CN101856579B - Novel energy-saving CO2 trapping process of improved potassium carbonate - Google Patents
Novel energy-saving CO2 trapping process of improved potassium carbonate Download PDFInfo
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- CN101856579B CN101856579B CN2010101966726A CN201010196672A CN101856579B CN 101856579 B CN101856579 B CN 101856579B CN 2010101966726 A CN2010101966726 A CN 2010101966726A CN 201010196672 A CN201010196672 A CN 201010196672A CN 101856579 B CN101856579 B CN 101856579B
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- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 title claims abstract description 28
- 229910000027 potassium carbonate Inorganic materials 0.000 title claims abstract description 7
- 238000000034 method Methods 0.000 title abstract description 32
- 239000002250 absorbent Substances 0.000 claims abstract description 51
- 230000002745 absorbent Effects 0.000 claims abstract description 51
- 238000010521 absorption reaction Methods 0.000 claims abstract description 48
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000003795 desorption Methods 0.000 claims abstract description 14
- WFCSWCVEJLETKA-UHFFFAOYSA-N 2-piperazin-1-ylethanol Chemical compound OCCN1CCNCC1 WFCSWCVEJLETKA-UHFFFAOYSA-N 0.000 claims abstract description 13
- WUUHFRRPHJEEKV-UHFFFAOYSA-N tripotassium borate Chemical compound [K+].[K+].[K+].[O-]B([O-])[O-] WUUHFRRPHJEEKV-UHFFFAOYSA-N 0.000 claims abstract description 13
- 230000008878 coupling Effects 0.000 claims abstract description 6
- 238000010168 coupling process Methods 0.000 claims abstract description 6
- 238000005859 coupling reaction Methods 0.000 claims abstract description 6
- 238000005516 engineering process Methods 0.000 claims description 17
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims description 14
- 229940072033 potash Drugs 0.000 claims description 14
- 235000015320 potassium carbonate Nutrition 0.000 claims description 14
- 241000282326 Felis catus Species 0.000 claims description 13
- 238000010438 heat treatment Methods 0.000 claims description 13
- 239000000203 mixture Substances 0.000 claims description 12
- 238000003860 storage Methods 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 10
- 239000000126 substance Substances 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 6
- 239000007791 liquid phase Substances 0.000 claims description 4
- 239000012071 phase Substances 0.000 claims description 4
- 238000011084 recovery Methods 0.000 claims description 4
- 230000001502 supplementing effect Effects 0.000 claims description 4
- 235000011181 potassium carbonates Nutrition 0.000 claims description 3
- 230000008929 regeneration Effects 0.000 claims description 3
- 238000011069 regeneration method Methods 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000003889 chemical engineering Methods 0.000 abstract description 2
- TYJJADVDDVDEDZ-UHFFFAOYSA-M potassium hydrogencarbonate Chemical compound [K+].OC([O-])=O TYJJADVDDVDEDZ-UHFFFAOYSA-M 0.000 abstract 1
- 230000001172 regenerating effect Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 34
- 239000003245 coal Substances 0.000 description 12
- 229910052799 carbon Inorganic materials 0.000 description 7
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 239000005431 greenhouse gas Substances 0.000 description 4
- 239000003595 mist Substances 0.000 description 4
- SIXOAUAWLZKQKX-UHFFFAOYSA-N carbonic acid;prop-1-ene Chemical compound CC=C.OC(O)=O SIXOAUAWLZKQKX-UHFFFAOYSA-N 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 229920000151 polyglycol Polymers 0.000 description 3
- 239000010695 polyglycol Substances 0.000 description 3
- 238000010248 power generation Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- GQPLMRYTRLFLPF-UHFFFAOYSA-N Nitrous Oxide Chemical compound [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 2
- GLUUGHFHXGJENI-UHFFFAOYSA-N Piperazine Chemical compound C1CNCCN1 GLUUGHFHXGJENI-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000001311 chemical methods and process Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000005262 decarbonization Methods 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000006116 polymerization reaction Methods 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- XTHFKEDIFFGKHM-UHFFFAOYSA-N Dimethoxyethane Chemical compound COCCOC XTHFKEDIFFGKHM-UHFFFAOYSA-N 0.000 description 1
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 1
- 229910018503 SF6 Inorganic materials 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 239000012190 activator Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 235000013312 flour Nutrition 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000001272 nitrous oxide Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- SFZCNBIFKDRMGX-UHFFFAOYSA-N sulfur hexafluoride Chemical compound FS(F)(F)(F)(F)F SFZCNBIFKDRMGX-UHFFFAOYSA-N 0.000 description 1
- 229960000909 sulfur hexafluoride Drugs 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
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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
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a novel energy-saving CO2 trapping process of improved potassium carbonate, which belongs to the technical field of chemical engineering and relates to the procedures of absorbing and removing CO2 from intermediate/high-pressure gas mixed with synthetic gas, shift gas and IGCC gas. The process comprises the following steps of: (1) adopting a water solution of potassium carbonate and adding the promoters of hydroxyethyl piperazine and potassium borate for absorbing the CO2; and (2) desorbing and regenerating the pregnant solution of an absorbent by thermal coupling. The invention provides the novel process for absorbing and trapping the CO2 by adopting the water solution of the potassium carbonate and adding the promoters of the hydroxyethyl piperazine and the potassium borate. In the process, virgin gas containing the CO2 is absorbed and decarbonized by the potassium carbonate solution added with the promoters of the hydroxyethyl piperazine and the potassium borate, the absorption pregnant solution after absorbing the CO2 is desorbed and regenerated by thermal coupling, and the CO2 obtained by desorption is discharged out of a battery limit. Compared with the prior art, the invention can lower the comprehensive energy consumption by 20 to 30 percent.
Description
Technical field
The invention belongs to technical field of chemical engineering.Be particularly related to the mesohigh GAS ABSORPTION of mixing and remove CO from synthesis gas, conversion gas and IGCC gas
2A kind of energy-conservation capture CO that improves potash
2New technology.
Background technology
Since the industrial revolution, especially since the 1950's, the artificial greenhouse gas emissions that produce constantly increase, and cause a series of disasters such as temperature raises, melt in the glacier, and sea level rise, have caused worldwide extensive concern.The greenhouse gases that can know at present mainly contain carbon dioxide, methane, nitrous oxide, hydrogen fluorine carbide, perfluocarbon and sulfur hexafluoride, wherein CO
2Content the highest, the life-span is long, and greenhouse gases are had the greatest impact, and also is the root that causes terrestrial climate to warm.Reducing carbon-based fuel, increasing the low use of talking fuel and carbon-free fuel is the hope of following global sustainable development, but the actual carbon emission reduction operation of distance still has no small distance, from the maturity of technology and feasibility analysis, and in coming few decades, CO
2Trapping technique will be the important measures of reply global warming and reduction of greenhouse gas discharge.Especially based on the CO of coal-based chemical process and power generation process
2Capture will be the emphasis that carbon captures.
Reduce the CO of power plant
2Discharging is just very important.Whole coal gas combined cycle (IGCC-Integrated Gasification Combined Cycle) electricity generation system has high generating efficiency, again environment is had fabulous affinity, is a kind of promising clean coal power generation technology.
Coal-based chemical process totally can be divided into gasification, liquefaction and solidify (coking or destructive distillation) three kinds of processing modes; Wherein coal gasification is the tap of coal-based chemical industry; Account for 3～5% of coal consumption; Be the 3rd purposes that is only second to thermal power generation and coal tarization, the further aggravation along with the alternative oil trend of coal in China expects the year two thousand twenty and will account for 15%～20% of coal consumption.
In sum, mesohigh CO
2Capture is based on the common problem of coal-based industrial process carbon emission reduction, is the key issue of coal-based industrial process carbon emission reduction.
The unstripped gas that the present invention was directed against like Coal Chemical Industry synthesis gas, conversion gas and IGCC gas, contains 30～50% CO
2, concentration is higher, and pressure is higher, generally greater than 2000KPa, is fit to adopt the Physical Absorption method to absorb CO
2Gas.
Comparatively ripe Physical Absorption method decarbonization process has the low-temperature rectisol method (to be called the Rectisol method abroad in the industry both at home and abroad at present; CN 94101447.9), the propene carbonate method (is called the Flour method abroad; CN 91101928) and polyglycol dimethyl ether process (be called the Selexol method abroad; CN 200710015805) and potash method (claiming the Benfield method abroad, CN 1089263C).
The low-temperature rectisol method has that absorbability is big, selectivity good, gas purification degree is high, the characteristics of absorbent good stability, but has that technological process is long, equipment investment big (the anti-low temperature material below-30 ℃ of needs), absorbent toxicity is big and needs are paid shortcomings such as external great number patented technology expense; Because having to depress at higher branch, propene carbonate can absorb CO effectively
2, and under lower pressure, can not need heat and the characteristics of easy desorb, its technological process, especially desorption technique can obtain suitable simplification, but because absorptive capacity is limited, the absorbent internal circulating load is bigger, energy consumption is bigger; Polyglycol dimethyl ether process has that absorbability is strong, the characteristics of absorbent loss little (steam forces down); But NHD must be through artificial synthetic; The absorbent cost is high, and this absorbent molecular weight is bigger, easily polymerization takes place and causes damage in regenerative process.The technology that the potash method is developed the earliest (US.2886405) adopts single tower desorb, and it is big to absorb energy consumption.Improved the energy-saving process of activators such as having formed double tower desorb and interpolation piperazine afterwards on this basis, energy consumption decreases, but the cost of decarburization is still higher.，
Long to existing low-temperature rectisol method technological process, equipment investment is big; Propene carbonate method absorbing agent absorption capacity is little, internal circulating load is big; And polymerization losses, higher deficiency and the defective of potash method desorb energy consumption take place in polyglycol dimethyl ether process solvent easily; The inventor has proposed a kind of interpolation promoter hydroxyethyl piperazine and potassium borate of adopting and has improved the decarbonization process of traditional solution of potassium carbonate as absorbent, and in technology, adopts the thermal coupling desorb further to reduce the whole energy consumption that captures.
Summary of the invention
The purpose of this invention is to provide a kind of employing and improve potash absorption CO
2Capture new technology, it is characterized in that this technology comprises the steps:
1) adopt wet chemical to add promoter hydroxyethyl piperazine and potassium borate absorption CO
2,
Contain CO
2Unstripped gas and the purified gas that comes out from 3 tops, absorption tower gas heat exchanger 1 by preheating after, 3 bottoms get into the absorption tower from the absorption tower; From the solution of potassium carbonate that contains promoter hydroxyethyl piperazine and potassium borate of absorbent storage tank and absorbent lean solution from desorber 6 bottoms; 3 tops get into the absorption tower from the absorption tower after the heat exchange in liquid heat-exchanger 2; Unstripped gas and absorbent be counter current contacting in absorption tower 3, CO
2Being absorbed agent absorbs; The absorption tower temperature is controlled at 70～115 ℃, and pressure is controlled at 2.5MPa～3.5MPa; In the absorption tower, remove CO
2Purified gas and unstripped gas heat exchange after temperature reduce to 40～65 ℃ after from the absorption tower toward next operation, absorbed CO
2The absorbent rich solution send into preparatory desorber 4 and carry out preparatory desorb;
2) the thermal coupling desorption and regeneration of absorbent rich solution
Absorbent rich solution from the absorption tower still is sent into preparatory desorber 4 from the middle part, the tower still is with preparatory desorb reboiler 5 heating, and the desorb reboiler adopts the 8～10kg/cm that provides from the system share engineering in advance
2Steam as the heating thermal source, in advance the desorber temperature is controlled at 110～180 ℃, pressure is controlled at 0.2MPa～0.5MPa, the steam of desorb cat head is sent into desorption tower reboiler 7 as the heating thermal source in advance;
Liquid phase from preparatory desorber 4 adds desorber 6 from the middle part; The tower still is with 7 heating of desorb reboiler; The thermal source of desorb reboiler 7 is used the steam from preparatory desorber 4 tops; The desorber temperature is controlled at 80～130 ℃, and pressure is controlled at 0.01MPa～0.1MPa, send the absorbent storage tank after the absorbent heat exchange on the desorption barren solution of desorber 6 and entering absorption tower.
The gas phase at desorber 6 tops and send separation of C O in the vapour liquid separator 8 in the lump from the steam condensate vapour mixture at preparatory desorber top
2And water, wherein CO
2Be discharged into recovery process, water returns the absorbent storage tank and uses as supplementing water.
Said absorbent is a wet chemical, and wherein the content of potash is 20～35wt%, and promoter hydroxyethyl piperazine content is at 1～3wt%, and potassium borate content is at 0.1～0.8wt%, and surplus is a water.
Description of drawings
A kind of employing of Fig. 1 improves potash and absorbs CO
2Capture the new technology principle flow chart.
Among the figure: the 4 preparatory desorber 5 preparatory desorb reboiler 6 desorbers 7 desorb reboilers 8 gas-liquid separator jars of 1 gas heat exchanger, 2 liquid heat-exchangers, 3 absorption towers
The specific embodiment
The present invention provides a kind of employing to improve potash absorption CO
2Capture new technology, this technology comprises:
1) adopt wet chemical to add promoter hydroxyethyl piperazine, potassium borate absorption CO
2
2) the thermal coupling desorption and regeneration of absorbent rich solution.
Below in conjunction with accompanying drawing and embodiment technology provided by the invention is further described.
In Fig. 1, remove CO as unstripped gas and absorption tower cat head with the mist shown in the table 1
2Purified gas in gas heat exchanger 1, carry out heat exchange; After the heat exchange; The unstripped gas temperature rises to 70 ℃, gets into absorption tower 3 from the bottom, from 30 ℃ of absorbents of absorbent storage tank; Wherein absorbent is that 25wt%, promoter are that 1.2wt% and potassium borate content are 0.22wt% for hydroxyethyl piperazine content for potash content, and all the other are water.After the heat exchange of desorber still lean solution, temperature is 30 ℃, gets into the absorption tower from top, and unstripped gas and absorbent be counter current contacting and generation absorption mass transfer in tower, and the absorbent flow is 257821KG-MOL/HR.86 ℃ of absorption tower tower top temperatures, pressure 2.84MPa; 91 ℃ of column bottom temperatures, pressure 2.85MPa.Remove CO
2After purified gas and unstripped gas heat exchange after be cooled to 50 ℃ and be sent to next operation, its composition (mole fraction) is as shown in table 2.
Absorbent rich solution from absorption tower 3 is sent into preparatory desorber 4 from the middle part, desorb reboiler 5 adopts from the 8kg/cm outside the battery limit (BL) in advance
2Steam as the heating thermal source.The desorber tower top temperature is 117 ℃ in advance, pressure 0.16MPa; 122 ℃ of column bottom temperatures, pressure 0.17MPa.The steam of desorb cat head is sent into desorption tower reboiler 7 as the heating thermal source in advance.
Liquid phase (absorbent rich solution) from preparatory desorber 4 adds desorber 6 from the middle part, desorb Tata still is with 7 heating of desorb reboiler, and the thermal source of desorb reboiler 7 is used the steam from preparatory desorb cat head.103 ℃ of desorber tower top temperatures, pressure 0.11MPa; 106 ℃ of column bottom temperatures, pressure 0.12MPa.Send the absorbent storage tank after the absorbent heat exchange on the desorption barren solution of desorber still and entering absorption tower.
Desorb cat head gas phase and send separation of C O in the vapour liquid separator in the lump from the preparatory desorb cat head steam condensate vapour mixture of desorption tower reboiler
2And water, 30 ℃ of temperature, pressure 0.11MPa, CO
2Be discharged into recovery process, its composition (mole fraction) is as shown in table 3.Wherein water returns the absorbent storage tank and uses as supplementing water.
Table 1 contains CO
2The mist primary condition:
Table 2 absorbent rich solution composition (mole fraction)
Table 3 vapor-liquid separation mixture
Embodiment 2:
In Fig. 1, remove CO as unstripped gas and absorption tower cat head with the mist shown in the table 4
2Purified gas in gas heat exchanger 1, carry out heat exchange; After the heat exchange; The unstripped gas temperature rises to 72 ℃, gets into absorption tower 3 from the bottom, from 30 ℃ of absorbents of absorbent storage tank; Wherein absorbent is that 25wt%, promoter are that 2.1wt% and potassium borate content are 0.66wt% for hydroxyethyl piperazine content for potash content, and surplus is a water.After the heat exchange of desorber still lean solution, temperature is 30 ℃, gets into the absorption tower from top, and unstripped gas and absorbent be counter current contacting and generation absorption mass transfer in tower, and the absorbent flow is 236155 KG-MOL/HR.89 ℃ of absorption tower tower top temperatures, pressure 2.84MPa; 94 ℃ of column bottom temperatures, pressure 2.85MPa.Remove CO
2After purified gas and unstripped gas heat exchange after be cooled to 45 ℃ and be discharged into down operation, its composition (mole fraction) is as shown in table 5.
Absorbent rich solution from absorption tower 3 is sent into preparatory desorber 4 from the middle part, desorb reboiler 5 adopts from the 8kg/cm outside the battery limit (BL) in advance
2Steam as the heating thermal source.The desorber tower top temperature is 118 ℃ in advance, pressure 0.16MPa; 124 ℃ of column bottom temperatures, pressure 0.17MPa.The steam of desorb cat head is sent into desorption tower reboiler 7 as the heating thermal source in advance.
Liquid phase (absorbent rich solution) from preparatory desorber 4 adds desorber 6 from the middle part, desorb Tata still is with 7 heating of desorb reboiler, and the thermal source of this reboiler is used the steam from preparatory desorb cat head.104 ℃ of desorber tower top temperatures, pressure 0.11MPa; 108 ℃ of column bottom temperatures, pressure 0.12MPa.Send the absorbent storage tank after the absorbent heat exchange on the desorption barren solution of desorber still and entering absorption tower.
Desorb cat head gas phase and send separation of C O in the vapour liquid separator in the lump from the preparatory desorb cat head steam condensate vapour mixture of desorption tower reboiler
2And water, 30 ℃ of temperature, pressure 0.11MPa, CO
2Be discharged into recovery process, its composition (mole fraction) is as shown in table 6.Wherein water returns the absorbent storage tank and uses as supplementing water.
Table 4: contain CO
2The mist primary condition
Table 5 absorbent rich solution composition (mole fraction)
Table 6 vapor-liquid separation mixture
Claims (2)
1. one kind is adopted improvement potash to absorb CO
2Capture new technology, it is characterized in that this technology comprises the steps:
1) adopt wet chemical to add promoter hydroxyethyl piperazine and potassium borate absorption CO
2,
Contain CO
2Unstripped gas and the purified gas that comes out from top, absorption tower (3) gas heat exchanger (1) by preheating after, (3) bottom gets into the absorption tower from the absorption tower; From the solution of potassium carbonate that contains promoter hydroxyethyl piperazine and potassium borate of absorbent storage tank and absorbent lean solution from desorber (6) bottom; (3) top gets into the absorption tower from the absorption tower after the heat exchange in liquid heat-exchanger (2); Unstripped gas and absorbent be counter current contacting in absorption tower (3), CO
2Being absorbed agent absorbs; The absorption tower temperature is controlled at 70～115 ℃, and pressure is controlled at 2.5MPa～3.5MPa; In the absorption tower, remove CO
2Purified gas and unstripped gas heat exchange after temperature reduce to 40～65 ℃ after from the absorption tower toward next operation, absorbed CO
2The absorbent rich solution send into preparatory desorber (4) and carry out preparatory desorb;
2) the thermal coupling desorption and regeneration of absorbent rich solution
Absorbent rich solution from absorption tower (3) is sent into preparatory desorber (4) from the middle part, the tower still is with preparatory desorb reboiler (5) heating, and desorb reboiler (5) adopts the 8～10kg/cm that provides from the system share engineering in advance
2Steam as the heating thermal source, in advance the desorber temperature is controlled at 110～180 ℃, pressure is controlled at 0.2MPa～0.5MPa, the steam of desorb cat head is sent into desorb reboiler (7) as the heating thermal source in advance;
Liquid phase from preparatory desorber (4) adds desorber (6) from the middle part; The tower still heats with desorb reboiler (7); The thermal source of desorb reboiler (7) is used the steam from preparatory desorb cat head; The desorber temperature is controlled at 80～130 ℃, and pressure is controlled at 0.01MPa～0.1MPa, send the absorbent storage tank after the absorbent heat exchange on the desorption barren solution of desorber (6) and entering absorption tower;
The gas phase at desorber (6) top and send separation of C O in the vapour liquid separator (8) in the lump from the steam condensate vapour mixture at preparatory desorber top
2And water, wherein CO
2Deliver to recovery process, water returns the absorbent storage tank and uses as supplementing water.
2. said employing improves potash absorption CO according to claim 1
2Capture new technology, it is characterized in that said absorbent is a wet chemical, wherein the content of potash is 20～35wt%; Promoter is hydroxyethyl piperazine content at 1～3wt% and potassium borate content at 0.1～0.8wt%, and surplus is a water.
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| CN2010101966726A CN101856579B (en) | 2010-06-02 | 2010-06-02 | Novel energy-saving CO2 trapping process of improved potassium carbonate |
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| CN102784544B (en) * | 2012-08-03 | 2014-09-03 | 中国华能集团清洁能源技术研究院有限公司 | IGCC (Integrated Gasification Combined Cycle) based pre-combustion CO2 capture system |
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| CN112452109B (en) * | 2020-12-31 | 2021-08-27 | 双盾环境科技有限公司 | Desorption SO for improving desulfurization absorbent2Efficient process |
| CN114712990B (en) * | 2022-03-17 | 2023-08-08 | 中国华能集团清洁能源技术研究院有限公司 | CO (carbon monoxide) 2 Regeneration device and process method |
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| CN1006041B (en) * | 1985-05-08 | 1989-12-13 | 南京化学工业公司研究院 | Composite Catalytic Potassium Carbonate Solution for Removing Carbon Dioxide in Mixed Gas |
| JPH06210129A (en) * | 1993-01-20 | 1994-08-02 | Mitsubishi Heavy Ind Ltd | Waste gas treatment |
| CN1137753C (en) * | 2000-12-19 | 2004-02-11 | 中国冶金建设集团鞍山焦化耐火材料设计研究总院 | Process for removing CO2 and H2S from biological gas |
| CN101456537B (en) * | 2007-12-11 | 2011-06-15 | 南化集团研究院 | Method for reducing carbon dioxide in GTL synthesis cycle gas |
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