WO2022253256A1 - 一种利用二氧化碳和水合成甲醇的装置及方法 - Google Patents
一种利用二氧化碳和水合成甲醇的装置及方法 Download PDFInfo
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- WO2022253256A1 WO2022253256A1 PCT/CN2022/096528 CN2022096528W WO2022253256A1 WO 2022253256 A1 WO2022253256 A1 WO 2022253256A1 CN 2022096528 W CN2022096528 W CN 2022096528W WO 2022253256 A1 WO2022253256 A1 WO 2022253256A1
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- carbon dioxide
- water
- air
- methanol
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 438
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 347
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 224
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 200
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 109
- 238000000034 method Methods 0.000 title claims abstract description 32
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 title claims abstract description 24
- 230000002194 synthesizing effect Effects 0.000 title claims abstract description 17
- 230000008929 regeneration Effects 0.000 claims abstract description 60
- 238000011069 regeneration method Methods 0.000 claims abstract description 60
- 238000010521 absorption reaction Methods 0.000 claims abstract description 59
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 57
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 57
- 238000010438 heat treatment Methods 0.000 claims abstract description 24
- 230000004888 barrier function Effects 0.000 claims abstract description 22
- 230000006835 compression Effects 0.000 claims abstract description 19
- 238000007906 compression Methods 0.000 claims abstract description 19
- 239000007788 liquid Substances 0.000 claims description 167
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 61
- 229910052799 carbon Inorganic materials 0.000 claims description 61
- 238000010248 power generation Methods 0.000 claims description 43
- 230000002745 absorbent Effects 0.000 claims description 15
- 239000002250 absorbent Substances 0.000 claims description 15
- 230000005611 electricity Effects 0.000 claims description 13
- 239000000126 substance Substances 0.000 claims description 9
- 230000036571 hydration Effects 0.000 claims description 7
- 238000006703 hydration reaction Methods 0.000 claims description 7
- 239000002699 waste material Substances 0.000 claims description 7
- 239000007789 gas Substances 0.000 abstract description 50
- 230000008569 process Effects 0.000 abstract description 10
- 230000009467 reduction Effects 0.000 abstract description 6
- 239000005431 greenhouse gas Substances 0.000 abstract description 3
- 239000002994 raw material Substances 0.000 abstract description 3
- 238000006243 chemical reaction Methods 0.000 description 12
- 238000005516 engineering process Methods 0.000 description 7
- 229910052739 hydrogen Inorganic materials 0.000 description 7
- 239000001257 hydrogen Substances 0.000 description 7
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 6
- 230000009471 action Effects 0.000 description 5
- 230000008859 change Effects 0.000 description 5
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 4
- 230000018109 developmental process Effects 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000005868 electrolysis reaction Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 230000010354 integration Effects 0.000 description 3
- 150000001412 amines Chemical class 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000002608 ionic liquid Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 239000013154 zeolitic imidazolate framework-8 Substances 0.000 description 2
- MFLKDEMTKSVIBK-UHFFFAOYSA-N zinc;2-methylimidazol-3-ide Chemical compound [Zn+2].CC1=NC=C[N-]1.CC1=NC=C[N-]1 MFLKDEMTKSVIBK-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 241000282414 Homo sapiens Species 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 230000005495 cold plasma Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- -1 ethylene, propylene Chemical group 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 239000003348 petrochemical agent Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
-
- 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
- B01D53/1418—Recovery of products
-
- 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
- B01J19/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
- B01J19/087—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electric or magnetic energy
- B01J19/088—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electric or magnetic energy giving rise to electric discharges
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
Definitions
- the application belongs to the technical field of greenhouse gas emission reduction and resource utilization, and specifically relates to a device and method for synthesizing methanol by utilizing carbon dioxide and water.
- direct carbon capture from the air is less restricted by location and can be widely carried out in various places. Moreover, direct carbon capture from the air can reduce the concentration of CO 2 in the air and can solve the problem of "storage". "The problem.
- Methanol is one of the hydrogenation products of CO2 . It is the most simple saturated monohydric alcohol. As a basic organic chemical raw material, its consumption is second only to ethylene, propylene and benzene. It is mainly used in plastics, fine chemicals, petrochemicals, etc. field. In addition, methanol is also a new type of clean energy, which can be used as a vehicle fuel due to its good anti-knock properties and high octane number.
- a device for synthesizing methanol from carbon dioxide and water including an air carbon capture system and a methanol synthesis system;
- the air carbon capture system includes an air compression device, a carbon dioxide absorption device, a carbon dioxide regeneration device, and a carbon dioxide storage device connected in sequence;
- the methanol synthesis system includes a water storage device, a water heating device, a gas mixing device and a methanol synthesis device connected in sequence, the gas outlet of the carbon dioxide storage device is connected to the carbon dioxide inlet of the gas mixing device; the methanol synthesis device is a medium barrier discharge reactor.
- the air carbon capture system also includes,
- a heat exchange device is arranged between the carbon dioxide absorption device and the carbon dioxide regeneration device, the heat exchange device has a rich liquid inlet, a rich liquid outlet, a lean liquid inlet and a lean liquid outlet, the rich liquid inlet of the heat exchange device is connected to the The rich liquid outlet of the carbon dioxide absorption device is connected, and the rich liquid outlet of the heat exchange device is connected with the rich liquid inlet of the carbon dioxide regeneration device.
- a cold rich liquid pump is arranged between the rich liquid inlet of the heat exchange device and the rich liquid outlet of the carbon dioxide absorption device;
- a rich liquid storage device and a hot rich liquid pump connected in sequence are arranged between the rich liquid outlet of the heat exchange device and the rich liquid inlet of the carbon dioxide regeneration device;
- a carbon dioxide compression device is arranged between the carbon dioxide regeneration device and the carbon dioxide storage device.
- the carbon dioxide regeneration device has a rich liquid inlet, a carbon dioxide outlet, a lean liquid inlet and a lean liquid outlet, and a hot lean liquid pump is arranged between the lean liquid outlet of the carbon dioxide regeneration device and the lean liquid inlet of the heat exchange device ;
- a heating device is arranged between the lean liquid outlet and the lean liquid inlet of the carbon dioxide regeneration device.
- the carbon dioxide absorption device has an air inlet, a rich liquid outlet, a lean liquid inlet and an air outlet
- the air outlet of the air compression device is connected to the air inlet of the carbon dioxide absorption device
- the lean liquid outlet of the heat exchange device is A lean liquid storage device and a cold lean liquid pump connected in sequence are arranged between the lean liquid inlet of the carbon dioxide absorbing device.
- the gas mixing device has a carbon dioxide inlet, a water vapor inlet and a mixed gas outlet, and a carbon dioxide valve is arranged between the gas outlet of the carbon dioxide storage device and the carbon dioxide inlet of the gas mixing device, A water vapor valve is arranged between the water heating device and the water vapor inlet of the gas mixing device; a water pump is arranged between the water storage device and the water heating device.
- the carbon dioxide absorption device is a carbon dioxide absorption tower, and a carbon dioxide absorbent is arranged in the absorption tower;
- the carbon dioxide regeneration device is a carbon dioxide regeneration tower.
- a renewable energy power generation system is also included, and the waste electricity generated by the renewable energy power generation system supplies power for the air carbon capture system and the methanol synthesis system.
- the present application provides a method for synthesizing methanol by using carbon dioxide and water, which is carried out by using the above-mentioned device.
- the method includes the following steps: when the renewable energy power generation system has a power-suppression output, drive the air carbon capture system to work, and use the chemical absorption method to directly capture carbon dioxide from the air, and the captured carbon dioxide is synthesized in methanol It reintegrates with water in the system to form methanol.
- the device for synthesizing methanol from carbon dioxide and water uses the air carbon capture system to directly capture carbon from the air, and then uses the dielectric barrier discharge reactor in the methanol synthesis system to recombine methanol based on plasma CO2 and water, The continuous supply of CO 2 in the methanol synthesis process is realized, the transportation cost of raw materials is saved, and the resource utilization of CO 2 is realized while reducing carbon emissions.
- Equipment installation is less restricted by location, and is suitable for various places with renewable energy power generation. That is to say, the device provided by this application realizes the use of renewable energy to drive air to directly capture carbon and the use of CO2 and water to synthesize methanol at normal temperature and pressure through the integration of renewable energy power generation system, air carbon capture system and methanol synthesis system. It solves the problem of the consumption of renewable energy abandonment, and also achieves the multiple goals of carbon emission reduction and CO 2 resource utilization.
- Fig. 1 is the schematic diagram of the device utilizing carbon dioxide and hydration to synthesize methanol for the present application;
- Fig. 2 is the schematic diagram of the device for the present application to utilize carbon dioxide and hydration to synthesize methanol driven by a renewable energy power generation system;
- Fig. 3 is a schematic structural diagram of a dielectric barrier discharge reactor.
- 1-renewable energy power generation system 2-air carbon capture system; 3-methanol synthesis system; 4-air compression device; 5-carbon dioxide absorption device; 6-cold rich liquid pump; 7-heat exchange device; 8- Rich liquid storage device; 9-hot rich liquid pump; 10-carbon dioxide regeneration device; 11-heating device; 12-hot lean liquid pump; 13-lean liquid storage device; 14-cold lean liquid pump; 15-carbon dioxide compression device; 16-carbon dioxide storage device; 17-carbon dioxide valve; 18-gas mixing device; 19-water storage device; 20-water pump; 21-water heating device; 22-water vapor valve; 23-methanol synthesis device; 24-intake pipe; 25-outlet pipe; 26-advanced voltage; 27-ground electrode; 28-insulating medium; 29-gas distributor.
- the present application provides a device for utilizing carbon dioxide and water to synthesize methanol, including an air carbon capture system 2 and a methanol synthesis system 3;
- the air carbon capture system 2 includes an air compression device 4, a carbon dioxide absorption device 5, a carbon dioxide regeneration device 10, and a carbon dioxide storage device 16 connected in sequence;
- the methanol synthesis system 3 comprises a water storage device 19, a water heating device 21, a gas mixing device 18 and a methanol synthesis device 23 connected in sequence, and the gas outlet of the carbon dioxide storage device 16 is connected with the carbon dioxide inlet of the gas mixing device 18;
- the methanol synthesis unit 23 is a dielectric barrier discharge reactor.
- the air compression device 4 is an air compressor
- the carbon dioxide absorption device 5 is a carbon dioxide absorption tower
- a carbon dioxide absorbent is arranged in the absorption tower.
- the carbon dioxide absorbent can be monoethanolamine, mixed amine or porous liquid
- the porous liquid can be ZIF-8/ethylene glycol, ZSM-5/large-volume ionic liquid, and capture CO 2 in the air through the chemical reaction between CO 2 and the absorbent.
- the carbon dioxide regeneration device 10 may be a carbon dioxide regeneration tower, in which the carbon dioxide-rich liquid is decomposed at high temperature to release carbon dioxide.
- the temperature of the rich liquid in the regeneration tower is controlled to be 110-120°C.
- both the carbon dioxide absorption tower and the regeneration tower are packed towers, using inert metal packing, and the function of the packing is to ensure full contact between the gas-liquid two-phase.
- the carbon dioxide storage device 16 is a carbon dioxide storage tank
- the water storage device 19 is a water storage tank
- the water heating device 21 is a water heater
- the gas mixing device 18 is a gas mixer.
- the methanol synthesis unit 23 is a dielectric barrier discharge reactor.
- the dielectric barrier discharge reactor is a conventional dielectric barrier discharge reactor in the field, which can be purchased from the market or designed by the existing technology.
- the dielectric barrier discharge reactor is a dielectric barrier discharge device, including an inlet pipe 24, an outlet pipe 25, a high-level voltage 26, a ground electrode 27, an insulating medium 28 and a gas distributor 29 The mixed gas of carbon dioxide and water vapor enters from the inlet pipe 24, and the methanol gas synthesized is discharged from the outlet pipe 25.
- the device for synthesizing methanol from carbon dioxide and water uses the air carbon capture system 2 to directly capture carbon from the air, and then utilizes the dielectric barrier discharge reactor in the methanol synthesis system 3 to recombine CO 2 and water based on plasma Methanol realizes the continuous supply of CO2 in the process of methanol synthesis, saves the transportation cost of raw materials, and realizes the resource utilization of CO2 while reducing carbon emissions.
- a renewable energy power generation system 1 is also included, and the waste electricity generated by the renewable energy power generation system 1 supplies power for an air carbon capture system 2 and a methanol synthesis system 3 .
- the renewable energy power generation system 1 may be a wind power generation system or a photovoltaic power generation system.
- the renewable energy power generation system 1 can supply power to any energy-requiring components in the device to provide the required energy.
- the renewable energy power generation system 1 is connected with a reboiler to provide heat for the regeneration tower, and the renewable energy power generation system 1 is connected with a water heater to heat water into steam; The power generation system 1 is connected to the dielectric barrier discharge reactor.
- a plasma region is formed in the dielectric barrier discharge reactor, and the dielectric barrier discharge reaction is carried out.
- the water molecules are broken down by the discharge to produce chemically active hydrogen ion radicals. Further react with CO2 to synthesize methanol.
- plasma-based CO 2 and water directly synthesize methanol, which not only reduces the reaction process, but also avoids the additional energy consumption required for electrolysis of water to produce hydrogen, greatly improving energy utilization Rate.
- the molar ratio of water vapor and CO 2 gas when mixed is (6-12):1.
- This application utilizes the abandoned electricity generated by the renewable energy power generation system 1 to supply power for the air carbon capture system 2 and the methanol synthesis system 3, which not only does not affect the renewable energy power generation system 1, but also effectively solves the problem of electricity abandonment of renewable energy , and the renewable energy reserves are abundant, and the impact on the environment is small in the process of development and utilization.
- Using fluctuating new energy to drive the carbon capture system to directly capture CO 2 from the air can reduce the CO 2 content in the air, and in the process of carbon capture It is one of the important ways to mitigate global climate change without generating additional CO 2 .
- Using a dielectric barrier discharge reactor, based on plasma technology realizes the resource utilization of CO 2 at normal temperature and pressure.
- Equipment installation is less restricted by location, and is suitable for various places with renewable energy power generation. That is to say, the device provided by this application realizes the direct carbon capture by using renewable energy to drive air and the synthesis of methanol by using CO2 and water under normal temperature and pressure through the integration of renewable energy power generation system, air carbon capture system 2 and methanol synthesis system 3, It not only realizes the consumption problem of renewable energy abandonment, but also achieves the multiple goals of carbon emission reduction and CO2 resource utilization.
- the air carbon capture system 2 also includes,
- the heat exchange device 7 is arranged between the carbon dioxide absorption device 5 and the carbon dioxide regeneration device 10, the heat exchange device 7 has a rich liquid inlet, a rich liquid outlet, a lean liquid inlet and a lean liquid outlet, and the heat exchange device 7
- the rich liquid inlet is connected to the rich liquid outlet of the carbon dioxide absorption device 5
- the rich liquid outlet of the heat exchange device 7 is connected to the rich liquid inlet of the carbon dioxide regeneration device 10 .
- the heat exchange device 7 is a heat exchanger, and a heat exchanger is connected between the absorption tower and the rich liquid storage tank, which is beneficial to improving energy utilization and reducing costs.
- a cold rich liquid pump 6 is arranged between the rich liquid inlet of the heat exchange device 7 and the rich liquid outlet of the carbon dioxide absorption device 5;
- a rich liquid storage device 8 and a hot rich liquid pump 9 are arranged in sequence between the rich liquid outlet of the heat exchange device 7 and the rich liquid inlet of the carbon dioxide regeneration device 10; optionally, the rich liquid storage device 8 is Rich liquid storage tank.
- a carbon dioxide compression device 15 is arranged between the carbon dioxide regeneration device 10 and the carbon dioxide storage device 16 .
- the carbon dioxide compression device 15 is a carbon dioxide compressor.
- the carbon dioxide regeneration device 10 has a rich liquid inlet, a carbon dioxide outlet, a lean liquid inlet and a lean liquid outlet, the lean liquid outlet of the carbon dioxide regeneration device 10 and the lean liquid inlet of the heat exchange device 7 A hot lean liquid pump 12 is arranged between them;
- a heating device 11 is provided between the lean liquid outlet and the lean liquid inlet of the carbon dioxide regeneration device 10 .
- the heating device 11 is a reboiler. This application is equipped with a reboiler at the bottom of the regeneration tower, and the CO2 in the rich liquid is separated from the absorbent by heating the reboiler.
- the carbon dioxide absorption device 5 has an air inlet, a rich liquid outlet, a lean liquid inlet and an air outlet, the air outlet of the air compression device 4 is connected to the air inlet of the carbon dioxide absorption device 5, the Between the lean liquid outlet of the heat exchange device 7 and the lean liquid inlet of the carbon dioxide absorption device 5, a lean liquid storage device 13 and a cold lean liquid pump 14 are arranged in sequence.
- the lean liquid storage device 13 is a lean liquid storage tank.
- the gas mixing device 18 has a carbon dioxide inlet, a water vapor inlet and a mixed gas outlet, and the gas outlet of the carbon dioxide storage device 16 is connected to the carbon dioxide inlet of the gas mixing device 18.
- a carbon dioxide valve 17 is arranged between them, a water vapor valve 22 is arranged between the water heating device 21 and the water vapor inlet of the gas mixing device 18; a water pump is arranged between the water storage device 19 and the water heating device 21 20.
- the present application also provides a method for synthesizing methanol by utilizing carbon dioxide and water, which uses the above-mentioned device.
- the method includes the following steps: when the renewable energy power generation system 1 has a power-suppression output, drive the air carbon capture system 2 to work, and use the chemical absorption method to directly capture carbon dioxide from the air, and the captured carbon dioxide is In the methanol synthesis system 3, it is reintegrated with water to become methanol.
- the waste electricity in the renewable energy power generation system 1 supplies power for the air carbon capture system 2 and the methanol synthesis system 3; the air enters the carbon dioxide absorption tower through the air compressor, and the carbon capture chemical absorbent (monoethanolamine) in the absorption tower , mixed amine or porous liquid) to selectively absorb CO2 , and the rich liquid after absorbing CO2 flows out from the rich liquid outlet at the bottom of the absorption tower and enters the rich liquid storage tank through a heat exchanger; the rich liquid in the rich liquid storage tank It is sent to the carbon dioxide regeneration tower through pipelines for CO2 regeneration.
- the air enters the carbon dioxide absorption tower through the air compressor, and the carbon capture chemical absorbent (monoethanolamine) in the absorption tower , mixed amine or porous liquid) to selectively absorb CO2
- the rich liquid after absorbing CO2 flows out from the rich liquid outlet at the bottom of the absorption tower and enters the rich liquid storage tank through a heat exchanger
- the rich liquid in the rich liquid storage tank It is sent to the carbon dioxide
- the lean liquid containing absorbent flows out from the bottom of the regeneration tower and is sent to the lean liquid storage tank through a heat exchanger for standby; the CO2 gas obtained during the regeneration process is compressed by carbon dioxide
- the water in the water storage tank is mixed with the CO in the carbon dioxide storage tank after passing through the water heater in the gas mixer, and then the mixed gas is transported to the methanol synthesis unit 23 through pipelines The reaction was carried out to obtain methanol.
- the present embodiment provides a kind of device utilizing carbon dioxide and hydration to synthesize methanol, including air carbon capture system 2 and methanol synthesis system 3;
- the air carbon capture system 2 includes an air compression device 4, a carbon dioxide absorption device 5, a carbon dioxide regeneration device 10, and a carbon dioxide storage device 16 connected in sequence;
- the methanol synthesis system 3 comprises a water storage device 19, a water heating device 21, a gas mixing device 18 and a methanol synthesis device 23 connected in sequence, and the gas outlet of the carbon dioxide storage device 16 is connected with the carbon dioxide inlet of the gas mixing device 18;
- the methanol synthesis unit 23 is a dielectric barrier discharge reactor;
- Described air compression device 4 is an air compressor, and carbon dioxide absorption device 5 is a carbon dioxide absorption tower, is provided with a carbon dioxide absorbent in the absorption tower, and the carbon dioxide absorbent is monoethanolamine;
- the carbon dioxide regeneration device 10 can be a regeneration tower, and the carbon dioxide-rich liquid is decomposed under high temperature in the regeneration tower to release carbon dioxide, and the temperature of the rich liquid in the regeneration tower is controlled to be 110°C;
- the carbon dioxide storage device 16 is a carbon dioxide storage tank
- the water storage device 19 is a water storage tank
- the water heating device 21 is a water heater
- the gas mixing device 18 is a gas mixer
- the methanol synthesis device 23 is a dielectric barrier discharge reactor, as shown in Figure 3, the dielectric barrier discharge reactor includes an inlet pipe 24, an outlet pipe 25, a high-level voltage 26, a ground electrode 27, an insulating medium 28 and a gas distributor 29;
- the air carbon capture system 2 also includes,
- the heat exchange device 7 is arranged between the carbon dioxide absorption device 5 and the carbon dioxide regeneration device 10, the heat exchange device 7 has a rich liquid inlet, a rich liquid outlet, a lean liquid inlet and a lean liquid outlet, and the heat exchange device 7
- the rich liquid inlet is connected with the rich liquid outlet of the carbon dioxide absorption device 5, and the rich liquid outlet of the heat exchange device 7 is connected with the rich liquid inlet of the carbon dioxide regeneration device 10;
- FIG. 2 it also includes a renewable energy power generation system 1, and the abandoned electricity generated by the renewable energy power generation system 1 supplies power for an air carbon capture system 2 and a methanol synthesis system 3, and the renewable energy power generation system 1 can be wind power system;
- the heat exchange device 7 is a heat exchanger, and a cold rich liquid pump 6 is arranged between the rich liquid inlet of the heat exchange device 7 and the rich liquid outlet of the carbon dioxide absorption device 5;
- a rich liquid storage device 8 and a hot rich liquid pump 9 are arranged in sequence between the rich liquid outlet of the heat exchange device 7 and the rich liquid inlet of the carbon dioxide regeneration device 10; optionally, the rich liquid storage device 8 is rich liquid storage tank;
- a carbon dioxide compression device 15 is arranged between the carbon dioxide regeneration device 10 and the carbon dioxide storage device 16 .
- the carbon dioxide compression device 15 is a carbon dioxide compressor;
- the carbon dioxide regeneration device 10 has a rich liquid inlet, a carbon dioxide outlet, a lean liquid inlet and a lean liquid outlet, and a hot lean liquid pump 12 is arranged between the lean liquid outlet of the carbon dioxide regeneration device 10 and the lean liquid inlet of the heat exchange device 7 ;
- a heating device 11 is provided between the lean liquid outlet and the lean liquid inlet of the carbon dioxide regeneration device 10 .
- the heating device 11 is a reboiler
- the carbon dioxide absorption device 5 has an air inlet, a rich liquid outlet, a lean liquid inlet and an air outlet, the air outlet of the air compression device 4 is connected with the air inlet of the carbon dioxide absorption device 5, and the lean liquid outlet of the heat exchange device 7 is A lean liquid storage device 13 and a cold lean liquid pump 14 connected in sequence are arranged between the lean liquid inlet of the carbon dioxide absorption device 5 .
- the lean liquid storage device 13 is a lean liquid storage tank;
- the gas mixing device 18 has a carbon dioxide inlet, a water vapor inlet and a mixed gas outlet, and a carbon dioxide valve 17 is arranged between the gas outlet of the carbon dioxide storage device 16 and the carbon dioxide inlet of the gas mixing device 18, A water vapor valve 22 is arranged between the water heating device 21 and the water vapor inlet of the gas mixing device 18; a water pump 20 is arranged between the water storage device 19 and the water heating device 21;
- Methanol is prepared from CO 2 based on the above-mentioned device: when the renewable energy power generation system 1 has a power-suspended output, the air carbon capture system 2 is driven to work, and monoethanolamine is used as a chemical absorbent to directly capture CO 2 from the air; in methanol synthesis In system 3, water vapor and CO 2 gas are mixed at a ratio of 8:1 and then reformed into methanol under the action of plasma at room temperature and pressure.
- This embodiment provides a kind of device that utilizes carbon dioxide and water to synthesize methanol, and its difference compared with embodiment 1 is that described renewable energy power generation system 1 is a photovoltaic power generation system, porous liquid (ZIF-8/ethylene glycol) As a chemical absorbent, in the methanol synthesis system 3, water vapor and CO gas are mixed at a ratio of 10:1 and then reformed into methanol under the action of plasma at normal temperature and pressure.
- renewable energy power generation system 1 is a photovoltaic power generation system, porous liquid (ZIF-8/ethylene glycol)
- ZIF-8/ethylene glycol porous liquid
- water vapor and CO gas are mixed at a ratio of 10:1 and then reformed into methanol under the action of plasma at normal temperature and pressure.
- This embodiment provides a kind of device that utilizes carbon dioxide and water to synthesize methanol, and its difference compared with embodiment 1 is that described renewable energy generation system 1 is a wind power generation system, porous liquid (ZSM-5/large-volume ionic liquid ) as a chemical absorbent, in the methanol synthesis system 3, water vapor and CO 2 gas are mixed at a ratio of 12:1 and then reformed into methanol under the action of plasma at normal temperature and pressure.
- renewable energy generation system 1 is a wind power generation system, porous liquid (ZSM-5/large-volume ionic liquid ) as a chemical absorbent, in the methanol synthesis system 3, water vapor and CO 2 gas are mixed at a ratio of 12:1 and then reformed into methanol under the action of plasma at normal temperature and pressure.
- This embodiment provides a method for utilizing carbon dioxide and hydration to synthesize methanol, which is carried out by using the above-mentioned device, and includes the following steps:
- the discarded electricity in the renewable energy power generation system 1 supplies power for the air carbon capture system 2 and the methanol synthesis system 3;
- the top of the tower enters the absorption tower, and the absorbent in the absorption tower is in reverse contact with the air.
- the absorbent selectively absorbs CO 2 , and the decarbonized air is discharged from the top of the absorption tower to the atmosphere, and the rich CO 2 after absorbing
- the cold rich liquid pump 6 exchanges heat with the lean liquid from the regeneration tower at the heat exchanger, and then flows to the rich liquid storage tank for storage;
- the rich liquid in the rich liquid storage tank enters into the regeneration tower through the hot rich liquid pump 9 for regeneration.
- a reboiler is installed at the bottom of the tower, and the reboiler is driven by the renewable energy power generation system 1 for regeneration.
- the tower provides heat; the lean liquid regenerated from the regeneration tower passes through the hot lean liquid pump 12 and exchanges heat with the cold rich liquid from the absorption tower at the heat exchanger, then flows to the lean liquid storage tank and continues to be recycled;
- the CO 2 gas from the top of the regeneration tower is stored in the carbon dioxide storage tank through the carbon dioxide compressor, and is used for the synthesis of methanol;
- the water in the water storage tank enters the water heater for gasification after passing through the water pump 20.
- the electric energy required by the water heater comes from the renewable energy power generation system 1, and the gasified water vapor passes through the water vapor valve After 22, it enters the gas mixer; the CO2 gas from the air carbon capture system 2 enters the gas mixer after passing through the carbon dioxide valve 17 from the carbon dioxide storage tank; Mixing, then the mixed gas enters the methanol synthesis device 23, and uses dielectric barrier discharge cold plasma to reform CO 2 at normal temperature and pressure.
- a plasma region is formed to carry out dielectric barrier discharge reaction
- water molecules are broken down by discharge to produce chemically active hydrogen ion radicals, which further react with CO 2 to synthesize methanol.
- the device for synthesizing methanol from carbon dioxide and water drives the air carbon capture system 2 to work when the renewable energy power generation system 1 has a power-suppression output, and uses the chemical absorption method to directly capture carbon dioxide from the air.
- methanol synthesis system 3 carbon dioxide is reformed into methanol with water under the reaction conditions of normal temperature and pressure under the action of plasma.
- the device is mainly composed of renewable energy power generation system 1, air carbon capture system 2 and methanol synthesis system 3.
- the integration of the system is as follows: the waste electricity generated by the renewable energy system provides electricity and heat consumption for the air carbon capture system 2 and the methanol synthesis system 3, and the air carbon capture system 2 uses chemical absorption to capture CO2 in the air Collection, the captured CO 2 and water are mixed in a certain ratio and then enter the methanol synthesis device 23. Under the action of plasma, the CO 2 and water are reformed into methanol under the reaction conditions of normal temperature and pressure.
- This application uses the waste electricity generated by renewable energy to drive the entire integrated system, and realizes the reformation of CO2 into methanol under normal temperature and pressure, which effectively improves the absorption capacity of renewable energy power generation, and reduces carbon emissions while reducing carbon emissions.
- the resource utilization of CO2 is realized; in addition, due to the existence of rich liquid storage tanks, lean liquid storage tanks, CO2 storage tanks and water storage tanks, the integrated system can operate flexibly and has a high ability to accept fluctuating new energy .
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Abstract
本申请属于温室气体减排及资源化利用技术领域，具体涉及一种利用二氧化碳和水合成甲醇的装置及方法。本申请提供的利用二氧化碳和水合成甲醇的装置，包括空气捕碳系统和甲醇合成系统；空气捕碳系统包括依次连接的空气压缩装置、二氧化碳吸收装置、二氧化碳再生装置、二氧化碳储存装置；甲醇合成系统包括依次连接的水储存装置、水加热装置、气体混合装置和甲醇合成装置，所述二氧化碳储存装置的出气口与气体混合装置的二氧化碳进气口连接；所述甲醇合成装置为介质阻挡放电反应器。本申请提供的利用二氧化碳和水合成甲醇的装置可实现甲醇合成过程中CO 2的连续供应，节省了原料的运输成本，在降低碳减排的同时实现了CO 2的资源化利用。
Description
相关申请的交叉引用
本申请要求在2021年6月3日提交中国专利局、申请号为202110620397.4、申请名称为“一种利用二氧化碳和水合成甲醇的装置及方法”的中国专利申请的优先权，其全部内容通过引用的方式并入本文中。
本申请属于温室气体减排及资源化利用技术领域，具体涉及一种利用二氧化碳和水合成甲醇的装置及方法。
全球气候变化是人类可持续发展的最大威胁，应对气候变化是关乎生存发展权的非传统国家安全问题，应对气候变化以控制CO
2排放为主要目标。工业以及电力行业等是CO
2的集中稳定排放源，约占CO
2排放总量的50％。针对这些固定点源的CO
2减排，主要是利用CO
2捕集与封存(CCUS)技术，此技术是一种具有大规模CO
2减排潜力的技术。但是，除了工业以及电力行业等固定点源的CO
2排放，还有接近50％分布源排放的CO
2，从空气中直接捕碳技术可对这些分布源的CO
2进行捕集和利用。与CCUS技术从燃煤电厂捕碳不同，从空气中直接捕碳受地点限制较小，可以在各地广泛开展，而且，从空气中直接捕碳能降低空气中CO
2的浓度，可以解决“存量”的问题。
目前，人们对能源的需求量越来越大，化石燃料的储量逐渐减少，且燃烧化石燃料造成的温室效应问题日趋严重，如何将CO
2等温室气体转换为有价值的清洁能源成为了一个亟需解决的问题。甲醇是CO
2加氢产物之一，它是结构最为简 单的饱和一元醇，作为基础有机化工原料，其消费量仅次于乙烯、丙烯和苯，主要用于塑料、精细化学品、石油化工等领域。此外，甲醇也是一种新型的清洁能源，由于其具有良好的抗爆性和高辛烷值，可以作为车用燃料。目前工业上通过CO
2及氢气制备甲醇的流程一般需要在高温高压的条件(30个大气压及200℃以上)下进行，这种高温高压的条件不但限制了甲醇的规模化生产，而且造成了额外的能源浪费。
因此，开发一种空气直接捕碳与利用二氧化碳和水在常温常压下合成甲醇的装置和方法具有重要的意义。
发明内容
为了克服上述现有技术中空气中二氧化碳易引起温室效应，且利用二氧化碳制甲醇需要在高温高压下进行的缺点，进而提供一种空气中直接捕碳与利用二氧化碳和水在常温常压下合成甲醇的装置和方法。
为了达到上述目的，本申请采用以下技术方案予以实现：
一种利用二氧化碳和水合成甲醇的装置，包括空气捕碳系统和甲醇合成系统；
空气捕碳系统包括依次连接的空气压缩装置、二氧化碳吸收装置、二氧化碳再生装置、二氧化碳储存装置；
甲醇合成系统包括依次连接的水储存装置、水加热装置、气体混合装置和甲醇合成装置，所述二氧化碳储存装置的出气口与气体混合装置的二氧化碳进气口连接；所述甲醇合成装置为介质阻挡放电反应器。
可选的，所述空气捕碳系统还包括，
换热装置，设置于所述二氧化碳吸收装置和二氧化碳再生装置之间，所述换热装置具有富液进口、富液出口、贫液进口和贫液出口，所述换热装置的富液进 口与二氧化碳吸收装置的富液出口连接，所述换热装置的富液出口与二氧化碳再生装置的富液进口连接。
可选的，所述换热装置的富液进口与二氧化碳吸收装置的富液出口之间设置有冷富液泵；
所述换热装置的富液出口与二氧化碳再生装置的富液进口之间设置有依次连接的富液储存装置和热富液泵；
所述二氧化碳再生装置和二氧化碳储存装置之间设置有二氧化碳压缩装置。
可选的，所述二氧化碳再生装置具有富液进口、二氧化碳出口、贫液进口和贫液出口，所述二氧化碳再生装置的贫液出口与换热装置的贫液进口之间设置有热贫液泵；
所述二氧化碳再生装置的贫液出口和贫液进口之间设置有加热装置。
可选的，所述二氧化碳吸收装置具有空气进口、富液出口、贫液进口和空气出口，所述空气压缩装置的出气口与二氧化碳吸收装置的空气进口连接，所述换热装置的贫液出口与二氧化碳吸收装置的贫液进口之间设置有依次连接的贫液储存装置和冷贫液泵。
可选的，所述气体混合装置具有二氧化碳进气口、水蒸气进气口和混合气体出气口，所述二氧化碳储存装置的出气口与气体混合装置的二氧化碳进气口之间设置有二氧化碳阀门，所述水加热装置和气体混合装置的水蒸气进气口之间设置有水蒸气阀门；所述水储存装置和水加热装置之间设置有水泵。
可选的，所述二氧化碳吸收装置为二氧化碳吸收塔，吸收塔内设置有二氧化碳吸收剂；
所述二氧化碳再生装置为二氧化碳再生塔。
可选的，还包括可再生能源发电系统，所述可再生能源发电系统产生的弃电为空气捕碳系统和甲醇合成系统供电。
本申请提供一种利用二氧化碳和水合成甲醇的方法，采用上述所述的装置进行。
可选的，所述方法包括如下步骤：当可再生能源发电系统具有弃电输出时，驱动空气捕碳系统工作，利用化学吸收法直接从空气中捕集二氧化碳，捕集得到的二氧化碳在甲醇合成系统中与水重整合成为甲醇。
与现有技术相比，本申请具有以下有益效果：
本申请提供的利用二氧化碳和水合成甲醇的装置，利用空气捕碳系统从空气中直接捕碳，然后利用甲醇合成系统中介质阻挡放电反应器，基于等离子体的CO
2和水重整合成甲醇，实现了甲醇合成过程中CO
2的连续供应，节省了原料的运输成本，在降低碳减排的同时实现了CO
2的资源化利用。
进一步的，利用可再生能源发电系统产生的弃电为空气捕碳系统和甲醇合成系统供电，不仅不会对可再生能源发电系统产生影响，还有效解决了可再生能源的弃电问题，且可再生能源储量丰富，在开发利用过程中对环境影响较小，利用波动性新能源驱动捕碳系统直接从空气中捕集CO
2，能够降低空气中CO
2含量，并且在捕碳过程中不产生附加的CO
2，是缓解全球气候变化的重要途径之一。利用介质阻挡放电反应器，基于等离子体技术，实在了常温常压下CO
2的资源化利用，与CO
2和氢气催化加氢制甲醇相比，既减少了反应流程，还能避免电解水制氢所需要的额外能耗。可再生能源发电、空气直接捕碳和甲醇合成三者有效集成，整个系统可灵活运行，当有弃电时系统运行，无弃电时系统可以停止运行；同时富液储存装置、贫液储存装置、二氧化碳储存装置、水储存装置的存在，将捕碳 的吸收环节、捕碳的解析环节、CO
2的利用环节独立控制，有利于提高集成系统接受波动性新能源的能力。设备安装受地点约束较少，适用于有可再生能源发电的多种场所。即本申请提供的装置通过再生能源发电系统，空气捕碳系统和甲醇合成系统的集成，实现了利用可再生能源驱动空气直接捕碳与利用CO
2和水在常温常压下合成甲醇，既实现了可再生能源弃电的消纳问题，同时还达到了碳减排、CO
2资源化利用的多重目标。
图1为本申请利用二氧化碳和水合成甲醇的装置的示意图；
图2为本申请利用可再生能源发电系统驱动的二氧化碳和水合成甲醇的装置的示意图；
图3为介质阻挡放电反应器结构示意图。
其中：1-可再生能源发电系统；2-空气捕碳系统；3-甲醇合成系统；4-空气压缩装置；5-二氧化碳吸收装置；6-冷富液泵；7-换热装置；8-富液储存装置；9-热富液泵；10-二氧化碳再生装置；11-加热装置；12-热贫液泵；13-贫液储存装置；14-冷贫液泵；15-二氧化碳压缩装置；16-二氧化碳储存装置；17-二氧化碳阀门；18-气体混合装置；19-水储存装置；20-水泵；21-水加热装置；22-水蒸气阀门；23-甲醇合成装置；24-进气管；25-出气管；26-高级电压；27-接地电极；28-绝缘介质；29-气体分布器。
为了使本技术领域的人员更好地理解本申请方案，下面将结合本申请实施例中的附图，对本申请实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例仅仅是本申请一部分的实施例，而不是全部的实施例。基于本申请中的 实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例，都应当属于本申请保护的范围。
需要说明的是，术语“包括”和“具有”以及他们的任何变形，意图在于覆盖不排他的包含，例如，包含了一系列步骤或单元的过程、方法、系统、产品或设备不必限于清楚地列出的那些步骤或单元，而是可包括没有清楚地列出的或对于这些过程、方法、产品或设备固有的其它步骤或单元。
下面结合附图对本申请做进一步详细描述：
如图1和图2所示，本申请提供了一种利用二氧化碳和水合成甲醇的装置，包括空气捕碳系统2和甲醇合成系统3；
空气捕碳系统2包括依次连接的空气压缩装置4、二氧化碳吸收装置5、二氧化碳再生装置10、二氧化碳储存装置16；
甲醇合成系统3包括依次连接的水储存装置19、水加热装置21、气体混合装置18和甲醇合成装置23，所述二氧化碳储存装置16的出气口与气体混合装置18的二氧化碳进气口连接；所述甲醇合成装置23为介质阻挡放电反应器。
可选的，所述空气压缩装置4为空气压缩机，二氧化碳吸收装置5为二氧化碳吸收塔，吸收塔内设置有二氧化碳吸收剂，可选的，二氧化碳吸收剂可以为单乙醇胺、混合胺或多孔液体，所述多孔液体可为ZIF-8/乙二醇、ZSM-5/大体积离子液体，通过CO
2与吸收剂之间的化学反应来捕集空气中的CO
2。
可选的，二氧化碳再生装置10可为二氧化碳再生塔，二氧化碳富液在再生塔中在高温作用下进行解析进而释放二氧化碳，可选的，控制再生塔内富液温度为110-120℃。
可选的，所述二氧化碳吸收塔和再生塔均为填料塔，采用惰性金属填料，填 料的作用是保证气液两相充分接触。
可选的，二氧化碳储存装置16为二氧化碳储存罐，水储存装置19为水储存罐、水加热装置21为水加热器、气体混合装置18为气体混合器。
可选的，甲醇合成装置23为介质阻挡放电反应器，所述介质阻挡放电反应器为本领域常规介质阻挡放电反应器，可通过市购获得或通过现有技术自行设计获得。可选的，如图3所示，所述介质阻挡放电反应器为一种介质阻挡放电装置，包括进气管24、出气管25、高级电压26、接地电极27、绝缘介质28和气体分布器29；二氧化碳和水蒸气的混合气体从进气管24中进入，合成的甲醇气体从出气管25中排出。
本申请提供的利用二氧化碳和水合成甲醇的装置，利用空气捕碳系统2从空气中直接捕碳，然后利用甲醇合成系统3中介质阻挡放电反应器，基于等离子体的CO
2和水重整合成甲醇，实现了甲醇合成过程中CO
2的连续供应，节省了原料的运输成本，在降低碳减排的同时实现了CO
2的资源化利用。
在一可选实施例中，如图2所示，还包括可再生能源发电系统1，所述可再生能源发电系统1产生的弃电为空气捕碳系统2和甲醇合成系统3供电。可选的，所述可再生能源发电系统1可为风力发电系统或光伏发电系统。可选的，可再生能源发电系统1可为装置内任何需要能量的部件进行供电，以提供所需的能量。可选的，所述可再生能源发电系统1与再沸器连接，以为再生塔提供热量，所述可再生能源发电系统1与水加热器连接，将水加热为水蒸气；所述可再生能源发电系统1与介质阻挡放电反应器连接，通电后介质阻挡放电反应器内形成等离子区，进行介质阻挡放电反应，反应中水分子被放电击穿产生了化学性质活跃的氢离子基，氢离子基进一步与CO
2发生反应合成甲醇。与CO
2和氢气催化加氢制甲 醇相比，基于等离子体的CO
2和水直接合成甲醇，既减少了反应流程，还能避免电解水制氢所需要的额外能耗，大大提高了能源利用率。
可选的，在甲醇合成系统3的气体混合器中，为保证CO
2充分转化，水蒸气和CO
2气体混合时的摩尔比为(6～12)：1。
本申请利用可再生能源发电系统1产生的弃电为空气捕碳系统2和甲醇合成系统3供电，不仅不会对可再生能源发电系统1产生影响，还有效解决了可再生能源的弃电问题，且可再生能源储量丰富，在开发利用过程中对环境影响较小，利用波动性新能源驱动捕碳系统直接从空气中捕集CO
2，能够降低空气中CO
2含量，并且在捕碳过程中不产生附加的CO
2，是缓解全球气候变化的重要途径之一。利用介质阻挡放电反应器，基于等离子体技术，实在了常温常压下CO
2的资源化利用，与CO
2和氢气催化加氢制甲醇相比，既减少了反应流程，还能避免电解水制氢所需要的额外能耗。可再生能源发电、空气直接捕碳和甲醇合成三者有效集成，整个系统可灵活运行，当有弃电时系统运行，无弃电时系统可以停止运行；同时富液储存装置8、贫液储存装置13、二氧化碳储存装置16、水储存装置19的存在，将捕碳的吸收环节、捕碳的解析环节、CO
2的利用环节独立控制，有利于提高集成系统接受波动性新能源的能力。设备安装受地点约束较少，适用于有可再生能源发电的多种场所。即本申请提供的装置通过再生能源发电系统，空气捕碳系统2和甲醇合成系统3的集成，实现了利用可再生能源驱动空气直接捕碳与利用CO
2和水在常温常压下合成甲醇，既实现了可再生能源弃电的消纳问题，同时还达到了碳减排、CO
2资源化利用的多重目标。
在一可选实施例中，所述空气捕碳系统2还包括，
换热装置7，设置于所述二氧化碳吸收装置5和二氧化碳再生装置10之间， 所述换热装置7具有富液进口、富液出口、贫液进口和贫液出口，所述换热装置7的富液进口与二氧化碳吸收装置5的富液出口连接，所述换热装置7的富液出口与二氧化碳再生装置10的富液进口连接。
可选的，所述换热装置7为换热器，吸收塔与富液储存罐之间连接有换热器，有利于提高能源的利用率，降低成本。
在一可选实施例中，所述换热装置7的富液进口与二氧化碳吸收装置5的富液出口之间设置有冷富液泵6；
所述换热装置7的富液出口与二氧化碳再生装置10的富液进口之间设置有依次连接的富液储存装置8和热富液泵9；可选的，所述富液储存装置8为富液储存罐。
所述二氧化碳再生装置10和二氧化碳储存装置16之间设置有二氧化碳压缩装置15。可选的，所述二氧化碳压缩装置15为二氧化碳压缩机。
在一可选实施例中，所述二氧化碳再生装置10具有富液进口、二氧化碳出口、贫液进口和贫液出口，所述二氧化碳再生装置10的贫液出口与换热装置7的贫液进口之间设置有热贫液泵12；
所述二氧化碳再生装置10的贫液出口和贫液进口之间设置有加热装置11。可选的，所述加热装置11为再沸器。本申请在再生塔底部设有再沸器，通过再沸器加热的方式将富液中的CO
2与吸收剂分离。
在一可选实施例中，所述二氧化碳吸收装置5具有空气进口、富液出口、贫液进口和空气出口，所述空气压缩装置4的出气口与二氧化碳吸收装置5的空气进口连接，所述换热装置7的贫液出口与二氧化碳吸收装置5的贫液进口之间设置有依次连接的贫液储存装置13和冷贫液泵14。可选的，所述贫液储存装置13 为贫液储存罐。
在一可选实施例中，所述气体混合装置18具有二氧化碳进气口、水蒸气进气口和混合气体出气口，所述二氧化碳储存装置16的出气口与气体混合装置18的二氧化碳进气口之间设置有二氧化碳阀门17，所述水加热装置21和气体混合装置18的水蒸气进气口之间设置有水蒸气阀门22；所述水储存装置19和水加热装置21之间设置有水泵20。
本申请还提供一种利用二氧化碳和水合成甲醇的方法，该方法采用如上所述的装置。
可选的，所述方法包括如下步骤：当可再生能源发电系统1具有弃电输出时，驱动空气捕碳系统2工作，利用化学吸收法直接从空气中捕集二氧化碳，捕集得到的二氧化碳在甲醇合成系统3中与水重整合成为甲醇。
在本申请中可再生能源发电系统1中的弃电为空气捕碳系统2和甲醇合成系统3供电；空气通过空气压缩机进入二氧化碳吸收塔，吸收塔中的碳捕集化学吸收剂(单乙醇胺、混合胺或多孔液体)对CO
2进行选择性吸收，吸收CO
2后的富液自吸收塔底部的富液出口流出后经过换热器进入富液储存罐；富液储存罐中的富液经过管路输送至二氧化碳再生塔进行CO
2再生，再生后含有吸收剂的贫液从再生塔的底部流出并经过换热器输送至贫液储存罐备用；再生过程得到的CO
2气体经二氧化碳压缩机送至二氧化碳储存罐；水储存罐中的水经过水加热器后与二氧化碳储存罐中的CO
2在气体混合器中进行混合，之后将混合后的气体经过管路输送至甲醇合成装置23中进行反应，从而得到甲醇。
以下通过具体的实施例阐述本申请方案。
实施例1
参见图1和图2，本实施例提供了一种利用二氧化碳和水合成甲醇的装置，包括空气捕碳系统2和甲醇合成系统3；
空气捕碳系统2包括依次连接的空气压缩装置4、二氧化碳吸收装置5、二氧化碳再生装置10、二氧化碳储存装置16；
甲醇合成系统3包括依次连接的水储存装置19、水加热装置21、气体混合装置18和甲醇合成装置23，所述二氧化碳储存装置16的出气口与气体混合装置18的二氧化碳进气口连接；所述甲醇合成装置23为介质阻挡放电反应器；
所述空气压缩装置4为空气压缩机，二氧化碳吸收装置5为二氧化碳吸收塔，吸收塔内设置有二氧化碳吸收剂，二氧化碳吸收剂为单乙醇胺；
二氧化碳再生装置10可为再生塔，二氧化碳富液在再生塔中在高温作用下进行解析进而释放二氧化碳，控制再生塔内富液温度为110℃；
二氧化碳储存装置16为二氧化碳储存罐，水储存装置19为水储存罐、水加热装置21为水加热器、气体混合装置18为气体混合器；
甲醇合成装置23为介质阻挡放电反应器，如图3所示，所述介质阻挡放电反应器包括进气管24、出气管25、高级电压26、接地电极27、绝缘介质28和气体分布器29；
所述空气捕碳系统2还包括，
换热装置7，设置于所述二氧化碳吸收装置5和二氧化碳再生装置10之间，所述换热装置7具有富液进口、富液出口、贫液进口和贫液出口，所述换热装置7的富液进口与二氧化碳吸收装置5的富液出口连接，所述换热装置7的富液出口与二氧化碳再生装置10的富液进口连接；
如图2所示，还包括可再生能源发电系统1，所述可再生能源发电系统1产 生的弃电为空气捕碳系统2和甲醇合成系统3供电，所述可再生能源发电系统1可为风力发电系统；
所述换热装置7为换热器，所述换热装置7的富液进口与二氧化碳吸收装置5的富液出口之间设置有冷富液泵6；
所述换热装置7的富液出口与二氧化碳再生装置10的富液进口之间设置有依次连接的富液储存装置8和热富液泵9；可选的，所述富液储存装置8为富液储存罐；
所述二氧化碳再生装置10和二氧化碳储存装置16之间设置有二氧化碳压缩装置15。所述二氧化碳压缩装置15为二氧化碳压缩机；
所述二氧化碳再生装置10具有富液进口、二氧化碳出口、贫液进口和贫液出口，所述二氧化碳再生装置10的贫液出口与换热装置7的贫液进口之间设置有热贫液泵12；
所述二氧化碳再生装置10的贫液出口和贫液进口之间设置有加热装置11。所述加热装置11为再沸器；
所述二氧化碳吸收装置5具有空气进口、富液出口、贫液进口和空气出口，所述空气压缩装置4的出气口与二氧化碳吸收装置5的空气进口连接，所述换热装置7的贫液出口与二氧化碳吸收装置5的贫液进口之间设置有依次连接的贫液储存装置13和冷贫液泵14。所述贫液储存装置13为贫液储存罐；
所述气体混合装置18具有二氧化碳进气口、水蒸气进气口和混合气体出气口，所述二氧化碳储存装置16的出气口与气体混合装置18的二氧化碳进气口之间设置有二氧化碳阀门17，所述水加热装置21和气体混合装置18的水蒸气进气口之间设置有水蒸气阀门22；所述水储存装置19和水加热装置21之间设置有水 泵20；
基于上述装置中进行CO
2制备甲醇：当可再生能源发电系统1具有弃电输出时，驱动空气捕碳系统2工作，利用单乙醇胺作为化学吸收剂直接从空气中捕集CO
2；在甲醇合成系统3，水蒸气和CO
2气体按照8：1的比例混合后在等离子体作用下于常温常压下重整为甲醇。
实施例2
本实施例提供了一种利用二氧化碳和水合成甲醇的装置，其与实施例1相比区别在于，所述可再生能源发电系统1是光伏发电系统，多孔液体(ZIF-8/乙二醇)作为化学吸收剂，在甲醇合成系统3，水蒸气和CO
2气体按照10：1的比例混合后在等离子体作用下于常温常压下重整为甲醇。
实施例3
本实施例提供了一种利用二氧化碳和水合成甲醇的装置，其与实施例1相比区别在于，所述可再生能源发电系统1是风力发电系统，多孔液体(ZSM-5/大体积离子液体)作为化学吸收剂，在甲醇合成系统3，水蒸气和CO
2气体按照12：1的比例混合后在等离子体作用下于常温常压下重整为甲醇。
实施例4
本实施例提供一种利用二氧化碳和水合成甲醇的方法，采用上述所述的装置进行，包括如下步骤：
可再生能源发电系统1中的弃电为空气捕碳系统2和甲醇合成系统3供电；空气通过空气压缩机进入二氧化碳吸收塔底部，来自贫液储存罐的贫液经冷贫液泵14后自塔顶进入吸收塔，吸收塔中的吸收剂和空气逆向接触，吸收剂对CO
2进行选择性吸收，脱碳处理后的空气自吸收塔的塔顶排到大气中，吸收CO
2后的 富液自吸收塔底部的富液出口流出后，经冷富液泵6在换热器处与来自再生塔的贫液进行换热后，流向富液储存罐储存；
当再生塔工作时，富液储存罐中的富液经热富液泵9进入在再生塔中进行再生，塔底设有再沸器，再沸器由可再生能源发电系统1驱动，为再生塔提供热量；从再生塔中再生后的贫液经热贫液泵12后在换热器处与来自吸收塔的冷富液换热后，流向贫液储存罐，继续循环使用；
从再生塔的顶部出来的CO
2气体经二氧化碳压缩机进入二氧化碳储存罐保存，用于甲醇的合成；
在甲醇合成系统3中，水储存罐中的水经水泵20后进入水加热器进行气化，水加热器所需的电能来自可再生能源发电系统1，气化后的水蒸气经水蒸气阀门22后进入气体混合器；来自空气捕碳系统2的CO
2气体从二氧化碳储存罐经二氧化碳阀门17后进入气体混合器；在气体混合器处，水蒸气和CO
2气体按照10：1的比例进行混合，随后混合气进入甲醇合成装置23中，于常温常压下利用介质阻挡放电冷等离子体重整CO
2，甲醇合成装置23与可再生能源发电系统1通电后形成等离子区，进行介质阻挡放电反应，反应中水分子被放电击穿产生了化学性质活跃的氢离子基，氢离子基进一步与CO
2发生反应合成甲醇。
本申请提供的利用二氧化碳和水合成甲醇的装置，当可再生能源发电系统1具有弃电输出时，驱动空气捕碳系统2工作，利用化学吸收法直接从空气中捕集二氧化碳，捕集得到的二氧化碳在甲醇合成系统3，在等离子体作用下，于常温常压的反应条件下与水重整为甲醇。装置主要由可再生能源发电系统1、空气捕碳系统2和甲醇合成系统3组成。该系统的集成方式如下：可再生能源系统产生的弃电为空气捕碳系统2和甲醇合成系统3提供电耗和热耗，空气捕碳系统2采 用化学吸收法对空气中的CO
2进行捕集，捕集得到的CO
2和水以一定的比例混合后进入甲醇合成装置23，在等离子体作用下，于常温常压的反应条件下将CO
2和水重整为甲醇。本申请利用可再生能源产生的弃电来驱动整个集成系统，在常温常压下实现了CO
2重整为甲醇，有效提升了可再生能源发电的消纳能力，并在降低碳减排的同时实现了CO
2的资源化利用；此外，由于富液储存罐、贫液储存罐、CO
2储存罐和水储存罐的存在，集成系统可灵活运行，具有较高的接受波动性新能源的能力。
以上内容仅为说明本申请的技术思想，不能以此限定本申请的保护范围，凡是按照本申请提出的技术思想，在技术方案基础上所做的任何改动，均落入本申请权利要求书的保护范围之内。
Claims (10)
- 一种利用二氧化碳和水合成甲醇的装置，其特征在于，包括空气捕碳系统和甲醇合成系统；空气捕碳系统包括依次连接的空气压缩装置、二氧化碳吸收装置、二氧化碳再生装置、二氧化碳储存装置；甲醇合成系统包括依次连接的水储存装置、水加热装置、气体混合装置和甲醇合成装置，所述二氧化碳储存装置的出气口与气体混合装置的二氧化碳进气口连接；所述甲醇合成装置为介质阻挡放电反应器。
- 根据权利要求1所述的利用二氧化碳和水合成甲醇的装置，其特征在于，所述空气捕碳系统还包括，换热装置，设置于所述二氧化碳吸收装置和二氧化碳再生装置之间，所述换热装置具有富液进口、富液出口、贫液进口和贫液出口，所述换热装置的富液进口与二氧化碳吸收装置的富液出口连接，所述换热装置的富液出口与二氧化碳再生装置的富液进口连接。
- 根据权利要求2所述的利用二氧化碳和水合成甲醇的装置，其特征在于，所述换热装置的富液进口与二氧化碳吸收装置的富液出口之间设置有冷富液泵；所述换热装置的富液出口与二氧化碳再生装置的富液进口之间设置有依次连接的富液储存装置和热富液泵；所述二氧化碳再生装置和二氧化碳储存装置之间设置有二氧化碳压缩装置。
- 根据权利要求3所述的利用二氧化碳和水合成甲醇的装置，其特征在于， 所述二氧化碳再生装置具有富液进口、二氧化碳出口、贫液进口和贫液出口，所述二氧化碳再生装置的贫液出口与换热装置的贫液进口之间设置有热贫液泵；所述二氧化碳再生装置的贫液出口和贫液进口之间设置有加热装置。
- 根据权利要求4所述的利用二氧化碳和水合成甲醇的装置，其特征在于，所述二氧化碳吸收装置具有空气进口、富液出口、贫液进口和空气出口，所述空气压缩装置的出气口与二氧化碳吸收装置的空气进口连接，所述换热装置的贫液出口与二氧化碳吸收装置的贫液进口之间设置有依次连接的贫液储存装置和冷贫液泵。
- 根据权利要求1-5任一项所述的利用二氧化碳和水合成甲醇的装置，其特征在于，所述气体混合装置具有二氧化碳进气口、水蒸气进气口和混合气体出气口，所述二氧化碳储存装置的出气口与气体混合装置的二氧化碳进气口之间设置有二氧化碳阀门，所述水加热装置和气体混合装置的水蒸气进气口之间设置有水蒸气阀门；所述水储存装置和水加热装置之间设置有水泵。
- 根据权利要求1-6任一项所述的利用二氧化碳和水合成甲醇的装置，其特征在于，所述二氧化碳吸收装置为二氧化碳吸收塔，吸收塔内设置有二氧化碳吸收剂；所述二氧化碳再生装置为二氧化碳再生塔。
- 根据权利要求1-7任一项所述的利用二氧化碳和水合成甲醇的装置，其 特征在于，还包括可再生能源发电系统，所述可再生能源发电系统产生的弃电为空气捕碳系统和甲醇合成系统供电。
- 一种利用二氧化碳和水合成甲醇的方法，其特征在于，采用权利要求1-8任一项所述的装置进行。
- 根据权利要求9所述的利用二氧化碳和水合成甲醇的方法，其特征在于，所述方法包括如下步骤：当可再生能源发电系统具有弃电输出时，驱动空气捕碳系统工作，利用化学吸收法直接从空气中捕集二氧化碳，捕集得到的二氧化碳在甲醇合成系统中与水重整合成为甲醇。
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