CN107198967A - Multiple-effect membrane regeneration plant and method for gas purification solvent reclamation - Google Patents
Multiple-effect membrane regeneration plant and method for gas purification solvent reclamation Download PDFInfo
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- CN107198967A CN107198967A CN201610154934.XA CN201610154934A CN107198967A CN 107198967 A CN107198967 A CN 107198967A CN 201610154934 A CN201610154934 A CN 201610154934A CN 107198967 A CN107198967 A CN 107198967A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/364—Membrane distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/366—Apparatus therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2653—Degassing
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2669—Distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2317/00—Membrane module arrangements within a plant or an apparatus
- B01D2317/02—Elements in series
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0001—Separation or purification processing
- C01B2210/0009—Physical processing
- C01B2210/001—Physical processing by making use of membranes
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0001—Separation or purification processing
- C01B2210/0009—Physical processing
- C01B2210/001—Physical processing by making use of membranes
- C01B2210/0012—Physical processing by making use of membranes characterised by the membrane
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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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention belongs to industrial gas purifying separation field, a kind of solvent reclamation device and method for amine method gas purification is provided, it is characterized in, by one group of continuous degassing film and heat exchanger connection, using the method for multiple-effect membrane distillation the sour gas in solvent being separated from solution.The present invention combines the advantage of membrane distillation and multi-effect distilling technology, compared with traditional filler regenerator, process provided by the present invention can effectively reduce entrapment solvent loss, multiple-effect evaporation is combined by film regeneration, the steam waste heat that regeneration can be made full use of to produce, solvent one way heating simultaneously, the cold liquid backflow without packed tower, can be greatly decreased regeneration energy consumption.Also have operation temperature and pressure limit wide simultaneously, the features such as solvent loss is small can be widely applicable for the operating process such as physics regeneration, chemical regeneration, the physical chemistry regeneration of gas purification.
Description
Technical field
The present invention relates to a kind of amine method gas purification solvent regeneration system and method, belong to industrial gas purifying separation field.
Background technology
A large amount of with fossil fuel use, substantial amounts of carbon dioxide greenhouse gas is discharged into air, the bad weather and environmental disruption that global warming is caused increasingly sharpen, amine method decarburization technique is more and more paid attention to the advantage of the low fractional pressure carbon dioxide in flue gas after its trapping burning, and traditional amine method decarburization technique, energy consumption during the trapping of amine method carbon account for more than the 70% of carbon trapping cost, how energy consumption that carbon trap process is reduced, it is the bottleneck that carbon trapping technique is promoted, in order to effectively reduce regeneration energy consumption, it is necessary to develop novel dissolvent regeneration techniques.
Film distillation technology can intercept the characteristic of liquid using hydrophobic type degassing film by gas phase, and under the promotion of film both sides sour gas gaseous phase partial pressure difference, the sour gas dissolved in solvent is separated, and reach the purpose of solvent reclamation.Patent CN101822931A provides a kind of carbon dioxide enriched absorbent solution hollow fiber membrane contactorses and depressurizes renovation process, the method that coordinating with steam rapid heat cycle is purged is regenerated by vacuum decompression, realize the regeneration of solvent at a lower temperature, the problem of technology is present is the physical dissolution active force that low-temperature reduced-pressure regeneration only overcomes sour gas disengaging solvent, chemical energy consumption necessary to chemical absorption solvents regeneration can not be overcome, only can be suitably used for Physical Absorption with pressure and regenerative process；Patent CN101524613B provides a kind of method for absorbent regeneration, by membrane module as a unit, rich solution is in shell side, gas walks tube side, gas-liquid regeneration separation is carried out under 2.5-20kPa absolute pressures by vavuum pump, 30-70 DEG C of operation temperature, this method except regeneration temperature is low be difficult to overcome chemical resistance in addition to, it is high to vacuum dependency degree, and vacuum takes out vacuum distillation and says higher than air-distillation energy consumption from energy consumption angle, in addition solution walks the mass transfer specific surface area that shell side significantly reduces solution, and regeneration efficiency is low.
The characteristics of multiple-effect evaporation imitates low using the operation pressure of aftereffect than before, the indirect steam for introducing preceding effect is used as the heating medium of aftereffect, i.e. the heating chamber of aftereffect turns into the indirect steam condenser of preceding effect, and the only first effect needs to consume steam, and regeneration energy consumption can be greatly reduced in this operation.The B of patent CN 102179057 provide a kind of local forced circulation desalting method for multi-effect evaporation system, the solid salt separated out in feed liquid can be transferred out by this method from multi-effect evaporation system in time, the heterogeneous thing system separation process available for the multi-effect evaporation system for having solid precipitation；The A of patent CN 102976538 provide a kind of liter film and falling film type multi-effect water distillator, using liter film and the technical pattern of falling film evaporation, it is, by an effect or the bottom of one, 2nd effect evaporator, to realize in tube side of intaking and naturally equally distributed evaporation mode by raw water.
The content of the invention
The present invention combines the advantage of both the above technology, Multistage Membranes regeneration method is taken to separate the sour gas in solvent, it is wide with operation temperature and pressure limit, energy consumption is low, the features such as solvent loss is small, can be widely applicable for the operating process such as physics regeneration, chemical regeneration, the physical chemistry regeneration of gas purification.
The device that the present invention is provided includes multistage continuous degassing film and heat exchanger and supporting aspiration pump connection, and solvent is absorbed heat in heat exchanger, and deaerated regeneration in degassing film, and regeneration gas is conveyed as the thermal source of next effect by aspiration pump.
The present invention is used for the method for gas purification solvent reclamation, is characterized in using said apparatus, is connected by one group of continuous degassing film and heat exchanger, using the method for multiple-effect membrane distillation the sour gas in solvent is separated from solution.Absorb the solution after acid gas and initially enter first order heat exchanger（2）, by the steam for entering heat exchanger（3）Heating, the solution after heating（5）Into in membrane regeneration plant（6）, solution enters by the intracavitary of hollow hydrophobic film, and the sour gas and vapor in solution enter through hydrophobic membrane outside the chamber of film, the gas after separation（9）By aspiration pump（28）It is transported to the heat exchanger of next effect regeneration（8）It is middle to be heated as regeneration thermal source from one-level membrane module（6）Solution after degassing（7）, the solution after reheating（10）Into second membrane module（11）In, sour gas and vapor in solution enter through hydrophobic membrane outside the chamber of film, the gas after separation（17）By aspiration pump（29）It is transported to the heat exchanger of next effect regeneration（18）It is middle to be heated as regeneration thermal source from one-level membrane module（11）Solution after degassing（16）, multiple-effect membrane distillation is carried out successively according to this approach；Regeneration steam after heat exchange passes through condensation separation, obtains the carbon dioxide of high-purity, and condensed water merges with solution, keeps the water balance of system.
Degassing film used of the invention is hydrophobicity degassing film, and its material can be polytetrafluoroethylhollow hollow fiber membrane or pass through the modified inoranic membrane of dehydration.
Heating vapor (steam) temperature used in the present invention is in 110-160 DEG C, 60-130 DEG C of membrane module operation temperature.
The equipment of bright the be used as aspiration pump of this law can be to provide the blower fan or vavuum pump of tiny structure, and degassing film surface operation pressure limit is 0.1-1 atmospheric pressure (absolute pressure).The present invention uses multi-effect distilling for cocurrent adding material, and effect number scope is 3-10.
Compared with traditional filler in raw tower, process provided by the present invention can effectively reduce entrapment solvent loss；Multiple-effect evaporation is combined by film regeneration, the steam waste heat that regeneration can be made full use of to produce, while solvent one way is heated, regeneration energy consumption can be greatly decreased in the cold liquid backflow without packed tower.
Brief description of the drawings
Fig. 1 is present invention method schematic flow sheet.
In figure, 1. absorbing liquid enters vapor heat exchanger, 2. steam heater, 3. steam enters, 4. steam goes out, 5. solution enters membrane module after heating, 6. one-level regenerates membrane module, 7. solution goes out one-level film regeneration module, 8. secondary heat exchanger, 9. indirect steam enters aspiration pump 28, 10. solution enters second membrane module, 11. second membrane module, 12. regeneration gas enters condenser after heat exchange, 13. regeneration gas is mixed after heat exchange, 14. regeneration gas enters condenser, 15. condenser, 16. solution enters three-level heat exchanger, 17. indirect steam enters aspiration pump 29, 18. three-level heat exchanger, 19. solution enters three-level membrane module, 20. three-level membrane module, 21. regeneration gas enters aspiration pump 30, 22. solution enters blender after regeneration, 23. regenerate gas separating device, 24. regeneration gas goes out system, 25. regeneration gas condensate liquid, 26. blender, 27. solution after regeneration, 28. aspiration pump, 29. aspiration pump, 30. aspiration pump, 31. regeneration gas goes out aspiration pump, 32. regeneration gas goes out aspiration pump, 33. regeneration gas goes out aspiration pump.
Embodiment
The present invention is described in detail in reference to embodiment and accompanying drawing.
Following examples are connected by one group of continuous degassing film and heat exchanger referring to accompanying drawing 1, using the method for multiple-effect membrane distillation the sour gas in solvent are separated from solution.Absorb the solution after acid gas and initially enter first order heat exchanger（2）, by the steam for entering heat exchanger（3）Heating, the solution after heating（5）Into in membrane regeneration plant（6）, solution enters by the intracavitary of hollow hydrophobic film, and the sour gas and vapor in solution enter through hydrophobic membrane outside the chamber of film, the gas after separation（9）By aspiration pump（28）It is transported to the heat exchanger of next effect regeneration（8）It is middle to be heated as regeneration thermal source from one-level membrane module（6）Solution after degassing（7）, the solution after reheating（10）Into second membrane module（11）In, sour gas and vapor in solution enter through hydrophobic membrane outside the chamber of film, the gas after separation（17）By aspiration pump（29）It is transported to the heat exchanger of next effect regeneration（18）It is middle to be heated as regeneration thermal source from one-level membrane module（11）Solution after degassing（16）, multiple-effect membrane distillation is carried out successively according to this approach；Regeneration steam after heat exchange passes through condensation separation, obtains the carbon dioxide of high-purity, and condensed water merges with solution, keeps the water balance of system.
Embodiment
1
Certain solvent 1m3, containing MEA（MEA）3.0mol/L, wherein dissolving CO21.2mol/L, 95 DEG C of temperature, pressure 0.3MPa enters triple effect membrane regeneration plant provided by the present invention, and operating method is with described in the content of the invention, solvent C O after processing20.4mol/L, 40 DEG C of temperature consumes 139 DEG C of 53 kilograms of low-pressure steams altogether.
Comparative example
1
Certain solvent 1m3, containing MEA（MEA）3.0mol/L, wherein dissolving CO21.2mol/L, 95 DEG C of temperature, pressure 0.3MPa enters triple effect membrane regeneration plant provided by the present invention, and operating method is with described in the content of the invention, solvent C O after processing20.4mol/L, 40 DEG C of temperature consumes 139 DEG C of 68 kilograms of low-pressure steams altogether.
The two compares, using triple effect film renovation process can steam saving 22%, solvent reclamation energy consumption can effectively be reduced using the method for the bright offer of this law.
Claims (7)
1. a kind of multiple-effect membrane regeneration plant for gas purification solvent reclamation, it is characterized in that it includes multistage continuous degassing film and heat exchanger and supporting aspiration pump connection, solvent is absorbed heat in heat exchanger, and deaerate regeneration in degassing film, and regeneration gas is conveyed as the thermal source of next effect by aspiration pump.
2. it is used for gas purification method for regenerating solvent as claimed in claim 1, it is characterized in that being connected by one group of continuous degassing film and heat exchanger, using the method for multiple-effect membrane distillation the sour gas in solvent is separated from solution, absorb the solution after acid gas and initially enter first order heat exchanger（2）, by the steam for entering heat exchanger（3）Heating, the solution after heating（5）Into in membrane regeneration plant（6）, solution enters by the intracavitary of hollow hydrophobic film, and the sour gas and vapor in solution enter through hydrophobic membrane outside the chamber of film, the gas after separation（9）By aspiration pump（28）It is transported to the heat exchanger of next effect regeneration（8）It is middle to be heated as regeneration thermal source from one-level membrane module（6）Solution after degassing（7）, the solution after reheating（10）Into second membrane module（11）In, sour gas and vapor in solution enter through hydrophobic membrane outside the chamber of film, the gas after separation（17）By aspiration pump（29）It is transported to the heat exchanger of next effect regeneration（18）It is middle to be heated as regeneration thermal source from one-level membrane module（11）Solution after degassing（16）, multiple-effect membrane distillation is carried out successively according to this approach；Regeneration steam after heat exchange passes through condensation separation, obtains the carbon dioxide of high-purity, and condensed water merges with solution, keeps the water balance of system.
3. method as claimed in claim 2, it is characterised in that degassing film used is hydrophobicity degassing film, its material is polytetrafluoroethylhollow hollow fiber membrane or the inoranic membrane by dehydration modification.
4. method as claimed in claim 2, it is characterised in that heating vapor (steam) temperature is in 110-160 DEG C, 60-130 DEG C of membrane module operation temperature.
5. method as claimed in claim 2, it is characterised in that the equipment for being used as aspiration pump is to provide the blower fan of tiny structure, or vavuum pump.
6. method as claimed in claim 2, it is characterised in that degassing film surface operation pressure limit is 0.1-1 atmospheric pressure (absolute pressure), by the control to suction pressure, to control the operating condition of membrane distillers at different levels.
7. method as claimed in claim 2, it is characterised in that multi-effect distilling is cocurrent adding material, and effect number scope is 3-10.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610154934.XA CN107198967A (en) | 2016-03-18 | 2016-03-18 | Multiple-effect membrane regeneration plant and method for gas purification solvent reclamation |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610154934.XA CN107198967A (en) | 2016-03-18 | 2016-03-18 | Multiple-effect membrane regeneration plant and method for gas purification solvent reclamation |
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| Publication Number | Publication Date |
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| CN107198967A true CN107198967A (en) | 2017-09-26 |
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| CN201610154934.XA Pending CN107198967A (en) | 2016-03-18 | 2016-03-18 | Multiple-effect membrane regeneration plant and method for gas purification solvent reclamation |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2019204974A1 (en) * | 2018-04-24 | 2019-10-31 | Petroliam Nasional Berhad (Petronas) | System and method for solvent regeneration |
| CN110538574A (en) * | 2019-09-11 | 2019-12-06 | 华北电力大学 | High-efficient vacuum membrane distillation system |
| CN111111451A (en) * | 2020-01-17 | 2020-05-08 | 吕剑阳 | Reduced pressure multi-effect membrane distillation method and device thereof |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101632901A (en) * | 2008-07-21 | 2010-01-27 | 天津海之凰科技有限公司 | Heat-recovery vacuum membrane distillation component device and vacuum membrane distillation method |
-
2016
- 2016-03-18 CN CN201610154934.XA patent/CN107198967A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101632901A (en) * | 2008-07-21 | 2010-01-27 | 天津海之凰科技有限公司 | Heat-recovery vacuum membrane distillation component device and vacuum membrane distillation method |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2019204974A1 (en) * | 2018-04-24 | 2019-10-31 | Petroliam Nasional Berhad (Petronas) | System and method for solvent regeneration |
| CN110538574A (en) * | 2019-09-11 | 2019-12-06 | 华北电力大学 | High-efficient vacuum membrane distillation system |
| CN111111451A (en) * | 2020-01-17 | 2020-05-08 | 吕剑阳 | Reduced pressure multi-effect membrane distillation method and device thereof |
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Application publication date: 20170926 |
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