CN117229819A - Method for deeply removing sulfide in fuel gas - Google Patents
Method for deeply removing sulfide in fuel gas Download PDFInfo
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- CN117229819A CN117229819A CN202210649468.8A CN202210649468A CN117229819A CN 117229819 A CN117229819 A CN 117229819A CN 202210649468 A CN202210649468 A CN 202210649468A CN 117229819 A CN117229819 A CN 117229819A
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- 239000002737 fuel gas Substances 0.000 title claims abstract description 61
- 238000000034 method Methods 0.000 title claims abstract description 39
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 title claims description 23
- 239000007789 gas Substances 0.000 claims abstract description 104
- -1 alcohol amine Chemical class 0.000 claims abstract description 44
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 41
- 230000003647 oxidation Effects 0.000 claims abstract description 40
- 239000002250 absorbent Substances 0.000 claims abstract description 33
- 230000002745 absorbent Effects 0.000 claims abstract description 33
- 239000002904 solvent Substances 0.000 claims abstract description 27
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 26
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 claims abstract description 26
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 26
- 239000003463 adsorbent Substances 0.000 claims abstract description 23
- QMMFVYPAHWMCMS-UHFFFAOYSA-N Dimethyl sulfide Chemical compound CSC QMMFVYPAHWMCMS-UHFFFAOYSA-N 0.000 claims abstract description 21
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical group [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 18
- JJWKPURADFRFRB-UHFFFAOYSA-N carbonyl sulfide Chemical compound O=C=S JJWKPURADFRFRB-UHFFFAOYSA-N 0.000 claims abstract description 16
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 claims abstract description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 15
- QGJOPFRUJISHPQ-UHFFFAOYSA-N Carbon disulfide Chemical compound S=C=S QGJOPFRUJISHPQ-UHFFFAOYSA-N 0.000 claims abstract description 12
- 150000003568 thioethers Chemical class 0.000 claims abstract description 11
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 claims abstract description 10
- XTHFKEDIFFGKHM-UHFFFAOYSA-N Dimethoxyethane Chemical compound COCCOC XTHFKEDIFFGKHM-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000002202 Polyethylene glycol Substances 0.000 claims abstract description 9
- 230000001590 oxidative effect Effects 0.000 claims abstract description 9
- 229920001223 polyethylene glycol Polymers 0.000 claims abstract description 9
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 9
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims abstract description 8
- 229910017053 inorganic salt Inorganic materials 0.000 claims abstract description 8
- 239000003960 organic solvent Substances 0.000 claims abstract description 8
- 239000007800 oxidant agent Substances 0.000 claims abstract description 8
- 239000005708 Sodium hypochlorite Substances 0.000 claims abstract description 7
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims abstract description 7
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 claims abstract description 5
- 229910000027 potassium carbonate Inorganic materials 0.000 claims abstract description 5
- STCOOQWBFONSKY-UHFFFAOYSA-N tributyl phosphate Chemical compound CCCCOP(=O)(OCCCC)OCCCC STCOOQWBFONSKY-UHFFFAOYSA-N 0.000 claims abstract description 5
- BZSXEZOLBIJVQK-UHFFFAOYSA-N 2-methylsulfonylbenzoic acid Chemical compound CS(=O)(=O)C1=CC=CC=C1C(O)=O BZSXEZOLBIJVQK-UHFFFAOYSA-N 0.000 claims abstract description 4
- VKJKEPKFPUWCAS-UHFFFAOYSA-M potassium chlorate Chemical compound [K+].[O-]Cl(=O)=O VKJKEPKFPUWCAS-UHFFFAOYSA-M 0.000 claims abstract description 4
- SATVIFGJTRRDQU-UHFFFAOYSA-N potassium hypochlorite Chemical compound [K+].Cl[O-] SATVIFGJTRRDQU-UHFFFAOYSA-N 0.000 claims abstract description 4
- 239000012286 potassium permanganate Substances 0.000 claims abstract description 3
- 238000001179 sorption measurement Methods 0.000 claims description 23
- 229910001220 stainless steel Inorganic materials 0.000 claims description 23
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 claims description 18
- KDSNLYIMUZNERS-UHFFFAOYSA-N 2-methylpropanamine Chemical compound CC(C)CN KDSNLYIMUZNERS-UHFFFAOYSA-N 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 239000002808 molecular sieve Substances 0.000 claims description 10
- 238000012856 packing Methods 0.000 claims description 10
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 10
- 239000007864 aqueous solution Substances 0.000 claims description 9
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 claims description 8
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 claims description 8
- LVTYICIALWPMFW-UHFFFAOYSA-N diisopropanolamine Chemical compound CC(O)CNCC(C)O LVTYICIALWPMFW-UHFFFAOYSA-N 0.000 claims description 8
- 150000001412 amines Chemical class 0.000 claims description 7
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims description 6
- 229940043276 diisopropanolamine Drugs 0.000 claims description 5
- AHXXIYFEJGGBMG-UHFFFAOYSA-N 1-[2-(tert-butylamino)ethoxy]ethanol Chemical compound CC(O)OCCNC(C)(C)C AHXXIYFEJGGBMG-UHFFFAOYSA-N 0.000 claims description 4
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 claims description 3
- 102100032373 Coiled-coil domain-containing protein 85B Human genes 0.000 claims description 3
- 101000868814 Homo sapiens Coiled-coil domain-containing protein 85B Proteins 0.000 claims description 3
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 claims description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 2
- 229910052573 porcelain Inorganic materials 0.000 claims description 2
- 239000010935 stainless steel Substances 0.000 claims description 2
- 150000003464 sulfur compounds Chemical class 0.000 claims 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 43
- 229910052717 sulfur Inorganic materials 0.000 description 43
- 239000011593 sulfur Substances 0.000 description 43
- 238000010521 absorption reaction Methods 0.000 description 32
- 239000000945 filler Substances 0.000 description 25
- 238000006477 desulfuration reaction Methods 0.000 description 17
- 230000023556 desulfurization Effects 0.000 description 17
- 239000007788 liquid Substances 0.000 description 15
- 230000008569 process Effects 0.000 description 14
- 238000010438 heat treatment Methods 0.000 description 12
- 239000002253 acid Substances 0.000 description 9
- 238000012546 transfer Methods 0.000 description 9
- 239000000919 ceramic Substances 0.000 description 8
- 230000000694 effects Effects 0.000 description 8
- 125000001741 organic sulfur group Chemical group 0.000 description 8
- 230000009471 action Effects 0.000 description 7
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 230000003197 catalytic effect Effects 0.000 description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 5
- 239000003546 flue gas Substances 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 3
- 230000003009 desulfurizing effect Effects 0.000 description 3
- 238000004090 dissolution Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- BDHFUVZGWQCTTF-UHFFFAOYSA-M sulfonate Chemical compound [O-]S(=O)=O BDHFUVZGWQCTTF-UHFFFAOYSA-M 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- CBTVGIZVANVGBH-UHFFFAOYSA-N aminomethyl propanol Chemical compound CC(C)(N)CO CBTVGIZVANVGBH-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 229940043237 diethanolamine Drugs 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- ZXEKIIBDNHEJCQ-UHFFFAOYSA-N isobutanol Chemical compound CC(C)CO ZXEKIIBDNHEJCQ-UHFFFAOYSA-N 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 230000016507 interphase Effects 0.000 description 1
- 229940035429 isobutyl alcohol Drugs 0.000 description 1
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- 239000000463 material Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052976 metal sulfide Inorganic materials 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 231100000956 nontoxicity Toxicity 0.000 description 1
- 230000005501 phase interface Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
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- 239000002002 slurry Substances 0.000 description 1
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- 238000004227 thermal cracking Methods 0.000 description 1
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- 239000002912 waste gas Substances 0.000 description 1
Landscapes
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a method for deeply removing sulfides in fuel gas, which comprises the following steps: (1) removing hydrogen sulfide gas by an organic alcohol amine absorbent; (2) The fuel gas after removing the hydrogen sulfide gas is contacted and reacted with an oxidation solvent to remove methyl mercaptan, methyl sulfide and residual hydrogen sulfide, wherein the oxidation solvent comprises 1 to 10 percent of organic alcohol amine, 0.5 to 20 percent of organic solvent, 2 to 38 percent of oxidant, 0.2 to 1 percent of inorganic salt and the balance of water, and the organic solvent is at least one of tributyl phosphate, dimethylformamide, N-methylpyrrolidone and polyethylene glycol dimethyl ether; the oxidant is at least one of sodium hypochlorite, sodium chlorate, potassium hypochlorite, potassium chlorate, hydrogen peroxide and potassium permanganate; the inorganic salt is sodium carbonate and/or potassium carbonate; (3) And (3) adsorbing the fuel gas from which the hydrogen sulfide, methyl mercaptan and dimethyl sulfide are removed by using an adsorbent to remove carbonyl sulfide and carbon disulfide.
Description
Technical Field
The invention belongs to the technical field of fuel desulfurization, and particularly relates to a method for deeply removing sulfides in fuel gas.
Background
Crude oil can produce a large amount of by-product gaseous hydrocarbon in the processes of atmospheric and vacuum distillation, catalytic cracking, catalytic reforming, hydrocracking, delayed coking and the like, and the by-product gaseous hydrocarbon is called as refinery gas, and the refinery gas is separated into C through gas separation 2 The hydrocarbons below are desulfurized with alcohol amine and mostly used as fuel gas for heating furnaces. The sulfur content of the fuel gas is generally 20-100 mg/m 3 Hydrogen sulfide is used as main sulfur-containing substance, and a small amount of organic sulfides such as methyl mercaptan, methyl sulfide, carbonyl sulfide and the like are contained.
When the fuel gas is burnt in the heating furnace, sulfide is oxidized to generate SO 2 ，SO 2 Some of them are further oxidized to form SO 3 ，SO 3 Generating sulfuric acid steam when meeting water vapor. When the temperature of the flue gas is reduced to sulfuric acidWhen the dew point is reached, sulfuric acid vapor is condensed on the metal surfaces of the heating furnace body and the heating furnace air preheater, and sulfuric acid dew point corrosion is formed. In order to avoid corrosion, the design value of the flue gas temperature of the heating grate is at least 15 ℃ above the acid dew point temperature of the flue gas, so that the flue gas temperature of the heating furnace in the current refinery is generally controlled to be 120-160 ℃, and the thermal efficiency of the heating furnace is 91-93%.
Currently, the fuel gas in use in a heating furnace is treated by alcohol amine (MDEA) desulfurization. The alcohol amine desulfurization adopts a conventional gravity absorption tower, an alcohol amine absorbent and sulfur-containing dry gas are in reverse contact in the tower to carry out mass transfer, sulfide (mainly hydrogen sulfide) is absorbed to form an absorption rich solution, and the desulfurized gas is discharged from the top of the tower and is used as fuel gas for a heating furnace. The absorption rich liquid is heated in a desorption tower to desorb acid gas through temperature rise, the acid gas enters a sulfur recovery device to produce sulfur products, and the absorption lean liquid is recycled to the absorption tower for reuse. The alcohol amine desulfurization mainly comprises the steps of absorbing and removing hydrogen sulfide gas, has high selectivity to the hydrogen sulfide gas and general absorption effect on mercaptan, thioether, carbonyl sulfide and other sulfur-containing compounds, and the sulfur content in the alcohol amine desulfurization treated gas is still 20-100 mg/m 3 The quality improvement and efficiency improvement requirements of the heating furnace cannot be met. The alcohol amine desulfurization adopts a conventional gravity absorption tower, so that the mass transfer efficiency is required to be further improved, the occupied area is large, the tower body is high, the auxiliary equipment requirements are high, the energy consumption is high, and the process flow and the operation are complex.
The supergravity technology is a novel chemical process strengthening technology developed in recent years, under the condition of supergravity field, liquid is sheared and torn into a micron-to-nanometer liquid film, liquid yarn and liquid drop under the action of a high-speed rotating packed bed, a huge interphase contact area is formed, and meanwhile, the updating rate of a phase interface is very high, so that the gas-liquid mass transfer efficiency can be greatly improved by 1-3 orders of magnitude, the occupied area of the device can be greatly reduced, and the production efficiency and the capacity of the device are improved. The occupied area of the supergravity device is greatly reduced, the tower height is greatly reduced, the liquid holdup is reduced, and the equipment investment and the operation cost can be reduced. The supergravity device has the characteristics of quick starting, simple operation, strong adaptability and the like, and has been well applied to the treatment of flue gas, tail gas and waste gas. The supergravity technology is applied to the deep desulfurization process of the fuel gas, and has good prospect.
CN 110982566A discloses a process for removing organic sulfur from natural gas, which adopts catalytic adsorption type organic sulfur desulfurizing agent to make catalytic hydrolysis or catalytic thermal cracking conversion of organic sulfur into hydrogen sulfide, then the hydrogen sulfide is reacted with active component in the catalytic adsorption type organic sulfur desulfurizing agent to produce metal sulfide, so that it can be removed. The catalytic adsorption reaction is carried out at high temperature, and the operations of heat exchange, pressurization and the like are needed, so that the process is complex. And the impact resistance and the long-period running activity of the catalyst are difficult to ensure.
CN 104548926A discloses an organic sulfur removal process, in which a gas containing carbonyl sulfur is treated with an organic sulfur hydrogenation catalyst in a hydrogen atmosphere to convert the carbonyl sulfur into hydrogen sulfide, and then the hydrogen sulfide is removed under the action of a desulfurizing agent, thereby realizing high-efficiency removal of sulfide. The catalytic hydrogenation reaction is carried out at high temperature and high pressure and is only aimed at removing carbonyl sulfide gas.
CN 207987130U discloses a associated gas desulfurization and sweetening system, which comprises an acid gas absorption tower, an oxidation reactor, a bag filter and an organic sulfur conversion tower. In the acid gas absorption tower, hydrogen sulfide in the gas is catalyzed and oxidized to generate sulfur simple substance, the gas with the hydrogen sulfide removed is heated by a gas-liquid separation tank and then enters an organic sulfur (mercaptan) non-hydrogenation catalytic conversion tower, and the mercaptan is converted into hydrogen sulfide and then returns to the acid gas absorption tower for treatment; the sulfur solution generated in the acid gas absorption tower enters an oxidation reactor to complete the recovery of the reaction activity of the catalyst (Fe 2+ Oxidized) and returned to the acid gas absorption tower, and filtering out the sulfur product in the sulfur slurry from the oxidation reactor in a bag filter. The process adopts a conventional absorption tower, so that the mass transfer efficiency is low; the organic mercaptan is converted under the high temperature and catalysis conditions, so that the energy consumption is high; and the process flow is complex, and the impact resistance and the long-period operation activity of the catalyst are difficult to ensure.
The mode of removing organic sulfide in gas in the prior art is to generate inorganic sulfur through catalytic reaction at high temperature and high pressure, and then treat the inorganic sulfur, so that the process is relatively complex, the impact resistance and activity of the catalyst are difficult to ensure, and the mass transfer effect of a conventional absorption tower is required to be improved.
Disclosure of Invention
The invention aims to provide a method for deeply removing sulfides in fuel gas.
In order to achieve the above object, the present invention provides a method for deeply removing sulfide in fuel gas, comprising the steps of:
(1) Removing hydrogen sulfide gas by using an organic alcohol amine absorbent;
(2) The fuel gas after removing the hydrogen sulfide gas is contacted and reacted with an oxidation solvent to remove methyl mercaptan, methyl sulfide and residual hydrogen sulfide, wherein the oxidation solvent comprises 1 to 10 percent of organic alcohol amine, 0.5 to 20 percent of organic solvent, 2 to 38 percent of oxidant, 0.2 to 1 percent of inorganic salt and the balance of water, and the organic solvent is at least one of tributyl phosphate, dimethylformamide, N-methylpyrrolidone and polyethylene glycol dimethyl ether; the oxidant is at least one selected from sodium hypochlorite, sodium chlorate, potassium hypochlorite, potassium chlorate, hydrogen peroxide and potassium permanganate; the inorganic salt is sodium carbonate and/or potassium carbonate;
(3) And (3) adsorbing the fuel gas from which the hydrogen sulfide, methyl mercaptan and dimethyl sulfide are removed by using an adsorbent to remove carbonyl sulfide and carbon disulfide.
According to the method for deeply removing sulfide in fuel gas, in the step (2), the polyethylene glycol dimethyl ether is polyethylene glycol dimethyl ether with a carbon chain length of 3-8.
The method for deeply removing sulfide in fuel gas comprises the following steps that in the step (1), an organic alcohol amine absorbent is an aqueous solution of N-methyldiethanolamine MDEA and sterically hindered amine, wherein the sterically hindered amine is at least one of isobutolamine AMP, tert-butylaminoethoxyethanol TBEE and 2- (tert-butylaminoethyl) diethyl ether, the mass ratio of the N-methyldiethanolamine MDEA to the sterically hindered amine is 1.15-2.5:1, and the mass fraction of the organic alcohol amine absorbent is 16-80%.
The method for deeply removing sulfide in fuel gas comprises the step (2), wherein the organic alcohol amine is at least one of N-methyldiethanolamine MDEA, isobutolamine AMP, monoethanolamine MEA, diethanolamine DEA and diisopropanolamine DIPA.
The invention relates to a method for deeply removing sulfide in fuel gas, wherein the adsorbent in the step (3) is Cu 2+ 、Zn 2+ 、Ag + Molecular sieve based fine desulfurization adsorbent which is an active component.
The method for deeply removing sulfide in fuel gas disclosed by the invention is carried out in a hypergravity reactor in both the step (1) and the step (2).
The method for deeply removing sulfide in fuel gas comprises the steps that rotating filler in a hypergravity reactor is regular stainless steel wire gauze filler or stainless steel corrugated plate filler, preferably regular stainless steel wire gauze filler, and the specific surface area of the filler is 900-1200 m 2 /m 3 Preferably 1000 to 1200m 2 /m 3 。
The method for deeply removing sulfide in fuel gas comprises the following reaction conditions of a hypergravity reactor in the step (1): the hypergravity factor is 20-150, the operating pressure is 0.1-0.8 MPa, the temperature is normal temperature, and the liquid-gas ratio is 2.0-50.0L/m 3 The residence time of the gas in the packing layer is 0.02-2.0 s.
The method for deeply removing sulfide in fuel gas comprises the following reaction conditions of a hypergravity reactor in the step (2): the hypergravity factor is 30-150, the operating pressure is 0.1-0.6 MPa, the temperature is normal temperature, and the liquid-gas ratio is 2.0-50.0L/m 3 The residence time of the gas in the packing layer is 0.05-2.0 s.
The method for deeply removing sulfide in fuel gas comprises the following steps of (3) carrying out in a fixed bed reactor, wherein the height of a bed layer is 100mm, two ends of the bed layer are filled with porcelain balls, the adsorption temperature is normal temperature, the pressure is 0.1-0.6 MPa, and the airspeed is 0.5-1.5 h -1 。
The invention has the beneficial effects that:
the organic solvent in the oxidation solvent promotes the mutual dissolution of other components, increases the dissolution of the organic sulfide component in the oxidation solvent, greatly improves the absorption and dissolution effects of the organic sulfide, and the oxidant can directly oxidize organic sulfide molecules (methyl mercaptan and methyl sulfide) with low concentration absorbed and dissolved in the oxidation solvent into stable sulfonate, so that the inorganic salt provides an alkaline environment, increases the internal disturbance of fluid, increases the mass transfer driving force and further improves the purification efficiency.
The organic alcohol amine absorbent and the oxidation solvent consist of organic alcohol amine, organic solvent, oxidant, inorganic salt and water, and have the advantages of wide sources, low price, no toxicity and harm, simple preparation and safe transportation and storage. Organic alcohol amine absorbent for acid gas H 2 High S selectivity, high absorption capacity and CO conversion 2 The co-absorption rate is low. The super-gravity absorption mass transfer efficiency is high, the occupied area of equipment is small, the consumption of the absorbent or the oxidation solvent is small, the process operation is simple, the energy consumption is low, and the impact resistance is high.
The process has simple flow and strong pertinency, thoroughly removes sulfide in the refinery fuel gas, and can reduce the total sulfur content in the refinery fuel gas to 1mg/m 3 The temperature of the exhaust gas of the heating furnace is reduced, the heat efficiency of the heating furnace is improved, and the liquid circulation quantity and the energy consumption are greatly reduced.
Drawings
FIG. 1 is a schematic diagram of a process flow for deeply removing sulfides in fuel gas according to the present invention.
Detailed Description
The present invention will be specifically described below by way of examples. It is noted herein that the following examples are given solely for the purpose of illustration and are not to be construed as limiting the scope of the invention, as many insubstantial modifications and variations of the invention will become apparent to those skilled in the art in light of the above disclosure.
As shown in figure 1, the process for deeply removing sulfide in fuel gas comprises the steps that the fuel gas firstly passes through a supergravity reactor to enable an organic alcohol amine absorbent to absorb and remove hydrogen sulfide gas. The fuel gas enters the outer cavity from the gas inlet 1 of the hypergravity reactor of the absorption unit, passes through the rotary packed bed to enter the inner cavity under the action of pressure, is discharged from the gas outlet pipe in the center, and is finally discharged from the gas outlet 1; the organic alcohol amine absorbent enters from the middle axial absorbent inlet of the hypergravity reactorThe liquid is uniformly distributed by a liquid distributor and then sprayed on a supergravity rotating packed bed layer, and flows outwards along the radial direction under the action of centrifugal force generated by high-speed rotation, falls down after hitting a static outer cavity wall, and is discharged to an absorbent storage tank from an absorbent outlet at the bottom. The absorbent is continuously recycled under the action of the pump. The fuel gas and the organic alcohol amine absorbent are reversely contacted in the super-gravity rotating filler bed layer to finish mass transfer, namely H in the fuel gas 2 S gas is absorbed into the absorbent to complete H in the fuel gas 2 S is purified and removed.
The absorbent rich liquid is removed from the absorbent regeneration device, the regenerated absorption lean liquid is returned to the absorbent storage tank for recycling, and the regenerated H is regenerated 2 S gas sulfur removal recovery unit, further recycle the sulfur resource. Fresh absorbent with a certain proportion is supplemented as required to ensure that the circulating absorbent has stable absorption capacity and absorption effect, and continuous long-period operation of the device is realized.
The fuel gas from which the hydrogen sulfide gas is removed is further subjected to oxidation reaction by a hypergravity reactor, so that a small amount of methyl mercaptan, dimethyl sulfide and other gases in the fuel gas are oxidized into sulfonate and the like to be removed, and a small amount of H which is not absorbed completely is ensured at the same time 2 The S gas is absorbed again and removed. Completion H from gas outlet 1 2 The fuel gas removed by the S gas enters the outer cavity of the hypergravity reactor from the gas inlet 2 of the hypergravity reactor of the oxidation unit, passes through the rotary filler to enter the inner cavity under the action of pressure, is discharged from a gas outlet pipe in the center, and is finally discharged from the gas outlet 2; the oxidation solvent enters from the middle axial oxidation solvent inlet of the hypergravity reactor, is uniformly distributed by the liquid distributor and then is sprayed on the hypergravity rotating packed bed layer, flows outwards along the radial direction under the centrifugal force generated by high-speed rotation, falls down after hitting the static outer cavity wall, and is discharged to the oxidation solvent storage tank from the oxidation solvent outlet at the bottom. The oxidation solvent is continuously recycled under the action of a pump. H is removed 2 The fuel gas of the S gas is reversely contacted with the oxidation solvent in the super-gravity rotating packing bed layer to finish the oxidation mass transfer, namely, a small amount of methyl mercaptan, dimethyl sulfide and other gases in the fuel gas are oxidized into sulfonate and the like to be removed.
The fresh agent with a certain proportion is supplemented to the oxidation solvent storage tank according to the requirement, so that the circulating oxidation solvent is ensured to have stable oxidation performance, and continuous long-period operation of the device is realized.
And the fuel gas from which the hydrogen sulfide, the methyl mercaptan and the methyl sulfide are removed is subjected to an adsorption unit, and residual organic sulfides such as carbonyl sulfide, carbon disulfide and the like are removed through an efficient adsorption material.
Example 1
Treating fuel gas of a certain refinery, wherein the total sulfur content of an air inlet is 20-30 mg/m 3 Adopting super-gravity absorption, wherein the filler of the super-gravity device is stainless steel wire mesh, and the specific surface area is 1200 square meters/m 3 The supergravity factor is 60, the operating pressure is 0.1MPa, the temperature is normal, and the liquid-gas ratio is 15L/m 3 The gas residence time is 0.72s, the absorbent is 30% organic alcohol amine aqueous solution, and the organic alcohol amine comprises N-methyldiethanolamine and isobutylamine with the mass ratio of 2:1. Adopting supergravity oxidation, wherein the filler of the supergravity device is stainless steel wire mesh, and the specific surface area is 1200 square meters/m 3 The supergravity factor is 40, the operating pressure is 0.1MPa, the temperature is normal, and the liquid-gas ratio is 20L/m 3 The gas residence time was 0.72s, the oxidation solvent included N-methyldiethanolamine 8%, polyethylene glycol dimethyl ether (average molecular weight 250, shanghai Yi En chemical technology Co., ltd.) 5%, sodium hypochlorite 6%, sodium carbonate 1%, and water the balance. And a fixed bed adsorption bed layer is adopted, the height of the bed layer is 100mm, and two ends of the bed layer are filled with ceramic balls with phi 3mm, wherein the diameter of the ceramic balls is about 10 mm. The adsorbent is Ag + The molecular sieve based fine desulfurization adsorbent as an active component has the adsorption temperature of normal temperature, the pressure of 0.1MPa and the space velocity of 0.6h -1 。
After the device runs stably, taking out a gas sample of the gas port according to the standard HJ 732-2014, and detecting the total sulfur content to be 1mg/m by a total sulfur analyzer 3 The following is given.
Example 2
Treating the fuel gas of a certain refinery, wherein the total sulfur content of an air inlet is 30-50/m 3 Adopting super-gravity absorption, wherein the filler of the super-gravity device is stainless steel wire mesh, and the specific surface area is 1200 square meters/m 3 The hypergravity factor is 80, the operating pressure is 0.1MPa,at normal temperature, the liquid-gas ratio is 15L/m 3 The gas residence time is 1.44s, the absorbent is an organic alcohol amine aqueous solution with the mass ratio of 50%, and the organic alcohol amine comprises N-methyldiethanolamine and tert-butylaminoethoxyethanol TBEE with the mass ratio of 1.5:1. Adopting supergravity oxidation, wherein the filler of the supergravity device is stainless steel wire mesh, and the specific surface area is 1200 square meters/m 3 The supergravity factor is 100, the operating pressure is 0.1MPa, the temperature is normal, and the liquid-gas ratio is 5L/m 3 The gas residence time is 1.44s, and the oxidation solvent comprises 6% of isobutylamine, 10% of tributyl phosphate, 30% of sodium hypochlorite, 0.2% of sodium carbonate and the balance of water. And a fixed bed adsorption bed layer is adopted, the height of the bed layer is 100mm, and two ends of the bed layer are filled with ceramic balls with the height of phi 3mm of about 10 mm. The adsorbent is Ag + The molecular sieve based fine desulfurization adsorbent as an active component has the adsorption temperature of normal temperature, the pressure of 0.1MPa and the airspeed of 1.0h -1 。
After the device runs stably, taking out a gas sample of the gas port according to the standard HJ 732-2014, and detecting the total sulfur content to be 1mg/m by a total sulfur analyzer 3 The following is given.
Example 3
Treating the fuel gas of a certain refinery, wherein the total sulfur content of an air inlet is 50-60/m 3 Adopting super-gravity absorption, wherein the filler of the super-gravity device is stainless steel wire mesh, and the specific surface area is 1200 square meters/m 3 The supergravity factor is 100, the operating pressure is 0.1MPa, the temperature is normal, and the liquid-gas ratio is 30L/m 3 The gas residence time is 0.36s, the absorbent is an aqueous solution of organic alcohol amine with the mass ratio of 32 percent, and the organic alcohol amine comprises N-methyldiethanolamine and 2- (tert-butylaminoethyl) ether with the mass ratio of 1.2:1. Adopting supergravity oxidation, wherein the filler of the supergravity device is stainless steel wire mesh, and the specific surface area is 1200 square meters/m 3 The supergravity factor is 80, the operating pressure is 0.1MPa, the temperature is normal, and the liquid-gas ratio is 30L/m 3 The gas residence time is 0.36s, and the oxidation solvent comprises 6% of isobutylamine, 2% of diethanolamine DEA, 10% of dimethylformamide, 20% of potassium hypochlorite, 0.2% of potassium carbonate and the balance of water. And a fixed bed adsorption bed layer is adopted, the height of the bed layer is 100mm, and two ends of the bed layer are filled with ceramic balls with the height of phi 3mm of about 10 mm. The adsorbent is Ag + As active ingredientThe molecular sieve based fine desulfurization adsorbent has the adsorption temperature of normal temperature, the pressure of 0.1MPa and the airspeed of 1.2h -1 。
After the device runs stably, taking out a gas sample of the gas port according to the standard HJ 732-2014, and detecting the total sulfur content to be 1mg/m by a total sulfur analyzer 3 The following is given.
Example 4
Treating the fuel gas of a certain refinery, wherein the total sulfur content of an air inlet is 60-80/m 3 Adopting super-gravity absorption, wherein the filler of the super-gravity device is stainless steel wire mesh, and the specific surface area is 1200 square meters/m 3 The supergravity factor is 120, the operating pressure is 0.5MPa, the temperature is normal, and the liquid-gas ratio is 40L/m 3 The gas residence time is 0.24s, the absorbent is an organic alcohol amine aqueous solution with the mass ratio of 50 percent, and the organic alcohol amine comprises N-methyldiethanolamine and 2- (tert-butylaminoethyl) ether with the mass ratio of 1.15:1. Adopting supergravity oxidation, wherein the filler of the supergravity device is stainless steel wire mesh, and the specific surface area is 1200 square meters/m 3 The supergravity factor is 120, the operating pressure is 0.5MPa, the temperature is normal, and the liquid-gas ratio is 40L/m 3 The gas residence time is 0.24s, the oxidation solvent comprises monoethanolamine 2%, diisopropanolamine DIPA2%, dimethylformamide 15%, potassium chlorate 10%, potassium carbonate 0.2% and water in balance. And a fixed bed adsorption bed layer is adopted, the height of the bed layer is 100mm, and two ends of the bed layer are filled with ceramic balls with the height of phi 3mm of about 10 mm. The adsorbent is Ag + The molecular sieve based fine desulfurization adsorbent as an active component has the adsorption temperature of normal temperature, the pressure of 0.5MPa and the airspeed of 1.2h -1 。
After the device runs stably, taking out a gas sample of the gas port according to the standard HJ 732-2014, and detecting the total sulfur content to be 1mg/m by a total sulfur analyzer 3 The following is given.
Example 5
Treating the fuel gas of a certain refinery, wherein the total sulfur content of an air inlet is 80-100/m 3 The super-gravity absorption is adopted, the filler of the super-gravity device is stainless steel wire mesh, and the specific surface area is 1000 square meters/m 3 The supergravity factor is 30, the operating pressure is 0.1MPa, the temperature is normal, and the liquid-gas ratio is 10L/m 3 The gas residence time is 1.44s, the mass ratio of the absorbent is60% aqueous solution of organic alcohol amine comprising N-methyldiethanolamine and isobutanol amine AMP in a mass ratio of 2.5:1. Adopting supergravity oxidation, wherein the filler of the supergravity device is stainless steel wire mesh, and the specific surface area is 1000 square meters/m 3 The supergravity factor is 100, the operating pressure is 0.1MPa, the temperature is normal, and the liquid-gas ratio is 40L/m 3 The gas residence time is 1.44s, and the oxidation solvent comprises isobutyl alcohol amine AMP 8%, diisopropanolamine DIPA2%, N-methylpyrrolidone 12%, sodium chlorate 10%, sodium carbonate 0.8% and water balance. And a fixed bed adsorption bed layer is adopted, the height of the bed layer is 100mm, and two ends of the bed layer are filled with ceramic balls with the height of phi 3mm of about 10 mm. The adsorbent is Cu 2+ The molecular sieve based fine desulfurization adsorbent as an active component has the adsorption temperature of normal temperature, the pressure of 0.1MPa and the airspeed of 1.0h -1 。
After the device runs stably, taking out a gas sample of the gas port according to the standard HJ 732-2014, and detecting the total sulfur content to be 1mg/m by a total sulfur analyzer 3 The following is given.
Example 6
Treating the fuel gas of a certain refinery, wherein the total sulfur content of an air inlet is 60-80/m 3 The super-gravity absorption is adopted, the filler of the super-gravity device is stainless steel wire mesh, and the specific surface area is 1000 square meters/m 3 The supergravity factor is 100, the operating pressure is 0.1MPa, the temperature is normal, and the liquid-gas ratio is 25L/m 3 The gas residence time is 0.72s, the absorbent is 26% organic alcohol amine water solution, and the organic alcohol amine comprises N-methyldiethanolamine and isobutanol amine AMP with the mass ratio of 1.5:1. Adopting supergravity oxidation, wherein the filler of the supergravity device is stainless steel wire mesh, and the specific surface area is 1000 square meters/m 3 The supergravity factor is 80, the operating pressure is 0.1MPa, the temperature is normal, and the liquid-gas ratio is 25L/m 3 The gas residence time is 0.72s, the oxidation solvent is 2% of N-methyldiethanolamine MDEA, 6% of diisopropanolamine DIPA, 12% of N-methylpyrrolidone, 30% of hydrogen peroxide, 0.8% of sodium carbonate and the balance of water. And a fixed bed adsorption bed layer is adopted, the height of the bed layer is 100mm, and two ends of the bed layer are filled with ceramic balls with the height of phi 3mm of about 10 mm. The adsorbent is Cu 2+ Molecular sieve based fine desulfurization adsorbent as active component and its adsorption process at normal temperatureTemperature, pressure 0.1MPa and airspeed 0.8h -1 。
After the device runs stably, taking out a gas sample of the gas port according to the standard HJ 732-2014, and detecting the total sulfur content to be 1mg/m by a total sulfur analyzer 3 The following is given.
Comparative example 1
Treating the fuel gas of a certain refinery, wherein the total sulfur content of an air inlet is 30-50/m 3 Absorbing by an absorption tower, wherein the filler of the absorption tower is stainless steel wire gauze, and the specific surface area is 800 square meters/m 3 Operating pressure 0.1MPa, temperature normal temperature and liquid-gas ratio 25L/m 3 The absorbent is an organic alcohol amine aqueous solution with the mass ratio of 50%, and the organic alcohol amine comprises N-methyldiethanolamine and tert-butylaminoethoxyethanol TBEE with the mass ratio of 1.5:1. Oxidizing with a filler tower, wherein the filler is stainless steel wire mesh, and the specific surface area is 800 square meters per meter 3 Operating pressure 0.1MPa, temperature normal temperature and liquid-gas ratio 25L/m 3 The oxidation solvent comprises 6% of isobutylamine, 10% of tributyl phosphate, 30% of sodium hypochlorite, 0.2% of sodium carbonate and the balance of water. And a fixed bed adsorption bed layer is adopted, the height of the bed layer is 100mm, and two ends of the bed layer are filled with ceramic balls with the height of phi 3mm of about 10 mm. The adsorbent is Ag + The molecular sieve based fine desulfurization adsorbent as an active component has the adsorption temperature of normal temperature, the pressure of 0.1MPa and the airspeed of 1.0h -1 。
After the device runs stably, taking out a gas sample of the gas port according to the standard HJ 732-2014, and detecting the total sulfur content of 12.62 mg/m by a total sulfur analyzer 3 。
Comparative example 2
Treating the fuel gas of a certain refinery, wherein the total sulfur content of an air inlet is 60-80/m 3 Adopting super-gravity absorption, wherein the filler of the super-gravity device is stainless steel wire mesh, and the specific surface area is 1200 square meters/m 3 The supergravity factor is 120, the operating pressure is 0.1MPa, the temperature is normal, and the liquid-gas ratio is 40L/m 3 The gas residence time is 0.24s, the absorbent is 68% organic alcohol amine water solution, and the organic alcohol amine comprises N-methyl diethanol amine and 2- (tert-butylaminoethyl) ether with the mass ratio of 1.15:1. The adsorbent is Ag + Molecular sieve based fine desulfurization adsorbent as active component and adsorption process is adsorption temperatureThe pressure is 0.5MPa and the airspeed is 1.2h at normal temperature -1 。
After the device runs stably, taking out a gas sample of the gas port according to the standard HJ 732-2014, and detecting the total sulfur content of 32.1 mg/m by a total sulfur analyzer 3 。
Comparative example 3
Treating fuel gas of a certain refinery, wherein the total sulfur content of an air inlet is 20-30 mg/m 3 Adopting super-gravity absorption, wherein the filler of the super-gravity device is stainless steel wire mesh, and the specific surface area is 1200 square meters/m 3 The supergravity factor is 40, the operating pressure is 0.1MPa, the temperature is normal, and the liquid-gas ratio is 15L/m 3 The gas residence time is 0.72s, the absorbent is 30% organic alcohol amine aqueous solution, and the organic alcohol amine comprises N-methyldiethanolamine and isobutylamine with the mass ratio of 2:1. Adopting supergravity oxidation, wherein the filler of the supergravity device is stainless steel wire mesh, and the specific surface area is 1200 square meters/m 3 The supergravity factor is 40, the operating pressure is 0.1MPa, the temperature is normal, and the liquid-gas ratio is 20L/m 3 The gas residence time is 0.72s, the oxidation solvent is 8% of N-methyldiethanolamine, 5% of polyethylene glycol dimethyl ether (average molecular weight is 250, shanghai Yi En chemical technology Co., ltd.), 12% of sodium hypochlorite, 1% of sodium carbonate and the balance of water.
After the device runs stably, taking out a gas sample of the gas port according to the standard HJ 732-2014, and detecting the total sulfur content of 4.86 mg/m by a total sulfur analyzer 3 。
Of course, the present invention is capable of other various embodiments and its several details are capable of modification and variation in light of the present invention by one skilled in the art without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (10)
1. A method for deeply removing sulfides in fuel gas, comprising the steps of:
(1) Removing hydrogen sulfide gas by using an organic alcohol amine absorbent;
(2) The fuel gas after removing the hydrogen sulfide gas is contacted and reacted with an oxidation solvent to remove methyl mercaptan, methyl sulfide and residual hydrogen sulfide, wherein the oxidation solvent comprises 1 to 10 percent of organic alcohol amine, 0.5 to 20 percent of organic solvent, 2 to 38 percent of oxidant, 0.2 to 1 percent of inorganic salt and the balance of water, and the organic solvent is at least one of tributyl phosphate, dimethylformamide, N-methylpyrrolidone and polyethylene glycol dimethyl ether; the oxidant is at least one selected from sodium hypochlorite, sodium chlorate, potassium hypochlorite, potassium chlorate, hydrogen peroxide and potassium permanganate; the inorganic salt is sodium carbonate and/or potassium carbonate;
(3) And (3) adsorbing the fuel gas from which the hydrogen sulfide, methyl mercaptan and dimethyl sulfide are removed by using an adsorbent to remove carbonyl sulfide and carbon disulfide.
2. The method for deeply removing sulfide from fuel gas according to claim 1, wherein the polyethylene glycol dimethyl ether in the step (2) is polyethylene glycol dimethyl ether with a carbon chain length of 3-8.
3. The method for deeply removing sulfides from fuel gas according to claim 1, wherein the organic alcohol amine absorbent in the step (1) is an aqueous solution of N-methyldiethanolamine MDEA and a sterically hindered amine, wherein the sterically hindered amine is at least one of isobutylamine AMP, tert-butylaminoethoxyethanol TBEE and 2- (tert-butylaminoethyl) diethyl ether, the mass ratio of N-methyldiethanolamine MDEA to the sterically hindered amine is 1.15-2.5:1, and the mass fraction of the organic alcohol amine absorbent is 16-80%.
4. The method for deep removal of sulfides in fuel gas according to claim 1, characterized in that the organic alcohol amine in step (2) is at least one of N-methyldiethanolamine MDEA, isobutolamine AMP, monoethanolamine MEA, diethanolamine DEA and diisopropanolamine DIPA.
5. The method for deep removal of sulfur compounds from fuel gas as claimed in claim 1, wherein said adsorbent in step (3) is Cu 2+ 、Zn 2+ 、Ag + Molecular sieve based fine removal as an active componentSulfur adsorbent.
6. The method for deep removal of sulfur compounds from a fuel gas as set forth in claim 1, wherein both step (1) and step (2) are carried out in a supergravity reactor.
7. The method for deeply removing sulfides from fuel gas according to claim 6, characterized in that the rotating packing in the supergravity reactor is structured stainless steel wire gauze packing or stainless steel corrugated plate packing, preferably structured stainless steel wire gauze packing, and the specific surface area of the packing is 900-1200 m 2 /m 3 Preferably 1000 to 1200m 2 /m 3 。
8. The method for deeply removing sulfur compounds from fuel gas according to claim 6, wherein the reaction conditions of the supergravity reactor in the step (1) are as follows: the hypergravity factor is 20-150, the operating pressure is 0.1-0.8 MPa, the temperature is normal temperature, and the liquid-gas ratio is 2.0-50.0L/m 3 The residence time of the gas in the packing layer is 0.02-2.0 s.
9. The method for deeply removing sulfur compounds from fuel gas according to claim 6, wherein the reaction conditions of the supergravity reactor in the step (2) are as follows: the hypergravity factor is 30-150, the operating pressure is 0.1-0.6 MPa, the temperature is normal temperature, and the liquid-gas ratio is 2.0-50.0L/m 3 The residence time of the gas in the packing layer is 0.05-2.0 s.
10. The method for deeply removing sulfide from fuel gas according to claim 1, wherein the step (3) is carried out in a fixed bed reactor, the height of the bed is 100mm, both ends of the bed are filled with porcelain balls, the adsorption temperature is normal temperature, the pressure is 0.1-0.6 MPa, and the space velocity is 0.5-1.5 h -1 。
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