CN117125673B - Large-scale carbon capture system - Google Patents
Large-scale carbon capture system Download PDFInfo
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- CN117125673B CN117125673B CN202311063275.5A CN202311063275A CN117125673B CN 117125673 B CN117125673 B CN 117125673B CN 202311063275 A CN202311063275 A CN 202311063275A CN 117125673 B CN117125673 B CN 117125673B
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- desulfurization
- decarburization
- heat exchanger
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- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 23
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 22
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 195
- 239000007788 liquid Substances 0.000 claims abstract description 142
- 238000005261 decarburization Methods 0.000 claims abstract description 122
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 119
- 230000023556 desulfurization Effects 0.000 claims abstract description 119
- 238000001816 cooling Methods 0.000 claims abstract description 70
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 44
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 44
- 238000000926 separation method Methods 0.000 claims abstract description 42
- 238000001704 evaporation Methods 0.000 claims abstract description 41
- 230000008020 evaporation Effects 0.000 claims abstract description 37
- 238000005406 washing Methods 0.000 claims abstract description 35
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000004202 carbamide Substances 0.000 claims abstract description 27
- 238000005262 decarbonization Methods 0.000 claims abstract description 10
- 239000007789 gas Substances 0.000 claims description 182
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 39
- 239000007921 spray Substances 0.000 claims description 25
- 229910052757 nitrogen Inorganic materials 0.000 claims description 20
- 238000005192 partition Methods 0.000 claims description 17
- 238000006243 chemical reaction Methods 0.000 claims description 12
- 239000000945 filler Substances 0.000 claims description 9
- 238000004891 communication Methods 0.000 claims description 7
- 238000005507 spraying Methods 0.000 claims description 7
- 230000008859 change Effects 0.000 claims description 6
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 239000002912 waste gas Substances 0.000 claims 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 14
- 239000003245 coal Substances 0.000 description 10
- 238000005265 energy consumption Methods 0.000 description 10
- 229910052739 hydrogen Inorganic materials 0.000 description 9
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 239000001569 carbon dioxide Substances 0.000 description 7
- 230000004888 barrier function Effects 0.000 description 6
- 230000009286 beneficial effect Effects 0.000 description 5
- 230000003009 desulfurizing effect Effects 0.000 description 5
- 230000002194 synthesizing effect Effects 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 238000002309 gasification Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 230000000149 penetrating effect Effects 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 239000004743 Polypropylene Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000000975 co-precipitation Methods 0.000 description 1
- 238000011278 co-treatment Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- -1 polypropylene Polymers 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1468—Removing hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C273/00—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups
- C07C273/02—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds
- C07C273/04—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds from carbon dioxide and ammonia
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D21/0001—Recuperative heat exchangers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/16—Hydrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/304—Hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
- B01J2219/00004—Scale aspects
- B01J2219/00006—Large-scale industrial plants
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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
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0415—Purification by absorption in liquids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0485—Composition of the impurity the impurity being a sulfur compound
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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
- 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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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Inorganic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention provides a large-scale carbon capture system which comprises a primary cooling heat exchanger, a first gas-liquid separation tank, a low-temperature methanol washing tower and CO 2 Evaporation heat exchanger, second gas-liquid separation tank, flash tank and CO 2 Gas compressor, urea synthesizer and CO 2 An analytical tower; a desulfurization chamber and a decarbonization chamber are arranged in the low-temperature methanol washing tower, the primary cooling heat exchanger is communicated with a first gas-liquid separation tank, the first gas-liquid separation tank is communicated with the desulfurization chamber, and the desulfurization chamber is communicated with CO 2 The evaporation heat exchanger is communicated; the evaporation heat exchanger is communicated with a second gas-liquid separation tank, the second gas-liquid separation tank is communicated with a flash tank, the flash tank is communicated with the evaporation heat exchanger, and the evaporation heat exchanger is communicated with CO 2 The gas compressor is communicated with CO 2 The gas compressor is communicated with the urea synthesis device; the second gas-liquid separation tank is also communicated with the decarburization chamber, and a second liquid outlet is communicated with CO 2 The analysis tower is communicated with CO 2 Analytical column and CO 2 The gas compressor is communicated. The large-scale carbon capture system of the present invention is less energy consuming than prior art when carbon capture is performed.
Description
Technical Field
The invention relates to the technical field of coal chemical industry, in particular to a large-scale carbon capture system.
Background
The energy structure of China is rich in coal, lean in gas and less in oil, so that under the condition of rich coal resources, the coal chemical industry is greatly developed, and the clean, efficient and energy-saving coal gasification technology becomes a key development direction. Conversion gas obtained by pressurized gasification of coalThe parameters are generally: 40 ℃ and 5.8Mpa; the main component is CO 2 ：44.416％，H 2 ：54.246％，H 2 S：0.497％，CO：0.398％，H 2 O:0.251%. Change of H in gas 2 S and CO 2 If the acid gas is not purified, the acid gas can cause catalyst poisoning in the subsequent reaction process. The low-temperature methanol washing process is widely applied to the acid gas removal process of coal methanol, coal natural gas and coal synthetic ammonia in the coal chemical industry, and has better selectivity to carbon dioxide and sulfides, large treatment capacity and high purification efficiency.
The low-temperature methanol washing process in the prior art uses low-temperature methanol liquid with the temperature of minus 50 ℃ to minus 60 ℃ as an absorbent to absorb H in the conversion gas 2 S、CO 2 CO is absorbed by the shift gas through a washing tower with low-temperature methanol washing 2 And H 2 And (3) sending the qualified S to a liquid nitrogen washing device, absorbing trace impurities such as argon, methane and the like in the converted gas, and simultaneously providing the synthesis gas with the hydrogen-nitrogen ratio of 3:1 for the subsequent ammonia synthesis process. When the low-temperature methanol liquid absorbs enough CO 2 After that, by CO 2 The low-pressure analysis is carried out on the low-temperature methanol liquid by the analysis tower, so that CO absorbed by the low-temperature methanol liquid 2 Release and then release CO 2 Collecting and pressurizing by a compressor in multiple stages, and delivering the pressurized urea to a urea synthesizing device for synthesizing urea to realize carbon capture, namely CO 2 Is included in the collection of the liquid.
In the prior art, the circulation amount of the low-temperature methanol liquid required to be used in carbon capture is large, so that the required cold energy is large and the energy consumption is large; further, the CO obtained by low-temperature methanol liquid low-pressure analysis 2 The pressure of the gas is small and needs to be controlled by CO 2 The gas can be sent to the urea synthesis device for synthesizing urea after multi-stage pressurization, and more energy sources are required to be consumed during multi-stage pressurization.
Disclosure of Invention
The application provides a large-scale carbon capture system to solve the technical problem of high energy consumption existing in the prior art when carbon capture is performed.
The invention provides a large-scale carbon capture system, which adopts the following technical scheme:
a large-scale carbon capture system comprises a methanol spray device, a primary cooling heat exchanger, a first gas-liquid separation tank, a low-temperature methanol washing tower and CO 2 Evaporation heat exchanger, second gas-liquid separation tank, flash tank and CO 2 Gas compressor, urea synthesizer and CO 2 An analytical tower; a desulfurization chamber and a decarburization chamber are arranged in the low-temperature methanol washing tower, and the desulfurization chamber is used for absorbing H 2 S gas, decarbonization chamber for absorbing CO 2 The gas, the desulfurization chamber and the decarburization chamber are separated by a middle partition board, a decarburization liquid spray head is fixedly arranged on the chamber wall of the decarburization chamber, and a second liquid outlet is formed on the chamber wall of the decarburization chamber; the methanol spray device is communicated with a conversion gas input pipeline, the primary cooling heat exchanger is communicated with the methanol spray device through a pipeline, the primary cooling heat exchanger is used for liquefying moisture contained in the conversion gas, the primary cooling heat exchanger is also communicated with the inlet of a first gas-liquid separation tank through a pipeline, the outlet of the first gas-liquid separation tank is communicated with a desulfurization chamber of a low-temperature methanol washing tower through a pipeline, and the air outlet of the desulfurization chamber is communicated with CO through a pipeline 2 The evaporation heat exchanger is communicated; CO 2 The evaporation heat exchanger enables the shift gas after desulfurization to contain part of CO 2 The gas liquefaction, the evaporation heat exchanger is communicated with a second gas-liquid separation tank through a pipeline, the second gas-liquid separation tank is communicated with a flash tank through a pipeline, and the second gas-liquid separation tank enables CO to be obtained 2 Liquid enters a flash tank which is communicated with an evaporation heat exchanger through a pipeline, and CO 2 The liquid enters an evaporation heat exchanger to absorb heat and change into gas, and the evaporation heat exchanger is connected with CO through a pipeline 2 The gas compressor is communicated with CO 2 The gas compressor is communicated with the urea synthesis device through a pipeline; the second gas-liquid separation tank is also communicated with a decarburization chamber of the low-temperature methanol washing tower through a pipeline, and the second liquid outlet is communicated with CO through a pipeline 2 The analysis tower is communicated with CO 2 The analysis tower is connected with CO through a pipeline 2 The gas compressor is communicated.
The beneficial effects of adopting above-mentioned technical scheme are: absorption of H in shift gas by desulfurization chamber 2 S gas, retain H in the converted gas 2 And CO 2 Gas, realize CO 2 And H is 2 S separation, then by CO 2 The evaporating heat exchanger carries out secondary cooling treatment to make most of CO in the converted gas 2 The gas is liquefied, so that the amount of gas input into the decarburization chamber is reduced, the required circulation amount of decarburization liquid is reduced, and the energy consumption is further reduced. In addition, CO is fed to the urea synthesis plant for urea synthesis 2 Part of the gas is formed by CO 2 The liquid is gasified, and the other part is obtained by CO 2 Resolving by a resolving tower, and obtaining by CO 2 CO obtained by gasification of liquid 2 The pressure of the gas is higher than that of CO 2 Resolving the obtained CO by a resolving tower 2 The pressure of the gas is high. CO sent to a urea synthesis plant for urea synthesis in the prior art 2 The gases are all CO 2 The total CO obtained in the present application is thus obtained by analysis in a resolving tower 2 The gas is pressurized to the required pressure, which requires the energy consumption of the compressor, compared with the CO obtained in the prior art 2 The gas needs to consume less energy of the compressor when being pressurized to the required pressure.
Further, an upper desulfurization baffle plate and a lower desulfurization baffle plate are fixedly arranged in the desulfurization chamber, the upper desulfurization baffle plate and the lower desulfurization baffle plate divide the desulfurization chamber into a desulfurization air inlet chamber, a desulfurization middle chamber and a desulfurization air outlet chamber which are sequentially arranged from bottom to top, an air inlet is formed in the chamber wall of the desulfurization air inlet chamber, a desulfurization piece is fixedly arranged in the desulfurization middle chamber, the desulfurization piece comprises a desulfurization pipe and granular fillers filled in the desulfurization pipe, the desulfurization pipe is communicated with the desulfurization air inlet chamber, the desulfurization pipe is communicated with the desulfurization air outlet chamber, an air outlet is formed in the chamber wall of the desulfurization air outlet chamber, and a desulfurization liquid spray head is arranged on the chamber wall of the desulfurization air outlet chamber; the upper decarburization partition plate and the lower decarburization partition plate are fixedly arranged in the decarburization chamber, the upper decarburization partition plate and the lower decarburization partition plate divide the decarburization chamber into a decarburization air inlet chamber, a decarburization middle chamber and a decarburization air outlet chamber which are sequentially arranged from bottom to top, an air inlet is formed in the chamber wall of the decarburization air inlet chamber, a second liquid outlet is formed in the bottom of the decarburization air inlet chamber, a decarburization part is fixedly arranged in the decarburization middle chamber and comprises a decarburization pipe and granular fillers filled in the decarburization pipe, the decarburization pipe is communicated with the decarburization air inlet chamber, the decarburization pipe is communicated with the decarburization air outlet chamber, an air outlet is formed in the chamber wall of the decarburization air outlet chamber, and a decarburization liquid spray head is fixedly arranged on the chamber wall of the decarburization air outlet chamber.
The beneficial effects of adopting above-mentioned technical scheme are: when the gas is used, the gas enters the decarburization air inlet chamber and then enters the decarburization pipe, then enters the decarburization air outlet chamber, the decarburization liquid sprayed by the decarburization liquid spray head flows downwards into the decarburization air inlet chamber through the decarburization pipe, and the surface of the granular filler filled in the decarburization pipe forms a liquid film because the decarburization liquid flows downwards through the decarburization pipe, so that the gas can be more fully contacted with the decarburization liquid when entering the decarburization pipe and flowing upwards, and CO contained in the gas can be further caused 2 The gas is more fully absorbed.
Further, the device also comprises a pre-cooling heat exchanger, wherein the pre-cooling heat exchanger is arranged at the air outlet of the desulfurization chamber and is communicated with CO 2 The precooling heat exchanger is used for precooling the gas after desulfurization treatment on a pipeline of the evaporation heat exchanger; communicating CO 2 Analytical column and CO 2 The pipeline of the gas compressor firstly passes through a pre-cooling heat exchanger, then passes through a primary cooling heat exchanger and is connected to the CO 2 On gas compressor, so that CO 2 CO resolved by the resolving tower 2 Absorbing heat in the pre-cooling heat exchanger and the first-stage cooling heat exchanger in sequence and then conveying the heat to the CO 2 A gas compressor.
The beneficial effects of adopting above-mentioned technical scheme are: due to CO 2 CO released from decarbonizing liquid resolved by resolving tower 2 The gas carries a part of the cold energy and releases CO 2 The gas is sequentially conveyed into the pre-cooling heat exchanger and the primary cooling heat exchanger to exchange heat, and the released CO is fully utilized 2 The cooling capacity of the gas, thereby reducing the energy consumption.
Further, the device is washed to the liquid nitrogen still including the gas outlet of decarbonization air chamber and liquid nitrogen washing device intercommunication through the pipeline, and liquid nitrogen washing device still communicates with synthesis gas collection device through the pipeline, and the pipeline that communicates liquid nitrogen washing device and synthesis gas collection device is through precooling heat exchanger earlier, then connects on synthesis gas collection device again through first order cooling heat exchanger for the synthesis gas after liquid nitrogen washing is carried to synthesis gas collection device after absorbing heat in precooling heat exchanger and first order cooling heat exchanger in proper order.
The beneficial effects of adopting above-mentioned technical scheme are: the cold carried by the synthesis gas can be fully utilized, so that the energy consumption is reduced.
Further, the flash tank is also communicated with a shift gas input pipeline through a pipeline to convert CO 2 Flash gas obtained by flashing liquid is added into a conversion gas input pipeline.
Further, the evaporating heat exchanger is communicated with CO 2 The pipeline of the gas compressor is firstly connected with the CO after passing through the primary cooling heat exchanger 2 On a gas compressor, so that CO formed in the evaporation heat exchanger is evaporated 2 Absorbing heat in the primary cooling heat exchanger and then conveying the heat to CO 2 A gas compressor.
The beneficial effects of adopting above-mentioned technical scheme are: liquid CO 2 Heat is absorbed in the evaporating heat exchanger to change into gaseous CO 2 And then the residual cold is still carried, and is conveyed into the primary cooling heat exchanger to serve as a cold source to continuously exchange heat, so that the residual cold is utilized more fully, and the energy consumption is further reduced.
Drawings
The above, as well as additional purposes, features, and advantages of exemplary embodiments of the present application will become readily apparent from the following detailed description when read in conjunction with the accompanying drawings. Several embodiments of the present application are illustrated by way of example, and not by way of limitation, in the figures of the accompanying drawings and in which like reference numerals refer to similar or corresponding parts and in which:
FIG. 1 is a schematic diagram of a system architecture of a large-scale carbon capture system according to an embodiment of the present invention;
FIG. 2 is a schematic diagram showing the overall structure of a low-temperature methanol scrubber in an embodiment of the present invention;
FIG. 3 is a cross-sectional view of one view of a cryogenic methanol scrubber in an embodiment of the invention;
FIG. 4 is a cross-sectional view of another view of a cryogenic methanol scrubber in an embodiment of the invention;
fig. 5 is a schematic structural view of a desulfurizing member according to an embodiment of the present invention.
Reference numerals illustrate:
1. a change gas input conduit; 2. a methanol spraying device; 3. a primary cooling heat exchanger; 4. a first gas-liquid separation tank; 5. a low temperature methanol scrubber; 51. a desulfurization chamber; 511. a desulfurization baffle is arranged; 512. a lower desulfurization partition; 513. a desulfurization intake chamber; 514. a desulfurization intermediate chamber; 515. desulfurizing out the air chamber; 516. a first liquid outlet; 517. a desulfurizing member; 5171. a desulfurization tube; 5172. a lower fixing tube; 5173. an upper fixing tube; 518. desulfurizing liquid spray head; 52. a decarburization chamber; 521. a decarburization baffle plate is arranged on the upper part; 522. a lower decarburization barrier; 523. a decarburization intake chamber; 524. a decarburization intermediate chamber; 525. decarburizing to obtain a gas chamber; 526. a second liquid outlet; 527. decarburization member; 5271. a decarburization pipe; 5272. a lower support tube; 5273. an upper support tube; 528. a decarbonization liquid spray head; 53. a middle partition plate; 6. CO 2 An analytical tower; 7. precooling a heat exchanger; 8. CO 2 An evaporative heat exchanger; 9. a second gas-liquid separation tank; 10. a flash tank; 11. a liquid nitrogen washing device; 12. CO 2 A gas compressor; 13. a urea synthesis device; 14. and a synthesis gas collection device.
Detailed Description
The following description of the embodiments of the present application will be made clearly and fully with reference to the accompanying drawings, in which it is to be understood by those skilled in the art that the embodiments described below are some, but not all, of the embodiments of the present disclosure. All other embodiments, which can be made by those skilled in the art based on the embodiments herein without making any inventive effort, are intended to be within the scope of the present application.
Referring to fig. 1, the large-scale carbon capture system of the embodiment of the application comprises a methanol spray device 2, a primary cooling heat exchanger 3, a first gas-liquid separation tank 4, a low-temperature methanol washing tower 5 and a CO 2 Analytical tower 6, precooling heat exchanger 7, CO 2 An evaporation heat exchanger 8, a second gas-liquid separation tank 9, a flash tank 10, a liquid nitrogen washing device 11 and CO 2 A gas compressor 12, a urea synthesis plant 13 and a synthesis gas collection plant 14. Methanol spray device 2, first-stage cooling heat exchanger 3, first gas-liquid separation tank 4 and CO 2 Analytical tower 6, precooling heat exchanger 7, CO 2 An evaporation heat exchanger 8, a second gas-liquid separation tank 9,Flash tank 10, liquid nitrogen washing device 11, and CO 2 The gas compressor 12, the urea synthesis device 13 and the synthesis gas collection device 14 are all of the prior art, and therefore the structure and the working principle thereof will not be described in detail.
Referring to fig. 2 to 5, a desulfurization chamber 51 and a decarburization chamber 52 are provided in the low-temperature methanol washing column 5, and the desulfurization chamber 51 and the decarburization chamber 52 are isolated by an intermediate partition 53. The desulfurization chamber 51 is fixedly provided with an upper desulfurization baffle 511 and a lower desulfurization baffle 512, and the upper desulfurization baffle 511 and the lower desulfurization baffle 512 divide the desulfurization chamber 51 into a desulfurization inlet chamber 513, a desulfurization middle chamber 514 and a desulfurization outlet chamber 515 which are sequentially arranged from bottom to top. An air inlet is formed in the wall of the desulfurization air inlet chamber 513, and a first liquid outlet 516 is formed in the bottom of the desulfurization air inlet chamber 513. The desulfurization intermediate chamber 514 is fixedly provided with a desulfurization member 517, the desulfurization member 517 comprises a desulfurization tube 5171 and a granular filler (not shown in the figure) filled in the desulfurization tube 5171, the desulfurization tube 5171 is in a spiral shape, and two ends of the desulfurization tube 5171 are in a closed structure. In this embodiment, the particulate filler is polypropylene. The lower end of the desulfurization tube 5171 is fixedly connected with a lower fixing tube 5172, the lower end of the lower fixing tube 5172 is fixedly arranged on the lower desulfurization baffle plate 512 in a penetrating manner, and the lower fixing tube 5172 is used for communicating the desulfurization tube 5171 with the desulfurization air inlet chamber 513. The upper end of the desulfurization tube 5171 is fixedly connected with an upper fixing tube 5173, the upper end of the upper fixing tube 5173 is fixedly arranged on the upper desulfurization partition 511 in a penetrating manner, and the upper fixing tube 5173 is used for communicating the desulfurization tube 5171 with the desulfurization outlet air chamber 515. The chamber wall of the desulfurization gas outlet chamber 515 is provided with a gas outlet, the chamber wall of the desulfurization gas outlet chamber 515 is also fixedly provided with a plurality of desulfurization liquid spray heads 518, and the desulfurization liquid spray heads 518 are positioned below the gas outlet of the desulfurization gas outlet chamber 515. Desulfurization solution spray head 518 is used to spray carbon dioxide-rich methanol solution.
With continued reference to fig. 2-5, an upper decarburization barrier 521 and a lower decarburization barrier 522 are fixedly provided within the decarburization chamber 52, and the upper decarburization barrier 521 and the lower decarburization barrier 522 divide the decarburization chamber 52 into a decarburization intake 523, a decarburization intermediate 524 and a decarburization exit 525 which are provided in this order from bottom to top. An air inlet is formed in the wall of the decarburization air inlet chamber 523, a second liquid outlet 526 is formed in the wall of the decarburization air inlet chamber 523, and the second liquid outlet 526 is located below the air inlet. Decarburization member 527 is fixedly provided in decarburization intermediate chamber 524. The decarburization member 527 includes a decarburization pipe 5271 and a granular packing filled in the decarburization pipe 5271, wherein the decarburization pipe 5271 is formed in a spiral shape, and both ends of the decarburization pipe 5271 are closed. In this embodiment, the granular packing in the decarburization pipe 5271 is the same as the granular packing in the desulfurization pipe 5171. The lower end of the decarburization pipe 5271 is fixedly connected with a lower support pipe 5272, the lower end of the lower support pipe 5272 is fixedly arranged on the lower decarburization baffle 522 in a penetrating manner, and the lower support pipe 5272 is used for communicating the decarburization pipe 5271 with the decarburization air inlet chamber 523. An upper support pipe 5273 is fixedly connected to the upper end of the decarburization pipe 5271, the upper end of the upper support pipe 5273 is fixedly arranged on the upper decarburization barrier 521 in a penetrating manner, and the upper support pipe 5273 is used for communicating the decarburization pipe 5271 with the decarburization air outlet chamber 525. An air outlet is formed in the top of the decarburization air outlet chamber 525, a plurality of decarburization liquid spray heads 528 are fixedly arranged on the chamber wall of the decarburization air outlet chamber 525, and the decarburization liquid spray heads 528 are located below the air outlet of the decarburization air outlet chamber 525. Decarbonization liquid spray head 528 is used to spray lean methanol liquid.
With continued reference to fig. 1, the methanol spraying device 2 is connected to a shift gas input pipeline 1, the shift gas input pipeline 1 is used for conveying shift gas obtained by pressurizing and gasifying coal into the methanol spraying device 2, and the methanol spraying device 2 sprays methanol liquid into the shift gas, so that the methanol liquid can prevent water contained in the shift gas from freezing. The primary cooling heat exchanger 3 is communicated with the methanol spraying device 2 through a pipeline, and the primary cooling heat exchanger 3 is also communicated with the inlet of the first gas-liquid separation tank 4 through a pipeline. After the conversion gas is sprayed by the methanol liquid, the methanol liquid is conveyed into the first-stage cooling heat exchanger 3 through a pipeline to carry out first-stage cooling treatment, so that the contained water is liquefied, and gas-liquid separation is realized in the first gas-liquid separation tank 4, so that gas A is obtained. The gas A is simply called the residual gas after separating the water in the converted gas, and is just a code number.
Referring to fig. 1 and 3, the outlet of the first gas-liquid separation tank 4 is connected to the inlet of the desulfurization inlet chamber 513 of the low-temperature methanol scrubber 5 through a pipe, and the gas a is introduced into the desulfurization chamber 51 for desulfurization treatment. Gas a enters the desulfurization inlet chamber 513, then enters the desulfurization pipe 5171, and then enters the desulfurization outlet chamber 515. The methanol liquid rich in carbon dioxide sprayed by the desulfurizing liquid spray head 518 is subjected to dehydrationThe sulfur tube 5171 flows down into the desulfurization intake chamber 513 and then flows out through the first liquid outlet 516 at the bottom of the desulfurization intake chamber 513 to be collected. Because the methanol liquid rich in carbon dioxide flows downwards through the desulfurization tube 5171, a liquid film is formed on the surface of the granular filler filled in the desulfurization tube 5171, so that the gas A can be more fully contacted with the methanol liquid rich in carbon dioxide when entering the desulfurization tube 5171 and flowing upwards, and H contained in the gas A is formed 2 The S gas is more fully absorbed.
With continued reference to fig. 1 and 3, the air outlet of the desulfurization air outlet chamber 515 is communicated with the pre-cooling heat exchanger 7 through a pipeline, the gas a after desulfurization treatment enters the pre-cooling heat exchanger 7 for pre-cooling treatment, and the temperature of the gas a is further reduced, so that the CO contained in the gas a is realized 2 The gas is pre-cooled before liquefaction. The precooling heat exchanger 7 is communicated with an evaporation heat exchanger through a pipeline, and the evaporation heat exchanger is communicated with a second gas-liquid separation tank 9 through a pipeline. The precooled gas A enters an evaporation heat exchanger to be subjected to secondary cooling treatment, and the temperature is further reduced to ensure that most of CO is contained 2 Liquefying the gas, and performing gas-liquid separation in a second gas-liquid separation tank 9 to obtain gas B and CO 2 A liquid. The gas B is simply called the residual gas after gas-liquid separation, and is just a code.
With continued reference to fig. 1, the second gas-liquid separation tank 9 is in communication with the flash tank 10 through a pipe, and a pressure reducing valve is provided on the pipe between the second gas-liquid separation tank 9 and the flash tank 10. In use, CO in the second gas-liquid separation tank 9 2 Liquid enters the flash tank 10 through a pipeline to realize CO treatment 2 Reduced pressure flash vaporization of liquid to CO 2 Dissolved H in liquid 2 And CO precipitation to form flash vapor. One side of the flash tank 10 is communicated with the conversion gas input pipeline 1 through a pipeline, and when in use, flash gas enters the conversion gas input pipeline 1 through the pipeline and is mixed with the conversion gas to realize H 2 And recycling of CO. The other side of the flash tank 10 is communicated with an evaporation heat exchanger through a pipeline, a pressure reducing valve is also arranged on the pipeline between the flash tank 10 and the evaporation heat exchanger, and the evaporation heat exchanger is also communicated with the primary cooling heat exchanger 3 through a pipeline. When in use, the flash evaporation is performed under reduced pressurePost CO 2 Liquid enters an evaporation heat exchanger to be used as a cold source, liquid CO 2 Heat is absorbed in the evaporating heat exchanger to change into gaseous CO 2 Then gaseous CO 2 And the heat exchange is carried out after the heat exchange is carried out in the primary heat exchange cooling device as a cold source. The primary cooling heat exchanger 3 is connected with CO through a pipeline 2 The gas compressor 12 is connected with CO 2 The gas compressor 12 is also in communication with the urea synthesis device 13 via a pipe. When in use, the first-stage cooling heat exchanger 3 absorbs heat CO 2 Gas enters CO 2 The gas compressor 12 is pressurized with gaseous CO 2 Is fed to a urea synthesis plant 13 for urea synthesis.
With continued reference to fig. 1 and 3, the second gas-liquid separation tank 9 is also in communication with the gas inlet of the decarbonization inlet chamber 523 of the low-temperature methanol scrubber 5 via a pipe, and the gas B enters the decarbonization chamber 52 for decarbonization treatment to remove CO in the gas B 2 And (3) gas to obtain purified gas. The gas B enters the decarburization inlet chamber 523, then enters the decarburization pipe 5271, and then enters the decarburization exit chamber 525. The lean methanol liquid ejected from the decarburization liquid nozzle 528 flows down into the decarburization intake chamber 523 through the decarburization pipe 5271 and then flows out through the second outlet 526 of the decarburization intake chamber 523. Since the lean methanol liquid flows downwards through the decarburization pipe 5271, a liquid film is formed on the surface of the granular filler filled in the decarburization pipe 5271, so that the gas B can be more fully contacted with the lean methanol liquid when entering the decarburization pipe 5271 and flowing upwards, and CO contained in the gas B is formed 2 The gas is more fully absorbed.
With continued reference to fig. 1 and 3, the second outlet 526 is in communication with the CO via a conduit 2 The analysis tower 6 is communicated with CO 2 The analysis tower 6 is communicated with the pre-cooling heat exchanger 7 through a pipeline, the pre-cooling heat exchanger 7 is also communicated with the primary cooling heat exchanger 3 through a pipeline, and the primary cooling heat exchanger 3 is also communicated with CO through a pipeline 2 The gas compressor 12 communicates. When in use, CO is absorbed 2 Methanol liquid of gas enters CO 2 The inside of the analysis tower 6 is analyzed to release CO 2 Gas, released CO 2 The gas firstly enters the pre-cooling heat exchanger 7 to be used as a cold source for heat exchange, and then enters the primary cooling heat exchanger3, continuously exchanging heat by taking the heat-exchanging medium as a cold source, and then entering CO 2 The gas compressor 12 is pressurized and finally fed to the urea synthesis plant 13 for urea synthesis.
With continued reference to fig. 1 and 3, the gas outlet of the decarbonization gas outlet chamber 525 is communicated with the liquid nitrogen washing device 11 through a pipeline, and the purified gas enters the liquid nitrogen washing device 11 to be subjected to liquid nitrogen washing, so as to remove non-hydrogen components in the purified gas, and obtain the synthesis gas containing nitrogen and hydrogen. The liquid nitrogen washing device 11 is communicated with the pre-cooling heat exchanger 7 through a pipeline, and the pre-cooling heat exchanger 7 is communicated with the primary cooling heat exchanger 3 through a pipeline. The synthesis gas is firstly conveyed into the pre-cooling heat exchanger 7 for primary heat exchange, and the synthesis gas after primary heat exchange is conveyed into the primary cooling heat exchanger 3 for secondary heat exchange, so that the synthesis gas provides cold for the pre-cooling heat exchanger 7 and the primary cooling heat exchanger 3, and the recycling of the cold carried by the synthesis gas is realized. The primary cooling heat exchanger 3 is communicated with the synthesis gas collecting device 14 through a pipeline, and the synthesis gas subjected to secondary heat exchange is conveyed into the synthesis gas collecting device 14 for collection.
The parameters of the shift gas processed by the large-scale carbon capture system in the embodiment of the application are as follows: 40 ℃ and 5.8Mpa; the main component is CO 2 ：44.416％，H 2 ：54.246％，H 2 S：0.497％，CO：0.398％，H 2 O:0.251%. The parameters of the liquid methanol rich in carbon dioxide used are-19.75 ℃, 5.71Mpa and the gas temperature after desulfurization treatment is-6.69 ℃. The pre-cooling treatment reduces the temperature of the gas A to-20.32 ℃, the secondary cooling treatment reduces the temperature of the gas A to-32.6 ℃ and CO 2 The parameters of the liquid were-32.6℃and 5.69MPa. The temperature of flash gas is-34.82 ℃, and the liquid CO after flash vaporization 2 The parameter of (C) is-34.82 ℃, 2.1Mpa, CO 2 The parameters are changed into-40 ℃ and 0.57MPa after the pressure is reduced again, and the gaseous CO is used as a cold source 2 After the heat exchange in the primary heat exchange cooling device is completed, the parameters are changed to 30 ℃, 0.57MPa, and the parameters before the heat exchange of the synthetic gas are-27.85 ℃ and 5.43MPa. Parameters of purge gas: the temperature is less than minus 62 ℃; CO 2 Less than or equal to 10vppm; total sulfur is less than or equal to 0.1vppm; CH (CH) 3 OH is less than or equal to 80vppm; the total recovery rate of hydrogen is more than or equal to 99.6%; total pressure drop of the device: less than or equal to 0.20MPa. CO 2 The analysis tower 6 analyzes the mixture to obtainCO of (c) 2 The parameters of the gas before heat exchange are-27.85 ℃ and 0.14Mpa, and the parameters after heat exchange are 30 ℃ and 0.14Mpa. The quality of the methanol used in the method accords with the national standard industrial methanol superior (GB 338-2011) standard of the people's republic of China.
The implementation principle of the embodiment of the large-scale carbon capture system is as follows: the H in the gas A can be removed by adopting the methanol liquid rich in carbon dioxide to carry out low-temperature methanol washing on the gas A 2 S gas, H in gas A is reserved 2 And CO 2 Gas, realize CO 2 And H is 2 S is separated, and then secondary cooling treatment is carried out to lead most of CO 2 The gas B is obtained by liquefying the gas, so that the circulating amount of the lean methanol liquid required by low-temperature methanol washing is reduced, and the energy consumption is further reduced. In addition, CO supplied to the urea synthesizing device 13 for synthesizing urea 2 Part of the gas is formed by CO 2 The liquid is gasified, the other part is obtained by carrying out reduced pressure flash evaporation treatment on the methanol-rich liquid, and the other part is obtained by CO 2 CO obtained by gasification of liquid 2 The pressure of the gas is higher than that of CO obtained by the decompression flash evaporation treatment of the methanol-rich liquid 2 The pressure of the gas is high. CO prior art to be sent to the urea synthesis plant 13 for urea synthesis 2 The gases are all obtained by flash evaporation of methanol-rich liquid under reduced pressure, so that the total CO obtained in the application 2 The gas is pressurized to the required pressure, which requires the energy consumption of the compressor, compared with the CO obtained in the prior art 2 The gas needs to consume less energy of the compressor when being pressurized to the required pressure. In addition, the CO released from the methanol-rich liquid is fully utilized in the application 2 Gaseous, liquid CO 2 Endothermic converted gaseous CO 2 The cold carried by the synthesis gas is utilized, so that the cold required to be provided by the whole is reduced, and the energy consumption is further reduced.
The foregoing is a preferred embodiment of the present invention and it should be noted that modifications and adaptations to those skilled in the art may be made without departing from the principles of the present invention and are intended to be comprehended within the scope of the present invention.
Claims (6)
1. A large-scale carbon capture system is characterized by comprising a methanol spray device (2), a primary cooling heat exchanger (3), a first gas-liquid separation tank (4), a low-temperature methanol washing tower (5) and CO 2 An evaporation heat exchanger (8), a second gas-liquid separation tank (9), a flash tank (10) and CO 2 Gas compressor (12), urea synthesis device (13) and CO 2 A resolving tower (6);
a desulfurization chamber (51) and a decarburization chamber (52) are arranged in the low-temperature methanol washing tower (5), and the desulfurization chamber (51) is used for absorbing H 2 S gas, a decarbonization chamber (52) for CO absorption 2 The gas, the desulfurization chamber (51) and the decarburization chamber (52) are isolated by an intermediate baffle plate (53), a decarburization liquid spray head (528) is fixedly arranged on the chamber wall of the decarburization chamber (52), and a second liquid outlet (526) is formed on the chamber wall of the decarburization chamber (52);
the methanol spraying device (2) is communicated with a conversion gas input pipeline (1), the primary cooling heat exchanger (3) is communicated with the methanol spraying device (2) through a pipeline, the primary cooling heat exchanger (3) is used for liquefying moisture contained in conversion gas, the primary cooling heat exchanger (3) is also communicated with an inlet of the first gas-liquid separation tank (4) through a pipeline, an outlet of the first gas-liquid separation tank (4) is communicated with a desulfurization chamber (51) of the low-temperature methanol washing tower (5) through a pipeline, and an air outlet of the desulfurization chamber (51) is communicated with CO through a pipeline 2 The evaporation heat exchanger (8) is communicated; CO 2 An evaporation heat exchanger (8) for making the shift gas after desulfurization contain part of CO 2 The gas is liquefied, the evaporation heat exchanger is communicated with a second gas-liquid separation tank (9) through a pipeline, the second gas-liquid separation tank (9) is communicated with a flash evaporation tank (10) through a pipeline, and the second gas-liquid separation tank (9) enables CO to be obtained 2 Liquid enters a flash tank (10), the flash tank (10) is communicated with an evaporation heat exchanger through a pipeline, and CO 2 The liquid enters an evaporation heat exchanger to absorb heat and change into gas, and the evaporation heat exchanger is connected with CO through a pipeline 2 The gas compressor (12) is communicated with CO 2 The gas compressor (12) is communicated with the urea synthesis device (13) through a pipeline;
the second gas-liquid separation tank (9) is also communicated with a decarburization chamber (52) of the low-temperature methanol washing tower (5) through a pipeline, and the second liquid outlet (526) is communicated with CO through a pipeline 2 The analysis tower (6) is communicated with CO 2 The analysis tower (6) is connected with CO through a pipeline 2 The gas compressor (12) is in communication.
2. The large-scale carbon capturing system according to claim 1, wherein an upper desulfurization partition plate (511) and a lower desulfurization partition plate (512) are fixedly arranged in the desulfurization chamber (51), the upper desulfurization partition plate (511) and the lower desulfurization partition plate (512) divide the desulfurization chamber (51) into a desulfurization inlet chamber (513), a desulfurization middle chamber (514) and a desulfurization outlet chamber (515) which are sequentially arranged from bottom to top, an air inlet is formed in the chamber wall of the desulfurization inlet chamber (513), a desulfurization member (517) is fixedly arranged in the desulfurization middle chamber (514), the desulfurization member (517) comprises a desulfurization pipe (5171) and a granular filler filled in the desulfurization pipe (5171), the desulfurization pipe (5171) is communicated with the desulfurization inlet chamber (513), the desulfurization pipe (5171) is communicated with the desulfurization outlet chamber (515), an air outlet is formed in the chamber wall of the desulfurization outlet chamber (515), and a desulfurization liquid spray head (518) is arranged in the chamber wall of the desulfurization outlet chamber (515);
an upper decarburization partition plate (521) and a lower decarburization partition plate (522) are fixedly arranged in the decarburization chamber (52), the upper decarburization partition plate (521) and the lower decarburization partition plate (522) divide the decarburization chamber (52) into a decarburization inlet chamber (523), a decarburization middle chamber (524) and a decarburization outlet chamber (525) which are sequentially arranged from bottom to top, an air inlet is formed in the chamber wall of the decarburization inlet chamber (523), a second liquid outlet (526) is formed in the bottom of the decarburization inlet chamber (523), a decarburization part (527) is fixedly arranged in the decarburization middle chamber (524), the decarburization part (527) comprises a decarburization pipe (5271) and granular filler filled in the decarburization pipe (5271), the decarburization pipe (5271) is communicated with the decarburization inlet chamber (523), an air outlet is formed in the chamber wall of the decarburization outlet chamber (525), and a decarburization liquid spray head (528) is fixedly arranged on the chamber wall of the decarburization outlet chamber (525).
3. The large-scale carbon capturing system according to claim 2, further comprising a pre-cooling heat exchanger (7), wherein the pre-cooling heat exchanger (7) is arranged at an air outlet communicating the desulfurization chamber (51) with the CO 2 On a pipeline of the evaporation heat exchanger (8), the precooling heat exchanger (7) is used for precooling the gas after desulfurization treatment; communicating CO 2 Analytical column (6) and CO 2 Tube of gas compressor (12)The waste gas passes through a pre-cooling heat exchanger (7) and then passes through a first-stage cooling heat exchanger (3) and is connected to CO 2 On the gas compressor (12) such that CO 2 CO analyzed by the analysis tower (6) 2 Absorbing heat in the pre-cooling heat exchanger (7) and the first-stage cooling heat exchanger (3) in sequence and then conveying the heat to the CO 2 A gas compressor (12).
4. The large-scale carbon capturing system according to claim 3, further comprising a liquid nitrogen washing device (11), wherein the gas outlet of the decarburization gas outlet chamber (525) is communicated with the liquid nitrogen washing device (11) through a pipeline, the liquid nitrogen washing device (11) is also communicated with the synthesis gas collecting device (14) through a pipeline, and the pipeline which is communicated with the liquid nitrogen washing device (11) and the synthesis gas collecting device (14) passes through the pre-cooling heat exchanger (7) first and then passes through the first-stage cooling heat exchanger (3) and is connected to the synthesis gas collecting device (14) again, so that the synthesis gas after liquid nitrogen washing is sequentially subjected to heat absorption in the pre-cooling heat exchanger (7) and the first-stage cooling heat exchanger (3) and then is conveyed to the synthesis gas collecting device (14).
5. The large-scale carbon capture system according to claim 1, wherein the flash tank (10) is also in communication with a shift gas input conduit (1) through a conduit for CO 2 The flash gas obtained by flashing the liquid is added into the shift gas input pipeline (1).
6. The large scale carbon capture system of claim 1, wherein the evaporative heat exchanger is in communication with the CO 2 The pipeline of the gas compressor (12) is firstly connected with the CO after passing through the first-stage cooling heat exchanger (3) 2 On a gas compressor (12) such that CO formed in the evaporation heat exchanger is evaporated 2 Absorbing heat in the primary cooling heat exchanger (3) and then conveying the heat to CO 2 A gas compressor (12).
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| CN207933375U (en) * | 2018-01-10 | 2018-10-02 | 上海朴力节能环保科技有限公司 | Low-temp methanol washes the device of journey mesohigh recycling carbon dioxide |
| CN110228792A (en) * | 2019-06-30 | 2019-09-13 | 新乡中新化工有限责任公司 | A kind of synthesis gas depth decarburization technique |
| CN111303945A (en) * | 2020-03-12 | 2020-06-19 | 华南理工大学 | Low-temperature methanol washing process method and device with low energy consumption and high carbon capture rate |
| CN113234496A (en) * | 2021-05-25 | 2021-08-10 | 刘金成 | Low-temperature methanol-rich solution flash steam CO2And H2S removing device |
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| CN102660339B (en) * | 2012-04-27 | 2014-04-30 | 阳光凯迪新能源集团有限公司 | Gas-steam efficient cogeneration process and system based on biomass gasification and methanation |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN207933375U (en) * | 2018-01-10 | 2018-10-02 | 上海朴力节能环保科技有限公司 | Low-temp methanol washes the device of journey mesohigh recycling carbon dioxide |
| CN110228792A (en) * | 2019-06-30 | 2019-09-13 | 新乡中新化工有限责任公司 | A kind of synthesis gas depth decarburization technique |
| CN111303945A (en) * | 2020-03-12 | 2020-06-19 | 华南理工大学 | Low-temperature methanol washing process method and device with low energy consumption and high carbon capture rate |
| CN113234496A (en) * | 2021-05-25 | 2021-08-10 | 刘金成 | Low-temperature methanol-rich solution flash steam CO2And H2S removing device |
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