CN113310063A - Device and method for capturing and purifying carbon dioxide in glass kiln flue gas - Google Patents
Device and method for capturing and purifying carbon dioxide in glass kiln flue gas Download PDFInfo
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- CN113310063A CN113310063A CN202110182303.XA CN202110182303A CN113310063A CN 113310063 A CN113310063 A CN 113310063A CN 202110182303 A CN202110182303 A CN 202110182303A CN 113310063 A CN113310063 A CN 113310063A
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 307
- 239000003546 flue gas Substances 0.000 title claims abstract description 179
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 176
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 155
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 155
- 239000011521 glass Substances 0.000 title claims abstract description 52
- 238000000034 method Methods 0.000 title claims abstract description 47
- 238000001179 sorption measurement Methods 0.000 claims abstract description 137
- 239000007789 gas Substances 0.000 claims abstract description 81
- 239000007788 liquid Substances 0.000 claims abstract description 51
- 238000001816 cooling Methods 0.000 claims abstract description 15
- 239000012535 impurity Substances 0.000 claims abstract description 15
- 238000007670 refining Methods 0.000 claims abstract description 15
- 238000006477 desulfuration reaction Methods 0.000 claims description 64
- 230000023556 desulfurization Effects 0.000 claims description 61
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 57
- 238000005406 washing Methods 0.000 claims description 53
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims description 42
- 239000002918 waste heat Substances 0.000 claims description 31
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 27
- 230000008569 process Effects 0.000 claims description 25
- 239000000428 dust Substances 0.000 claims description 23
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 17
- 238000003795 desorption Methods 0.000 claims description 15
- 238000005057 refrigeration Methods 0.000 claims description 14
- 239000003463 adsorbent Substances 0.000 claims description 12
- 230000006835 compression Effects 0.000 claims description 10
- 238000007906 compression Methods 0.000 claims description 10
- 229910052799 carbon Inorganic materials 0.000 claims description 9
- 239000002994 raw material Substances 0.000 claims description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- 238000011033 desalting Methods 0.000 claims description 7
- 230000003009 desulfurizing effect Effects 0.000 claims description 7
- 238000004064 recycling Methods 0.000 claims description 7
- 230000008929 regeneration Effects 0.000 claims description 6
- 238000011069 regeneration method Methods 0.000 claims description 6
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 5
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 5
- 239000000945 filler Substances 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 claims description 5
- 239000012452 mother liquor Substances 0.000 claims description 5
- 238000000746 purification Methods 0.000 claims description 5
- 238000006479 redox reaction Methods 0.000 claims description 5
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 4
- 239000002904 solvent Substances 0.000 claims description 4
- 238000009423 ventilation Methods 0.000 claims description 4
- 239000000779 smoke Substances 0.000 claims description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims 5
- 239000012717 electrostatic precipitator Substances 0.000 claims 5
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- 238000002425 crystallisation Methods 0.000 claims 2
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 11
- 230000009467 reduction Effects 0.000 description 8
- 238000006722 reduction reaction Methods 0.000 description 8
- 238000007664 blowing Methods 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 238000007710 freezing Methods 0.000 description 5
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- 229910052757 nitrogen Inorganic materials 0.000 description 5
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 3
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Inorganic materials [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 description 3
- 229910052938 sodium sulfate Inorganic materials 0.000 description 3
- 239000002912 waste gas Substances 0.000 description 3
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
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- 125000002485 formyl group Chemical class [H]C(*)=O 0.000 description 2
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical group N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
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- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
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Images
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
-
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
-
- 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
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- 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
- B01D53/1481—Removing sulfur dioxide or sulfur trioxide
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- 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
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
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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
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
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- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
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- B01D2251/2062—Ammonia
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
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- B01D2252/10—Inorganic absorbents
- B01D2252/103—Water
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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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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- 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
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- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Inorganic Chemistry (AREA)
- Separation Of Gases By Adsorption (AREA)
- Treating Waste Gases (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
The invention relates to the technical field of carbon dioxide recovery, in particular to a device and a method for capturing and purifying carbon dioxide in flue gas of a glass kiln, which comprises a carbon dioxide flue gas pretreatment system, a carbon dioxide capture system and a carbon dioxide refining system which are sequentially connected, wherein the flue gas pretreatment system is connected with the glass kiln and is used for pretreating the flue gas discharged by the glass kiln; the carbon dioxide capture system is used for further absorbing SO2 and NOX in the carbon dioxide, rapidly cooling and dedusting the flue gas, and adsorbing and desorbing the carbon dioxide into high-concentration carbon dioxide gas by a pressure swing adsorption method; the carbon dioxide refining system can compress and dry carbon dioxide, and liquid carbon dioxide products are prepared after impurities are removed. The device for capturing and purifying the carbon dioxide in the glass kiln flue gas provided by the invention can be used for capturing and concentrating the CO2 in the flue gas, so that the emission of the carbon dioxide and other pollutants to the atmosphere is reduced.
Description
Technical Field
The invention relates to the technical field of carbon dioxide recovery, in particular to a device and a method for capturing and purifying carbon dioxide in glass kiln smoke.
Background
Global warming is the biggest challenge facing mankind in the early century, and is not only an environmental problem but also an economic, political, human development and the like problem. From the late nineteenth century, the global air temperature has gone out steadily for thousands of years, entered the ascent passage, and may continue to rise substantially. In the atmosphere, the temperature rise is very strongly correlated with the rapid increase in the concentration of greenhouse gases, including carbon dioxide (CO2), methane (CH4), Nitrogen Oxides (NOX), chlorofluorocarbons (CFCS) and water vapor (H2O). While carbon dioxide is the most dominant greenhouse gas, its increased content contributes approximately 60% to the enhancement of the greenhouse effect.
Currently, the main industries of CO2 emission in China are high energy consumption industries such as electric power, steel, building materials, chemical industry and the like, wherein the building material industry accounts for about 15% of the emission of CO2 in national energy activities. As a pillar type industry of economic construction in China, the building material industry makes great contribution to economic development and social progress, and simultaneously consumes a large amount of resources and energy.
The carbon capture utilization and sequestration refers to an industrial process of separating carbon dioxide from an industrial emission source or directly utilizing or sequestering the carbon dioxide to realize CO2 emission reduction, is a novel technology with large-scale carbon dioxide emission reduction potential, is expected to realize low-carbon utilization of fossil energy, and is widely considered as one of the most important technologies for coping with global climate change and controlling greenhouse gas emission. The capture and separation of CO2 in the flue gas are the basis and precondition for realizing emission reduction measures such as the sealing and comprehensive utilization of the flue gas. At present, each large power generation group and oil system in China are also built into an industrial demonstration device for CO2 capture successively. But the carbon capture technology in the building material field, especially in the glass industry, is still blank.
As the temperature of flue gas after combustion in the glass kiln is up to 1200 ℃, the temperature of a waste heat boiler is required to be controlled at 600-650 ℃, and the temperature is generally reduced by mixing air, CO2 in the flue gas is diluted by a large amount of N2, so that the capture of carbon dioxide is very difficult.
Disclosure of Invention
The invention aims to solve the defects of the prior art and provides a device and a method for capturing and purifying carbon dioxide in glass kiln flue gas.
In order to achieve the purpose, the device for capturing and purifying the carbon dioxide in the flue gas of the glass kiln comprises a carbon dioxide flue gas pretreatment system, a carbon dioxide capture system and a carbon dioxide refining system which are sequentially connected, wherein the flue gas pretreatment system is connected with the glass kiln and is used for carrying out pretreatment of denitration, desulfurization, dust removal and temperature reduction on the flue gas discharged by the glass kiln; the carbon dioxide capture system comprises a water washing desulfurizing tower, and the water washing desulfurizing tower further absorbs SO in the pretreated carbon dioxide2And NOXThe temperature is rapidly reduced, and carbon dioxide is absorbed and desorbed into high-concentration carbon dioxide gas by a pressure swing adsorption method; the carbon dioxide refining system can compress and dry high-concentration carbon dioxide gas, and further remove impurities to prepare food-grade liquid carbon dioxide products.
The invention also has the following preferable technical scheme:
further, the flue gas pretreatment system comprises a flue gas waste heat boiler connected with the glass kiln, a flue gas electric dust removal device, a flue gas denitration device, a flue gas desulfurization device and a flue gas recirculation device, wherein a high-temperature section of the flue gas waste heat boiler is connected with the flue gas electric dust removal device, flue gas enters the flue gas electric dust removal device for dust collection after passing through the high-temperature section of the waste heat boiler, the flue gas electric dust removal device is connected with the flue gas denitration device, the flue gas is fully and uniformly mixed with ammonia water in a flue and then enters the flue gas denitration device, oxidation-reduction reaction denitration is carried out, the flue gas denitration device is connected with a low-temperature section of the flue gas waste heat boiler, and the flue gas is reintroduced into the heat exchange after denitration is completed; one path of the flue gas waste heat boiler is connected with the carbon dioxide capturing system through the draught fan and the flue gas desulfurization device, and the other path of the flue gas waste heat boiler leads the flue gas at the outlet of the waste heat boiler into the inlet of the waste heat boiler through the circulating fan.
Furthermore, the carbon dioxide capture system comprises a water washing desulfurization and denitrification device, the water washing desulfurization and denitrification device comprises a water washing desulfurization tower, filler is stored in the water washing desulfurization tower, the flue gas after desulfurization and denitrification of the glass kiln enters the tower from the lower part of the desulfurization water washing tower, the flue gas is cooled and dedusted at the bottom, the flue gas enters the middle part and is in countercurrent contact with desulfurization liquid flowing from top to bottom to avoid carbon and deacidify, sulfur dioxide and nitric oxide are absorbed by a solvent, the flue gas is purified after water washing and desulfurization and denitrification, the flue gas is cooled and divided by a raw material cooler and a gas-liquid separator and then is sent to an adsorption and desorption device through an induced draft fan, wherein the water washing desulfurization tower is connected with a first cooler and is used for cooling the water washing liquid to below 40 ℃ through heat exchange and then returning to the water washing desulfurization tower for cooling water washing work, and the NaOH desulfurization solution after absorbing sulfur dioxide and nitric oxide is prepared into a solution, neutralizing sulfate to NaNO3And Na2SO4And mother liquor separated by a salt-liquid separator after being cooled and crystallized by a desalting cooler is pumped back to the water washing desulfurizing tower for recycling.
Furthermore, the carbon dioxide capture system also comprises an adsorption and desorption device, wherein the adsorption and desorption device comprises a pressure swing adsorption device, and two ends of the pressure swing adsorption device are respectively connected with the water washing desulfurization and denitrification device and the carbon dioxide refining system. The adsorption and desorption device comprises at least 7 pressure swing adsorption devices, wherein fillers and adsorbents are stored in the pressure swing adsorption devices and are used for absorbing easily-adsorbed components in the purified flue gas, the difficultly-adsorbed components flow out from the top of the tower, are subjected to denitration and are then emptied, and the ventilation is stopped when the adsorption front edge of the easily-adsorbed components reaches the top of the tower.
Furthermore, the carbon dioxide refining system comprises a compression adsorption device, a freezing liquefaction device and a rectification and finished product storage device.
In another aspect of the invention, the method for capturing and purifying the carbon dioxide in the flue gas of the glass kiln comprises the following steps:
s1, pretreating the flue gas with carbon dioxide generated by the glass kiln, wherein the pretreatment comprises dust removal and desulfurization and denitrification treatment;
s2, washing the pretreated flue gas with water, and performing desulfurization and denitrification to obtain purified flue gas;
s3, preparing high-purity carbon dioxide gas by adopting a pressure swing adsorption process to desorb carbon dioxide from the purified flue gas;
s4, compressing, adsorbing, freezing, liquefying and rectifying the high-purity carbon dioxide gas to obtain the food-grade carbon dioxide.
Further, the step S1 includes the following steps:
s11, enabling the flue gas containing carbon dioxide generated by the glass kiln to enter a flue gas waste heat boiler;
s12, enabling the flue gas to enter a flue gas electric dust removal device for dust collection after passing through a high-temperature section of a waste heat boiler;
s13, fully and uniformly mixing the flue gas with ammonia water in the flue, and enabling the flue gas to enter a flue gas denitration device for carrying out oxidation-reduction reaction denitration;
s14, after denitration is completed, the flue gas is guided into the flue gas waste heat boiler again for heat exchange; after heat exchange, the carbon dioxide is introduced into the carbon dioxide capture system through the draught fan and the flue gas desulfurization device.
Further, the step S2 includes the following steps
S21, enabling the pretreated flue gas to enter a desulfurization water washing tower from the lower part of the tower, and cooling and dedusting the flue gas at the bottom by using water washing liquid which can be recycled by a cooler;
s22, enabling the flue gas subjected to temperature reduction and dust removal to enter the middle part of a desulfurization water washing tower, and carrying out carbon avoidance and deacidification by countercurrent contact with a desulfurization solution flowing from top to bottom to absorb sulfur dioxide and nitrogen oxide in the flue gas;
s23, cooling and water-separating the flue gas subjected to water washing, desulfurization and denitrification through a raw material cooler and a gas-liquid separator, and conveying the flue gas to an adsorption and desorption device through a draught fan;
s24, adding the desulfurization solution absorbing sulfur dioxide and nitrogen oxide into NaOH solution to neutralize sulfate into NaNO3And Na2SO4And mother liquor is separated out by a salt-liquid separator after being cooled and crystallized by a desalting cooler and is returned to the water washing desulfurizing tower by a pump for recycling.
Further, the step S3 includes the following steps:
s31, enabling the flue gas subjected to water washing, desulfurization and denitrification to enter a 7-seat pressure swing adsorption tower;
s32, each pressure swing adsorption device stores fillers and adsorbents, easily-adsorbed components in the gas are absorbed, difficultly-adsorbed components flow out from the top of the tower and are exhausted after denitration, when the adsorption front edge of the easily-adsorbed components reaches the top of the tower, ventilation is stopped, after 3 times of uniform reduction with other towers, carbon dioxide in the adsorption tower is primarily enriched, and then high-purity carbon dioxide gas in the adsorption tower is placed into a carbon dioxide buffer tank for use in a liquid carbon dioxide working section through a reverse arrangement step;
and S33, after the reverse discharge is finished, uniformly rising for 3 times through other towers, finally rising the pressure of the tail gas at the top, and then entering the next adsorption cycle again, wherein 2 adsorption towers are in the processes of feeding, adsorbing and producing the carbon dioxide gas at any moment, so that the feed gas feeding and the product gas production are continuously carried out.
Further, the step S4 includes the following steps:
s41, introducing the carbon dioxide product gas with the purity of 95.0% in the pressure swing adsorption tower into a compression adsorption device for further pressure adsorption, and leading out the product gas without impurities from the top;
s42, liquefying the product gas without impurities by a refrigeration liquefying device;
and S43, the carbon dioxide which is changed into liquid state enters a rectification and finished product storage device for rectification and then is stored, and the gas escaping from the tower top of the rectification tower is used as the regeneration gas of the compression adsorption device.
Advantageous effects of the invention
The device and the method for capturing and purifying the carbon dioxide in the glass kiln flue gas have the advantages that: the concentration of carbon dioxide discharged after combustion of the pure oxygen glass kiln is about 30-40%, the temperature of flue gas after combustion of the glass kiln is as high as 1200 ℃, and the temperature of a waste heat boiler is required to be controlled at 600-650 ℃, so that the flue gas is cooled by mixing air, CO2 in the flue gas is diluted by a large amount of N2, and the capture of the carbon dioxide is very difficult. For the carbon dioxide capture process, the content of carbon dioxide determines the capture process and capture efficiency, so that the method for cooling the original glass kiln by using cold air is changed, the flue gas of the glass kiln after desulfurization, denitrification, temperature reduction and dust removal is reintroduced into the waste heat power generation boiler by the circulating fan, and the purpose of cooling is realized by circulating the flue gas on the premise of not changing the content of CO 2.
The pure oxygen glass kiln can generate a large amount of flue gas with high CO2 content, wherein the flue gas contains 30-40% of carbon dioxide, 2-4% of nitrogen, 3-10% of oxygen, 50-60% of water and the balance of impurities such as carbon monoxide, nitrogen oxide, sulfur dioxide, dust and the like. The method comprises the steps of firstly, carrying out pretreatment of denitration, desulfurization, dust removal and temperature reduction on flue gas of the glass kiln through a flue gas pretreatment part, so that the flue gas index meets the requirements of a carbon capture process. Because the flue gas contains a small amount of acidic gases such as SO2, NOX, CO and the like, an alkali washing method is needed for deep removal, the flue gas after being treated by the flue gas pretreatment part is subjected to carbon-avoiding and deacidification pretreatment by a desulfurization water washing tower, the flue gas is cooled and dedusted, acidic impurities in the flue gas are removed, water vapor is removed, and then the concentration of carbon dioxide is concentrated to be more than 95% by a pressure swing adsorption device to form high-concentration carbon dioxide gas. And then 95% of carbon dioxide gas is conveyed to a carbon dioxide refining part, is introduced into a buffer tank through a fan, then enters a compressor for pressurization, enters a desulfurization bed after cooling water diversion and pressure stabilization, sulfide is adsorbed by a desulfurizing agent in the desulfurization bed under the action of pressure, the desulfurized gas enters an adsorption tower, an adsorbent in the adsorption tower adopts three combinations to remove impurities such as hydrocarbons, alcohols, aldehydes, ethers, moisture and the like, and the gas without the impurities is led out from the top of the adsorption bed and returns to an interstage outlet of the compressor. Then is cooled and liquefied by a freezing and liquefying device and enters a rectifying tower. The light components of nitrogen and oxygen are all removed from the tower top, and a high-purity carbon dioxide product with the purity of more than 99.9 percent is obtained at the tower bottom. The carbon dioxide product is stored and transported through the finished product storage tank, and the use requirement is met. After the operation, the flue gas basically does not contain carbon dioxide any more, the near zero emission of the carbon dioxide in the glass production line is realized, the emission of the original sulfur dioxide and nitrogen oxide is rapidly reduced, the emission of the sulfur dioxide is reduced to 5mg/Nm3, and the pollution to the environment is greatly reduced. Provides a new idea for the clean production of industrial enterprises and has good social benefit.
Drawings
FIG. 1 is a schematic structural diagram of a glass kiln flue gas carbon dioxide capture and purification device according to the present invention;
FIG. 2 is a schematic structural diagram of a pretreatment device for carbon dioxide flue gas in flue gas of a glass kiln, which is disclosed by the invention;
FIG. 3 is a schematic structural diagram of a glass kiln flue gas carbon dioxide water washing desulfurization device of the present invention;
FIG. 4 is a schematic structural diagram of a glass kiln flue gas carbon dioxide pressure swing adsorption device according to the present invention;
FIG. 5 is a schematic structural view of a carbon dioxide refining section of a glass kiln flue gas according to the present invention;
in the drawings are labeled: 1-flue gas pretreatment system, 2-carbon dioxide capture system, 3-carbon dioxide refining system, 4-glass kiln, 5-chimney, 6-washing desulfurization and denitrification device, 7-adsorption and desorption device, 8-surge tank, 9-compressor, 10-desulfurization bed, 11-adsorption bed, 12-liquefaction device, 13-refrigeration device, 14-rectifying tower, 15, finished product storage tank, 101-flue gas waste heat boiler, 102-flue gas dust removal device, 103-denitrification device, 104-induced draft fan, 105-desulfurization device, 106-circulating fan, 201-washing desulfurization tower, 202-first cooler, 203-second cooler, 204-raw material cooler, 205-gas-liquid separator, 206-NaOH solution, 207-desulfurization solution buffer tank, 208-desalting cooler and 209-salt liquid separating tank.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
As shown in fig. 1, the embodiment provides a flue gas pretreatment device for capturing and purifying carbon dioxide, which comprises a glass kiln, a flue gas waste heat boiler, a flue gas denitration device, a flue gas desulfurization device, a flue gas dust removal device and a flue gas recirculation device.
Referring to fig. 2, the flue gas at the outlet of the glass kiln is introduced into the flue gas waste heat boiler through a draught fan and a connecting pipeline. After the flue gas passes through the high-temperature section of the waste heat boiler, the flue gas enters a flue gas dust removal device for dust collection, after the dust collection, the flue gas is fully and uniformly mixed with ammonia water in a flue and then enters a flue gas denitration device, the flue gas denitration device is an SCR (selective catalytic reduction) reactor, and NO (nitric oxide) in the flue gasXAnd NH3And carrying out oxidation reduction reaction under the action of the catalyst to generate nitrogen and water, thereby completing the denitration process. Enters a desulphurization device after passing through a waste heat boiler to realize that the concentration of particulate matters at a flue gas outlet is less than 5mg/Nm3，SO2Concentration < 30mg/Nm3，NOXConcentration < 100mg/Nm3And the flue gas index requirement of the carbon dioxide capture system is met.
The original system adopts a cold air mixing cooling mode to realize that the temperature of high-temperature flue gas at the outlet of a furnace kiln is reduced to 650 ℃, the invention changes the mode of circulating flue gas to reduce the temperature to keep the concentration of carbon dioxide not reduced into a boiler flue gas circulating mode, and extracts the waste gas at the outlet of the waste heat boiler of 170 ℃ and mixes the waste gas into the flue gas at the outlet of the furnace kiln by replacing cold air through a circulating fan, thereby realizing that the temperature of the flue gas is reduced to 600 and 650 ℃ and the flue gas enters the waste heat boiler of the flue gas. In order to ensure the micro-positive pressure of the glass kiln, the flue gas access point needs to be behind the regulating gate valve of the glass kiln. The circulating air quantity is adjusted through an electric butterfly valve of the circulating fan.
The carbon dioxide trapping part comprises a water washing desulfurization and denitrification device and an adsorption desorption device.
Referring to fig. 3, the water washing desulfurization and denitration device comprises a water washing desulfurization tower, flue gas enters the tower from the lower part of the water washing tower under the action of an induced draft fan, the flue gas is rapidly cooled, meanwhile, trace dust carried in the gas is cleaned by a solvent, the temperature of the flue gas entering the desulfurization water washing tower is as high as 140 ℃, the temperature of the flue gas entering the desulfurization water washing tower can be rapidly raised, the temperature of the flue gas can be rapidly raised after entering the desulfurization water washing tower, the lower part of the water washing tower is connected with a first cooler, the temperature of the water washing liquid raised to about 80 ℃ is lowered to below 40 ℃ through heat exchange, the water washing liquid is returned to the desulfurization tower for cooling and water washing, then the flue gas enters the middle part and is in countercurrent contact with desulfurization liquid flowing from top to bottom to avoid carbon and deacidify, sulfur dioxide and nitrogen oxides are absorbed by the solvent, and the absorbed desulfurization solution is neutralized into NaNO through adding NaOH solution to obtain NaNO3And Na2SO4And the crystal is cooled and crystallized by a desalting cooler and then is separated from the system. The mother liquor separated by the salt-liquid separator is pumped back to the water washing desulfurizing tower for recycling. After water washing, desulfurization and denitrification, the flue gas is purified and cooled, and is sent to an adsorption and desorption device by a draught fan.
Referring to fig. 4, the adsorption and desorption device adopts a pressure swing adsorption natural desorption process, which is a 7-2-3-BD process, i.e., 7 adsorption towers in total, 2 adsorption towers being in an adsorption state, and 3 times of pressure equalization and reverse desorption processes. Above-mentioned flue gas gets into 2 adsorption towers that pressure swing adsorption device is in adsorption state, easily adsorb the component in the gas like carbon dioxide, water etc. is absorbed earlier, difficult adsorption component is like components such as nitrogen gas oxygen etc. and flows out evacuation after the denitration by the top of the tower, stop ventilating when the absorption forward position of easily adsorbing the component is about to arrive the top of the tower soon, carry out 3 after all descending with other towers, tentatively carry out the enrichment with the carbon dioxide in the adsorption tower, then put into carbon dioxide buffer tank through the negative step of putting high-purity carbon dioxide gas in the adsorption tower and supply carbon dioxide compression adsorption device to use. After the reverse discharge is finished, the tail gas enters the next adsorption cycle again after being subjected to 3 times of uniform rising and final rising of the top tail gas with other towers. The whole operation process is carried out at the temperature of the raw material gas entering the tower, and each adsorption tower enters the next cycle after the steps of adsorption, 3 times of pressure equalizing drop, reverse discharging, 3 times of pressure equalizing rise, final pressure rise and the like in sequence.
Table 1: process timing chart of adsorption tower in 7-2-3-BD flow
In the table: adsorption A, three-time average voltage drop (ED 1-ED 3), reverse discharge D, average voltage rise (ER 3-ER 1) and final voltage rise FR.
Adsorption A: and opening the program control valves V-A1 and V-A2, enabling the feed gas to enter the adsorption tower A, adsorbing easily-adsorbed components mainly comprising carbon dioxide on the surface of an adsorbent, absorbing easily-adsorbed components in the gas such as carbon dioxide, water and the like by the adsorbent, and allowing components not easily adsorbed such as nitrogen, oxygen and the like to flow out from the top of the adsorption tower A through the program control valve V-A2 as adsorption waste gas. And when the time of the adsorption step is over, closing the valves V-A1 and V-A2 to terminate the adsorption, and introducing the feed gas into another adsorption tower which finishes the final pressure boosting step, namely an adsorption tower B for adsorption.
Average pressure drop ED 1: opening the program control valves V-A4 and V-D4, carrying out pressure equalization on the adsorption tower A which finishes the adsorption step and the adsorption tower D which finishes the ER2 pressure equalization rise step, closing the V-A4 after the pressures of the two adsorption towers are basically equalized, and finishing the ED1 pressure equalization drop step of the adsorption tower A.
Average pressure drop ED 2: and continuously opening the program control valves V-A4 and V-E4, carrying out pressure equalization on the adsorption tower A which finishes the adsorption step and the adsorption tower E which finishes the ER3 pressure equalization rise step, closing the V-A4 and the V-E4 after the pressures of the two adsorption towers are basically equalized, and finishing the step of equalizing pressure drop ED2 of the adsorption tower A.
Average pressure drop ED 3: and (3) continuing to open the program control valves V-A4 and V-F4, carrying out pressure equalization on the adsorption tower A which finishes the adsorption step and the adsorption tower F which finishes the reverse release step D, and closing the V-A4 and the V-F4 after the pressures of the two adsorption towers are basically balanced to finish the step of equalizing pressure drop ED3 of the adsorption tower A.
Reverse amplification D: the programmable valve V-A3 was opened, and the gas in adsorption column A, which completed ED3 step, was vented from the bottom and the pressure was reduced. The reverse bleed gas was passed through valve V-A3 to a CO2 surge tank. When the pressure of the adsorption tower A is reduced to the normal pressure, the V-A3 is closed, and the reverse discharging step is completed.
Pressure-equalizing lift ER 1: after the reverse discharging step is finished, opening the program control valves V-A4 and V-C4, carrying out pressure equalization on the adsorption tower A and the adsorption tower C which finishes equal pressure drop of ED2, closing the valve V-C4 when the pressures of the two towers are basically equal, and finishing equal pressure rise ER1 of the adsorption tower A.
Pressure-equalizing lift ER 2: and after the step of increasing the ER1 by the uniform pressure is finished, opening the program control valves V-A4 and V-D4, equalizing the pressure of the adsorption tower A and the adsorption tower D which finishes the step of increasing the pressure of the ED1 by the uniform pressure, and closing the valve V-D4 when the pressure of the two towers is basically equal to each other to finish the step of increasing the ER2 by the uniform pressure of the adsorption tower A.
Pressure-equalizing lift ER 3: and after the step of increasing the ER2 by the uniform pressure is finished, opening the program control valves V-A4 and V-E4, equalizing the pressure of the adsorption tower A and the adsorption tower E which finishes the adsorption step, closing the valve V-E4 when the pressure of the two towers is basically equal, and finishing the step of increasing the ER3 by the uniform pressure of the adsorption tower A.
Final boost FR: after the pressure equalizing and raising step is completed, the program control valves V-A1 and V-A3 at the inlet and outlet ends of the adsorption tower at the final pressure raising (FR) step are opened with different opening degrees through a control program, so that the product gas and the feed gas can be simultaneously used for final pressure raising according to different proportional flow rates, and the pressure fluctuation of the product gas and the feed gas is reduced.
It can be seen from the process timing chart that in the process of pressure equalization and rise or pressure equalization of the adsorption towers, another group of adsorption towers are also in the process of pressure equalization, so the corresponding programmable valves should be opened, for example, when the adsorption tower A is in the process of pressure equalization and drop ED1, the programmable valves V-A4 and V-C4 are opened, and meanwhile, the adsorption tower E and the adsorption tower G are in the process of pressure equalization and rise ER3, so V-E5 and V-G5 are opened to satisfy the requirement that two groups of adsorption towers complete the pressure equalization operation at the same time.
And the carbon dioxide gas after desorption enters the carbon dioxide refining system, and the carbon dioxide refining system comprises a compression adsorption device, a freezing liquefaction device and a rectification and finished product storage device.
Referring to fig. 5, the compression adsorption device comprises a buffer tank, a compressor, two desulfurization beds and three adsorption beds, wherein the carbon dioxide feed gas with the purity of 95.0% from the pressure swing adsorption device firstly enters the buffer tank, and a temperature gauge and a pressure gauge are arranged on an inlet pipeline of the buffer tank to detect two process data. Then the gas enters a CO2 compressor, the carbon dioxide gas at the outlet of the second-stage compression after compression firstly enters a desulfurization bed, sulfide is absorbed by a desulfurizer in the bed under the action of pressure, the desulfurized gas enters an absorption tower, and the absorbent in the absorption tower adopts three combinations to remove impurities such as hydrocarbon, alcohol, aldehyde, ether, moisture and the like. The gas freed from impurities is withdrawn from the top of the adsorption bed and returned to the outlet between the compressor stages. In addition, the CO2 gasified in the process of conveying the rectifying tower to the product tank and the CO2 gas gasified by heat dissipation on the surface of equipment are mixed and then return to an interstage outlet of the compressor, so that the lost CO2 is effectively recovered, and the product yield is improved. The mixed gas enters a refrigeration liquefaction device after being compressed by the compressor in three stages.
The adsorption bed is provided with 3 adsorption towers, each tower sequentially passes through the continuous operation process of adsorption A, heating H and cold blowing C, adsorption and regeneration are circularly reciprocated and are continuously and stably (see table 2) by program control, compared with the double-tower process, the adsorption-heating-cold blowing process continuous operation of the adsorbent during working is less in adsorbent consumption, less in gas consumption for regeneration and high in equipment efficiency. The gas escaping from the top of the rectifying tower is used as the regeneration gas of the adsorbent, and no external regeneration gas pollutes the bed layer.
Table 2: operation state of adsorption tower in different periods
Adsorption A: and opening the program control valves V-X1 and V-X2, enabling the feed gas to enter the adsorption tower X, adsorbing impurities such as moisture on the surface of the adsorbent, and enabling the carbon dioxide to flow out from the top of the adsorption tower A through the program control valve V-X2. At the end of the adsorption step time, the valves V-X1 and V-X2 are closed to terminate the adsorption, and the raw material gas enters another adsorption tower Z which has completed the cold blowing step for adsorption.
Heating H: opening the program control valves V-X3 and V-X4, leading the regenerated gas heated by steam and the raw material gas flow to reversely pass through the adsorption tower, leading the adsorbed impurities to flow out of the adsorption tower along with the regenerated gas, and regenerating the adsorbent. At the end of the heating step time, valves V-X3 and V-X4 were closed.
And C, cold blowing: opening the program control valves V-X5 and V-X6, introducing the gas escaping from the top of the rectification into the adsorption tower X which finishes the heating step to finish the cold blowing step, and closing the valves V-X5 and V-X6. The adsorption-heating-cold blowing process was repeated.
The freezing liquefaction device comprises a refrigeration compressor, a condenser, a liquid storage device, a pressure regulating valve, a liquefaction device, a gas-liquid separator and a pipeline, wherein the refrigeration compressor is in a screw type or a piston type, and a refrigerant is liquid ammonia or Freon. The whole refrigeration liquefaction device is a circulation process, gaseous refrigerant enters a refrigeration compressor to be compressed, the compressor is connected with an evaporative condenser, the gaseous refrigerant is condensed into liquid refrigerant in the evaporative condenser, and the liquid refrigerant is stored in a liquid receiver.
The liquid refrigerant from the liquid reservoir is divided into four paths: one path of the gas is throttled and cooled by a regulating valve and then is led into a liquefying device, and the cooling capacity is transferred to the carbon dioxide gas in the heat exchanger tube array, so that the carbon dioxide gas is cooled and liquefied, and is sent to a rectifying tower together with the light component gas. The liquid refrigerant between the liquefier tubes is vaporized and enters the gas-liquid separator, and the gas refrigerant returns to the refrigeration compressor for recycling.
The second path of liquid refrigerant in the liquid reservoir enters the raw material cooler after being throttled and depressurized by the regulating valve, the raw material gas in the tube is cooled to about 10 ℃, most of water in the gas is liquefied under the condition, and the liquefied water is separated in the water diversion tank. The liquid refrigerant is vaporized and enters the gas-liquid separator, and the gas refrigerant is returned to the refrigeration compressor.
And the third path of liquid refrigerant in the liquid reservoir is throttled and cooled by an adjusting valve and then introduced into a desalting cooler for crystallizing and using by-products of desulfurization and denitrification. The liquid refrigerant between the liquefier tubes is vaporized and enters the gas-liquid separator, and the gas refrigerant is returned to the refrigeration compressor.
And the fourth path of liquid refrigerant in the liquid receiver is throttled and cooled by an adjusting valve and then is introduced into a shell of a full condenser at the top of the rectification tower to be used for condensing tower top fractions in the condenser, the shell liquid refrigerant is vaporized and enters a gas-liquid separator, and the gas refrigerant is also returned to the refrigeration compressor for recycling.
The outlet pressure of the refrigeration compressor is between 2.0 and 2.6MPa (g), the pressure after passing through the regulating valve is between 0.1 and 0.35MPa, and the temperature is between minus 40 ℃ and minus 5 ℃.
The rectification and finished product storage device comprises a rectification tower and a food-grade product storage tank. The carbon dioxide is frozen, cooled and liquefied by a CO2 liquefying device and then enters a rectifying tower, light components of nitrogen and oxygen are all removed from the top of the tower, a high-purity carbon dioxide product with the purity of more than 99.9 percent is obtained at the bottom of the tower and is sent to a food-grade CO2 finished product storage tank for filling bottles or filling tank cars.
All parts are connected through pipelines with different pipe diameters, pipes, valves and flowmeters are arranged on the pipelines, detection instruments such as pressure meters and thermometers are installed on the pipelines, detection instruments such as pressure meters, temperature meters and liquid levels and safety facilities such as safety valves and pressure reducing valves are also installed on the equipment, instrument parameters of key parts are uniformly controlled by a PLC or DCS system program, and the automatic control device has the functions of measuring, adjusting, recording, alarming and the like and is operated automatically.
The above description is only for the specific embodiments of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be within the technical scope of the present invention, and the technical solutions and novel concepts according to the present invention should be covered by the scope of the present invention.
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