest of tubes 70 respectively in evaporimeter E and regenerator G, and evaporimeter nest of tubes 50 and regenerator nest of tubes 70 arrange point-blank relative to the flowing of heat source gas GH.
Below, the heat source gas first supplied to evaporimeter E is called GH1, the heat source gas supplied to regenerator G through evaporator E is called GH3.And, the heat source gas of discharging through regenerator G is called GH5.But, not need heat source gas to divide into when the gas of each several part flowing or blanket process heat source gas time, only call with the Reference numeral of GH.
If form as the manner, then being configured to flows outside many vertical heat-transfer pipes crossingly with vertical heat-transfer pipe heat source gas GH, and many vertical heat-transfer pipes form evaporimeter nest of tubes and regenerator nest of tubes respectively in evaporimeter and regenerator, evaporimeter nest of tubes and regenerator nest of tubes arrange point-blank relative to the flowing of heat source gas, therefore, when being utilized as the thermal source of evaporimeter and regenerator by waste gas larger for volume flow, the pressure loss that flow resistance can be caused suppresses for lower.Therefore, it is possible to the power being used for making this heat source gas flow is suppressed, for less, can improve energy-saving effect.
The sorption type heat pump of second method of the present invention is, in the sorption type heat pump of first method, such as shown in Fig. 3, regenerator upper tube sheet 72 is formed with the plate of evaporimeter upper tube sheet 52 by one, and regenerator lower tube sheet 73 is formed with the plate of evaporimeter lower tube sheet 53 by one.
If form as the manner, then regenerator upper tube sheet and evaporimeter upper tube sheet are formed by the plate of one, regenerator lower tube sheet and evaporimeter lower tube sheet are formed by the plate of one, therefore manufacture efficiency higher, and easily make evaporimeter and regenerator form adjacently.And then, can easily the interval between evaporimeter and regenerator be configured to less.
The sorption type heat pump of Third Way of the present invention, such as, shown in Fig. 1, Fig. 3, Fig. 4, in the sorption type heat pump of first method or second method, regenerator nest of tubes 70 relative to the flow arrangement of heat source gas GH in evaporimeter nest of tubes 50 downstream.
And then, typically such as shown in Fig. 3, Fig. 4, also side plate 54a, 54b, 74a, 74b can be possessed, this side plate 54a, 54b, 74a, 74 cooperate with each tube sheet 52,53,72,73 and evaporimeter nest of tubes 50 and regenerator nest of tubes 70 are interdicted with extraneous gas, and form the stream of heat source gas GH with each tube sheet 52,53,72,73.
If form as the manner, then regenerator nest of tubes is relative to the flow arrangement of heat source gas in evaporimeter nest of tubes downstream, and therefore heat source gas temperature in evaporimeter reduces and to supply to regenerator afterwards to a certain degree.Therefore, it is possible to the mistake of the absorbing liquid suppressing high-temperature gas to cause concentrates, the danger of crystallization.
The receipts heat pump of fourth way of the present invention, in the sorption type heat pump of Third Way, such as shown in Fig. 5, possess: bypass flow path 91, in the stream 60 of heat source gas GH from the end in evaporimeter nest of tubes 50 downstream, bypass (by-pass) is carried out to regenerator nest of tubes 70, heat source gas GH is flowed to regenerator nest of tubes 70 downstream; With flowing limiting member 92, the flowing of the heat source gas GH in bypass flow path 91 is limited.
At this, " restriction " can be " restriction " that do not comprise " blocking ", but comprises the concept of " blocking " typically.
If form as the manner, then can the heat that adds in regenerator be limited, can the concentrated or crystallization of the surplus of decrease uptake liquid.
The sorption type heat pump of the present invention the 5th mode, in the sorption type heat pump of Third Way or fourth way, such as shown in Fig. 5, possesses flowing limiting member 93, this flowing limiting member 93, in the stream 60 of heat source gas GH, limits the flowing of heat source gas GH between evaporimeter nest of tubes 50 and regenerator nest of tubes 70.
At this, restriction " can be " restriction " that do not comprise " blocking ", but comprise the concept of " blocking " typically.
If form as the manner, then to possess in the stream of heat source gas between evaporimeter nest of tubes and regenerator nest of tubes the flowing limiting member that the flowing of heat source gas limits, therefore with the flowing limiting member acting in conjunction limited the flowing of the heat source gas in bypass flow path, easily the heat source gas amount flowed in bypass flow path is regulated.
The sorption type heat pump of the present invention the 6th mode, in the sorption type heat pump of first method to the mode of one of the 5th mode, such as shown in Fig. 7 or Fig. 8, comprise regenerator upper tube sheet 72 ground and form regenerator upper header tank (header) 75, comprise regenerator lower tube sheet 73 ground and form regenerator lower header tank 76, possess the downspout 77 that absorbing liquid Ali is declined from regenerator upper header tank 75 to regenerator lower header tank 76.
If form as the manner, then absorbing liquid is supplied to regenerator lower header tank, rises to regenerator upper header tank in vertical heat-transfer pipe during flowing after being heated.In order to heat in a effective manner, preferred absorbing liquid circulates between regenerator lower header tank and regenerator upper header tank via vertical heat-transfer pipe.Downspout contributes to the circulation of absorbing liquid.
In order to solve above-mentioned problem, the sorption type heat pump of the present invention the 7th mode, such as, shown in Figure 10 (a), Figure 12, Figure 13, possesses: the first evaporimeter E1, is heated and make it evaporate by heat source fluid GH1 to cold-producing medium; First absorber A1, is absorbed in the cold-producing medium after evaporation in the first evaporimeter E1, utilizes absorption heat to heat heated medium W1; First regenerator G1, by heat source fluid GH4, absorbing liquid Ali absorption refrigeration agent in the first absorber A1 being reduced to concentration heats, and this absorbing liquid Ali is regenerated; Second evaporimeter E2, is heated cold-producing medium by heat source fluid GH2 and this cold-producing medium is evaporated; Second absorber A2, is absorbed in the cold-producing medium after evaporation in the second evaporimeter E2, utilizes absorption heat to heat heated medium; And Second reactivator G2, by heat source fluid GH3, absorbing liquid absorption refrigeration agent in the second absorber A2 being reduced to concentration heats, and makes this regeneration of absorption solution; First evaporimeter E1, the second evaporimeter E2, Second reactivator G2 and the first regenerator G1, configure successively from heat source fluid GH upstream side towards downstream in the stream 60 that heat source fluid GH flows.
Below, first the heat source fluid (such as waste gas) supplied to evaporimeter E1 is called GH1, the heat source fluid supplied to evaporimeter E2 through evaporator E1 is called GH2, the heat source fluid supplied to regenerator G2 through evaporator E2 is called GH3, the heat source fluid flowed into regenerator G1 through regenerator G2 is called GH4.And, the heat source fluid of discharging through regenerator G1 is called GH5.In addition, not need heat source fluid (such as waste gas) to divide into when the heat source fluid of each several part flowing or master process heat source body time, only call with the Reference numeral of GH.
If form as the manner, then in the second evaporimeter, cold-producing medium evaporates with low temperature compared with the first evaporimeter, and in above-mentioned Second reactivator, cold-producing medium regenerates with high temperature compared with the first regenerator.First absorber works with roughly the same temperature with the absorbing liquid of the second absorber.In addition, the flow arrangement of the heat source fluid that the second and first regenerator is such relative to heat source gas is in the downstream of the first and second evaporimeters, and therefore heat source fluid reduces the rear to the second and first regenerator supply of certain degree at the first and second evaporator temperatures.Therefore, it is possible to the surplus of the absorbing liquid suppressing high temperature heat source fluid to cause concentrates, the danger of crystallization.By arranging the feeding order of heat source fluid as described above, the evaporimeter evaporated at high temperature side and the regenerator regenerated at low temperature side are combined, and the evaporimeter evaporated at low temperature side and regenerator regenerate at high temperature side are combined, therefore, it is possible to by heat source fluid utilization to low temperature as much as possible.
And then, also can possess the first condenser and the second condenser that refrigerant gas vaporized in the first regenerator and Second reactivator are carried out respectively to condensation.First condenser and the second condenser can possess individually, also can as common condenser.If be set to common, then can make overall small compact.
The heat pump that sorption type heat pump is following typically: draw to the first absorber A1 from the first evaporimeter E1, draw the heat that heat source fluid GH holds from the second evaporimeter E2 to the second absorber A2, heated medium is heated.
The sorption type heat pump of eighth mode of the present invention, in the sorption type heat pump of the 7th mode, such as, shown in Figure 12, heat source fluid GH is heat source gas, and the first evaporimeter E1 and the second evaporimeter E2 has respectively: evaporimeter upper tube sheet 152,252; Evaporimeter lower tube sheet 153,253; And many vertical heat-transfer pipes 151,251, be arranged between evaporimeter upper tube sheet 152,252 and evaporimeter lower tube sheet 153,253, inner side flowing has aqueous above-mentioned cold-producing medium; First regenerator G1 and Second reactivator G2 has respectively: regenerator upper tube sheet 172,272; Regenerator lower tube sheet 173,273; And many vertical heat-transfer pipes 171,271, be arranged between regenerator upper tube sheet 172,272 and regenerator lower tube sheet 173,273, inner side flowing has absorbing liquid ALi; Be configured to outside many vertical heat-transfer pipes 151,251,171,271 with vertical heat-transfer pipe 151,251,171,271 crossing flowings have heat source gas GH; Many vertical heat-transfer pipes 151,251,271,171 are in the first evaporimeter E1, the second evaporimeter E2, Second reactivator G2, the first regenerator G1, form the first evaporimeter nest of tubes 150, second evaporimeter nest of tubes 250, Second reactivator nest of tubes 270, first regenerator nest of tubes 170 respectively, first evaporimeter nest of tubes 150, second evaporimeter nest of tubes 250, Second reactivator nest of tubes 270 and the first regenerator nest of tubes 170, arrange point-blank relative to the flowing of heat source gas GH.
If form as the manner, then being configured to flows in the outside of many vertical heat-transfer pipes crossingly with vertical heat-transfer pipe heat source gas GH, and many vertical heat-transfer pipes are at the first evaporimeter, second evaporimeter, Second reactivator, in first regenerator, form the first evaporimeter nest of tubes respectively, second evaporimeter nest of tubes, Second reactivator nest of tubes, first regenerator nest of tubes, first evaporimeter nest of tubes, second evaporimeter nest of tubes, Second reactivator nest of tubes and the first regenerator nest of tubes arrange point-blank relative to the flowing of heat source gas GH, therefore when heat source gas such for waste gas larger for volume flow is utilized as the thermal source of evaporimeter and regenerator, can the pressure loss that flow resistance causes be suppressed lower.Therefore, it is possible to make the power that this heat source gas flows suppress less by being used for, energy-saving effect can be improved.
The sorption type heat pump of the present invention the 9th mode, in the sorption type heat pump of the 7th mode or eighth mode, such as shown in Figure 14, possess: bypass flow path 91, in the stream of heat source gas GH, from the end in the second evaporimeter E2 downstream, bypass is carried out to Second reactivator G2, heat source gas GH is flowed to Second reactivator G2 downstream; With flowing limiting member 92, the flowing of the heat source gas GH in bypass flow path 91 is limited.
At this, " restriction " can be " restriction " that do not comprise " blocking ", but comprises the concept of " blocking " typically.
If form as the manner, then can concentrate the surplus easily producing absorbing liquid or crystallization Second reactivator in the heat that adds limit.Therefore, it is possible to the surplus of decrease uptake liquid is concentrated or crystallization.
The sorption type heat pump of the present invention the tenth mode, in the sorption type heat pump of the 7th mode to one of the 9th mode mode, such as shown in Figure 10 (a), first absorber A1 and the second absorber A2 is configured to heat the water W1 as heated medium and produce the water vapour S of the pressure of more than atmospheric pressure, and this sorption type heat pump possesses the gas-liquid separator 11 be separated with adjoint water by the water vapour S of generation.
If form as the manner, then the first absorber and the second absorber are configured to heat the water as heated medium and produce the water vapour of the pressure of more than atmospheric pressure, and this sorption type heat pump possesses the gas-liquid separator be separated with adjoint water by the water vapour of generation, therefore, it is possible to till the heat source fluid of relative low temperature is used low temperature as far as possible, draw heat from this heat source fluid and generate water vapour simultaneously, and then the water vapour after adjoint moisture is separated can be obtained.
The sorption type heat pump of the present invention the 11 mode, in the sorption type heat pump of the 7th mode to the mode of one of the tenth mode, such as shown in Figure 10 (b), possesses heat exchanger B, this heat exchanger B, in the stream 60 of heat source fluid GH, utilizes the heat of heat source fluid GH directly to produce water vapour at the first evaporimeter E1 upstream side.
If form as the manner, then the order in the feeding path of heat source fluid GH is heat exchanger B, the first evaporimeter E1, the second evaporimeter E2, Second reactivator G2 and the first regenerator G1.Possess and utilize the heat of heat source fluid GH directly to produce the heat exchanger B of water vapour at the first evaporimeter E1 upstream side in the stream 60 of heat source fluid GH, therefore the supplying temperature of heat source fluid GH be can more than the temperature of direct generating steam S time, by heat source fluid GH, make-up water W1 is directly heated, can direct generating steam.
Invention effect
According to this first invention, the pressure loss that the flow resistance of the such heat source gas of the larger waste gas of volume flow causes can be suppressed, can the power being used for heat source gas is flowed be suppressed less, can suppress to weaken energy-saving effect.
In addition, according to this second invention, a kind of sorption type heat pump that can reclaim the heat of heat source fluid as much as possible can be provided.
Accompanying drawing explanation
Fig. 1 is the flow graph of the structure of the sorption type heat pump representing first embodiment of the invention.
Fig. 2 is the Dühring's diagram of the state of the absorbing liquid represented in Fig. 1 flow graph.
Fig. 3 is the evaporimeter and regenerator that use in the sorption type heat pump to first embodiment of the invention, by upper header tank local incised notch after from oblique upper observe stereogram.
Fig. 4 is the evaporimeter and regenerator that use in the sorption type heat pump to first embodiment of the invention, from the top view of the axial top view of vertical heat-transfer pipe after being dismantled by header box.
Fig. 5 is the evaporimeter and regenerator that use in the sorption type heat pump to second embodiment of the invention, from the top view of the axial top view of vertical heat-transfer pipe after being dismantled by header box.
Fig. 6 is the vapor (steam) temperature that produces for parameter represents the line chart of the generation steam heat relative to exhaust gas entrance temperature.
Fig. 7 is the sectional view that the master be described the structure of the example 1 of the generator used in embodiments of the present invention looks sectional view, side cross-sectional, view, top view and downspout.
Fig. 8 looks sectional view and side cross-sectional, view to the master that the structure of the example 2 of the generator used in embodiments of the present invention is described.
Fig. 9 is the figure representing factory's used heat table according to temperature range.
Figure 10 is the flow graph of the structure of the sorption type heat pump representing third embodiment of the invention, a () is overall flow graph, the first evaporimeter E1 and heat exchanger B is taken out the local flow graph represented by (b) in the variation of the 3rd embodiment.
Figure 11 is the Dühring's diagram of the absorbing liquid state represented in the flow graph of Figure 10 (a).
Figure 12 is the evaporimeter and regenerator that use in the sorption type heat pump to third embodiment of the invention, the stereogram observed from oblique upper after by upper header tank incised notch.
Figure 13 is the evaporimeter and regenerator that use in the sorption type heat pump to third embodiment of the invention, from the top view of the axial top view of vertical heat-transfer pipe after being dismantled by header box.
Figure 14 is the evaporimeter and regenerator that use in the sorption type heat pump to four embodiment of the invention, from the top view of the axial top view of vertical heat-transfer pipe after being dismantled by header box.
Figure 15 is the flow graph of the structure of the sorption type heat pump represented in the past.
Description of reference numerals
2,3 absorbing liquid transfer pipelines
5 refrigerant liquid transfer pipelines
7 make-up water transfer pipelines
8 steam supply pipelines
11 gas-liquid separators
16,17,116,117,216,217 refrigerant vapour transfer tubes
21 control device
22 absorbing liquid sprayers
23 by heating tube
30 cooling tubes
37 check-valves
38 check-valves
39 check-valves
40 check-valves
50 evaporimeter nest of tubes
51 vertical heat-transfer pipes
52 evaporimeter upper tube sheet
53 evaporimeter lower tube sheet
54a, 54b evaporimeter side plate
55 evaporimeter upper header tank
56 evaporimeter lower header tank
60 exhaust flow path
70 regenerator nest of tubes
71 vertical heat-transfer pipes
72 regenerator upper tube sheet
73 regenerator lower tube sheet
74a, 74b regenerator side plate
75 regenerator upper header tank
76 regenerator lower header tank
91 bypass flow path
92,93 baffle plates
100 sorption type heat pumps
100-1 first sorption type heat pump portion
100-2 second sorption type heat pump portion
102,103,202,203 absorbing liquid transfer pipelines
101 sorption type heat pumps
116,216 refrigerant vapour transfer tubes
122,222 absorbing liquid sprayers
123,223 by heating tube
139,239 check-valves
150,250 evaporimeter nest of tubes
151,251 vertical heat-transfer pipes
152,252 evaporimeter upper tube sheet
153,253 evaporimeter lower tube sheet
154a, 154b, 254a, 254b evaporimeter side plate
155,255 evaporimeter upper header tank
156,256 evaporimeter lower header tank
170,270 regenerator nest of tubes
171,271 vertical heat-transfer pipes
172,272 regenerator upper tube sheet
173,273 regenerator lower tube sheet
174a, 174b, 274a, 274b regenerator side plate
175,275 regenerator upper header tank
176,276 regenerator lower header tank
A, A1, A2 absorber (absorbent portion)
ALi absorbing liquid
B heat exchanger
C condenser (condensation part)
CS refrigerant vapour
CL refrigerant liquid
DEN concentration sensor
E, E1, E2 evaporimeter
G, G1, G2, G11, G12 regenerator
GH, GH0, GH1, GH2, GH3, GH4, GH5, GH6 waste gas
L1, L2, L3, L101, L201, L102, L202 liquid surface level sensor
P pressure sensor
P1, P101, P201 solution pump
The pressure of Pr1 gas-liquid separator
P4 refrigerated medium pump (cold-producing medium boosting component)
P12, P13 supply-water pump
S steam
V1 steam valve
V3, V103, V203 cold-producing medium supply valve
W1 make-up water
WC cooling water
X1, X101, X201 solution heat exchanger
X2 heat exchanger
Detailed description of the invention
Below, with reference to accompanying drawing, embodiments of the present invention are described.In addition, in the various figures, give identical or similar Reference numeral for mutually identical or suitable part, and the repetitive description thereof will be omitted.
With reference to the flow graph of Fig. 1, the structure of the sorption type heat pump of first embodiment of the invention is described.Sorption type heat pump 101 possesses: absorber A, is carried out the absorption of refrigerant vapour CS (cold-producing medium is such as water) by absorbing liquid ALi (such as lithium bromide water solution); Regenerator G, makes refrigerant vapour CS evaporate from absorbing liquid Ali, carries out the regeneration of absorbing liquid Ali; Evaporimeter E, utilizes refrigerant liquid CL to produce refrigerant vapour CS; And condenser C, make refrigerant vapour CS condensation become refrigerant liquid CL.Under absorber A, regenerator G, evaporimeter E, condenser C are in a pressure respectively, the pressure of evaporimeter E is equal in practical with the pressure of absorber A, and the pressure of regenerator G is equal in practical with the pressure of condenser C.
Absorber A possesses: (1) absorbing liquid sprayer 22, and being transferred (supply) has absorbing liquid ALi as concentrated solution, is scattered by the absorbing liquid Ali that transfer comes to the inside of absorber A; (2) by heating tube 23, there is make-up water W1 by transfer, by the absorbing liquid ALi as weak solution after absorption refrigeration agent steam CS, the make-up water W1 that transfer comes is heated.The bottom of absorber A becomes enough for accumulating the absorbing liquid retention portion of absorbing liquid Ali.
Evaporimeter E possesses vertical heat-transfer pipe 51, the internal flow of this vertical heat-transfer pipe 51 has transfers from condenser C the refrigerant liquid CL of coming by refrigerant liquid transfer tube 5, by carrying out heating at the waste gas GH1 as heat source gas of flows outside, this refrigerant liquid CL is evaporated.In addition, possess liquid surface level sensor L1, this liquid surface level sensor L1 is arranged among the upper header tank 55 of evaporimeter E, detects the liquid level of the refrigerant liquid CL in evaporimeter E.Liquid surface level sensor L1 is regulated by control device 21 couples of cold-producing medium supply valve V3, maintain the liquid level of the cold-producing medium in evaporimeter E (in addition thus, cold-producing medium supply valve V3 also can not be set, and refrigerated medium pump P4 is set to frequency-conversion and speed-regulation motor drive refrigerated medium pump is regulated).In sorption type heat pump 101, the refrigerant vapour CS evaporated in evaporimeter E, delivers to absorber A via refrigerant vapour transfer tube 16.Be described in detail with reference to the structure of Fig. 3 ~ Fig. 5 to evaporimeter E.At this, waste gas in the various operations of factory, make use of high-temperature part typically after 200 DEG C of degree below gas.Can be the waste gas from boiler, also can be make use of high-temperature part after and from chimney discharge before gas.
Regenerator G possesses vertical heat-transfer pipe 71, the internal flow of this vertical heat-transfer pipe 71 has transfers from absorber A the absorbing liquid ALi of coming via absorbing liquid transfer pipeline 3, produce refrigerant vapour by heating this absorbing liquid ALi at the waste gas GH3 as heat source gas of flows outside, thus this absorbing liquid ALi is concentrated.This absorbing liquid Ali is in absorber A, reduce concentration after absorption refrigeration agent absorbing liquid and weak solution.In addition, possess liquid surface level sensor L2, this liquid surface level sensor L2 is arranged among the upper header tank 75 of regenerator G, detects the liquid level of the absorbing liquid Ali in regenerator G.Liquid surface level sensor L2 is regulated by control device 21 couples of solution pump P1, maintains the liquid level (in addition, also can replace the adjustment of solution pump P1 and arrange control valve) of the absorbing liquid in regenerator G thus.In sorption type heat pump 101, be sent to absorber A by the absorbing liquid Ali after regenerator G concentrates via absorbing liquid transfer tube 2.In addition, the refrigerant vapour CS produced at regenerator G is sent to condenser C via refrigerant vapour transfer tube 17.Be described in detail with reference to Fig. 3 ~ Fig. 5, Fig. 7, Fig. 8 structure to regenerator G.
Condenser C possesses cooling tube 30, and this cooling tube 30 is had cooling water WC by transfer, cools the refrigerant vapour CS being sent to condenser C from regenerator G.The temperature of cooling water WC is such as 32 DEG C at the entrance of cooling tube 30, is 37 DEG C in outlet.
Sorption type heat pump 101 possesses: (1) gas-liquid separator 11; (2) make-up water transfer pipeline 7, is connected with gas-liquid separator 11, transfers make-up water W1 to gas-liquid separator 11; (3) make-up water transfer pipeline 6, is transferred make-up water W1 from gas-liquid separator 11 to absorber A by heating tube 23; (4) make-up water transfer pipeline 10, makes make-up water W1 return from being transferred make-up water W1 by heating tube 23 to gas-liquid separator 11; And (5) steam supply pipeline 8, be connected with steam header box (not shown), the steam S (such as 180 DEG C) produced by gas-liquid separator 11 supplies to steam header box.
Sorption type heat pump 101 also possesses: (6) absorbing liquid transfer pipeline 2, connects regenerator G and absorber A, transferred by the absorbing liquid Ali as concentrated solution after regenerator G regenerates to the absorbing liquid sprayer 22 of absorber A; (7) absorbing liquid transfer pipeline 3, connect absorber A and regenerator G, the absorbing liquid Ali as weak solution accumulated by absorber A transfers to the regenerator lower header tank 76 of regenerator G; And (8) refrigerant liquid transfer pipeline 5, connect condenser C and evaporimeter E, condensed for condenser C refrigerant liquid CL is transferred to evaporimeter E.
Sorption type heat pump 101 also possesses (9) solution (absorbing liquid) heat exchanger X1, this solution (absorbing liquid) heat exchanger X1 via absorbing liquid transfer pipeline 2 to the absorbing liquid Ali as concentrated solution transferred by heated side and transfer via absorbing liquid between the absorbing liquid Ali as weak solution that pipeline 3 transfers to regenerator lower header tank 76 and carry out heat exchange.
Sorption type heat pump 101 also possesses heat exchanger X2, and this heat exchanger X2, at heated side flowing waste heat source GH6, via make-up water transfer pipeline 7 to by heated side transfer make-up water W1, carries out heat exchange.Heat exchanger X2 shows independently heat exchanger in the drawings, but preferably, the heat transfer part of heat exchanger X2 is arranged on the exhaust-gas flow be arranged in the middle of evaporimeter E inlet portion or evaporimeter E and regenerator G.
Absorbing liquid transfer pipeline 2 is provided with solution pump P1, and the absorbing liquid Ali after regenerator G regenerates by solution pump P1 transfers to absorber A.Solution pump P1 is arranged on the upstream side of solution heat exchanger X1.Refrigerant liquid transfer pipeline 5 is provided with the refrigerated medium pump P4 as cold-producing medium boosting component, and condensed for condenser C refrigerant liquid CL transfers to evaporimeter E by refrigerated medium pump P4.Make-up water transfer pipeline 7 is provided with supply-water pump P12, and make-up water W1 transfers to gas-liquid separator 11 by supply-water pump P12.And then be provided with check-valves 37 in the downstream of the supply-water pump P12 of make-up water transfer pipeline 7, prevent make-up water W1 adverse current.Make-up water transfer pipeline 6 is provided with supply-water pump P13, make-up water W1 transfers from gas-liquid separator 11 to by heating tube 23 by supply-water pump P13, and then from being transferred make-up water W1 by heating tube 23 to gas-liquid separator 11, make-up water W1 is returned via make-up water transfer pipeline 10, thus make-up water W1 is circulated.
In refrigerant liquid transfer pipeline 5, be provided with cold-producing medium supply valve V3 in the downstream of refrigerated medium pump P4, the flow of the refrigerant liquid CL of this cold-producing medium supply valve V3 subtend evaporimeter lower header tank 56 transfer adjusts.
In gas-liquid separator 11, be provided with the pressure sensor P that its pressure is detected, and be provided with the liquid surface level sensor L3 that the liquid level of the make-up water W1 that bottom is accumulated is detected.The steam valve V1 that the pressure of the steam S of supply is regulated is provided with at steam supply pipeline 8.Also as shown in Figure, the check-valves 38 of the adverse current of the steam prevented from steam header box (not shown) can be set at steam supply pipeline 8.If arrange check-valves 38, then independently can reliably prevent the adverse current of the steam from steam header box with the work of steam valve V1.Supplying temperature as the waste gas GH1 of heat source gas is such as 200 DEG C.The waste gas GH1 supplied to evaporimeter E is captured heat at evaporimeter E, becomes the waste gas GH3 that temperature is about 150 DEG C, and then flows into regenerator G, discharges after this to be become the waste gas GH5 of about 100 DEG C by capturing heat.
As already described, the waste gas first supplied to evaporimeter E is called GH1, the waste gas supplied to regenerator G through evaporator E is called GH3.And, the waste gas of discharging through regenerator G is called GH5.In addition, not need heat source gas to be distinguished as when the gas of each several part flowing or master process heat source gas time, only call with the Reference numeral of GH.
The preheating of make-up water W1, the high-temperature gas played till the gas GH3 of the pars intermedia of evaporimeter E and regenerator G preferably by the supply side from the such heat source gas of waste gas carries out.Or, not shown, but also can be undertaken by the heat exchanger utilizing the absorbing liquid of the entrance supplied to regenerator G to carry out heating, the heat exchanger that also can be undertaken by the refrigerant vapour utilizing evaporimeter E to produce heating is carried out.
Sorption type heat pump 101 possesses control device 21.Liquid level signal (not shown) from the expression liquid level of liquid surface level sensor L1 is sent to control device 21, sends signal from control device 21 to the control valve controlled the flow of refrigerant liquid CL and cold-producing medium supply valve V3.So, regulate the aperture of cold-producing medium supply valve V3 to make the liquid level of evaporimeter E for certain (but, be simplified shown as in the drawings and directly transmit control signal to cold-producing medium supply valve V3 from liquid surface level sensor L1).
Liquid level signal (not shown) from the expression liquid level of liquid surface level sensor L2 is sent to control device 21, send for controlling the flow of absorbing liquid Ali with the control signal (not shown) making liquid level remain certain level from control device 21 to the frequency-conversion and speed-regulation motor IN driven solution pump P1, thus the rotating speed of frequency-conversion and speed-regulation motor IN is regulated, the liquid level carrying out controlling to make regenerator G is necessarily (not in the drawings, be simplified shown as and directly send signal from liquid surface level sensor L2 to frequency-conversion and speed-regulation motor IN).
Liquid level signal (not shown) from the expression liquid level of the liquid surface level sensor L3 of gas-liquid separator 11 is sent to control device 21, control device 21 makes supply-water pump P12 On/Off (in the drawings, be simplified shown as directly send signal to supply-water pump P12 from liquid surface level sensor L3) liquid level to be remained roughly certain horizontal mode.In addition, also can send flow for controlling make-up water W1 from control device 21 to supply-water pump P12 (in fact to frequency-conversion and speed-regulation motor not shown as described above) with the control signal (not shown) making liquid level remain certain level, thus regulate the rotating speed of supply-water pump P12 to become certain to make the liquid level of gas-liquid separator 11.
Pressure signal (in figure dotted line) from the expression pressure of pressure sensor P is sent to control device 21, send for controlling the quantity delivered of steam S with the control signal (figure dotted line) making the pressure of gas-liquid separator 11 become setting Pr1 from control device 21 to steam valve V1, thus the aperture of steam regulation valve V1 becomes setting Pr1 to make the pressure of gas-liquid separator 11.Setting Pr1 preference is as being set as than steam header box pressure (0.05MPa degree) height a little.Waste gas GH1 and waste gas GH6, is illustrated as and is supplied in parallel, but also can in series or a part is in parallel and a part in series supplies.
Then, be described with reference to Fig. 1, Fig. 2 effect to the first embodiment.Fig. 2 is the Dühring's diagram (デ ュ mono-リ Application グ XIAN figure) of the state representing absorbing liquid and cold-producing medium, and the longitudinal axis is refrigerant temperature, and transverse axis is solution (absorbing liquid) temperature.From the absorbing liquid ALi as weak solution (state is the B2 position Fig. 2) that absorber A discharges, transfer pipeline 3 by absorbing liquid and to transfer and through solution heat exchanger X1.This absorbing liquid Ali, through over-heat-exchanger X1, is transferred from regenerator G to absorber A the absorbing liquid ALi as concentrated solution come via absorbing liquid transfer pipe arrangement 2 thus and is cooled (state of cooled absorbing liquid Ali is the B8 position Fig. 2).Transferred to regenerator lower header tank 76 by the cooled absorbing liquid ALi of solution heat exchanger X1.
Absorbing liquid Ali, during flowing through in vertical tube 71 from the regenerator lower header tank 76 (state of absorbing liquid Ali is the B5 position in Fig. 2) of regenerator G, is heated by waste gas GH3, and the cold-producing medium that absorbed liquid ALi absorbs is evaporated to refrigerant vapour CS.So, be concentrated, regenerate after as concentrated solution absorbing liquid Ali from be arranged on regenerator upper header tank 75 absorbing liquid outlet 2a flow out.The square hole that the upper header tank 75 of the regenerator G shown in Fig. 1 is represented by solid line is outlet 2a.In addition, coupled dotted line represents outlet header box.
The absorbing liquid ALi (state is the B4 position in Fig. 2) becoming concentrated solution transfers to the absorbing liquid sprayer 22 of absorber A via absorbing liquid transfer pipeline 2.Boosted by solution pump P1 during via absorbing liquid transfer pipeline 2, heated (state via the absorbing liquid Ali of absorbing liquid transfer pipeline 2 is the B7 position in Fig. 2) by the absorbing liquid ALi as weak solution that the transfer from absorber A to regenerator G comes at solution heat exchanger X1 afterwards, then transfer to the absorbing liquid sprayer 22 of absorber A.
In absorber A, from the absorbing liquid ALi as concentrated solution (state of absorbing liquid Ali is the B6 position Fig. 2) that absorbing liquid sprayer 22 scatters in absorber A, the refrigerant vapour CS evaporated in evaporimeter E is absorbed, utilize absorption heat to heat via by the make-up water W1 as heated medium of heating tube 23, and bottom absorber A, accumulate absorbing liquid ALi (state of absorbing liquid Ali is the B2 position in Fig. 2).
As mentioned above, solution pump P1 transfers the absorbing liquid Ali making the liquid level of the absorbing liquid Ali in regenerator G become certain flow like that from regenerator G to absorber A.Feeding amount is controlled by control device 21.By remaining necessarily by the liquid level of regenerator G, that can guarantee between the absorber A that difference that refrigerant vapour is pressed is larger and regenerator G is liquid-tight.Except being accumulated in the absorbing liquid in regenerator G, intrasystem absorbing liquid is mainly accumulated in bottom absorber A.Therefore, the enough capacity had for accumulating absorbing liquid are configured to bottom absorber A.The outlet side of the pump P1 of absorbing liquid transfer pipeline 2 is provided with check-valves 39.In the operation process of heat pump 101, the pressure ratio regenerator G of absorber A is high.Therefore, even pump P1 is stopped when heat pump 101 is stopped, if then absorbing liquid retains, flowing into from absorber A to regenerator G.The reversion of pump P1 is prevented by check-valves 39.In addition, if stopped by heat pump 101, then the absorbing liquid Ali originally remained in absorber A flows through absorbing liquid transfer pipeline 3 and remains in regenerator G.Therefore, regenerator upper header tank 75 is set to enough capacity of the absorbing liquid in receptacle system.Remain in the absorbing liquid ALi in regenerator upper header tank 75 during stopping, being sent to absorber A when the starting of heat pump 101 by level control.Or, also can be sent to absorber A in advance before feeding waste gas GH.
The refrigerant vapour CS evaporated at regenerator G is sent to condenser C via refrigerant vapour transfer tube 17.The refrigerant vapour CS delivering to condenser C is cooled by the cooling water WC via cooling tube 30 at condenser C, condensation and become refrigerant liquid CL (state is the D1 position in Fig. 2).The refrigerant liquid CL of condenser C boosts via cooled dose of pump P4 after refrigerant liquid transfer pipeline 5, and after being controlled flow by cold-producing medium supply valve V3, is sent to evaporimeter E.
Deliver to the refrigerant liquid CL of evaporimeter E, heated by waste gas GH1 during flowing through from evaporimeter lower header tank 56 inside vertical heat-transfer pipe 51 and evaporate (state of cold-producing medium is the D2 position in Fig. 2).The refrigerant vapour CS of evaporation is sent to absorber A via refrigerant vapour transfer tube 16, and in absorber A, absorbed liquid ALi absorbs.
Cold-producing medium supply valve V3 is conditioned aperture by control device 21, adds spatter the amount of the refrigerant liquid CL transferred from condenser C to evaporimeter E.That is, the liquid level of the refrigerant liquid CL accumulated at evaporimeter E is made to become necessarily such amount to the amount plus-minus of the refrigerant liquid CL of transfer.Carry out such control, be to carry out supply to the evaporation capacity of refrigerant liquid, and be in order to avoid refrigerated medium pump P4 suction gas.Except being trapped in the refrigerant liquid of evaporimeter E, the refrigerant liquid of entire system is accumulated in the bottom of condenser C.Therefore, the bottom of condenser C is configured to enough capacity of having for accumulating refrigerant liquid.If make heat pump 101 stop, then likely there is refrigerant liquid CL and transfer the danger of pipeline 5 to the condenser C adverse current than evaporimeter E low pressure from the evaporimeter E side that pressure is higher via refrigerant liquid.In order to avoid the reversion of the refrigerated medium pump P4 after so firm stopping, preferably check-valves 40 is set at the outlet side of refrigerated medium pump P4.Also can replace which and control device 21 is configured to, make when heat pump stops (if complete in level control, can become open when heat pump stops and can not adverse current be prevented) cold-producing medium supply valve V3 become full cut-off.
The make-up water W1 being supplied to make-up water transfer pipeline 7 is transferred by the supply-water pump P12 backward gas-liquid separator 11 that boosts.The make-up water W1 discharged from supply-water pump P12 is transferred to gas-liquid separator 11 by after waste gas GH6 heating among heat exchanger X2.
Flow to the make-up water W1 of gas-liquid separator 11 supply controls the rotating speed of supply-water pump P12 by control device 21 and is conditioned, and becomes certain with the liquid level of the make-up water W1 making accumulation in gas-liquid separator 11.Be adjusted to and make the liquid level of the make-up water W1 of gas-liquid separator 11 be certain, be in order to gas-liquid separator 11 supply with supply as steam S and the make-up water W1 of the corresponding amount of the make-up water W1 that have lost.
Be transferred to the make-up water W1 of gas-liquid separator 11, via make-up water transfer pipeline 6, by supply-water pump P13 boost after be sent to absorber A by heating tube 23, after utilizing the absorption of the absorbing liquid Ali of absorption refrigeration agent steam CS heat to be produced steam S by heating in absorber A, gas-liquid separator 11 is returned via make-up water transfer pipeline 10, and by steam and fluid separation applications.The steam S produced, via steam supply pipeline 8, by being controlled after steam valve V1 that device 21 controls carries out Flow-rate adjustment in the mode making the pressure of gas-liquid separator 11 and become the first authorized pressure Pr1, supplies to steam header box (not shown).
Control in the mode making the pressure of gas-liquid separator 11 become authorized pressure Pr1, the control carried out to make the pressure of gas-liquid separator 11 become the pressure higher than the pressure of steam header box (not shown), the pressure of gas-liquid separator 11 is set to all the time than the pressure of the pressure height certain pressure of steam header box, the steam S that sorption type heat pump 101 can be made to produce to the supply of steam header box, can stably supply steam S to load (not shown) side all the time.
By forming like that above, the sorption type heat pump 101 of present embodiment, the heat held by waste gas GH1 is drawn from evaporimeter E to absorber A and is heated the make-up water W1 as heated medium.In the present embodiment, make-up water W1 externally supplies become water vapour by heating after.
With reference to the stereogram of Fig. 3 and the top view of Fig. 4, to form first embodiment of the invention sorption type heat pump, the structure of evaporimeter E and regenerator G is described.Fig. 3 be to evaporimeter E and regenerator G by respective upper header tank local incised notch after from oblique upper observe stereogram.Fig. 4 is to evaporimeter E and regenerator G top view from top view after respective upper header tank being dismantled.In detail in this figure, the refrigerant liquid entrance of evaporimeter E, refrigerant vapour outlet and the absorbing liquid entrance of regenerator G, the diagram of absorbing liquid outlet is eliminated.
The evaporimeter E that the sorption type heat pump 101 of present embodiment possesses, possesses the upper tube sheet 52 of horizontal arrangement and the lower tube sheet 53 of configuration in parallel.Many vertical heat-transfer pipes 51 vertically configure between upper tube sheet 52 and lower tube sheet 53.Each vertical heat-transfer pipe 51 to be inserted in the hole worn respectively in upper tube sheet 52 and lower tube sheet 53 and by expander after, guaranteed air-tightness by seal welding.Many vertical heat-transfer pipes 51 are arranged as clathrate or staggered in rectangular area when observing from the axis direction of pipe, form the nest of tubes of a group.In the inner side of such many vertical heat-transfer pipes 51, flowing has aqueous refrigerant liquid CL.That is, evaporimeter E possesses the structure of water-tube boiler.
Equally, the regenerator G that the sorption type heat pump 101 of present embodiment possesses, possesses the upper tube sheet 72 of horizontal arrangement and the lower tube sheet 73 of configuration in parallel.Many vertical heat-transfer pipes 71 vertically configure between upper tube sheet 72 and lower tube sheet 73.Each vertical heat-transfer pipe 71 to be inserted in the hole worn respectively to upper tube sheet 72 and lower tube sheet 73 and by expander after, fetched by seal weld and guarantee air-tightness.Many vertical heat-transfer pipes 71 are arranged as clathrate or staggered in rectangular area when observing from tube axis direction, form the nest of tubes of a group.In the inner side of such many vertical heat-transfer pipes 71, flowing has absorbing liquid ALi.That is, regenerator G possesses the structure of water-tube boiler.
In the sorption type heat pump 101 of present embodiment, the upper tube sheet 52 of evaporimeter E and the upper tube sheet 72 of regenerator G are formed by the tube sheet of one, and the lower tube sheet 73 of the lower tube sheet 53 of evaporimeter E and regenerator G is formed by the tube sheet of one.Evaporimeter E and regenerator G is heated by common thermal source and waste gas GH, arranges, and is formed by a plate of one, can manufacture efficiently thus therefore, it is possible to adjacent.Between evaporimeter nest of tubes 50 and regenerator nest of tubes 70, as long as the header box of evaporimeter E and regenerator G can be formed, preferably configure as closely as possible.Or, be configured to the lower baffle plate as flowing limiting member that will illustrate as long as can insert, preferably configure as closely as possible.By closely configuring, the stream of waste gas GH can be prevented invalidly elongated, the flow losses of waste gas GH can be suppressed.
Be configured in the sorption type heat pump 101 of present embodiment, have waste gas GH1, GH3 the outside of evaporimeter E and regenerator G many vertical heat-transfer pipes 51,71 separately and vertical heat-transfer pipe 51,71 crossing flowings.Between the upper tube sheet 52 and lower tube sheet 53 of evaporimeter E, between the upper tube sheet 72 of regenerator G and lower tube sheet 73, be formed with the stream 60 of waste gas GH.In the present embodiment, waste gas GH flows via stream 60 and vertical heat-transfer pipe 51,71 right angle intersection.For heat-transfer pipe 51,71, make that waste gas GH makes refrigerant liquid CL in the outer flowing of pipe, absorbing liquid Ali flows inside pipe, therefore, it is possible to guarantee the stream 60 of waste gas GH significantly, avoids the high speed of flow velocity.
In addition, many vertical heat-transfer pipes 51,71 form evaporimeter nest of tubes 50 and regenerator nest of tubes 70 respectively in evaporimeter E and regenerator G, and evaporimeter nest of tubes 50 and regenerator nest of tubes 70 arrange point-blank relative to the flowing of waste gas GH.What is called arranges point-blank and refers to, the stream 60 of waste gas GH is not the such multi-path of so-called two paths or three-way, but the configuration of ground, unipath.In other words, refer to when discharge side being observed from the supply side of waste gas GH after evaporimeter nest of tubes 50 and regenerator nest of tubes 70 are dismantled, discharge side can be seen through through the stream 60 of waste gas GH from supply side.
Owing to arranging point-blank, therefore be the such gas of waste gas that the thermal capacity of per unit volume is less at thermal source, in order to obtain need heat and need to flow the heat source gas having very large volume flow time, can the pressure loss that flow resistance causes be suppressed lower.That is, the loss that corner loss or revolution cause can be reduced.Although easily become large for the power of the heat source gas flowing making waste gas such, can be suppressed less, can not energy-saving effect be weakened.
In the above embodiment, in evaporimeter E and regenerator G, upper tube sheet 52,72 is formed by the tube sheet of one each other, and lower tube sheet 53,73 is formed by the tube sheet of one each other, but also can distinguish split formation.If be arranged to split, then the configuration of evaporimeter E and regenerator G can decide according to situation alone respectively.When being arranged to split, it is also constant that evaporimeter nest of tubes 50 and regenerator nest of tubes 70 arrange this point point-blank relative to the flowing of waste gas GH1, GH3.In addition, when being arranged to split, also preferably both configure as closely as possible.This is to suppress lower by the loss of the stream of waste gas.
In the present embodiment, regenerator nest of tubes 70 relative to the flow arrangement of waste gas GH in the downstream of evaporimeter nest of tubes 50.
When thermal source is the such gas of waste gas, available temperature amplitude is larger.Such as with 200 DEG C of supplies, with 100 DEG C of discharges.In this case, the temperature difference of 100 DEG C is utilized.Therefore, when being utilized as thermal source by waste gas, the mistake that in the past there is the absorbing liquid that the gas because of relatively-high temperature causes concentrates, the danger of crystallization.But, owing to regenerator nest of tubes 70 to be configured in the downstream of evaporimeter nest of tubes 50, therefore, supply to regenerator G after waste gas GH reduces temperature to a certain degree in evaporimeter E.Therefore, it is possible to the mistake of the absorbing liquid suppressing the part of the part be just supplied to, the in other words relatively-high temperature of waste gas GH to cause concentrates, the danger of crystallization.
And then, in the present embodiment, possess side plate 54a, 54b, 74a, 74b (with reference to Fig. 4), evaporimeter nest of tubes 50 and regenerator nest of tubes 70 interdict with extraneous gas by this side plate 54a, 54b, 74a, 74b, cooperate and form the stream of waste gas GH with each tube sheet 52,53,72,73.Also can replace side plate 54a, 54b, 74a, 74b and be set to water-cooling wall, but if be 250 DEG C of degree or it is following, typically be 200 DEG C of degree as waste gas, then can be made up of simple flat board (iron plate), become easy structure.That is, can not be the structure in interlayer collecting in multi-ply construction as water-cooling wall with the fluid of pressure, and monolayer constructions will or veneer structure can be become.In the sorption type heat pump of present embodiment, evaporimeter E and regenerator G becomes the pressure vessel of the pressure of more than atmospheric pressure mostly.In this case, each upper header tank 55,75 and lower header tank 56,76 header box of evaporimeter (in the sorption type heat pump especially) are under pressure, but because side plate 54a, 54b, 74a, 74b are not water-cooling wall but simple individual layer is dull and stereotyped, therefore, it is possible to easily carry out the reply of intensity.
In addition, as already described, evaporimeter E and regenerator G is evaporimeter nest of tubes 50 and regenerator nest of tubes 70 in other words, arranges point-blank relative to the flowing of waste gas GH.This configuration can typically realize as follows: side plate 54a and side plate 74a be formed as one plane, side plate 54b is same with side plate 74b formed one plane, preferably respectively to be formed by single flat board, and evaporimeter upper tube sheet 52 and regenerator upper tube sheet 72 be formed as one plane, evaporimeter lower tube sheet 53 is same with regenerator lower tube sheet 73 be formed as one plane, preferably respectively to be formed by single flat board.
The extraneous gas side of side plate 54a, 54b, 74a, 74b is preferably provided with heat-insulating material.Though temperature is not too high, this is to make available heat not be expelled to outside.And be the safety in order to human body.
And then, in the present embodiment, evaporimeter E and regenerator G arranges evaporimeter upper header tank 55 and regenerator upper header tank 75 in the mode covered the opening portion on respective nest of tubes 50,70 top, arranges evaporimeter lower header tank 56 (refrigerant liquid supply chamber) and regenerator lower header tank 76 (solution supply chamber) in the mode covered the opening of bottom.Evaporimeter upper header tank 55 also can double as gas-liquid separation chamber.Form if so, then can realize the simplification constructed.
With reference to the top view of Fig. 5, the combination of the evaporimeter E used in the second embodiment of the present invention and regenerator G is described.Fig. 5 is to the top view of vertical heat-transfer pipe 51,71 from axis direction and top view after each upper header tank dismounting by evaporimeter E and generator G.In the present embodiment, possess bypass flow path 91, this bypass flow path 91 in the stream 60 of the waste gas GH as heat source gas, from the end in the downstream of evaporimeter nest of tubes 50, bypass is carried out to regenerator nest of tubes 70, makes waste gas GH flow to the downstream of above-mentioned regenerator nest of tubes 70.
Bypass flow path 91 is whole or a part of by waste gas GH1 or the waste gas GH3 after evaporimeter nest of tubes 50, avoids regenerator nest of tubes 70 ground and to lead the stream in its downstream.
At this, the end in the downstream of so-called evaporimeter nest of tubes 50 refers to, the part in the downstream of the vertical heat-transfer pipe 51 of waste gas GH1 flow direction most downstream, namely waste gas GH1 becomes the part of waste gas GH3 after all evaporators nest of tubes 50, and then the space segment be in other words preferably between evaporimeter nest of tubes 50 and regenerator nest of tubes 70, also can as shown in the figure, be the part of waste gas GH1 after many vertical heat-transfer pipes of evaporimeter nest of tubes 50 upstream side.That is, also can be the part of the space segment comprised between evaporimeter nest of tubes 50 and regenerator nest of tubes 70 or part more by the upstream a little than this part.Now, the beginning of preferred bypass flow path 91 does not extend to regenerator nest of tubes 70.The object arranging bypass flow path 91 is, prevents the surplus of the absorbing liquid in regenerator G from concentrating and then crystallization.
If the initial point of bypass flow path 91 to be set to waste gas GH1 becomes waste gas GH3 part through whole evaporimeter nest of tubes 50, then in evaporimeter E, can utilize the high-temperature part of waste gas GH1 as much as possible, this is preferred from the viewpoint of heat utilization.But, even if the initial point of bypass flow path 91 to be set to the part of waste gas GH1 after the vertical heat-transfer pipe 51 of certain degree radical of evaporimeter nest of tubes 50 upstream side, the heat of waste gas GH1 is also utilized in large quantities in evaporimeter E, can improve the flexibility that device is formed.That is, the space segment between evaporimeter nest of tubes 50 and regenerator nest of tubes 70 can be formed shortlyer, can the densification of implement device and the reduction of flow path resistance.
The baffle plate 92 that bypass flow is limited is possessed in bypass flow path 91.This is because bypass flow path 91 is to prevent the surplus of the absorbing liquid Ali in regenerator G from concentrating and then crystallization and arrange the stream that bypass flow path shunts enough waste gas GH3.Shunt with Shangdi needed for not needing.Baffle plate 92 preferably can not only limit the flow of waste gas GH3, can also interdict.From the viewpoint of recuperation of heat, interdict completely when the absorbing liquid concentration preferably in regenerator G is not in deathtrap.
In this embodiment, the concentration detector DEN (with reference to Fig. 1) that the concentration of the absorbing liquid Ali in regenerator G is detected preferably is possessed.This is to regulate the aperture of baffle plate 92 with answering with the relative concentration of the absorbing liquid Ali in regenerator G.Concentration detector DEN is arranged on the highest position of the concentration of the absorbing liquid Ali in regenerator G, is typically arranged in upper header tank 75.In addition, as shown in Figure 1, also can be arranged on the absorbing liquid transfer pipeline 2 guiding absorbing liquid Ali from upper header tank 75 to absorber A.In this case, preferably as far as possible close to the position of regenerator G.Concentration detector DEN is not limited to detector concentration being carried out to direct-detection, also can be the detector indirectly carrying out detecting.That is, also can be the detector that the density of the physical quantity suitable with concentration, such as absorbing liquid is detected.In this so-called concentration, it also can be the calculated value be associated with concentration.That is, concentration can be the value gone out according to density and temperature detection, also can be the value gone out according to velocity of sound and temperature detection, also can replace concentration and density based, proportion.In addition, also concentration can be inferred according to the relation between the solution temperature of regenerator outlet and the steam pressure (or dew point) of regenerator G.That is, also can calculate according to the vapor-liquid equilibrium relationship of solution.Affect more by force because the steam pressure of regenerator or dew point produce cooling water temperature, therefore also can judge according to solution temperature and cooling water temperature the danger that concentrates.Supposition like this or calculating are also modes of Concentration Testing.
In this embodiment, preferably also between evaporimeter E and regenerator G, furtherly, baffle plate 93 is set between evaporimeter nest of tubes 50 and regenerator nest of tubes 70.If possess bypass flow path 91 and baffle plate 92, then because the flow path resistance of regenerator nest of tubes 70 can make quite a large amount of waste gas GH3 flow to bypass flow path 91, but the amplitude of accommodation can be increased by arranging baffle plate 93.Baffle plate 93 is multi-blade type, is formed as by main part the flat board that vertical or horizontal Ground Split becomes multiple, can rotate centered by the length direction central shaft of respective lengthwise or the flat board of growing crosswise.If become multi-blade type, then do not need to arrange the space between evaporimeter E and regenerator G significantly, can easily by the combination densification of evaporimeter E and regenerator G.Baffle plate 92 also can be multi-blade type.
Baffle plate 93 preferably not only limits the flow of waste gas GH3, can also interdict.This is because, according to the concentration of the absorbing liquid in regenerator G, the situation of thinking temporarily to interdict completely also may be there is.Baffle plate 93 is set to interdict completely time, usual baffle plate 92 standard-sized sheet.
In addition, if arrange bypass flow path 91, then in appearance, side plate is not monolayer constructions will or veneer structure, and it is such to look like multi-ply construction.But the water-cooling wall that bypass flow path 91 is different from the multi-ply construction of interior pressure constructs.That is, when waste gas GH flows in exhaust flow path 60, low the arriving of pressure can unheeded degree.Therefore, side plate 54a, 54b, 74a, 74b can be set to monolayer constructions will or veneer structure this point, identical with the situation not being provided with bypass flow path 91.Only have in the arranged outside of side plate 54a, 54b, 74a, 74b of monolayer constructions will and do not need as pressure vessel by the bypass flow path 91 treated.
With reference to Fig. 6, be described as the exhaust gas entrance temperature of heat source gas and the relation produced between steam heat.In Fig. 6, transverse axis is the inlet temperature of the waste gas to heat utilization unit feeding, and the longitudinal axis is the heat of the steam produced in each device, adopts the temperature of the water vapour obtained in each device as parameter.The top is marked by "×" and solid line represents is the situation of the water vapour obtaining 180 DEG C in the sorption type heat pump of embodiments of the present invention.Below, respectively be from upper, to be marked by "×" and double dot dash line represents is the situation of the water vapour obtaining 140 DEG C in exhaust boiler, marked by " * " and dotted line represents is the situation of the water vapour obtaining 160 DEG C in exhaust boiler, what represented by " * " mark and solid line is the situation of the water vapour obtaining 180 DEG C in exhaust boiler.At this, produce steam heat by the heat when temperature 200 DEG C utilizes waste gas to 100 DEG C is set to 100, and relatively represent by numeral.
As known according to this line chart, if the inlet temperature of waste gas GH1 is 200 DEG C, want the water vapour S obtaining 180 DEG C, then in exhaust boiler, only obtain the heat of about 12, on the other hand, if use sorption type heat pump, obtain the heat of about 43.In addition, when the inlet temperature of waste gas GH1 is 180 DEG C, the heat that obviously can obtain in exhaust boiler is zero, and on the other hand, if use sorption type heat pump, can obtain the heat of about 32.
In addition with reference to the front view of Fig. 7, the example 1 being applicable to the regenerator G11 be used in present embodiment is described.In the figure, (a) is front view, and (b) is side view, and (c) is (a) A-A direction view, and (d) is the amplification sectional view 1 downspout 77 being extracted out expression.As already described, in regenerator G11, upper tube sheet 72, lower tube sheet 73, side plate 74a, 74b that upper header tank 75 is connected with lower header tank 76 are fenced up and form exhaust flow path 60.In this stream 60, flowing has the waste gas GH3 flowed into from evaporimeter E.The inflow entrance towards regenerator G11 of exhaust flow path 60, significantly opening.Preferably, do not reduce flow path cross sectional area from the evaporimeter E side of exhaust flow path 60 do not form a continuous print stream (in the figure 7, conveniently illustrating the situation that how much there is throttling stepwise) with not carrying out throttling.The outlet side of waste gas GH5 does not preferably carry out throttling too.This is to not bring stream to lose to waste gas as far as possible.
The absorbing liquid outlet 2a derived to absorbing liquid transfer pipeline 2 by absorbing liquid (concentrated solution) ALi-out is formed in upper header tank 75.Absorbing liquid outlet 2a is arranged at below compared with the liquid level by liquid surface level sensor L1 (with reference to Fig. 1) detection control.Absorbing liquid outlet 2a dives under liquid level, and thus as already described, what maintain between absorber A and regenerator G is liquid-tight.
The absorbing liquid entrance 3a imported from absorbing liquid transfer pipeline 3 by absorbing liquid (weak solution) ALi-in is formed in lower header tank 76.From the absorbing liquid ALi-in that absorbing liquid entrance 3a imports, being risen by heating in vertical heat-transfer pipe 71, arriving upper header tank 75.During absorbing liquid rises in vertical heat-transfer pipe 71, produce steam CS and be concentrated.The refrigerant vapour outlet 17a derived to refrigerant vapour transfer tube 17 by the steam CS of generation is formed in upper header tank 75.In the present embodiment, upper header tank 75 is also configured to the gas-liquid separator that the spittle of absorbing liquid and steam CS carried out being separated.Therefore, the space in upper header tank 75 is configured to enough capacity, so that the flow velocity of steam CS is reduced to the degree of enough carrying out gas-liquid separation.In addition, the not shown separator be made up of bending plate also can be set.
In the present embodiment, in a part for regenerator nest of tubes 70, also downspout 77 is provided with.The outside (exhaust gas side) of downspout 77 is covered by heat-insulating material 78.
With reference to Fig. 7, the effect of regenerator G11 is described.In vertical heat-transfer pipe 71, absorbing liquid ALi in pipe is heated by the waste gas GH3 outside pipe and seethes with excitement, become biphase gas and liquid flow, and blow out to upper header tank (gas-liquid separation chamber) 75, be separated into refrigerant vapour CS and absorbing liquid (concentrated solution) ALi.From lower header tank 76 to vertical heat-transfer pipe 71 underfeed absorbing liquid (weak solution) ALi.A part of the absorbing liquid Ali of gas-liquid separation chamber 75 returns lower header tank 76 via downspout 77, thus absorbing liquid Ali is circulated.Although downspout 77 is heated by the waste gas GH as thermal source owing to being positioned among regenerator nest of tubes 70, make to add heat by the heat-insulating material 78 outside downspout 77 and receive suppression.Therefore, even liquid phase state or containing steam, be also a small amount of.In downspout 77, if compare with the two-phase state in vertical heat-transfer pipe 71, then the apparent density of absorbing liquid Ali is comparatively large, and becomes sinking.That is, become the relation of (apparent density in the vertical heat-transfer pipe 71 of the apparent density > in downspout 77), therefore become sinking in downspout 77, in vertical heat-transfer pipe 71, become upwelling.
In addition, in the figure 7, illustrate the configuration of vertical heat-transfer pipe 71 with chessboard point, but also can be arranged to interconnected.In addition, illustrate vertical heat-transfer pipe 71 with light pipe (bear tube), but also part or all can be set to finned pipe.Heat transfer coefficient is more remarkable than hydraulic fluid side low at gas side, therefore by being set to band fin, can carry out the balance of inside and outside heat transfer coefficient well.As a result, compared with the situation being set to light pipe, the radical of heat-transfer pipe can be reduced significantly.
In the figure 7, downspout 77 to be arranged in regenerator nest of tubes 70, but can also as shown in Figure 8, to be arranged on regenerator nest of tubes 70 outside and then outside exhaust flow path 60.So, the absorbing liquid in downspout 77 is not heated by waste gas GH, and therefore the circulation of absorbing liquid Ali becomes better.
With reference to Fig. 8, the example 2 of regenerator is described.In the figure, (a) is front view, and (b) is side view.In this regenerator G12, further deflection plate 79A, 79B are set respectively in upper header tank 75 and lower header tank 76.In regenerator G12, absorbing liquid entrance 3a is arranged at the downstream of the flowing of waste gas GH in lower header tank 76, and absorbing liquid outlet 2a is arranged at the upstream side of the flowing of waste gas GH in upper header tank 75.
Deflection plate 79B configures more than one (being two in the drawings) in lower header tank 76, the downstream that this deflection plate 79B flows from waste gas GH, is splitting vertical heat-transfer pipe 71 with on the direction flowing into right angle of waste gas GH.Equally, deflection plate 79A configures more than one (being two in the drawings) in upper header tank 75, the downstream that this deflection plate 79A flows from waste gas GH, is splitting vertical heat-transfer pipe 71 with on the direction flowing into right angle of waste gas GH.
The height that the height of deflection plate 79A flows with being formed as that absorbing liquid (concentrated solution) Ali is overflowed from top.When arranging more than two, the downstream be highly formed as along with flowing from waste gas GH uprises successively towards upstream side.In illustrated example 2, deflection plate 79A and 79B is configured in position opposed up and down.In addition, downspout 77 with the region will split by more than one deflection plate 79A, mode that upper header tank 75 side carries out being connected with lower header tank 76 side, be arranged on outside exhaust flow path 60.
Form if so, then as shown by arrows in FIG., absorbing liquid Ali and waste gas GH becomes counter current flow on the whole.Therefore, it is possible to the MTD between the waste gas GH of heat source gas and absorbing liquid ALi is arranged to comparatively large, therefore compared with parallel flow or situation about just exchanging, can heat output be increased, can conduct heat efficiently.
In example 2, deflection plate 79A and deflection plate 79B is arranged on position completely opposed up and down, but the amount (not shown) of a vertical heat-transfer pipe more than 71 of also deflection plate 79B can being arranged to stagger to the upstream side that waste gas GH flows than deflection plate 79A.Form if so, then flow into the region adjacent with the upstream side in the region split by deflection plate 79A from a part for the absorbing liquid of lower header tank 76 rising.Form if so, even if then absorbing liquid Ali is not from the top overflow of deflection plate 79A, also can flow to the upstream side of waste gas GH successively.
In example 2, deflection plate 79A and deflection plate 79B is configured in position completely opposed up and down, downspout 77 is set to connect between the region opposed up and down of so segmentation, but also can be set to, intersect (The I hangs け) shape ground from the region of upper header tank 75 towards the neighboring region of lower header tank 76 and connect.Form if so, then rise to vertical heat-transfer pipe 71 from lower header tank 76 in initial region and be concentrated to a certain degree and reach the absorbing liquid ALi of upper header tank 75, it not the region being back to opposed lower header tank, but decline, therefore, it is possible to enter next concentration process to the region of adjacent lower header tank.In this case, also can be used together the downspout returned towards opposed region and staggered form downspout.
Inner at regenerator G, the equilibrium temperature change that the change in concentration that there is absorbing liquid Ali causes, and there is concentrated worry, therefore should be noted that the circulation of the absorbing liquid Ali in regenerator G.As example 1 or example 2, if arrange downspout 77 in regenerator G11, G12, then can produce the circulation of absorbing liquid between upper header tank 75 and lower header tank 76.On the other hand, in evaporimeter E, cold-producing medium CL evaporates and becomes steam CS, and therefore temperature is roughly certain, does not need as regenerator G, consider circulation.But also can downspout be set, promotes the flowing (upwelling) in heat-transfer pipe 51, realize the improvement of heat transfer.
Tube sheet can not only be set to common by evaporimeter E and regenerator G, and tank trunk can also be made to be integrated structure.
Below, with reference to accompanying drawing, the present invention third and fourth embodiment is described.In addition, identical with the situation of the first and second embodiments, in the various figures, give identical or similar Reference numeral for mutually identical or suitable part, and the repetitive description thereof will be omitted.
With reference to the flow graph of Figure 10, the structure of the sorption type heat pump of third embodiment of the invention is described.A () is the flow graph representing sorption type heat pump 100 entirety, (b) is the variation of the 3rd embodiment, shows the upstream side that possesses at the first evaporimeter E1 by the situation of heat source fluid to the heat exchanger B that make-up water directly heats.Sorption type heat pump 100 possesses the first sorption type heat pump portion 100-1 and the second sorption type heat pump portion 100-2.First sorption type heat pump portion 100-1 possesses: absorber A1, by absorbing liquid ALi (such as lithium bromide water solution) absorption refrigeration agent steam CS (cold-producing medium is such as water); Regenerator G1, makes refrigerant vapour CS evaporate from absorbing liquid Ali and carry out the regeneration of absorbing liquid Ali; Evaporimeter E1, utilizes refrigerant liquid CL to produce refrigerant vapour CS; And condenser C, make refrigerant vapour CS condensation become refrigerant liquid CL.The pressure of evaporimeter E1 is equal in practical with the pressure of absorber A1, and the pressure of regenerator G1 is equal in practical with the pressure of condenser C.
Second sorption type heat pump portion 100-2 and the first sorption type heat pump portion 100-1 identically possesses absorber A2, regenerator G2 and evaporimeter E2, and condenser uses the condenser C common with the first sorption type heat pump portion 100-1.Each structure member has substantially identical function in the first and second sorption type heat pump portions above.In addition, condenser also independently can possess in the first sorption type heat pump portion 100-1 and the second sorption type heat pump portion 100-2, if be set to common, and can the simplification of implement device.Illustrated is the situation of a common condenser.
Below, each structure member is explained to the first sorption type heat pump portion 100-1.For structure member corresponding in the first and second sorption type heat pump portions, suitably omit the description.In principle, in the first sorption type heat pump portion 100-1, the first place of three bit digital of Reference numeral is 1 to the Reference numeral of each structure member, and in the second sorption type heat pump portion 100-2, the first place of three bit digital of Reference numeral is 2, distinguishes.In absorber A1, A2, regenerator G1, G2 and evaporimeter E1, E2, after English alphabet, just add 1 or 2 distinguish.
Absorber A1 possesses: (1) absorbing liquid sprayer 122, and being transferred (supply) has absorbing liquid ALi as concentrated solution, is scattered by the absorbing liquid Ali that comes of transfer to absorber A1 inside; (2) by heating tube 123, there is make-up water W1 by transfer, by the absorbing liquid ALi as weak solution after absorption refrigeration agent steam CS, heat the make-up water W1 that transfer comes.The bottom of absorber A1 becomes the absorbing liquid retention portion enough accumulating absorbing liquid Ali.
Evaporimeter E1 possesses vertical heat-transfer pipe 151, this vertical heat-transfer pipe 151 has in internal flow transfers from condenser C the refrigerant liquid CL of coming by refrigerant liquid transfer tube 5, by heating this refrigerant liquid CL at the waste gas GH1 as heat source gas of flows outside, this refrigerant liquid CL is evaporated.In addition, possess liquid surface level sensor L101, this liquid surface level sensor L101 is arranged in the upper header tank 155 of evaporimeter E1, detects the liquid level of the refrigerant liquid CL in evaporimeter E1.Liquid surface level sensor L101, by control device 21 (common in first, second heat pump portion), regulates cold-producing medium supply valve V103, thus the liquid level of the cold-producing medium in evaporimeter E1 is maintained certain.In addition, cold-producing medium supply valve V103 also can not be set, and refrigerated medium pump P4 (common in first, second heat pump portion) is regulated the rotating speed of refrigerated medium pump for frequency-conversion and speed-regulation motor drives.In the drawings, refrigerated medium pump is common in first, second sorption type heat pump, but when separately maintaining the liquid level of evaporimeter E1, E2 regulating the rotating speed of refrigerated medium pump, refrigerated medium pump also can be arranged individually.This is because liquid level can produce up and down independently in evaporimeter E1 and evaporimeter E2.In sorption type heat pump 100, at the refrigerant vapour CS that evaporimeter E1 evaporates, be sent to absorber A1 via refrigerant vapour transfer tube 116.For the structure of evaporimeter E1, be described in detail with reference to Figure 12 ~ Figure 14.At this, waste gas is identical with the situation of the first embodiment, the second embodiment, typically in the factory, and the gas below 200 DEG C of degree make use of high-temperature part in various operation after.Also can be the waste gas from boiler, the gas before discharging from chimney after make use of high-temperature part.
Regenerator G1 possesses vertical heat-transfer pipe 171, this vertical heat-transfer pipe 171 has in internal flow transfers from absorber A1 the absorbing liquid ALi of coming via absorbing liquid transfer pipeline 103, by the waste gas GH4 as heat source gas in flows outside, this absorbing liquid ALi is heated, produce refrigerant vapour and this absorbing liquid ALi is concentrated.At this, waste gas GH4 is through evaporimeter E1, E2 and regenerator G2 and heat is utilized rear temperature have dropped waste gas to a certain degree.In addition, this absorbing liquid Ali is the absorbing liquid and the weak solution that reduce concentration in absorber A1 absorption refrigeration agent.In addition, possess liquid surface level sensor L102, this liquid surface level sensor L102 is arranged in the upper header tank 175 of regenerator G1, detects the liquid level of the absorbing liquid Ali in regenerator G1.Liquid surface level sensor L102 is regulated by control device 21 couples of solution pump P101, maintains the liquid level (in addition, also can replace the adjustment of solution pump P101 and arrange control valve) of the absorbing liquid in regenerator G1 thus.In the first sorption type heat pump portion 100-1, the absorbing liquid ALi after regenerator G1 concentrates, is sent to absorber A1 via absorbing liquid transfer tube 102.In addition, at the refrigerant vapour CS that regenerator G1 produces, condenser C is sent to via refrigerant vapour transfer tube 117 and refrigerant vapour transfer tube 17.At this, refrigerant vapour transfer tube 17 be with from the pipe transferring refrigerant vapour CS after refrigerant vapour transfer tube 217 afflux of regenerator G2 to condenser C.
And then, with reference to Figure 10 (a), the structure member of the second sorption type heat pump portion 100-2 is described.As mentioned above, for structure member common or suitable in first, second sorption type heat pump portion, suitably omit the description.
Absorber A2 possess using the absorbing liquid sprayer 222 that scatter inner as the absorbing liquid Ali of concentrated solution to absorber A2 and to make-up water W1 heat by heating tube 223.The bottom of absorber A2 becomes the absorbing liquid retention portion enough accumulating absorbing liquid Ali.
Evaporimeter E2 is configured in the downstream of evaporimeter E1 in exhaust flow path 60.Exhaust flow path 60 is the exhaust flow path being arranged in order evaporimeter E1, evaporimeter E2, regenerator G2 and regenerator G1.In addition, about the configuration of exhaust flow path 60 and each parts, describing in detail afterwards with reference to Figure 12.Evaporimeter E2 possesses vertical heat-transfer pipe 251, and this vertical heat-transfer pipe 251 has refrigerant liquid CL in internal flow, makes it evaporate by heating this refrigerant liquid CL at the waste gas GH2 of flows outside.At this, waste gas GH2 is that waste gas G1 is utilized by evaporimeter E1 and temperature reduces the waste gas to a certain degree.In addition, possess liquid surface level sensor L201, this is arranged in the upper header tank 255 of evaporimeter E2, detects the liquid level of the refrigerant liquid CL in evaporimeter E2.Liquid surface level sensor L201 is regulated by control device 21 couples of cold-producing medium supply valve V203, maintains the liquid level of the cold-producing medium in evaporimeter E2 thus.In evaporimeter E1, as already explained, also cold-producing medium supply valve V203 can not be set and make refrigerated medium pump P4 be that frequency-conversion and speed-regulation motor driving regulates refrigerated medium pump.Now, preferably with evaporimeter E1 with differently arranging refrigerated medium pump in addition.In sorption type heat pump 100, at the refrigerant vapour CS that evaporimeter E2 evaporates, be sent to absorber A2 via refrigerant vapour transfer tube 216.About the structure of evaporimeter E2, be described in detail with reference to Figure 12 ~ Figure 14 together with evaporimeter E1.
Regenerator G2, in exhaust flow path 60, is configured in the downstream of evaporimeter E2 and the upstream side of regenerator G1.Regenerator G2 possesses vertical heat-transfer pipe 271, this vertical heat-transfer pipe 271 has in internal flow transfers from absorber A2 the absorbing liquid ALi of coming via absorbing liquid transfer pipeline 203, by the waste gas GH3 as heat source gas in flows outside, this absorbing liquid ALi is heated, produce refrigerant vapour and this absorbing liquid ALi is concentrated.At this, waste gas GH3 is through evaporimeter E1 and evaporimeter E2 and heat is utilized, temperature have dropped the waste gas to a certain degree.In addition, this absorbing liquid Ali is the absorbing liquid and the weak solution that reduce concentration in absorber A2 absorption refrigeration agent.In addition, possess liquid surface level sensor L202, this liquid surface level sensor L202 is arranged in the upper header tank 275 of regenerator G2, detects the liquid level of the absorbing liquid Ali in regenerator G2.Liquid surface level sensor L202 is regulated by control device 21 couples of solution pump P201, maintains the liquid level (in addition, also can replace the adjustment of solution pump P201 and arrange control valve) of the absorbing liquid in regenerator G2 thus.In the second sorption type heat pump portion 100-2, the absorbing liquid ALi after regenerator G2 concentrates, is sent to absorber A2 via absorbing liquid transfer tube 202.In addition, at the refrigerant vapour CS that regenerator G2 produces, condenser C is sent to via refrigerant vapour transfer tube 217 and refrigerant vapour transfer tube 17.
Condenser C and sorption type heat pump 101 (with reference to Fig. 1) possess cooling tube 30 in the same manner, and in this cooling tube 30, flowing has cooling water WC, cools the refrigerant vapour CS being sent to condenser C from regenerator G1 and regenerator G2.The temperature of cooling water WC is such as 32 DEG C at the entrance of cooling tube 30, is 37 DEG C in outlet.
Sorption type heat pump 100 possesses: (1) gas-liquid separator 11; (2) make-up water transfer pipeline 7, is connected with gas-liquid separator 11, transfers make-up water W1 to gas-liquid separator 11; (3) make-up water transfer pipeline 6, is transferred make-up water W1 from gas-liquid separator 11 to absorber A1, A2 by heating tube 123,223; (4) make-up water transfer pipeline 110,210, makes make-up water W1 return from being transferred make-up water W1 by heating tube 123,223 to gas-liquid separator 11; And (5) steam supply pipeline 8, be connected with steam header box (not shown), the steam S produced at gas-liquid separator 11 (being such as 180 DEG C) is supplied to steam header box.
Sorption type heat pump 100 also possesses: (6) absorbing liquid transfer pipeline 102, is connected with absorber A1 regenerator G1, is transferred by the absorbing liquid Ali as concentrated solution after regenerator G1 regenerates to the absorbing liquid sprayer 122 of absorber A1; (6b) absorbing liquid transfer pipeline 202, is connected with absorber A2 regenerator G2, is transferred by the absorbing liquid Ali as concentrated solution after regenerator G2 regenerates to the absorbing liquid sprayer 222 of absorber A2; (7) absorbing liquid transfer pipeline 103, be connected with regenerator G1 absorber A1, the absorbing liquid Ali as weak solution accumulated by absorber A1 transfers to the regenerator lower header tank 176 of regenerator G1; (7b) absorbing liquid transfer pipeline 203, be connected with regenerator G2 absorber A2, the absorbing liquid Ali as weak solution accumulated by absorber A2 transfers to the regenerator lower header tank 276 of regenerator G2; And (8) refrigerant liquid transfer pipeline 5, condenser C is connected with evaporimeter E1, evaporimeter E2, the refrigerant liquid CL in condenser C condensation is transferred to evaporimeter E1 and evaporimeter E2.
Sorption type heat pump 100 also possesses: (9) solution (absorbing liquid) heat exchanger X101, via absorbing liquid transfer pipeline 102 to the absorbing liquid Ali as concentrated solution transferred by heated side and transfer via absorbing liquid between the absorbing liquid ALi as weak solution that pipeline 103 transfers to regenerator lower header tank 176 and carry out heat exchange; And (9b) solution (absorbing liquid) heat exchanger X201, via absorbing liquid transfer pipeline 202 to the absorbing liquid Ali as concentrated solution transferred by heated side and transfer via absorbing liquid between the absorbing liquid ALi as weak solution that pipeline 203 transfers to regenerator lower header tank 276 and carry out heat exchange.
Sorption type heat pump 100 is illustrated identical with in sorption type heat pump 101 (with reference to Fig. 1), also possesses heat exchanger X2, this heat exchanger X2, at heated side flowing waste heat source GH6, via make-up water transfer pipeline 7 to by heated side transfer make-up water W1, carries out heat exchange.Heat exchanger X2 represents with independently heat exchanger in the drawings, but preferably, the heat transfer part of heat exchanger X2 is arranged at the exhaust-gas flow be arranged in the middle of evaporimeter E1 inlet portion or evaporimeter E2 and regenerator G2.
In absorbing liquid transfer pipeline 102 and absorbing liquid transfer pipeline 202, be respectively arranged with solution pump P101 and solution pump P202, the absorbing liquid ALi respectively after regenerator G1 and regenerator G2 regenerates transfers respectively to absorber A1 and absorber A2 by solution pump P101 and solution pump P202.Solution pump P101 is arranged on the upstream side of solution heat exchanger X101, and solution pump P201 is arranged on the upstream side of solution heat exchanger X201.In refrigerant liquid transfer pipeline 5, be provided with the refrigerated medium pump P4 as cold-producing medium boosting component, the refrigerant liquid CL in condenser C condensation transfers to evaporimeter E1 and evaporimeter E2 by refrigerated medium pump P4.
In make-up water transfer pipeline 7, be identically provided with supply-water pump P12 with illustrated in sorption type heat pump 101 (with reference to Fig. 1), make-up water W1 transfers to gas-liquid separator 11 by supply-water pump P12.And then be provided with check-valves 37 in the downstream of the supply-water pump P12 of make-up water transfer pipeline 7, prevent make-up water W1 adverse current.Make-up water transfer pipeline 6 is provided with supply-water pump P13, make-up water W1 transfers from gas-liquid separator 11 to by heating tube 123,223 by supply-water pump P13, and then from being transferred make-up water W1 by heating tube 123,223 to gas-liquid separator 11, make-up water W1 is returned via make-up water transfer pipeline 110,210, thus make-up water W1 is circulated.
In refrigerant liquid transfer pipeline 5, be respectively arranged with cold-producing medium supply valve V103, V203 in the downstream of refrigerated medium pump P4, this cold-producing medium supply valve V103, V203 flow to the refrigerant liquid CL transferred towards evaporimeter lower header tank 156,256 adjusts.
Gas-liquid separator 11 is identical with the explanation in sorption type heat pump 101 (with reference to Fig. 1), therefore not repeat specification.
Supplying temperature as the waste gas GH1 of heat source gas is such as 200 DEG C.To the waste gas GH1 that evaporimeter E1 supplies, become waste gas GH2 at evaporimeter E1 by capturing heat and flow into evaporimeter E2, become the waste gas GH3 of about 150 DEG C of temperature by capturing heat at evaporimeter E2, and then flow into regenerator G2, being become waste gas GH4 at this by capturing heat and flow into regenerator G1, being discharged to be become the waste gas GH5 of about 100 DEG C by capturing heat at regenerator G1 after.
As already described, respectively the waste gas supplied to evaporimeter E1 is called GH1, the waste gas supplied to evaporimeter E2 through evaporator E1 is called GH2, the waste gas supplied to regenerator G2 through evaporator E2 is called GH3, the waste gas flowed into regenerator G1 through regenerator G2 is called GH4, the waste gas of discharging through regenerator G1 is called GH5.In addition, not need heat source gas to be distinguished as when the gas of each several part flowing or master process heat source gas time, only call with the Reference numeral of GH.
The preheating of make-up water W1, the high-temperature gas played till the gas GH3 of the pars intermedia of evaporimeter E2 and regenerator G2 preferably by the supply side from the such heat source gas of waste gas carries out.Or, although not shown, but also can be undertaken by the heat exchanger utilizing the absorbing liquid of the entrance supplied to regenerator G to carry out heating, also can be undertaken by the heat exchanger utilizing the refrigerant vapour produced at evaporimeter E1 or evaporimeter E2 to carry out heating.
Sorption type heat pump 100 possesses control device 21.Liquid level signal (not shown) from the expression liquid level of liquid surface level sensor L101 is sent to control device 21, sends signal from control device 21 to the control valve of the flow of control refrigerant liquid CL and cold-producing medium supply valve V103.So, regulate to make the liquid level of evaporimeter E1 to become necessarily (but be simplified shown as control signal in the drawings directly send to cold-producing medium supply valve V103 from liquid surface level sensor L101) to the aperture of cold-producing medium supply valve V103.Relation between liquid surface level sensor L201 with cold-producing medium supply valve V203 is also identical.
Liquid level signal (not shown) from the expression liquid level of liquid surface level sensor L102 is sent to control device 21, be used for making liquid level keep the mode of certain level to control the control signal (not shown) of the flow of absorbing liquid Ali from control device 21 to driving the frequency-conversion and speed-regulation motor INV of solution pump P101 to send, thus regulate the rotating speed of frequency-conversion and speed-regulation motor INV, be controlled to and the liquid level of regenerator G1 is become necessarily (be simplified shown as in the drawings and directly send signal from liquid surface level sensor L102 to frequency-conversion and speed-regulation motor INV).Liquid surface level sensor L202 is also identical with the relation between solution pump P201.
The control device 21 of gas-liquid separator 11 is identical with the explanation in sorption type heat pump 101 (with reference to Fig. 1), therefore not repeat specification.
Pressure signal (in figure dotted line) from the expression pressure of pressure sensor P is sent to control device 21, the control signal (figure dotted line) of the quantity delivered being used for steam regulation S is sent from control device 21 to steam valve V1, thus the aperture of steam regulation valve V1, be controlled to and make the pressure of gas-liquid separator 11 become setting Pr1, this control method is also identical with sorption type heat pump 101 (with reference to Fig. 1).
Then, with reference to Figure 10 (a) and Figure 11, the effect of the 3rd embodiment is described.Figure 11 is the Dühring's diagram of the state representing absorbing liquid and cold-producing medium, and the longitudinal axis is refrigerant temperature, and transverse axis is solution (absorbing liquid) temperature.
First, the first sorption type heat pump portion 100-1 is described.From the absorbing liquid ALi as weak solution (state is the B12 position Figure 11) that absorber A1 discharges, transfer pipeline 103 by absorbing liquid and to transfer and through solution heat exchanger X101.This absorbing liquid Ali, through over-heat-exchanger X101, is cooled (state of cooled absorbing liquid Ali is the B18 position Figure 11) by what transfer from regenerator G1 to absorber A1 via absorbing liquid transfer pipe arrangement 102 as concentrated solution absorbing liquid ALi thus.Transferred to regenerator lower header tank 176 by the cooled absorbing liquid Ali of solution heat exchanger X101.
Absorbing liquid Ali is during flowing through in vertical tube 171 from the regenerator lower header tank 176 (state of absorbing liquid Ali is the B15 position in Figure 11) of regenerator G1, heated by waste gas GH4, the cold-producing medium that absorbing liquid Ali absorbs is evaporated to refrigerant vapour CS.So, the absorbing liquid Ali as concentrated solution be concentrated, regenerated, flows out from the absorbing liquid outlet 102a being arranged on regenerator upper header tank 175.In the upper header tank 175 of the regenerator G1 shown in Figure 10, the square hole represented by solid line is outlet 102a.In addition, connected dotted line represents outlet header box.
Become the absorbing liquid ALi (state is the B14 position in Figure 11) of concentrated solution, transfer to the absorbing liquid sprayer 122 of absorber A1 via absorbing liquid transfer pipeline 102.Boosted by solution pump P101 during via absorbing liquid transfer pipeline 102, afterwards in solution heat exchanger X101, heated (state via the absorbing liquid Ali of absorbing liquid transfer pipeline 102 is the B17 position in Figure 11) by the absorbing liquid ALi as weak solution transferred from absorber A1 to regenerator G1, then transfer to the absorbing liquid sprayer 122 of absorber A1.
In absorber A1, from the absorbing liquid ALi as concentrated solution (state of absorbing liquid Ali is the B16 position Figure 11) that absorbing liquid sprayer 122 scatters in absorber A1, be absorbed in the refrigerant vapour CS that evaporimeter E1 evaporates, utilize absorption heat to heat via by the make-up water W1 as heated medium of heating tube 123, and bottom absorber A1, accumulate absorbing liquid Ali (state of absorbing liquid Ali is the B12 position in Figure 11).
As mentioned above, solution pump P101 transfers from regenerator G1 to absorber A1 and makes the liquid level of the absorbing liquid Ali in regenerator G1 become the absorbing liquid Ali of necessarily such flow.Feeding amount is controlled by control device 21.By remaining necessarily by the liquid level of regenerator G1, that can guarantee between the absorber A1 that difference that refrigerant vapour is pressed is larger and regenerator G1 is liquid-tight.Except except the absorbing liquid be detained in regenerator G1, intrasystem absorbing liquid is mainly accumulated in the bottom of absorber A1.Therefore, the bottom of absorber A1 is configured to enough capacity of having for accumulating absorbing liquid.The outlet side of the pump P101 of absorbing liquid transfer pipeline 102 is provided with check-valves 139.In the operation process of heat pump 100, the pressure of the pressure ratio regenerator G1 of absorber A1 is high.Therefore, if heat pump 100 to be stopped, stopping by pump P101, if then absorbing liquid has accumulation will flow into from absorber A1 to regenerator G1.The reversion of pump P101 is prevented by check-valves 139.In addition, if stopped by heat pump 100, then the absorbing liquid ALi accumulated in absorber A1, A2, respectively flows through absorbing liquid transfer pipeline 103,203 and accumulates in regenerator G1, G2 respectively.Therefore, regenerator upper header tank 175,275 is respectively enough to the capacity that intrasystem absorbing liquid is accommodated.Accumulate in the absorbing liquid ALi in regenerator upper header tank 175,275 during stopping, when heat pump 100 starts, be sent to absorber A1, A2 by level control.Or, also before feeding waste gas GH, absorber A1, A2 can be sent in advance.
The refrigerant vapour CS evaporated at regenerator G1 is sent to condenser C via refrigerant vapour transfer tube 117,17.The refrigerant vapour CS being sent to condenser C to be cooled by the cooling water WC via cooling tube 30 and condensation becomes refrigerant liquid CL (state is the D1 position in Figure 11) at condenser C.The refrigerant liquid CL of condenser C is via refrigerant liquid transfer pipeline 5, and cooled dose of pump P4 boosts, and is sent to evaporimeter E1 after being controlled flow by cold-producing medium supply valve V103.
Be sent to the refrigerant liquid CL of evaporimeter E1, during flowing through from evaporimeter lower header tank 156 inside vertical heat-transfer pipe 151, heated by waste gas GH1 and evaporate (state of cold-producing medium is the D2 position in Figure 11).The refrigerant vapour CS of evaporation is sent to absorber A1 via refrigerant vapour transfer tube 116, absorbs at absorber A1 absorbed liquid ALi.
Cold-producing medium supply valve V103 is conditioned aperture by control device 21, adds spatter the amount of the refrigerant liquid CL transferred from condenser C to evaporimeter E1.That is, certain amount is become to the liquid level that the amount of refrigerant liquid CL of transfer adds and subtracts the refrigerant liquid CL making evaporimeter E1 accumulate.Carrying out such control is to carry out supply to the evaporation capacity of refrigerant liquid, and is to make refrigerated medium pump P4 not suction gas.Except the refrigerant liquid be detained at evaporimeter E1 and evaporimeter E2, the refrigerant liquid of entire system is accumulated bottom condenser C.Therefore, the enough capacity had for accumulating absorbing liquid are configured to bottom condenser C.If stopped by heat pump 100, then refrigerant liquid CL likely transfers pipeline 5 to the condenser C adverse current than evaporimeter E1, E2 low pressure from evaporimeter E1, E2 side that pressure is higher via refrigerant liquid.In order to avoid the reversion of the refrigerated medium pump P4 after this firm stopping, preferably check-valves 40 is set at the outlet side of refrigerated medium pump P4.Also can replace which and control device 21 is configured to, make when heat pump stops (if complete in level control, become opening when heat pump stops and adverse current can not be prevented) cold-producing medium supply valve V103, V203 become full cut-off.
The effect of the second sorption type heat pump portion 100-2 is also identical with the first sorption type heat pump portion 100-1.The first place of three bit digital of the Reference numeral of each parts is replaced with 2 from 1.At this, be described centered by difference.From the B22 position that the state of the absorbing liquid Ali as weak solution of absorber A2 discharge is Figure 11.By the B28 position that the state of the cooled absorbing liquid Ali of solution heat exchanger X201 is in Figure 11.
This absorbing liquid Ali is during flowing through in vertical tube 271 from the regenerator lower header tank 276 (state of absorbing liquid Ali is the B25 position in Figure 11) of regenerator G2, heated by waste gas GH3, the cold-producing medium that absorbing liquid Ali absorbs is evaporated to refrigerant vapour CS.The temperature of waste gas GH3 is higher than the temperature of the waste gas G202 utilized in regenerator G1.So, the absorbing liquid Ali as concentrated solution be concentrated, regenerated, flows out from the absorbing liquid outlet 202a arranged regenerator upper header tank 275.
The absorbing liquid ALi (state is the B24 position in Figure 11) becoming concentrated solution transfers to the absorbing liquid sprayer 222 of absorber A2.Heated by the absorbing liquid ALi as weak solution transferred from absorber A2 to regenerator G2 during this period, the state of absorbing liquid Ali is the B27 position in Figure 11.
The absorbing liquid ALi as concentrated solution (state of absorbing liquid Ali is the B26 position in Figure 11) scattered in absorber A2, be absorbed in the refrigerant vapour CS that evaporimeter E2 evaporates, utilize absorption heat to heat via by the make-up water W1 as heated medium of heating tube 223, and bottom absorber A2, accumulate absorbing liquid ALi (state of absorbing liquid Ali is the B22 position in Figure 11).
The effect of solution pump P201, control device 21, check-valves 239 is identical with the first sorption type heat pump portion 100-1, therefore omits the description.
At the refrigerant vapour CS that regenerator G2 evaporates, be sent to condenser C with after the refrigerant vapour CS afflux evaporated at regenerator 1.Condenser C is cooled, condensation becomes refrigerant liquid CL to refrigerant vapour CS.In the present embodiment, condenser C is common with the first sorption type heat pump portion 100-1, state on the Dühring's diagram of therefore Figure 11 is identical with the D1 position illustrated in the first sorption type heat pump portion 100-1 (is not same position when condenser is not common, but when employing the cooling water WC of the same terms, become the position roughly the same with D1.)。The refrigerant liquid CL of condenser C is sent to evaporimeter E2 by cold-producing medium supply valve V203 by controlling flow.
Be sent to the refrigerant liquid CL of evaporimeter E2, heated by waste gas GH2 during flowing through from evaporimeter lower header tank 256 inside vertical heat-transfer pipe 251 and evaporate (state of cold-producing medium is the D3 position in Figure 11).The refrigerant vapour CS of evaporation is sent to absorber A2, absorbs at absorber A2 absorbed liquid ALi.As mentioned above, evaporimeter E2 is configured in evaporimeter E1 downstream in exhaust flow path 60, and therefore the refrigerant evaporating temperature of evaporimeter E2 is lower than the refrigerant evaporating temperature of evaporimeter E1.
Cold-producing medium supply valve V203 is identical with the situation of the first sorption type heat pump portion 100-1 with the effect of control device 21, therefore omits the description.
In present embodiment described above, absorption cycle is provided with two circulations (also can be more than three).These two circulations correspond to the first sorption type heat pump portion 100-1 and the second sorption type heat pump portion 100-2.First sorption type heat pump portion 100-1 is configured to comprise absorber A1, evaporimeter E1, regenerator G1 and condenser C1, second sorption type heat pump portion 100-2 is configured to comprise absorber A2, evaporimeter E2, regenerator G2 and condenser C2 (common with condenser C1 in the third embodiment), in an exhaust flow path 60, from the upstream side of exhaust-gas flow and high temperature side, be arranged in order structure member and evaporimeter E1, evaporimeter E2, regenerator G2 and the regenerator G1 of each circulation.
When having more than the 3rd, namely n-th (N >=3) sorption type heat pump portion 100 ~ n, from waste gas GH flow upstream side, be arranged in order evaporimeter E1, evaporimeter E2 ... evaporimeter En, regenerator Gn ... regenerator G2 and regenerator G1.
In the Dühring's diagram of Figure 11, such as, when n=3, increase the circulation that A3 is positioned at the below of A2, G3 is positioned at G2 right is such.
If increase n, what can expand EGT utilizes scope.In addition, for the heat transfer area of the evaporimeter and regenerator that obtain equal performance (quantity of steam), can be arranged to less compared with the situation being less than 2 with n.
As shown in Figure 10 (b), as modified embodiment of the present embodiment, the heat exchanger B of direct generating steam also can be set.The waste gas GH that is arranged on like this is to be useful during waste gas GH0 more than the temperature of the direct generating steam of entrance side.At heat exchanger B, by waste gas GH0, make-up water W1 is directly heated, direct generating steam.In this situation as shown in the figure, the feeding path of waste gas is set to the order of B, E1, E2, G2 and G1.
The sorption type heat pump 100 of this present embodiment possesses: the first sorption type heat pump portion 100-1, is combined by evaporimeter E1 higher for evaporating temperature and the lower regenerator G1 of regeneration temperature; With the second sorption type heat pump portion 100-2, evaporimeter E2 low for evaporating temperature (than evaporimeter E1) and the high regenerator G2 of regeneration temperature (than regenerator G1) is combined; Two sorption type heat pump portions possess the condenser C of common condensation temperature.In other words, to using the waste gas of high temperature side generate the evaporimeter of temperature refrigerant vapor and use in the downstream of exhaust-gas flow low temperature side waste gas to make the regenerator of regeneration of absorption solution (boiling point is not too high, and therefore enrichment is lower) combine.This is the first sorption type heat pump portion 100-1.Therefore, it is possible to carry out the circulation of the low concentration side on the Dühring's diagram shown in Figure 11, the waste gas of 200 DEG C can be utilized to obtain the water vapour of 180 DEG C.
Equally, the waste gas of low temperature side is to a certain degree reduced to serviceability temperature and the evaporimeter generating the refrigerant vapour of relative low temperature combines to make the regenerator of regeneration of absorption solution (boiling point is relatively high, enrichment is relatively high) with the waste gas of the side in the upstream side serviceability temperature of exhaust-gas flow relative high (lower but higher than the first regenerator G1 than the EGT used in the first evaporimeter E1).This is the second sorption type heat pump portion 100-2.Therefore, it is possible to carry out the circulation of the high concentration side on the Dühring's diagram shown in Figure 11, identical with the first sorption type heat pump portion 100-1, the waste gas of 200 DEG C can be utilized to obtain the water vapour of 180 DEG C.
Identical with sorption type heat pump 101 (with reference to Fig. 1), the make-up water W1 supplied to make-up water transfer pipeline 7 is transferred by the supply-water pump P12 backward gas-liquid separator 11 that boosts.The make-up water W1 discharged from supply-water pump P12 transfers to gas-liquid separator 11 after heat exchanger X2 is heated by waste gas GH6.
Identical with sorption type heat pump 101 (with reference to Fig. 1), the flow of the make-up water W1 supplied to gas-liquid separator 11 is adjusted to the make-up water W1 making to accumulate in gas-liquid separator 11 liquid level by being controlled by the rotating speed of control device 21 couples of supply-water pump P12 becomes certain.The liquid level of the make-up water W1 of gas-liquid separator 11 is adjusted to necessarily, be in order to gas-liquid separator 11 supply be supplied to as steam S and the corresponding amount of the make-up water W1 lost.
Be transferred to the make-up water W1 of gas-liquid separator 11, via make-up water transfer pipeline 6, by supply-water pump P13 boost after be sent to absorber A1, A2 by heating tube 123,223, heated by the absorption heat of the absorbing liquid Ali of absorption refrigeration agent steam CS at absorber A1, A2, produce steam S, be back to gas-liquid separator 11 via make-up water transfer pipeline 110,210, and steam is separated with liquid.The steam S produced is via steam supply pipeline 8, and the steam valve V1 controlled by being controlled device 21 is carried out Flow-rate adjustment in the mode making the pressure of gas-liquid separator 11 and become the first authorized pressure Pr1, supplies to steam header box (not shown).
Control in the mode making the pressure of gas-liquid separator 11 become authorized pressure Pr1, the control carried out to make the pressure of gas-liquid separator 11 become the pressure higher than the pressure of steam header box (not shown), the pressure of gas-liquid separator 11 is set to all the time than the pressure of the pressure height certain pressure of steam header box, the steam S that sorption type heat pump 100 can be made to produce to the supply of steam header box, can stably supply steam S to load (not shown) side all the time.This is also identical with sorption type heat pump 101 (with reference to Fig. 1).
By structure such above, the sorption type heat pump 100 of present embodiment, draws the heat that waste gas GH holds, heats the make-up water W1 as heated medium from evaporimeter E1 to absorber A1 and from evaporimeter E2 to absorber A2.In the present embodiment, make-up water W1 externally supplies become water vapour by heating after.
With reference to the stereogram of Figure 12 and the top view of Figure 13, to form third embodiment of the invention sorption type heat pump 100, the structure of evaporimeter E1, E2 and regenerator G2, G1 is described.Figure 12 is the stereogram observed from oblique upper after by respective upper header tank local incised notch evaporimeter E1, E2 and regenerator G2, G1.Figure 13 is to evaporimeter E1, E2 and regenerator G2, G1 top view from top view after respective upper header tank being removed.In detail in this figure, refrigerant liquid entrance and refrigerant vapour outlet, the absorbing liquid entrance of regenerator G2, G1 and the diagram of absorbing liquid outlet of evaporimeter E1, E2 is eliminated.
The evaporimeter E1 that the sorption type heat pump 100 of present embodiment possesses, possesses the upper tube sheet 152 of horizontal arrangement and the lower tube sheet 153 of configuration in parallel.Between upper tube sheet 152 and lower tube sheet 153, arranged perpendicular has many vertical heat-transfer pipes 151.Each vertical heat-transfer pipe 151 to be inserted in the hole worn respectively in upper tube sheet 152, lower tube sheet 153 and by expander after, guaranteed air-tightness by seal welding.Many vertical heat-transfer pipes 151, observe from tube axis direction rectangular area, are arranged as clathrate or staggered, form the nest of tubes of a group.In the inner side of such many vertical heat-transfer pipes 151, flowing has aqueous refrigerant liquid CL.That is, evaporimeter E1 possesses the structure of water-tube boiler.
The structure of evaporimeter E2 is except the downstream this point that the waste gas GH being positioned at evaporimeter E1 flows, identical with evaporimeter E1.That is, possess upper tube sheet 252 and lower tube sheet 253, between two tube sheets, be configured with many vertical heat-transfer pipes 251.Evaporimeter E2 and evaporimeter E 1 identically possesses the structure of water-tube boiler.
Equally, the regenerator G1 that the sorption type heat pump 100 of present embodiment possesses, possesses the upper tube sheet 172 of horizontal arrangement and the lower tube sheet 173 of configuration in parallel.Between upper tube sheet 172 and lower tube sheet 173, arranged perpendicular has many vertical heat-transfer pipes 171.Each vertical heat-transfer pipe 171 to be inserted in the hole worn respectively in upper tube sheet 172, lower tube sheet 173 and by expander after, guaranteed air-tightness by seal welding.Many vertical heat-transfer pipes 171 are observed from tube axis direction rectangular area, are arranged as clathrate or staggered, form the nest of tubes of a group.In the inner side of such many vertical heat-transfer pipes 171, flowing has absorbing liquid ALi.That is, regenerator G possesses the structure of water-tube boiler.
The structure of regenerator G2 is except being positioned at the upstream side that flows by waste gas GH than regenerator G1 and except the downstream this point being positioned at evaporimeter E2, identical with regenerator G1.That is, possess upper tube sheet 272 and lower tube sheet 273, between two tube sheets, be configured with many vertical heat-transfer pipes 271.Regenerator G2 and regenerator G1 identically possesses the structure of water-tube boiler.
In the sorption type heat pump 100 of present embodiment, the upper tube sheet 152,252 of evaporimeter E1, E2 and the upper tube sheet 172,272 of regenerator G1, G2 are formed by one tube sheet, and the lower tube sheet 173,273 of the lower tube sheet 153,253 of evaporimeter E1, E2 and regenerator G1, G2 is formed by one tube sheet.Evaporimeter E1, E2 and regenerator G2, G1, owing to being heated by common thermal source and waste gas GH, arrange therefore, it is possible to adjacent, are formed, thus can manufacture efficiently by a plate of one.Between evaporimeter nest of tubes 150,250 and regenerator nest of tubes 270,170, as long as the header box of evaporimeter E1, E2 and regenerator G2, G1 can be formed, then preferably configure as closely as possible.Or, as long as the baffle plate as flowing limiting member being configured to down to illustrate can be inserted, then preferably configure as closely as possible.By closely configuring, waste gas GH stream can be prevented invalidly elongated, the flow losses of waste gas GH can be suppressed.
In addition, above tube sheet also separately can be formed in each evaporimeter, regenerator.In addition, also can be common in evaporimeter E1 and evaporimeter E2, common in regenerator G2 and regenerator G1.This is because, when plant bulk is larger, from the view point of manufacture and carrying, sometimes preferably split.
Be configured at the sorption type heat pump 100 of present embodiment, in evaporimeter E1, E2 outside with regenerator G2, G1 many vertical heat-transfer pipes 151,251,271,171 separately, flow crossingly with this vertical heat-transfer pipe 151 grade and have waste gas GH1, GH2, GH3, GH4, and combustion gas GH5.Between the upper tube sheet 152,252 and lower tube sheet 153,253 of evaporimeter E1, E2, between the upper tube sheet 272,172 of regenerator G2, G1 and lower tube sheet 273,173, be formed with the stream 60 of waste gas GH.In the present embodiment, waste gas GH flows via stream 60 and vertical right angle intersection such as heat-transfer pipe 151 grade.Vertical heat-transfer pipe 151 grade flows outside have waste gas GH and inside pipe flowing have refrigerant liquid CL, absorbing liquid Ali, therefore, it is possible to guarantee the stream 60 of waste gas GH significantly, the high speed of flow velocity can be avoided.
In addition, many vertical heat-transfer pipes 151,251,271,171 form evaporimeter nest of tubes 150,250 and regenerator nest of tubes 270,170 respectively in evaporimeter E1, E2 and regenerator G2, G1, and evaporimeter nest of tubes 150,250 and regenerator nest of tubes 270,170 arrange point-blank relative to the flowing of waste gas GH.What is called arranges point-blank and refers to, the stream 60 of waste gas GH is not the such multi-path of so-called two paths or three-way, but the configuration of ground, unipath.In other words, refer to when observing discharge side from the supply side of waste gas GH after evaporimeter nest of tubes 150,250 and regenerator nest of tubes 270,170 being removed, discharge side can be seen through through the stream 60 of waste gas GH from supply side.
Owing to arranging point-blank, therefore be the such gas of waste gas that the thermal capacity of per unit volume is less at thermal source, in order to obtain need heat and need to flow the heat source gas having very large volume flow time, can the pressure loss that flow resistance causes be suppressed lower.That is, the loss that corner loss or revolution cause can be reduced.Although easily become large for the power of the heat source gas flowing making waste gas such, can be suppressed less, can not energy-saving effect be weakened.Especially as in the present embodiment, waste gas GH is via evaporimeter E1, E2, these at least four nest of tubes flowings of regenerator G2, G1, and therefore stream loss easily becomes large, thus effect arranged in a straight line is fine.
As previously described above, in evaporimeter E1, E2 and regenerator G2, G1, upper tube sheet each other, lower tube sheet each other, also can can't help the tube sheet of one is respectively formed, and is arranged respectively to split.If be arranged to split, then the configuration of evaporimeter E1, E2 and regenerator G2, G1 can decide according to situation alone respectively.When making each parts be set to split, it is also constant that evaporimeter nest of tubes 150,250 and regenerator nest of tubes 270,170 arrange this point point-blank relative to the flowing of waste gas GH1, GH2, GH3, GH4, GH5.In addition, when being arranged to split, preferably these parts configure as closely as possible.This is to suppress lower by the loss of the stream of waste gas.
In present embodiment, regenerator nest of tubes 270,170 relative to the flow arrangement of waste gas GH in the downstream of evaporimeter nest of tubes 150,250.
When thermal source is the such gas of waste gas, available temperature amplitude is larger.Such as with 200 DEG C of supplies, with 100 DEG C of discharges.In this case the temperature difference of 100 DEG C is utilized.Therefore, when being utilized as thermal source by waste gas, the mistake of the absorbing liquid that the gas that there is relatively-high temperature causes concentrates, the danger of crystallization.But owing to regenerator nest of tubes 270,170 to be configured in the downstream of evaporimeter nest of tubes 150,250, therefore, waste gas GH reduces in evaporimeter E1, E2 temperature and to supply to regenerator G2, G1 afterwards to a certain degree.Therefore, it is possible to the surplus of the absorbing liquid suppressing the part of upstream side part, the in other words relatively-high temperature of supply waste gas GH to cause concentrates, the danger of crystallization.
And then, in the present embodiment, possess side plate 154a, 154b, 254a, 254b, 274a, 274b, 174a, 174b (with reference to Figure 13), evaporimeter nest of tubes 150,250 and regenerator nest of tubes 270,170 and extraneous gas interdict by this side plate 154a, 154b, 254a, 254b, 274a, 274b, 174a, 174b, cooperate and form the stream of waste gas GH with each tube sheet 152,153,252,253,272,273,172,173.Also can replace side plate 154a etc. and be set to water-cooling wall, but if be 250 DEG C of degree or it is following, typically be 200 DEG C of degree as waste gas, then can be made up of simple flat board (iron plate), become easy structure.That is, can not be the structure in interlayer collecting in multi-ply construction as water-cooling wall with the fluid of pressure, and monolayer constructions will or veneer structure can be become.In the sorption type heat pump 100 of present embodiment, evaporimeter E1, E2 and regenerator G2, G1 become the pressure vessel of the pressure of more than atmospheric pressure mostly.In this case, each upper header tank 155,255,275,175 and lower header tank 156,256,276,176 header box of evaporimeter (in the sorption type heat pump especially) are under pressure, but because side plate is not water-cooling wall but simple individual layer is dull and stereotyped, therefore, it is possible to easily carry out the correspondence of intensity.In addition, in the present embodiment, inside the header box of regenerator, may negative pressure be become, but be not water-cooling wall but simple individual layer is dull and stereotyped, therefore, it is possible to easily tackle external pressure due to side plate.
In addition, as already described, evaporimeter E1, E2 and regenerator G2, G1, in other words evaporimeter nest of tubes 150,250 and regenerator nest of tubes 270,170, arrange point-blank relative to the flowing of waste gas GH.This configuration can typically realize as follows: side plate 154a, 254a and side plate 274a, 174a be formed as one plane, side plate 154b, 254b and side plate 274b, 174b be formed as equally one plane, preferably respectively to be formed by single flat board, and, evaporimeter upper tube sheet 152,252 and regenerator upper tube sheet 272,172 be formed as one plane, evaporimeter lower tube sheet 153,253 and regenerator lower tube sheet 273,173 be formed as equally one plane, preferably respectively to be formed by single flat board.
The extraneous gas side of side plate 154a, 154b, 254a, 254b, 274a, 274b, 174a, 174b is preferably provided with heat-insulating material.Though temperature is not too high, this is to make available heat not be expelled to outside.And be the safety in order to human body.
And then, in the present embodiment, evaporimeter E1, E2 and regenerator G2, G1 arrange evaporimeter upper header tank 155,255 and regenerator upper header tank 275,175 in the mode covered the upper opening portion of respective nest of tubes 150,250,270,170, arrange evaporimeter lower header tank 156,256 (refrigerant liquid supply chamber) and regenerator lower header tank 276,176 (solution supply chamber) in the mode covered lower openings.Evaporimeter upper header tank 155,255 also can double as gas-liquid separation chamber.Form if so, then can realize the simplification constructed.
With reference to the top view of Figure 14, the combination of evaporimeter E1, E2 of using in four embodiment of the invention and regenerator G2, G1 is described.Figure 14 is each upper header tank dismounting by evaporimeter E1, E2 and regenerator G2, G1, to the top view of vertical heat-transfer pipe 151,251,271,171 from axis direction, i.e. top view.In the present embodiment, possess bypass flow path 91, this bypass flow path 91 in the stream 60 of the waste gas GH as heat source gas, from the end in evaporimeter nest of tubes 250 downstream, bypass is carried out to regenerator nest of tubes 270, waste gas GH is flowed to the downstream of above-mentioned regenerator nest of tubes 270.
Bypass flow path 91 a whole or part of waste gas GH2 or the waste gas GH3 after evaporimeter nest of tubes 250 is avoided the stream that regenerator nest of tubes 270 ground guides to its downstream.Be configured in the present embodiment, bypass flow path 91 is relative regenerator nest of tubes 170 also bypass and streams guided to its downstream by waste gas GH3.
At this, the end in so-called evaporimeter nest of tubes 250 downstream refers to, part, i.e. the waste gas GH2 in vertical heat-transfer pipe 251 downstream of waste gas GH flow direction most downstream become the part of waste gas GH3 after all evaporators nest of tubes 250, and then in other words, be preferably the space segment between evaporimeter nest of tubes 250 and regenerator nest of tubes 270, but can as shown in the figure, be also the part of waste gas GH2 after many vertical heat-transfer pipes of evaporimeter nest of tubes 250 upstream side.That is, also can be the part of the space segment comprised between evaporimeter nest of tubes 250 and regenerator nest of tubes 270, or part more by the upstream a little than this part.Now, the beginning of preferred bypass flow path 91 does not extend to regenerator nest of tubes 270.The object arranging bypass flow path 91 is to prevent the surplus of the absorbing liquid in regenerator G2 from concentrating and then crystallization.
If the initial point of bypass flow path 91 to be set to waste gas GH2 becomes waste gas GH3 part through all evaporators nest of tubes 250, then can utilize the high-temperature part of waste gas GH2 in evaporimeter E2 as much as possible, this is preferred from the viewpoint of heat utilization.But, even if bypass flow path 91 initial point to be set to the part of waste gas GH2 after the vertical heat-transfer pipe 251 of certain degree radical of the upstream side of evaporimeter nest of tubes 250, the heat of waste gas GH2 is also utilized in large quantities in evaporimeter E2, can improve the flexibility that device is formed.That is, the space segment between evaporimeter nest of tubes 250 and regenerator nest of tubes 270 can be formed shortlyer, can the densification of implement device, the reduction of flow path resistance.
The baffle plate 92 that bypass flow is limited is possessed in bypass flow path 91.This is because bypass flow path 91 is to prevent the surplus of the absorbing liquid Ali in regenerator G2 from concentrating and then crystallization and arrange the stream that bypass flow path shunts enough waste gas GH3.Shunt with Shangdi needed for not needing.Baffle plate 92 preferably can not only limit the flow of waste gas GH3, can also interdict.From the viewpoint of recuperation of heat, interdict completely when the absorbing liquid concentration preferably in regenerator G2 is not in deathtrap.
In addition, in fig. 14, bypass flow path 91 is illustrated as, and carries out bypass, but at least carry out bypass to regenerator G2 to the both sides of regenerator G2 and regenerator G1.The upstream side that regenerator G2 is positioned at waste gas causes the reason that the surplus of absorbing liquid concentrates, the possibility of crystallization is higher.
In this embodiment, the concentration detector DEN (with reference to Figure 10) that the concentration of the absorbing liquid Ali in regenerator G2 is detected preferably is possessed.If compared by regenerator G1 and regenerator G2, then as shown in Dühring's diagram (with reference to Figure 11), in regenerator G2, there is crystallization, superfluous concentrated possibility.Therefore, the concentrating capacity of regenerator G2 is preferably regulated when the exit concentration of regenerator G2 rises.Therefore, possess concentration detector DEN, answer the aperture of ground controllable register 92 with the absorbing liquid ALi relative concentration in regenerator G, the influx of the waste gas towards regenerator G2 is added and spatters.Concentration detector DEN is arranged on the highest position of absorbing liquid ALi concentration in regenerator G2, is arranged on typically in upper header tank 275.In addition, as shown in Figure 10, also can be arranged on the absorbing liquid transfer pipeline 202 guiding absorbing liquid Ali from upper header tank 275 to absorber A2.In this case, preferably as far as possible close to the position of regenerator G2.Concentration detector DEN is not limited to detector concentration being carried out to direct-detection, also can be the detector indirectly carrying out detecting.That is, also can be the detector that the density of the physical quantity suitable with concentration, such as absorbing liquid is detected.In this so-called concentration, it also can be the calculated value be associated with concentration.That is, concentration can be the value gone out according to density and temperature detection, also can be the value gone out according to velocity of sound and temperature detection, also can replace concentration and density based, proportion.In addition, also concentration can be inferred according to the relation between the solution temperature of regenerator outlet and the steam pressure (or dew point) of regenerator G2.That is, also can calculate according to the vapor-liquid equilibrium relationship of solution.Affect more by force because the steam pressure of regenerator or dew point produce cooling water temperature, therefore also can judge according to solution temperature and cooling water temperature the danger that concentrates.Supposition like this or calculating are also modes of Concentration Testing.
In this embodiment, preferably also between evaporimeter E2 and regenerator G2, furtherly, baffle plate 93 is set between evaporimeter nest of tubes 250 and regenerator nest of tubes 270.If possess bypass flow path 91 and baffle plate 92, although then because the flow path resistance of regenerator nest of tubes 270 (and regenerator nest of tubes 170) can make quite a large amount of waste gas GH3 flow to bypass flow path 91, the amplitude of accommodation can be increased by arranging baffle plate 93 further.Baffle plate 93 is multi-blade type, is formed as by main part the flat board that vertical or horizontal Ground Split becomes multiple, can rotate centered by the length direction central shaft of respective lengthwise or the flat board of growing crosswise.If become multi-blade type, then do not need to arrange the space between evaporimeter E2 and regenerator G2 significantly, can easily by the combination densification of evaporimeter E1, E2 and regenerator G2, G1.Baffle plate 92 also can be multi-blade type.
Baffle plate 93 preferably not only limits the flow of waste gas GH3, can also interdict.This is because, according to the concentration of the absorbing liquid in regenerator G, the situation of thinking temporarily to interdict completely also may be there is.Baffle plate 93 is set to interdict completely time, usual baffle plate 92 standard-sized sheet.
In addition, if arrange bypass flow path 91, then in appearance, side plate 274b, 174b are not monolayer constructions will or veneer structure, and it is such to look like multi-ply construction.But the water-cooling wall that bypass flow path 91 is different from the multi-ply construction of interior pressure constructs.That is, when waste gas GH flows in exhaust flow path 60, low the arriving of pressure can unheeded degree.Therefore, side plate 274b, 174b can be set to monolayer constructions will or veneer structure this point, identical with the situation not being provided with bypass flow path 91.Only have in the arranged outside of side plate 274b, 174b of monolayer constructions will and do not need as pressure vessel by the bypass flow path 91 treated.
Three, the 4th embodiment is also identical with first, second embodiment, according to experiment calculation, if the inlet temperature of waste gas GH1 is 200 DEG C, obtain the water vapour S of 180 DEG C, the heat then obtained in exhaust boiler is about 12, therewith for, if use this sorption type heat pump, then obtain the heat of about 43.In addition, when EGT is 180 DEG C, the heat obtained in exhaust boiler is zero, on the other hand, if use this sorption type heat pump, can obtain the heat (with reference to Fig. 6) of about 32.
In addition, in the 3rd, the 4th embodiment, can little than first, second embodiment for the heat transfer area (device size) obtaining equal performance (quantity of steam).
Evaporimeter E1, E2 and regenerator G2, G1, not only tube sheet is common, also tank body can be set to Construction integration.
Industrial applicibility
Sorption type heat pump of the present invention, especially utilizes when heating from waste gas such heat source gas recovery heat heated medium.
Sorption type heat pump of the present invention, utilizes when utilizing thermal source outlet temperature difference significantly, especially utilizes reclaiming when heat heats heated medium from the such heat source gas of waste gas.
Claims (9)
1. a sorption type heat pump, wherein,
This sorption type heat pump possesses:
Evaporimeter, is heated cold-producing medium by the heat source gas using 100 DEG C and this cold-producing medium is evaporated;
Absorber, absorbs the above-mentioned cold-producing medium after evaporation, utilizes absorption heat to heat heated medium; And
Regenerator, the absorbing liquid by above-mentioned heat source gas absorption refrigeration agent in above-mentioned absorber being reduced to concentration is heated, and makes this regeneration of absorption solution,
Above-mentioned evaporimeter has:
Evaporimeter upper tube sheet;
Evaporimeter lower tube sheet; And
Many vertical heat-transfer pipes, are arranged between above-mentioned evaporimeter upper tube sheet and evaporimeter lower tube sheet, and inner side flowing has aqueous above-mentioned cold-producing medium,
Above-mentioned regenerator has:
Regenerator upper tube sheet;
Regenerator lower tube sheet; And
Many vertical heat-transfer pipes, are arranged between above-mentioned regenerator upper tube sheet and regenerator lower tube sheet, and inner side flowing has above-mentioned absorbing liquid,
Be configured to the outside at above-mentioned many vertical heat-transfer pipes, flow has above-mentioned heat source gas crossingly with above-mentioned vertical heat-transfer pipe,
Above-mentioned many vertical heat-transfer pipes form evaporimeter nest of tubes and regenerator nest of tubes respectively in above-mentioned evaporimeter and above-mentioned regenerator, and above-mentioned evaporimeter nest of tubes and regenerator nest of tubes arrange point-blank relative to the flowing of above-mentioned heat source gas,
Above-mentioned regenerator nest of tubes, relative to the flowing of above-mentioned heat source gas, is configured in the downstream of above-mentioned evaporimeter nest of tubes.
2. sorption type heat pump as claimed in claim 1, wherein,
Above-mentioned regenerator upper tube sheet and above-mentioned evaporimeter upper tube sheet are formed by the plate of one,
Above-mentioned regenerator lower tube sheet and above-mentioned evaporimeter lower tube sheet are formed by the plate of one.
3. sorption type heat pump as claimed in claim 1 or 2, wherein,
This sorption type heat pump possesses:
Bypass flow path, in the stream of above-mentioned heat source gas from the end in above-mentioned evaporimeter nest of tubes downstream, carries out bypass to above-mentioned regenerator nest of tubes, and above-mentioned heat source gas is flowed to above-mentioned regenerator nest of tubes downstream; And
Flowing limiting member, limits the flowing of the above-mentioned heat source gas in above-mentioned bypass flow path.
4. sorption type heat pump as claimed in claim 3, wherein,
This sorption type heat pump possesses:
Flowing limiting member, in the stream of above-mentioned heat source gas, limits the flowing of above-mentioned heat source gas between above-mentioned evaporimeter nest of tubes and regenerator nest of tubes.
5. sorption type heat pump as claimed in claim 1 or 2, wherein,
Form regenerator upper header tank with comprising above-mentioned regenerator upper tube sheet, form regenerator lower header tank with comprising above-mentioned regenerator lower tube sheet, this sorption type heat pump possesses makes above-mentioned absorbing liquid drop to the downspout of above-mentioned regenerator lower header tank from above-mentioned regenerator upper header tank.
6. a sorption type heat pump, wherein,
This sorption type heat pump possesses:
First evaporimeter, is heated cold-producing medium by heat source fluid and this cold-producing medium is evaporated;
First absorber, is absorbed in the cold-producing medium after evaporation in above-mentioned first evaporimeter, utilizes absorption heat to heat heated medium;
First regenerator, is heated the absorbing liquid reducing concentration in above-mentioned first absorber absorption refrigeration agent by above-mentioned heat source fluid, makes this regeneration of absorption solution;
Second evaporimeter, is heated cold-producing medium by above-mentioned heat source fluid and this cold-producing medium is evaporated;
Second absorber, is absorbed in the cold-producing medium after evaporation in above-mentioned second evaporimeter, utilizes absorption heat to heat heated medium; And
Second reactivator, is heated the absorbing liquid reducing concentration in above-mentioned second absorber absorption refrigeration agent by above-mentioned heat source fluid, makes this regeneration of absorption solution,
Above-mentioned first evaporimeter, the second evaporimeter, Second reactivator and the first regenerator, configure successively from the upstream side of above-mentioned heat source fluid towards downstream in the stream that above-mentioned heat source fluid flows,
Above-mentioned heat source fluid is heat source gas,
Above-mentioned first evaporimeter and the second evaporimeter have respectively:
Evaporimeter upper tube sheet;
Evaporimeter lower tube sheet; And
Many vertical heat-transfer pipes, are arranged between above-mentioned evaporimeter upper tube sheet and evaporimeter lower tube sheet, and inner side flowing has aqueous above-mentioned cold-producing medium,
Above-mentioned first regenerator and Second reactivator have respectively:
Regenerator upper tube sheet;
Regenerator lower tube sheet; And
Many vertical heat-transfer pipes, are arranged between above-mentioned regenerator upper tube sheet and regenerator lower tube sheet, and inner side flowing has above-mentioned absorbing liquid,
Be configured to the outside at above-mentioned many vertical heat-transfer pipes, flow has above-mentioned heat source gas crossingly with above-mentioned vertical heat-transfer pipe,
Above-mentioned many vertical heat-transfer pipes are in above-mentioned first evaporimeter, above-mentioned second evaporimeter, above-mentioned Second reactivator and above-mentioned first regenerator, form the first evaporimeter nest of tubes, the second evaporimeter nest of tubes, Second reactivator nest of tubes and the first regenerator nest of tubes respectively, above-mentioned first evaporimeter nest of tubes, above-mentioned second evaporimeter nest of tubes, above-mentioned Second reactivator nest of tubes and above-mentioned first regenerator nest of tubes arrange point-blank relative to the flowing of above-mentioned heat source gas.
7. sorption type heat pump as claimed in claim 6, wherein,
This sorption type heat pump possesses:
Bypass flow path, in the stream of above-mentioned heat source gas from the end in above-mentioned second evaporimeter downstream, carries out bypass to above-mentioned Second reactivator, and above-mentioned heat source gas is flowed to the downstream of above-mentioned Second reactivator; And
Flowing limiting member, limits the flowing of the above-mentioned heat source gas in above-mentioned bypass flow path.
8. sorption type heat pump as claimed in claims 6 or 7, wherein,
Above-mentioned first absorber and the second absorber are configured to heat the water as above-mentioned heated medium and produce the water vapour of the pressure of more than atmospheric pressure, and this sorption type heat pump possesses the gas-liquid separator generated water vapour and adjoint water being carried out being separated.
9. sorption type heat pump as claimed in claims 6 or 7, wherein,
This sorption type heat pump possesses:
Heat exchanger, in the stream of above-mentioned heat source fluid, utilizes the heat of above-mentioned heat source fluid directly to produce water vapour at the upstream side of above-mentioned first evaporimeter.
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
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| JP2010112592A JP5676914B2 (en) | 2010-05-14 | 2010-05-14 | Absorption heat pump |
| JP2010112593A JP5552363B2 (en) | 2010-05-14 | 2010-05-14 | Absorption heat pump |
| JP112593/2010 | 2010-05-14 | ||
| JP112592/2010 | 2010-05-14 |
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| CN102242982A CN102242982A (en) | 2011-11-16 |
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| JP6084485B2 (en) * | 2012-04-06 | 2017-02-22 | 荏原冷熱システム株式会社 | Absorption heat pump and operation method of absorption heat pump |
| JP6111094B2 (en) * | 2012-04-06 | 2017-04-05 | 荏原冷熱システム株式会社 | Absorption heat pump |
| CN109458751B (en) * | 2018-12-27 | 2024-04-02 | 双良节能***股份有限公司 | On-line detection density hot water type lithium bromide absorption type low-temperature water chilling unit |
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| CN1405517A (en) * | 2001-08-09 | 2003-03-26 | 株式会社荏原制作所 | Absorbing-type refrigerating-heating apparatus and generator thereof |
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| JPS61211668A (en) * | 1985-03-15 | 1986-09-19 | 松下電工株式会社 | Dehumidifier |
| JPH08261600A (en) * | 1995-03-22 | 1996-10-11 | Asahi Eng Co Ltd | Recovering method for exhaust heat |
| JP2002098435A (en) * | 2000-09-22 | 2002-04-05 | Kawasaki Thermal Engineering Co Ltd | Absorption freezer |
| JP2003222434A (en) * | 2002-01-30 | 2003-08-08 | Ebara Corp | Regenerator for exhaust gas drive absorption water heater-chiller |
| JP2003222437A (en) * | 2002-01-31 | 2003-08-08 | Ebara Corp | Absorption refrigerating machine |
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| CN1405517A (en) * | 2001-08-09 | 2003-03-26 | 株式会社荏原制作所 | Absorbing-type refrigerating-heating apparatus and generator thereof |
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