CN220413278U - CO using fossil energy as raw material 2 Trapping system - Google Patents
CO using fossil energy as raw material 2 Trapping system Download PDFInfo
- Publication number
- CN220413278U CN220413278U CN202320333928.6U CN202320333928U CN220413278U CN 220413278 U CN220413278 U CN 220413278U CN 202320333928 U CN202320333928 U CN 202320333928U CN 220413278 U CN220413278 U CN 220413278U
- Authority
- CN
- China
- Prior art keywords
- methanol
- low
- raw material
- liquid
- heat exchange
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000002994 raw material Substances 0.000 title claims abstract description 17
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 192
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000007788 liquid Substances 0.000 claims abstract description 26
- 238000005406 washing Methods 0.000 claims abstract description 24
- 239000003507 refrigerant Substances 0.000 claims abstract description 17
- 230000006835 compression Effects 0.000 claims abstract description 4
- 238000007906 compression Methods 0.000 claims abstract description 4
- 230000008929 regeneration Effects 0.000 claims description 20
- 238000011069 regeneration method Methods 0.000 claims description 20
- 238000003795 desorption Methods 0.000 claims description 12
- 238000005057 refrigeration Methods 0.000 claims description 11
- 238000010521 absorption reaction Methods 0.000 claims description 9
- 230000001502 supplementing effect Effects 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 8
- 230000001172 regenerating effect Effects 0.000 claims description 3
- 239000002826 coolant Substances 0.000 claims description 2
- 229910021529 ammonia Inorganic materials 0.000 abstract description 10
- 239000000126 substance Substances 0.000 abstract description 9
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 abstract description 7
- 239000004202 carbamide Substances 0.000 abstract description 7
- 239000003245 coal Substances 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000002309 gasification Methods 0.000 abstract description 3
- 238000003303 reheating Methods 0.000 abstract 1
- 150000003568 thioethers Chemical class 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 33
- 230000015572 biosynthetic process Effects 0.000 description 9
- 238000003786 synthesis reaction Methods 0.000 description 9
- 229910052799 carbon Inorganic materials 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 238000000034 method Methods 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 238000001704 evaporation Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000002253 acid Substances 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 description 3
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 description 3
- 235000012538 ammonium bicarbonate Nutrition 0.000 description 3
- 239000001099 ammonium carbonate Substances 0.000 description 3
- 230000003009 desulfurizing effect Effects 0.000 description 3
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 2
- AFCARXCZXQIEQB-UHFFFAOYSA-N N-[3-oxo-3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)propyl]-2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidine-5-carboxamide Chemical compound O=C(CCNC(=O)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F)N1CC2=C(CC1)NN=N2 AFCARXCZXQIEQB-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- IEJIGPNLZYLLBP-UHFFFAOYSA-N dimethyl carbonate Chemical compound COC(=O)OC IEJIGPNLZYLLBP-UHFFFAOYSA-N 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
Classifications
-
- 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
Landscapes
- Gas Separation By Absorption (AREA)
Abstract
The application provides a CO using fossil energy as raw material 2 A trapping system and. The application takes fossil energy (coal or oil) as raw material to gasify and then generates a large amount of CO for producing chemical products 2 And no longer vents to atmosphere, and the system captures all of it. The trapping system has high efficiency and CO 2 High purity>99.9 percent, the energy consumption of the device system is low. CO removal 2 The system is a low-temperature methanol washing device at the temperature of minus 60 ℃ and contains high-concentration CO 2 The raw material gas is first enriched with methanol (dissolved with CO) 2 ) Removal of sulfides by liquid CO 2 About 40% CO in the raw material gas is used as a refrigerant 2 Condensing liquid CO at high pressure 2 Directly captured, placed in a reservoir or directly utilized. When the feed gas is used to produce synthetic ammonia and further processed to urea, CO 2 For use as urea-producing raw material, liquid CO 2 Recovering cold by reheating gasification, and reducing CO for producing urea 2 Compression energy consumption.
Description
Technical Field
The utility model belongs to the field of chemical industry, and in particular relates to CO using fossil energy as a raw material 2 A trapping system.
Background
Fossil energy coal or oil is used as chemical raw material, and gasification products mainly comprise CO and H 2 、CO 2 And a small amount of H 2 S and other synthesis gases, according to different chemical products processed downstream, CO is partially or completely mixed with H 2 Conversion of O to H 2 And CO 2 Thus generating a large amount of CO 2 Must be removed.
At present, the CO can be washed by cold method and low temperature methanol 2 All absorb and are rich in CO 2 After regeneration of the methanol solution, all CO is resolved 2 Only when synthesis gas is used to produce synthetic ammonia and all is processed into urea can 40% of CO be utilized 2 All CO is produced in the process of using synthetic gas in producing industrial hydrogen, synthetic methanol, synthetic olefin, glycol, synthetic oil, synthetic natural gas, synthetic arene or methanol as material 2 And vented to atmosphere. CO has long been available 2 The emission of greenhouse gases seriously affects the temperature of the atmospheric environment, so CCUS (Carbon Capture Utilization and Storage), namely carbon capture, utilization and sealing are proposed; to achieve this, the capture of carbon is first resolved before it can be utilized and sequestered.
Fossil energy, in particular coalThe chemical industry is the chemical industry with high carbon chemical industry and high carbon emission, the active development of carbon trapping technology is urgent, and CO is trapped with high efficiency, high purity and low cost 2 Is pursued by the technicians in the field, and can further set up a safe and reliable total CO trapping device 2 The system.
Disclosure of Invention
The utility model provides a method for discharging CO by taking fossil energy as raw material 2 The gas is trapped for easy utilization and sequestration. In order to achieve the above purpose, the utility model provides a method for desulfurizing the synthesis gas in the low-temperature methanol washing system, namely using liquid CO 2 As refrigerant, CO with high concentration 2 Part of the water is directly condensed and recycled to occupy CO 2 About 40% of the total amount, can greatly reduce the amount of the catalyst used for absorbing CO 2 The energy consumption is reduced.
CO using fossil energy as raw material 2 A capture system of the CO 2 The trapping system comprises a low-temperature methanol washing device, wherein the low-temperature methanol washing device comprises a device for washing CO in raw material gas 2 Liquefied CO 2 Heat exchange condenser, CO 2 The heat exchange condenser is connected with CO 2 Absorption tower, CO 2 The absorption tower is connected with a methanol solution regeneration device through a low-temperature methanol washing and supplementing cooler, and the methanol solution regeneration device is connected with a device for regenerating CO 2 A liquefied refrigeration device; the CO 2 The heat exchange condenser and the low-temperature methanol washing and cooling device are all liquid CO 2 As a refrigerant.
Optionally, the CO 2 The heat exchange condenser is connected with a feed gas precooler.
Optionally, the CO 2 Liquid CO used as refrigerant in heat exchange condenser and low-temperature methanol washing and supplementing cooler 2 And after heat exchange, the liquid enters a refrigerating device for liquefaction.
Optionally, the CO 2 The capture system also includes CO 2 Reservoir, CO 2 Liquefied CO obtained by liquefying in heat exchange condenser and refrigerating device 2 Entering CO 2 In the reservoir, and CO 2 Liquid CO in a reservoir 2 As coolant to enter CO 2 The heat exchange condenser and the low-temperature methanol washing and supplementing cooler.
Optionally, CO 2 Liquid CO in a reservoir 2 And outputting and storing.
Optionally, the refrigeration device is CO 2 /NH 3 Cascade refrigeration device comprising a device for compressing atmospheric CO 2 Gas cylinder I for compression of high pressure CO 2 A gas II cylinder and a liquid ammonia refrigerator for condensing the compressed CO 2.
Optionally, the methanol solution regeneration device comprises a methanol solution regeneration device which comprises a methanol-rich solution low-pressure desorption system, a methanol-rich solution vacuum desorption system, a methanol-rich solution thermal regeneration system and a vacuum pump; the methanol-rich solution low-pressure desorption system is connected with the No. II cylinder, and the methanol-rich solution vacuum desorption system is connected with the No. I cylinder through the methanol-rich solution thermal regeneration system.
The method of the application can obtain the following beneficial effects:
the utility model provides a method for producing a large amount of CO generated by using fossil energy as raw material (coal or oil), especially using coal chemical industry as an example 2 And no longer vents to atmosphere, and the system captures all of it. Further more optimizing the liquid CO to be recovered 2 When directly used, such as processing synthetic ammonia into urea, can reheat gas under high pressure, not only recover cold energy, but also save CO 2 The compressor can be powered.
The utility model further optimizes the cold supplementing system for low-temperature methanol washing. With liquid CO 2 The refrigerant is used as a refrigerant to replace the conventional liquid ammonia refrigerant so as to meet the operation condition of cold supplement at-40 ℃. It is characterized in that firstly, due to liquid CO 2 The evaporation pressure is high, the molecular weight is far greater than that of ammonia, the investment of the device is reduced, and the energy consumption is saved; secondly, ammonia medium is poisonous, inflammable and explosive, and CO 2 Is inert gas, and improves the safety; thirdly, ammonia is used as a refrigerant, and once the low-temperature heat exchanger leaks, CO is dissolved out from the methanol solution 2 And the ammonium bicarbonate is generated after the ammonium bicarbonate reacts with ammonia, so that equipment and pipelines are blocked and stopped, and production is affected. And by CO 2 Can not occur when used as a refrigerant, and ensures more reliable and stable productionAnd (5) setting. CO of low pressure 0.16MPaGr analyzed by methanol solvent regeneration system 2 (CO 2 >98.5%) and atmospheric CO 2 (CO 2 >99%) no longer vents to atmosphere and is fed to CO 2 /NH 3 Is compressed and liquefied, and the whole liquid CO is captured and sent into the cascade refrigeration system of (2) 2 A reservoir. Small amounts of acid gases (H-containing) discharged from the regeneration system 2 S>30%) sulfur recovery system wherein CO 2 The content is less than 0.5%. Thus can realize the trapping of CO 2 Up to 99.5%.
The utility model further optimizes and ensures the CO discharged by the methanol washing and regenerating system 2 To CO 2 /NH 3 Cascade refrigeration system, step-by-step pressurization by combined refrigeration compressor unit, CO 2 Condensing into liquid state and recovering. Low pressure CO 2 Accounting for 32 percent of the total CO at normal pressure 2 Accounting for 28 percent, adding the CO recovered by direct liquefaction 2 The total recovery rate is more than 99.5%. For the cascade refrigerating unit, ammonia is refrigerated under standard working condition (-15 ℃) with low energy consumption, thus the whole CO 2 /NH 3 The refrigerating unit has high efficiency.
Drawings
FIG. 1 is a graph of CO from fossil energy of example 1 2 A schematic diagram of a trapping system;
FIG. 2 is a schematic diagram of a low temperature methanol washing apparatus according to example 1;
FIG. 3 is a CO provided in example 1 2 /NH 3 The structure of the cascade refrigeration system is schematically shown.
Detailed Description
The technical scheme of the utility model will be clearly and completely described below with reference to the accompanying drawings.
The components and connection relation of the system are shown in figure 1, wherein 1 represents a fossil energy (coal or oil) gas production system, and the system comprises a fossil energy gasification conversion device and a conversion device for adjusting the components of raw gas according to different production chemical products.
CO enriched output from a gas production system 2 The raw material gas of (2) enters the low-temperature methanol washing device through the pre-cooling heat exchanger (8). Wherein the precooling heat exchanger 8 is liquidCO 2 A heat exchanger for evaporating pre-cooled feed gas.
The low-temperature methanol washing device 2 comprises a raw material gas desulfurizing tower and CO 2 Condensing heat exchanger and CO 2 Absorption towers, etc., the specific structure of which can be seen with reference to fig. 2. The raw material gas is desulfurized by a desulfurizing tower, and the desulfurized gas does not enter CO first 2 The absorption tower will contain high concentration CO 2 The synthesis gas (pressure is 4.0-6.5 MPaG) enters into a liquid CO through a desulfurization purified gas cooler 2-2 2 Heat exchanger 2-3 for refrigerant, the total amount of CO is about 40% 2 Direct liquefaction, separated CO 2 Stored in tanks 2-4 (or re-heated for evaporation at high pressure). The rest of CO 2 In CO 2 The absorption tower 2-1 is absorbed by low temperature methanol to form a solution. CO re-entry of synthesis gas 2 The absorption tower can reduce 40% of methanol solvent and save the power consumption of the solution pump with the same quantity.
Recovered CO 2 Into high-pressure gas CO 2 Using system 9: including urea, sodium carbonate or dimethyl carbonate. If the synthesis ammonia from synthesis gas is processed into urea, the separated CO 2 Can be fully utilized and greatly save CO 2 Compression work.
CO absorption 2 The raw gas after the reaction enters a refined synthesis gas utilization system 10, and comprises a device for processing various types of synthesis gas into chemical products. Containing CO 2 The methanol solution is subjected to cold compensation by a low-temperature methanol washing and cooling device 3 and enters a methanol solution regeneration device 4. The low-temperature methanol washing and supplementing cooler 3 comprises 3 to 4 liquid CO 2 As a low temperature heat exchanger for the refrigerant and methanol solution. To ensure the operating condition of the methanol solution at-60 ℃, the solution must be continuously supplemented with cold. At present, the traditional flow is almost to use liquid ammonia for evaporation and cooling, but the temperature required for cooling is-40 ℃, and in actual operation, the evaporation of liquid ammonia at-40 ℃ is negative pressure, which is difficult to meet, especially in summer working conditions, and can only be maintained at-34 ℃ to-36 ℃. One side of the low-temperature heat exchanger is high-pressure methanol solution, and the other side is normal pressure or slightly negative pressure NH 3 When the heat exchanger leaks slightly, the CO overflows from the solution 2 With NH 3 The reaction generates ammonium bicarbonate crystals, which cause blockage and stopping. In addition NH 3 Molecular weight is much smaller than CO 2 And the pressure is very low, which leads to increased investment in the device. The utility model uses liquid CO 2 As a refrigerant, the refrigerant does not generate crystallization even if leaked, and can ensure the cooling supplement of MPaG at-40 ℃ to-50 ℃ and the pressure of 0.9 to 1.0, and evaporated CO 2 CO feeding 2 /NH 3 The compressor unit is liquefied, and the superiority is obvious.
The methanol solution regeneration device 4 comprises a methanol-rich low-pressure desorption system 4-1, a methanol-rich vacuum desorption system 4-2, a methanol-rich thermal regeneration system 4-3 and a vacuum compressor 4-4. Wherein the methanol-rich low pressure desorption system 4-1 analyzes CO of about 0.16MPaG 2 Gas, CO accounting for 32 percent of the total amount 2 Atmospheric CO sent by the methanol-rich vacuum desorption system 4-2 through the methanol-rich thermal regeneration system 4-3 2 Gas, CO accounting for 28 percent of the total amount 2 The method comprises the steps of carrying out a first treatment on the surface of the The methanol-rich thermal regeneration system discharges a small amount of CO 2 Is an acid gas of (a) a (c). The two CO streams 2 The gases are respectively sent to a refrigerating device for liquefaction and recovery.
The refrigerating device is CO 2 /NH 3 The cascade refrigeration system is shown in fig. 3. The CO 2 /NH 3 Cascade refrigeration system comprising high pressure CO 2 Liquid separating tank 5-1, low pressure CO 2 Liquid separating tank 5-1, atmospheric CO 2 A liquid separating tank 5-1, a combined compressor unit, etc. 0.16MPaG Low pressure CO 2 0.9 to 1.0MPaG high pressure CO from figure 3 2 Entering a No. II cylinder 5-4, and pressurizing to 2.2-2.4 MPaG through a compressor; atmospheric CO 2 The gas enters a No. I cylinder 5-5 and is independently compressed to 2.2-2.4 MPaG. The No. I cylinder and the No. II cylinder are connected with a compressor driving system 5-7 through a coupling 5-6. CO compressed by No. I cylinder and No. II cylinder 2 Firstly, cooling by using water coolers 5-8 and 5-10; then the liquid ammonia is condensed and evaporated in a liquid ammonia condensing evaporator 5-9, 5-11, liquid ammonia is used as a refrigerant, and CO is evaporated at the temperature of minus 15 DEG C 2 Liquefying and sending to a storage system. The gas ammonia is pressurized by a compressor and is water-cooled for liquefaction and cyclic utilization.
The capture system also includes liquid CO 2 A reservoir 7 for liquefying and recovering CO 2 All are stored by a low-temperature tank, and a small part of liquid CO 2 Entering CO 2 The heat exchange condenser and the low-temperature methanol washing and supplementing cooler are used as refrigerant, and then enter the refrigerating device 5 for recycling.
H 2 S concentration tower discharged with a small amount of CO 2 Acid gas of (2) into acid gas (H) 2 S) a sulfur recovery system 6.
The foregoing description is only a few examples of the present application and is not intended to limit the present application in any way, and although the present application is disclosed in the preferred examples, it is not intended to limit the present application, and any person skilled in the art may make some changes or modifications to the disclosed technology without departing from the scope of the technical solution of the present application, and the technical solution is equivalent to the equivalent embodiments.
Claims (4)
1. CO using fossil energy as raw material 2 A capturing system characterized in that the CO 2 The trapping system comprises a low-temperature methanol washing device, wherein the low-temperature methanol washing device comprises a device for washing CO in raw material gas 2 Liquefied CO 2 Heat exchange condenser, CO 2 The heat exchange condenser is connected with CO 2 Absorption tower, CO 2 The absorption tower is connected with a methanol solution regeneration device through a low-temperature methanol washing and supplementing cooler, and the methanol solution regeneration device is connected with a device for regenerating CO 2 A liquefied refrigeration device; the CO 2 The heat exchange condenser and the low-temperature methanol washing and cooling device are all liquid CO 2 As a refrigerant;
the refrigerating device is CO 2 /NH 3 Cascade refrigeration device comprising a device for compressing atmospheric CO 2 Gas cylinder I for compression of high pressure CO 2 Gas cylinder II for compressing CO 2 A condensed liquid ammonia refrigerator;
the methanol solution regeneration device comprises a methanol solution regeneration device which comprises a methanol-rich solution low-pressure desorption system, a methanol-rich solution vacuum desorption system, a methanol-rich solution thermal regeneration system and a vacuum pump; the methanol-rich solution low-pressure desorption system is connected with the No. II cylinder, and the methanol-rich solution vacuum desorption system is connected with the No. I cylinder through the methanol-rich solution thermal regeneration system.
2. The CO according to claim 1 2 A capturing system characterized in that the CO 2 The heat exchange condenser is connected with a feed gas precooler.
3. The CO according to claim 1 2 A capturing system characterized in that the CO 2 Liquid CO used as refrigerant in heat exchange condenser and low-temperature methanol washing and supplementing cooler 2 And after heat exchange, the liquid enters a refrigerating device for liquefaction.
4. The CO according to claim 1 2 A capturing system characterized in that the CO 2 The capture system also includes CO 2 Reservoir, CO 2 Liquefied CO obtained by liquefying in heat exchange condenser and refrigerating device 2 Entering CO 2 In the reservoir, and CO 2 Liquid CO in a reservoir 2 As coolant to enter CO 2 The heat exchange condenser and the low-temperature methanol washing and supplementing cooler.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320333928.6U CN220413278U (en) | 2023-02-27 | 2023-02-27 | CO using fossil energy as raw material 2 Trapping system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320333928.6U CN220413278U (en) | 2023-02-27 | 2023-02-27 | CO using fossil energy as raw material 2 Trapping system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220413278U true CN220413278U (en) | 2024-01-30 |
Family
ID=89653316
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202320333928.6U Active CN220413278U (en) | 2023-02-27 | 2023-02-27 | CO using fossil energy as raw material 2 Trapping system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220413278U (en) |
-
2023
- 2023-02-27 CN CN202320333928.6U patent/CN220413278U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP2117682B1 (en) | Configurations for carbon dioxide and hydrogen production from gasification streams | |
| CN101885993B (en) | Purification process for removing sulphur and carbon dioxide in gas by using two-step method | |
| CN105268283A (en) | Combined absorption carbon dioxide trapping and compressing treatment technology | |
| WO2010043859A1 (en) | High pressure physical absorption process for use in carbon capture in energy production processes | |
| CN103857456A (en) | Process for the removal of carbon dioxide from a gas | |
| CN112221327A (en) | Carbon dioxide ammonia capture and low-temperature liquefaction system and method for coal-fired power plant | |
| WO2010097047A1 (en) | Apparatus and method for compressing co2, system and method for separating and recovering co2 | |
| CN113758147A (en) | Carbon capture hydrogen plant before burning | |
| CN101637694B (en) | Method for separating and recycling CO2 from mixed gas containing CO2 | |
| CN220413278U (en) | CO using fossil energy as raw material 2 Trapping system | |
| FR3145601A1 (en) | DEVICE AND METHOD FOR RECOVERING CARBON DIOXIDE AND NITROGEN FROM COMBUSTION GASES | |
| CN213556279U (en) | Carbon dioxide ammonia method capturing and low-temperature liquefying system of coal-fired power plant | |
| KR102194763B1 (en) | Co2 recovery system having cooling function using low-temperature waste heat | |
| CN216347344U (en) | Device for realizing carbon capture and liquefaction by using ammonia crystallization method | |
| CN216303278U (en) | Direct liquefaction capture system of carbon dioxide under supercritical pressure | |
| CN118546707A (en) | CO using fossil energy as raw material2Capture system and CO2Trapping method | |
| CN111004082A (en) | System and method for removing carbon dioxide from C2 fraction | |
| CN113897229A (en) | Marine LNG gas supply system with carbon capture function | |
| CN213643154U (en) | Low-temperature methanol washing medium-pressure flash evaporation device | |
| CN109987583B (en) | Process for recovering hydrogen in tail gas in production of 1, 4-butanediol | |
| CN210410096U (en) | Separation system for carbon dioxide in medium-high pressure gas source | |
| CN113731117A (en) | Novel process for high-efficiency low-temperature methanol elution and pure recovery of carbon dioxide | |
| CN110756000A (en) | Carbon capture and refrigeration system by ammonia crystallization method | |
| GB2464368A (en) | A solvent regeneration process | |
| CN216550316U (en) | Marine LNG gas supply system with carbon capture function |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |