CN107120869B - Petrochemical plant low-temperature waste heat recycling system and method based on absorption heat exchange - Google Patents
Petrochemical plant low-temperature waste heat recycling system and method based on absorption heat exchange Download PDFInfo
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- CN107120869B CN107120869B CN201710475902.4A CN201710475902A CN107120869B CN 107120869 B CN107120869 B CN 107120869B CN 201710475902 A CN201710475902 A CN 201710475902A CN 107120869 B CN107120869 B CN 107120869B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B30/00—Heat pumps
- F25B30/04—Heat pumps of the sorption type
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
- F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B30/00—Heat pumps
- F25B30/06—Heat pumps characterised by the source of low potential heat
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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
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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
- 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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- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P80/00—Climate change mitigation technologies for sector-wide applications
- Y02P80/10—Efficient use of energy, e.g. using compressed air or pressurized fluid as energy carrier
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Abstract
Disclosed is a petrochemical plant low-temperature waste heat recycling system and method based on absorption heat exchange, the system comprises an absorption heat pump assembly (1, 2, 3, 4), a solution pump (6), a refrigerant pump (7), a heat exchanger (5) and corresponding connecting pipelines, a primary side pipeline (8), a secondary side pipeline (9) and a tertiary side pipeline (10), wherein the primary side pipeline (8) is configured to allow a first low-temperature material with medium-low-temperature waste heat in the petrochemical plant to be used as a driving heat source in an evaporator (1) and a generator (3) in sequence; the secondary side pipeline (9) is configured to allow a second low-temperature material to be preheated in the petrochemical plant to be preheated by absorbing heat generated by condensation of low-pressure working medium steam in the condenser (4); the tertiary side pipeline (10) is configured to allow a third low-temperature material to be preheated in the petrochemical plant to be preheated and heated through medium-high-temperature heat generated by mixing the concentrated absorbent solution in the absorber (2) with the high-pressure working medium steam.
Description
Technical Field
The invention relates to recycling of low-temperature waste heat of a petrochemical plant, in particular to a system and a method for recycling low-temperature waste heat of a petrochemical plant based on absorption heat exchange.
Technical Field
The waste heat resource in petrochemical industry accounts for 17% -67% of the total fuel consumption, and the recyclable waste heat resource accounts for 60% of the total waste heat resource. The waste heat in petrochemical industry is of various kinds, and mainly comprises product waste heat, circulating cooling water waste heat, flue gas waste heat and the like. Waste heat in the petrochemical industry can be classified into the following categories according to its grade: 1) The temperature range of the high-grade waste heat is about 150-350 ℃; 2) The temperature range of the waste heat is about 70-150 ℃; 3) Low grade waste heat, the temperature range is about 30-70 ℃.
At present, after the development of energy conservation and emission reduction work and the matched construction of corresponding engineering for many years, the high-grade waste heat and most of medium-grade waste heat of petrochemical enterprises are basically recycled. The low-grade waste heat is not recycled due to the huge residual heat and great recycling difficulty and the lack of an effective economic recycling technology, and can only be discharged into the environment through a circulating cooling tower. For example, 70 ℃ gasoline at the bottom of a petrochemical plant stabilizer tower needs water cooling to 40 ℃, while part of the material needs preheating from 30 ℃ to 40 ℃ and preheating from 50 ℃ to 90 ℃, and a large amount of gas or low-pressure steam is consumed for preheating the part of the material due to the large amount of the material. Therefore, how to further recycle the low-temperature waste heat realizes the gradual utilization of waste heat resources in petrochemical plants and the energy saving and emission reduction effects, and has great significance.
Disclosure of Invention
In one aspect of the invention, a petrochemical plant low-temperature waste heat recycling system based on absorption heat exchange is provided, comprising absorption heat pump assemblies 1, 2, 3 and 4, a solution pump 6, a refrigerant pump 7, a heat exchanger 5 and corresponding connecting pipelines, wherein the absorption heat pump assemblies comprise an evaporator 1, an absorber 2, a generator 3 and a condenser 4, the system further comprises a primary side pipeline 8 of heat source materials, a secondary side pipeline 9 of materials to be preheated and a tertiary side pipeline 10 of materials to be preheated, wherein,
the primary side pipeline 8 of the heat source material sequentially passes through the evaporator 1 and the generator 3 and is configured to allow a first low-temperature material with medium-low-temperature waste heat in a petrochemical plant to be used as a driving heat source in the evaporator 1 and the generator 3 in sequence;
the secondary side pipeline 9 of the material to be preheated passes through the condenser 4 and is configured to allow the second low-temperature material to be preheated in the petrochemical plant to be preheated and heated by absorbing heat generated by condensation of low-pressure working medium steam in the condenser 4 and then to be conveyed into the second process pipeline of the petrochemical plant;
the third-time side pipeline 10 of the material to be preheated passes through the absorber 2 and is configured to allow the third low-temperature material to be preheated in the petrochemical plant to be preheated and heated by absorbing the medium-high-temperature heat generated by mixing the concentrated absorbent solution in the absorber 2 with the high-pressure working medium steam, and then to be conveyed into the third process pipeline of the petrochemical plant;
the evaporator 1 is configured to allow working medium water therein to absorb heat of the first low-temperature material as a driving heat source by evaporation and evaporate into the high-pressure working medium steam into the absorber 2;
said absorber 2 is configured to allow the concentrated absorbent solution therein to mix with said high pressure working fluid vapor to generate heat at a medium to high temperature, thereby preheating said third low temperature material in said tertiary side line 10 of material to be preheated and allowing the diluted absorbent solution to be delivered to said generator 3 through said heat exchanger 5;
the generator 3 is configured to allow the first cryogenic material in the primary side of heat source material line 8 to heat the diluted absorbent solution as a driving heat source, form low pressure working medium vapor and a concentrated absorbent solution, and allow the low pressure working medium vapor to be delivered into the condenser 4;
the solution pump 6 is configured to deliver the concentrated absorbent solution in the generator 3 to the absorber 2 through the exchanger 5;
the heat exchanger 5 is configured to exchange heat between the concentrated absorbent solution delivered by the generator 3 and the diluted absorbent solution delivered by the absorber 2;
the condenser 4 is configured to allow the low-pressure working medium steam from the generator 3 to be cooled by the second low-temperature material in the material secondary side pipeline 9 to be preheated, thereby condensing the low-pressure working medium steam into working medium water, and preheating and heating the second low-temperature material; and
the refrigerant pump 7 is configured to deliver the working fluid water in the condenser 4 into the evaporator 1.
In another aspect of the present invention, there is provided a petrochemical plant low temperature waste heat recovery and utilization method based on absorption heat exchange, the method being used for a petrochemical plant low temperature waste heat recovery and utilization system based on absorption heat exchange, the system including absorption heat pump components 1, 2, 3 and 4, a solution pump 6, a refrigerant pump 7, a heat exchanger 5 and corresponding connecting lines, the absorption heat pump components including an evaporator 1, an absorber 2, a generator 3 and a condenser 4, the system further including a primary heat source material side line 8, a secondary heat source material side line 9 and a tertiary heat source material side line 10, the primary heat source material side line 8 passing through the evaporator 1 and the generator 3 in sequence, the secondary heat source material side line 9 passing through the condenser 4, the tertiary heat source material side line 10 passing through the absorber 2, the method comprising:
allowing a first low-temperature material with medium-low temperature waste heat in a petrochemical plant to enter a primary side pipeline 8 of the heat source material and serve as a driving heat source in the evaporator 1, so that working medium water in the evaporator 1 absorbs heat of the first low-temperature material through evaporation and evaporates into high-pressure working medium steam to enter the absorber 2;
allowing a third low-temperature material to be preheated in the petrochemical plant to enter a third-side pipeline 10 of the material to be preheated and allowing the concentrated absorbent solution in the absorber 2 to be mixed with the high-pressure working medium steam to generate heat at medium and high temperatures, thereby preheating the third low-temperature material, then conveying the third low-temperature material into a third process pipeline of the petrochemical plant and allowing the diluted absorbent solution to be conveyed to the generator 3 through the heat exchanger 5;
allowing said first cryogenic material in said primary heat source material side line 8 to heat said diluted absorbent solution in said generator 3 as a driving heat source to form low pressure working fluid vapor and a concentrated absorbent solution, allowing said low pressure working fluid vapor to be delivered to said condenser 4;
delivering the concentrated absorbent solution in the generator 3 to the absorber 2 through the exchanger 5 by the solution pump 6;
exchanging heat by the heat exchanger 5 between the concentrated absorbent solution fed by the generator 3 and the diluted absorbent solution fed by the absorber 2;
allowing a second low-temperature material to be preheated in the petrochemical plant to enter a material secondary side pipeline 9 to be preheated, preheating and heating by absorbing heat generated by condensation of low-pressure working medium steam in the condenser 4, and then conveying the material to a second process pipeline of the petrochemical plant, and condensing the low-pressure working medium steam into working medium water; and
the refrigerant pump 7 delivers the working fluid water from the condenser 4 to the evaporator 1.
The technical scheme of the invention has the advantages that: the low-temperature waste heat which is difficult to utilize in the prior art in the petrochemical industry is utilized, the materials which need to be cooled in the petrochemical factory are used as driving heat sources, and the materials which need to be preheated are used as low-temperature heat sources, so that the original preheating energy consumption of the petrochemical factory is reduced or even replaced, and the gradual gradient utilization of the energy in the petrochemical factory is realized.
Drawings
Fig. 1 is a schematic structural diagram of a petrochemical plant low-temperature waste heat recovery and utilization system based on absorption heat exchange according to an embodiment of the present invention; and
fig. 2 is a flow chart of a petrochemical plant low-temperature waste heat recovery and utilization method based on absorption heat exchange according to an embodiment of the invention.
Detailed Description
Embodiments of the present invention are described in detail below with reference to the accompanying drawings. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention to those skilled in the art. It will be apparent, however, to one skilled in the art that the present invention may be practiced without some of these specific details. Furthermore, it should be understood that the invention is not limited to specific described embodiments. Rather, the invention can be considered to be implemented with any combination of the following features and elements, whether or not they relate to different embodiments. Thus, the following aspects, features, embodiments and advantages are merely illustrative and should not be considered elements or limitations of the claims except where explicitly set out in a claim.
Referring now to fig. 1, a schematic diagram of a low temperature waste heat recovery system 100 for a petrochemical plant based on absorption heat exchange according to an embodiment of the present invention is shown. As shown in fig. 1, the low temperature waste heat recovery and utilization system 100 of the petrochemical plant comprises absorption heat pump assemblies 1, 2, 3 and 4, a solution pump 6, a refrigerant pump 7, a heat exchanger 5 and corresponding connecting pipelines, wherein the absorption heat pump assemblies comprise an evaporator 1, an absorber 2, a generator 3 and a condenser 4, wherein the system 100 further comprises a primary side pipeline 8 of heat source materials, a secondary side pipeline 9 of materials to be preheated and a tertiary side pipeline 10 of materials to be preheated, wherein,
the primary side pipeline 8 of the heat source material sequentially passes through the evaporator 1 and the generator 3 and is configured to allow a first low-temperature material with medium-low-temperature waste heat in a petrochemical plant to be used as a driving heat source in the evaporator 1 and the generator 3 in sequence;
the secondary side pipeline 9 of the material to be preheated passes through the condenser 4 and is configured to allow the second low-temperature material to be preheated in the petrochemical plant to be preheated and heated by absorbing heat generated by condensation of low-pressure working medium steam in the condenser 4 and then to be conveyed into the second process pipeline of the petrochemical plant;
the third-time side pipeline 10 of the material to be preheated passes through the absorber 2 and is configured to allow the third low-temperature material to be preheated in the petrochemical plant to be preheated and heated by absorbing the medium-high-temperature heat generated by mixing the concentrated absorbent solution in the absorber 2 with the high-pressure working medium steam, and then to be conveyed into the third process pipeline of the petrochemical plant;
the evaporator 1 is configured to allow working medium water therein to absorb heat of the first low-temperature material as a driving heat source by evaporation and evaporate into the high-pressure working medium steam into the absorber 2;
said absorber 2 is configured to allow the concentrated absorbent solution therein to mix with said high pressure working fluid vapor to generate heat at a medium to high temperature, thereby preheating said third low temperature material in said tertiary side line 10 of material to be preheated and allowing the diluted absorbent solution to be delivered to said generator 3 through said heat exchanger 5;
the generator 3 is configured to allow the first cryogenic material in the primary side of heat source material line 8 to heat the diluted absorbent solution as a driving heat source, form low pressure working medium vapor and a concentrated absorbent solution, and allow the low pressure working medium vapor to be delivered into the condenser 4;
the solution pump 6 is configured to deliver the concentrated absorbent solution in the generator 3 to the absorber 2 through the exchanger 5;
the heat exchanger 5 is configured to exchange heat between the concentrated absorbent solution delivered by the generator 3 and the diluted absorbent solution delivered by the absorber 2;
the condenser 4 is configured to allow the low-pressure working medium steam from the generator 3 to be cooled by the second low-temperature material in the material secondary side pipeline 9 to be preheated, thereby condensing the low-pressure working medium steam into working medium water, and preheating and heating the second low-temperature material;
the refrigerant pump 7 is configured to deliver the working fluid water in the condenser 4 into the evaporator 1.
In some embodiments, the absorption heat pump assemblies 1, 2, 3, and 4 may be, for example, temperature rising absorption heat pump assemblies.
In some embodiments, the absorption heat pump assembly 1, 2, 3 and 4 may further comprise the solution pump 6, the refrigerant pump 7, the heat exchanger 5 and corresponding connecting lines.
In some embodiments, the absorption heat pump modules 1, 2, 3, 4, etc. may be included in an absorption heat pump. Of course, the absorption heat pump may also comprise other components.
In some embodiments, the absorbent may be a lithium bromide solution. In other embodiments, the absorbent may be other absorbents, such as ammonia, and the like.
The first cryogenic material may be any cryogenic or medium material with waste heat in a petrochemical plant, for example a cryogenic or medium temperature liquid or gas such as water, oil gas, gasoline, diesel, etc.
In some embodiments, the temperature of the first cryogenic material at the primary side hot material inlet of the primary side heat source material conduit 8 (i.e. before entering the evaporator 1) is around 70 ℃, such as 65-75 ℃, or 60-80 ℃, and the temperature at the primary side hot material outlet of the primary side heat source material conduit 8 (i.e. after exiting the generator 3) is around 40 ℃, such as 35-50 ℃, or 30-50 ℃. The first low temperature material leaving the primary side hot material outlet may be discharged or may be fed into a process line of a petrochemical plant for further use. The system 100 according to the embodiment of the present invention can preheat other materials to be preheated by using low-temperature or medium-temperature materials having waste heat in petrochemical plants, which are hardly utilized in the prior art, as a driving heat source, without consuming a large amount of heat sources such as gas or low-pressure steam, etc. as the driving heat source, thereby saving a large amount of energy and reducing carbon emissions.
The second cryogenic material may be any cryogenic material in a petrochemical plant that needs to be preheated to a medium or low temperature, for example a low or medium temperature liquid or gas such as water, oil gas, gasoline, diesel, etc.
In some embodiments, the temperature of the second cryogenic material at the secondary side preheating material inlet of the secondary side conduit 9 for material to be preheated (i.e., prior to entering the condenser 4) is about 30 ℃, such as 25-35 ℃, or 20-40 ℃, and the temperature at the secondary side preheating material outlet of the secondary side conduit 9 for material to be preheated (i.e., after exiting the condenser 4) is about 45 ℃, such as 40-50 ℃, or 35-55 ℃. The system 100 according to the embodiment of the present invention not only uses waste heat to properly preheat the low-temperature materials to be preheated in the petrochemical plant by using the low-temperature materials to be preheated as the condensing agent of the condenser 4, but also saves energy and capital by not using special cooling water, cooling towers, etc. to provide the condensing agent for the condenser 4 while ensuring the correct operation of the system.
The third cryogenic material may be any cryogenic material in a petrochemical plant that needs to be preheated to a medium or high temperature, for example a low or medium temperature liquid or gas such as water, oil gas, gasoline, diesel, etc.
In some embodiments, the third cryogenic material has a temperature of about 50 ℃, such as 45-55 ℃, or 40-60 ℃, upon entering the tertiary side pre-heat material inlet of the tertiary side line 10 of material to be pre-heated (i.e., prior to entering the absorber 2), and a temperature of about 90 ℃, such as about 85-95 ℃, or 80-100 ℃ upon exiting the tertiary side pre-heat material outlet of the tertiary side line 10 of material to be pre-heated (i.e., after exiting the absorber 2). The system 100 according to the embodiment of the present invention heats the low-temperature materials to be preheated to a higher temperature by using the heat of the low-temperature materials having waste heat in the petrochemical plant, thereby saving energy while satisfying the process requirements.
The low-temperature waste heat recovery system for petrochemical plants based on absorption heat exchange according to the embodiments of the present invention has been described above with reference to the accompanying drawings, it should be noted that the above description and illustrations are only examples and are not limiting of the present invention. In other embodiments of the invention, the system may have more, fewer, or different components, and the connections, inclusions, and functional relationships between the components may be different from those described and illustrated. For example, typically multiple components may be combined into one large component. As another example, the names of the various components are not limiting on the invention.
Referring now to fig. 2, which is a schematic flow chart of a petrochemical plant low temperature waste heat recovery and utilization method based on absorption heat exchange according to an embodiment of the present invention, the method is used for a petrochemical plant low temperature waste heat recovery and utilization system based on absorption heat exchange (such as the system 100 according to the embodiment of the present invention described above) comprising absorption heat pump assemblies 1, 2, 3 and 4, a solution pump 6, a refrigerant pump 7, a heat exchanger 5, and corresponding connecting lines, the absorption heat pump assemblies comprising an evaporator 1, an absorber 2, a generator 3, and a condenser 4, the system further comprising a primary heat source material side line 8, a secondary heat source material side line 9 to be preheated and a tertiary heat source material side line 10 to be preheated, the primary heat source material side line 8 passing through the evaporator 1 and the generator 3 in sequence, the secondary heat source material side line 9 to be preheated passing through the condenser 4, the tertiary heat source material side line 10 to be preheated passing through the absorber 2), the method comprises the steps of:
in step 201, a first low-temperature material with medium-low temperature waste heat in a petrochemical plant is allowed to enter a primary side pipeline 8 of the heat source material and is used as a driving heat source in the evaporator 1, so that working medium water in the evaporator 1 absorbs heat of the first low-temperature material through evaporation and is evaporated into high-pressure working medium steam to enter the absorber 2;
in step 202, allowing a third low-temperature material to be preheated in the petrochemical plant to enter the material to be preheated tertiary side pipeline 10, and allowing the concentrated absorbent solution in the absorber 2 to be mixed with the high-pressure working medium steam to generate heat at medium and high temperatures, so as to preheat the third low-temperature material, then conveying the third low-temperature material into a third process pipeline of the petrochemical plant, and allowing the diluted absorbent solution to be conveyed to the generator 3 through the heat exchanger 5;
at step 203, allowing the first cryogenic material in the primary side line 8 of the heat source material to heat the diluted absorbent solution in the generator 3 as a driving heat source to form low pressure working medium vapor and a concentrated absorbent solution, allowing the low pressure working medium vapor to be delivered to the condenser 4;
at step 204, the concentrated absorbent solution in the generator 3 is conveyed by the solution pump 6 to the absorber 2 through the exchanger 5;
at step 205, heat is exchanged by the heat exchanger 5 between the concentrated absorbent solution delivered by the generator 3 and the diluted absorbent solution delivered by the absorber 2;
in step 206, allowing the second low-temperature material to be preheated in the petrochemical plant to enter the material secondary side pipeline 9 to be preheated, preheating and heating by absorbing heat generated by condensing low-pressure working medium steam in the condenser 4, and then conveying the material to a second process pipeline of the petrochemical plant, and condensing the low-pressure working medium steam into working medium water;
in step 207, the working fluid water in the condenser 4 is fed by the coolant pump 7 into the evaporator 1.
In some embodiments, the first cryogenic material in the primary side line 8 of the heat source material has a temperature of 60-80 ℃ when entering the evaporator 1 and a temperature of 30-50 ℃ when exiting the generator 3;
the temperature of the second low-temperature material in the secondary side pipeline 9 of the material to be preheated is 20-40 ℃ when entering the condenser 4, and the temperature of the second low-temperature material is 35-55 ℃ when leaving the condenser 4; and
the temperature of the third low-temperature material in the tertiary side pipeline 10 of the material to be preheated is 40-60 ℃ when entering the absorber 2, and 80-100 ℃ when leaving the absorber 2.
The method for recycling low-temperature waste heat of petrochemical plants according to the embodiments of the present invention has been described above with reference to the accompanying drawings, and it should be noted that the above description and illustrations are only examples and are not limiting of the present invention. In other embodiments of the invention, the method may have more, fewer, or different steps, and the order, inclusion, and functional relationship between steps may be different than that described and illustrated.
The invention provides a technical scheme for reasonably and gradiently utilizing low-temperature waste heat materials of petrochemical plants aiming at the distribution characteristics and waste heat grades of waste heat resources in the process flow of petrochemical industry. The technical scheme of the invention has the advantages that: the low-temperature waste heat which is difficult to utilize in the prior art in the petrochemical industry is utilized, the materials which need to be cooled in the petrochemical factory are used as driving heat sources, and the materials which need to be preheated are used as low-temperature heat sources, so that the original preheating energy consumption of the petrochemical factory is reduced or even replaced, and the gradual gradient utilization of the energy in the petrochemical factory is realized.
It should be pointed out that the technical scheme of the invention is not limited to petrochemical industry, and can be applied to preheating circulation of other industrial materials, thereby providing a new direction for low-temperature waste heat recovery and utilization.
Although the present invention has been disclosed above by way of example, the present invention is not limited thereto. Various changes and modifications may be made by one skilled in the art without departing from the spirit and scope of the invention, which is to be limited only by the language of the claims and the equivalents thereof.
Claims (4)
1. The utility model provides a petrochemical plant low temperature waste heat recovery utilizes system based on absorption heat transfer, includes absorption heat pump subassembly (1, 2, 3, 4), solution pump (6), coolant pump (7), heat exchanger (5) and corresponding connecting tube way, absorption heat pump subassembly includes evaporimeter (1), absorber (2), generator (3) and condenser (4), and wherein, this system still includes heat source material primary side pipeline (8), needs preheat material secondary side pipeline (9) and needs preheat material tertiary side pipeline (10), wherein,
the primary side pipeline (8) of the heat source material sequentially passes through the evaporator (1) and the generator (3) and is configured to allow a first low-temperature material with medium-low-temperature waste heat in a petrochemical plant to be used as a driving heat source in the evaporator (1) and the generator (3) in sequence;
the secondary side pipeline (9) of the material to be preheated passes through the condenser (4) and is configured to allow a second low-temperature material to be preheated in the petrochemical plant to be preheated and heated by absorbing heat generated by condensation of low-pressure working medium steam in the condenser (4) and then to be conveyed into a second process pipeline of the petrochemical plant;
the material to be preheated tertiary side pipeline (10) passes through the absorber (2) and is configured to allow a third low-temperature material to be preheated in the petrochemical plant to be preheated and heated by absorbing medium-high-temperature heat generated by mixing the concentrated absorbent solution in the absorber (2) with high-pressure working medium steam, and then conveying the medium-high-temperature heat to a third process pipeline of the petrochemical plant;
the evaporator (1) is configured to allow working medium water therein to absorb heat of the first low-temperature material as a driving heat source by evaporation and evaporate into the high-pressure working medium steam into the absorber (2);
the absorber (2) is configured to allow the concentrated absorbent solution therein to be mixed with the high pressure working medium steam to generate heat of medium and high temperature, thereby preheating the third low temperature material in the tertiary side pipeline (10) of the material to be preheated, and allowing the diluted absorbent solution to be conveyed to the generator (3) through the heat exchanger (5);
-the generator (3) is configured to allow the first low temperature material in the primary side of heat source material piping (8) to heat the diluted absorbent solution as a driving heat source, forming low pressure working medium vapour and a concentrated absorbent solution, and to allow the low pressure working medium vapour to be fed into the condenser (4);
-the solution pump (6) is configured to deliver the concentrated absorbent solution in the generator (3) to the absorber (2) through the exchanger (5);
-the heat exchanger (5) is configured to exchange heat between the concentrated absorbent solution delivered by the generator (3) and the diluted absorbent solution delivered by the absorber (2);
the condenser (4) is configured to allow the low-pressure working medium steam from the generator (3) to be cooled by the second low-temperature material in the material secondary side pipeline (9) to be preheated, thereby condensing the low-pressure working medium steam into working medium water, and simultaneously preheating the second low-temperature material to be heated; and
the coolant pump (7) is configured to feed the working fluid water in the condenser (4) into the evaporator (1).
2. The system of claim 1, wherein,
the temperature of the first low-temperature material in the primary side pipeline (8) of the heat source material is 60-80 ℃ when entering the evaporator (1) and 30-50 ℃ when leaving the generator (3);
the temperature of the second low-temperature material in the secondary side pipeline (9) of the material to be preheated is 20-40 ℃ when entering the condenser (4), and the temperature of the second low-temperature material is 35-55 ℃ when leaving the condenser (4); and
the temperature of the third low-temperature material in the tertiary side pipeline (10) of the material to be preheated is 40-60 ℃ when entering the absorber (2), and the temperature of the third low-temperature material is 80-100 ℃ when leaving the absorber (2).
3. A petrochemical plant low temperature waste heat recycling method based on absorption heat exchange, the method is used for a petrochemical plant low temperature waste heat recycling system based on absorption heat exchange, the system comprises an absorption heat pump assembly (1, 2, 3, 4), a solution pump (6), a refrigerant pump (7), a heat exchanger (5) and corresponding connecting pipelines, the absorption heat pump assembly comprises an evaporator (1), an absorber (2), a generator (3) and a condenser (4), the system further comprises a primary side pipeline (8) of heat source material, a secondary side pipeline (9) of material to be preheated and a tertiary side pipeline (10) of material to be preheated, the primary side pipeline (8) of heat source material sequentially passes through the evaporator (1) and the generator (3), the secondary side pipeline (9) of material to be preheated passes through the condenser (4), and the tertiary side pipeline (10) of material to be preheated passes through the absorber (2), the method comprises:
allowing a first low-temperature material with medium-low temperature waste heat in a petrochemical plant to enter a primary side pipeline (8) of the heat source material and be used as a driving heat source in the evaporator (1), so that working medium water in the evaporator (1) absorbs heat of the first low-temperature material through evaporation and evaporates into high-pressure working medium steam to enter the absorber (2);
allowing a third low-temperature material to be preheated in the petrochemical plant to enter a third-time side pipeline (10) of the material to be preheated and allowing a concentrated absorbent solution in the absorber (2) to be mixed with the high-pressure working medium steam to generate heat at medium and high temperatures, so as to preheat the third low-temperature material, then conveying the third low-temperature material into a third process pipeline of the petrochemical plant and allowing a diluted absorbent solution to be conveyed to the generator (3) through the heat exchanger (5);
allowing the first low temperature material in the primary side line (8) of the heat source material to heat the diluted absorbent solution in the generator (3) as a driving heat source to form low pressure working medium steam and a concentrated absorbent solution, allowing the low pressure working medium steam to be conveyed into the condenser (4);
-delivering the concentrated absorbent solution in the generator (3) to the absorber (2) through the exchanger (5) by the solution pump (6);
exchanging heat by the heat exchanger (5) between the concentrated absorbent solution delivered by the generator (3) and the diluted absorbent solution delivered by the absorber (2);
allowing a second low-temperature material to be preheated in the petrochemical plant to enter a material secondary side pipeline (9) to be preheated, preheating and heating by absorbing heat generated by condensation of low-pressure working medium steam in the condenser (4), and then conveying the material to a second process pipeline of the petrochemical plant, and condensing the low-pressure working medium steam into working medium water; and
the refrigerant pump (7) delivers the working fluid water from the condenser (4) to the evaporator (1).
4. The method of claim 3, wherein,
the temperature of the first low-temperature material in the primary side pipeline (8) of the heat source material is 60-80 ℃ when entering the evaporator (1) and 30-50 ℃ when leaving the generator (3);
the temperature of the second low-temperature material in the secondary side pipeline (9) of the material to be preheated is 20-40 ℃ when entering the condenser (4), and the temperature of the second low-temperature material is 35-55 ℃ when leaving the condenser (4); and
the temperature of the third low-temperature material in the tertiary side pipeline (10) of the material to be preheated is 40-60 ℃ when entering the absorber (2), and the temperature of the third low-temperature material is 80-100 ℃ when leaving the absorber (2).
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