CN215176152U - Absorption type refrigerating system utilizing acetic anhydride production reaction heat - Google Patents
Absorption type refrigerating system utilizing acetic anhydride production reaction heat Download PDFInfo
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- CN215176152U CN215176152U CN202121445235.3U CN202121445235U CN215176152U CN 215176152 U CN215176152 U CN 215176152U CN 202121445235 U CN202121445235 U CN 202121445235U CN 215176152 U CN215176152 U CN 215176152U
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- heat exchanger
- ammonia
- liquid
- acetic anhydride
- absorption refrigeration
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A30/00—Adapting or protecting infrastructure or their operation
- Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
- Y02A30/274—Relating to heating, ventilation or air conditioning [HVAC] technologies using waste energy, e.g. from internal combustion engine
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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
- Y02B30/625—Absorption based systems combined with heat or power generation [CHP], e.g. trigeneration
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- Sorption Type Refrigeration Machines (AREA)
Abstract
The utility model relates to an utilize absorption refrigeration system of acetic anhydride production reaction heat, relate to low-grade waste heat refrigeration technology field, including absorption refrigeration subassembly, tail gas absorbing device, waste heat exchanger is used for utilizing acetic anhydride production reaction heat and circulating water to carry out the heat transfer, absorption refrigeration subassembly is arranged in carrying again to waste heat exchanger and utilizing the difference in temperature that produces among the circulating water heat transfer cooling process to prepare liquid ammonia in order to accomplish the heat transfer cooling refrigeration process with fresh methyl alcohol after the circulating water heat transfer cooling after with waste heat exchanger heat transfer, and tail gas absorbing device is arranged in utilizing the organic component of low temperature state methyl alcohol recovery acetic anhydride production tail gas. The utility model discloses an absorption refrigeration utilizes acetic anhydride production reaction heat to prepare production recovery with cold as the drive heat source, replaces traditional ice maker, reaches the purpose of practicing thrift the electric energy, through the recovery to the reaction heat, has fully realized energy saving and consumption reduction.
Description
Technical Field
The utility model relates to a low-grade waste heat refrigeration technology field, concretely relates to utilize absorption refrigeration system of acetic anhydride production reaction heat.
Background
The methyl acetate carbonylation method is characterized in that methyl acetate, methanol and carbon monoxide undergo carbonylation reaction in the presence of methyl iodide and rhodium catalyst to generate acetic anhydride and co-produce acetic acid. The temperature of acetic anhydride reactant is about 150 ℃ and 180 ℃, the reaction heat is removed by adopting external circulation heat exchange, and hot water at 160 ℃ is prepared; the low-pressure tail gas of the light component removal tower in the rectification process enters an absorption tower, fresh methanol is cooled by utilizing liquid ammonia at the low temperature of-15 ℃ prepared by a screw ice machine, then the fresh methanol enters the absorption tower, and the main organic components such as methyl iodide and the like in the tail gas are absorbed by the low-temperature methanol and then recycled. When the low-temperature refrigerant of-15 ℃ is prepared, an electrically-driven screw ice machine is adopted, so that the power consumption is high, the production reaction temperature is high, the cooling water is used for cooling, and the production energy consumption is high. Therefore, an absorption refrigeration system utilizing the reaction heat of acetic anhydride production is proposed.
Disclosure of Invention
The utility model aims at providing an utilize absorption refrigeration system of acetic anhydride production reaction heat in order to solve above-mentioned problem, utilize methyl acetate carbonylation method reaction heat to prepare liquid ammonia for absorption refrigeration subassembly lasts the heat supply to replace screw rod ice maker to practice thrift the energy consumption.
The utility model discloses a following technical scheme realizes above-mentioned purpose:
an absorption refrigeration system utilizing reaction heat generated in the production of acetic anhydride comprises an absorption refrigeration component, a tail gas absorption device and a waste heat exchanger, the waste heat exchanger is used for exchanging heat with circulating water by utilizing reaction heat generated in the production of acetic anhydride, a hot water inlet and a hot water outlet of the waste heat exchanger are both communicated with the absorption refrigeration assembly, the absorption refrigeration component is used for transferring the circulating water after heat exchange of the waste heat exchanger to the waste heat exchanger after heat exchange and temperature reduction and preparing liquid ammonia by utilizing the temperature difference generated in the process of heat exchange and temperature reduction of the circulating water so as to complete the process of heat exchange, temperature reduction and refrigeration with fresh methanol, the methanol inlet end of the tail gas absorption device is connected with the low-temperature methanol outlet end of the absorption refrigeration component, the tail gas absorption device is used for recovering organic components in the low-pressure tail gas of the light component removal tower in the acetic anhydride production and rectification process by using the low-temperature methanol after the heat exchange, temperature reduction and refrigeration process.
As a further optimization scheme of the utility model, the reaction heat temperature of the acetic anhydride production is 150-.
As the utility model discloses a further optimization scheme, absorption refrigeration subassembly includes generator, absorber, circulating pump, condenser, evaporimeter, waste heat exchanger's hot and cold water is imported and exported respectively to the hot and cold water of generator, the poor solution exit linkage of generator is to the poor solution import of absorber, the rich solution export of absorber is imported through the rich solution of circulating pump connection generator, fresh methyl alcohol is let in to the feed liquor end of evaporimeter, tail gas absorbing device is connected to the play liquid end of evaporimeter, the ammonia import of ammonia exit linkage condenser of generator, the ammonia liquid exit linkage of condenser is to the ammonia liquid import of evaporimeter, the ammonia outlet linkage of evaporimeter is to the ammonia import of absorber.
As a further optimization scheme of the utility model, the absorption refrigeration subassembly still includes middle heat exchanger, the poor solution export of generator is connected to the poor solution import of absorber through middle heat exchanger and choke valve, the rich solution export of absorber is pumped out the rich solution import of connecting the generator through middle heat exchanger through the circulating pump.
As the utility model discloses a further optimization scheme, absorption refrigeration subassembly still includes gas-liquid heat exchanger, the ammoniacal liquor export of condenser is connected to the ammoniacal liquor import of evaporimeter through gas-liquid heat exchanger, the ammonia export of evaporimeter is connected to the ammonia import of absorber through gas-liquid heat exchanger.
As the utility model discloses a further optimization scheme, absorption refrigeration subassembly still includes the liquid ammonia storage tank, the ammoniacal liquor export of condenser is connected to the ammoniacal liquor import of liquid ammonia storage tank through gas-liquid heat exchanger, the ammoniacal liquor import of evaporimeter is connected through the relief pressure valve in the ammoniacal liquor export of liquid ammonia storage tank.
As a further optimization scheme of the utility model, the air inlet of the tail gas absorption device is connected with the tail gas outlet of the lightness-removing tower in the acetic anhydride production and rectification process.
The beneficial effects of the utility model reside in that: the utility model discloses the utilization is at the reaction heat in the acetic anhydride production process, carry out the continuous cycle heat transfer with the desalination circulating water with the reaction heat, for absorption refrigeration subassembly lasts the heat supply, replace traditional screw rod ice maker, practice thrift the energy consumption, the liquid ammonia of preparing establishes certain liquid level in the liquid ammonia storage tank, accomplish heat transfer cooling refrigeration process in the evaporimeter with fresh methyl alcohol, -15 ℃ methyl alcohol is getting into tail gas absorbing device, absorb main organic components such as methyl iodide in the low pressure tail gas of acetic anhydride production rectification process lightness-removing tower under the condition of low temperature attitude, carry out recycle.
Drawings
FIG. 1 is a schematic flow diagram of an absorption refrigeration system utilizing reaction heat from acetic anhydride production according to the present invention.
In the figure: 1. an absorber; 2. an intermediate heat exchanger; 3. a generator; 4. a condenser; 5. a gas-liquid heat exchanger; 6. an evaporator; 7. a pressure reducing valve; 8. a circulation pump; 9. a throttle valve; 10. a liquid ammonia storage tank; 11. a waste heat exchanger; 12. tail gas absorbing device.
Detailed Description
The present application will now be described in further detail with reference to the drawings, it should be noted that the following detailed description is given for illustrative purposes only and is not to be construed as limiting the scope of the present application, as those skilled in the art will be able to make numerous insubstantial modifications and adaptations to the present application based on the above disclosure.
As shown in fig. 1, the absorption refrigeration system using acetic anhydride to produce reaction heat in this embodiment includes an absorption refrigeration assembly, a tail gas absorption device 12, and a waste heat exchanger 11, where the waste heat exchanger 11 is configured to exchange heat with circulating water using reaction heat of acetic anhydride production reaction at a temperature of 150-, the tail gas absorption device 12 is used for recovering organic components in the low-pressure tail gas of the light component removal tower in the acetic anhydride production and rectification process by using the low-temperature methanol after the heat exchange, temperature reduction and refrigeration process.
The absorption refrigeration component comprises a generator 3, an absorber 1, a circulating pump 8, a condenser 4, an evaporator 6, an intermediate heat exchanger 2, a gas-liquid heat exchanger 5 and a liquid ammonia storage tank 10, wherein a cold water inlet and a hot water outlet of the generator 3 are respectively connected with a cold water inlet and a hot water outlet of a waste heat exchanger 11, a poor solution outlet of the generator 3 is connected to a poor solution inlet of the absorber 1 through the intermediate heat exchanger 2 and a throttle valve 9, a rich solution outlet of the absorber 1 is pumped out through the circulating pump 8 and connected with a rich solution inlet of the generator 3 through the intermediate heat exchanger 2, fresh methanol is introduced into a liquid inlet end of the evaporator 6, a liquid outlet end of the evaporator 6 is connected with a tail gas absorption device 12, an ammonia gas outlet of the generator 3 is connected with an ammonia gas inlet of the condenser 4, an ammonia gas outlet of the condenser 4 is connected to an ammonia gas inlet of the liquid ammonia storage tank 10 through the gas-liquid heat exchanger 5, and an ammonia gas outlet of the liquid ammonia storage tank 10 is connected with an ammonia gas inlet of the evaporator 6 through a pressure reducing valve 7, the ammonia gas outlet of the evaporator 6 is connected to the ammonia gas inlet of the absorber 1 through the gas-liquid heat exchanger 5.
A rich solution output end of the absorber 1 is connected to a rich solution input end of the generator 3 through a circulating pump 8 and an intermediate heat exchanger 2, and the rich solution in the absorber 1 is input into the generator 3; the reaction heat of reactants with the temperature of 150-; the ammonia gas in the generator 3 is conveyed into the condenser 4 through an ammonia gas pipeline, is cooled into ammonia liquid by circulating cooling water in the condenser 4, is conveyed into the gas-liquid heat exchanger 5 through an ammonia liquid pipeline, in the gas-liquid heat exchanger 5, after the ammonia liquid exchanges heat with the low-temperature ammonia gas coming out of the evaporator 6, the ammonia liquid is conveyed to an ammonia liquid storage tank, the prepared liquid ammonia establishes a certain liquid level in the ammonia liquid storage tank, the pressure is reduced to evaporation pressure through a pressure reducing valve 7, the liquid ammonia after pressure reduction enters an evaporator 6, absorbs the heat of fresh methanol as a cooling medium and is vaporized into ammonia gas under the evaporation pressure, the fresh methanol completes the heat exchange, temperature reduction and refrigeration processes in the evaporator 6, the methanol with low temperature of-15 ℃ enters a tail gas absorption device 12, absorbing main organic components such as methyl iodide and the like under the condition of a low-temperature state for recycling, and reheating ammonia gas by a gas-liquid heat exchanger 5 and then feeding the reheated ammonia gas into an absorber 1; the lean solution remained in the generator 3 in the generation process enters the intermediate heat exchanger 2, is subjected to heat exchange with the rich solution absorbed by the absorber 1, is throttled and depressurized and enters the absorber 1, and is mixed with the low-pressure ammonia gas from the evaporator 6 to absorb the low-pressure ammonia gas and restore the low-pressure ammonia gas to the original concentration to form the rich solution, and the gas-liquid heat exchanger 5 and the intermediate heat exchanger 2 in the system improve the heat utilization efficiency of the whole cycle. The absorption process is an exothermic process, cooling water is needed to cool the mixed solution in the absorber 1, the solution with the concentration recovered in the absorber 1 is boosted by the circulating pump 8, enters the intermediate heat exchanger 2 to exchange heat with the lean solution, and then is sent to the generator 3 to be circulated continuously.
The above-mentioned embodiments only represent some embodiments of the present invention, and the description thereof is specific and detailed, but not to be construed as limiting the scope of the present invention. It should be noted that, for those skilled in the art, without departing from the spirit of the present invention, several variations and modifications can be made, which are within the scope of the present invention.
Claims (7)
1. An absorption refrigeration system utilizing reaction heat generated in the production of acetic anhydride is characterized by comprising an absorption refrigeration component, a tail gas absorption device and a waste heat exchanger, the waste heat exchanger is used for exchanging heat with circulating water by utilizing reaction heat generated in the production of acetic anhydride, a hot water inlet and a hot water outlet of the waste heat exchanger are both communicated with the absorption refrigeration assembly, the absorption refrigeration component is used for transferring the circulating water after heat exchange of the waste heat exchanger to the waste heat exchanger after heat exchange and temperature reduction and preparing liquid ammonia by utilizing the temperature difference generated in the process of heat exchange and temperature reduction of the circulating water so as to complete the process of heat exchange, temperature reduction and refrigeration with fresh methanol, the methanol inlet end of the tail gas absorption device is connected with the low-temperature methanol outlet end of the absorption refrigeration component, the tail gas absorption device is used for recovering organic components in the low-pressure tail gas of the light component removal tower in the acetic anhydride production and rectification process by using the low-temperature methanol after the heat exchange, temperature reduction and refrigeration process.
2. The absorption refrigeration system as claimed in claim 1, wherein the temperature of the reaction heat for acetic anhydride production is 150-180 ℃, and the temperature of the circulating water after heat exchange with the reaction heat for acetic anhydride production is 140-170 ℃.
3. The absorption refrigeration system according to claim 1, wherein the absorption refrigeration assembly comprises a generator, an absorber, a circulating pump, a condenser and an evaporator, the cold and hot water inlet and outlet of the generator are respectively connected with the cold and hot water inlet and outlet of the waste heat exchanger, the lean solution outlet of the generator is connected to the lean solution inlet of the absorber, the rich solution outlet of the absorber is connected to the rich solution inlet of the generator through the circulating pump, fresh methanol is introduced into the liquid inlet of the evaporator, the liquid outlet of the evaporator is connected to the tail gas absorption device, the ammonia gas outlet of the generator is connected to the ammonia gas inlet of the condenser, the ammonia gas outlet of the condenser is connected to the ammonia gas inlet of the evaporator, and the ammonia gas outlet of the evaporator is connected to the ammonia gas inlet of the absorber.
4. The absorption refrigeration system according to claim 3 wherein the absorption refrigeration assembly further comprises an intermediate heat exchanger, the lean solution outlet of the generator is connected to the lean solution inlet of the absorber through the intermediate heat exchanger and a throttle valve, and the rich solution outlet of the absorber is pumped through a circulation pump through the intermediate heat exchanger and connected to the rich solution inlet of the generator.
5. The absorption refrigeration system for generating reaction heat by using acetic anhydride as claimed in claim 3, wherein the absorption refrigeration assembly further comprises a gas-liquid heat exchanger, the ammonia liquid outlet of the condenser is connected to the ammonia liquid inlet of the evaporator through the gas-liquid heat exchanger, and the ammonia gas outlet of the evaporator is connected to the ammonia gas inlet of the absorber through the gas-liquid heat exchanger.
6. The absorption refrigeration system for generating reaction heat by using acetic anhydride as claimed in claim 5, wherein the absorption refrigeration assembly further comprises a liquid ammonia storage tank, the ammonia liquid outlet of the condenser is connected to the ammonia liquid inlet of the liquid ammonia storage tank through a gas-liquid heat exchanger, and the ammonia liquid outlet of the liquid ammonia storage tank is connected to the ammonia liquid inlet of the evaporator through a pressure reducing valve.
7. The absorption refrigeration system using reaction heat in acetic anhydride production as claimed in claim 1, wherein the inlet of the tail gas absorption device is connected to the tail gas outlet of the light component removal column in the acetic anhydride production rectification process.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121445235.3U CN215176152U (en) | 2021-06-28 | 2021-06-28 | Absorption type refrigerating system utilizing acetic anhydride production reaction heat |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202121445235.3U CN215176152U (en) | 2021-06-28 | 2021-06-28 | Absorption type refrigerating system utilizing acetic anhydride production reaction heat |
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| CN215176152U true CN215176152U (en) | 2021-12-14 |
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| CN202121445235.3U Active CN215176152U (en) | 2021-06-28 | 2021-06-28 | Absorption type refrigerating system utilizing acetic anhydride production reaction heat |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115507564A (en) * | 2022-11-23 | 2022-12-23 | 安徽普泛能源技术有限公司 | Compound absorption refrigeration system with two-stage evaporation |
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2021
- 2021-06-28 CN CN202121445235.3U patent/CN215176152U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115507564A (en) * | 2022-11-23 | 2022-12-23 | 安徽普泛能源技术有限公司 | Compound absorption refrigeration system with two-stage evaporation |
| CN115507564B (en) * | 2022-11-23 | 2023-02-07 | 安徽普泛能源技术有限公司 | Compound absorption refrigeration system with two-stage evaporation |
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