CN108144318B - Associated gas desulfurization system - Google Patents
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- CN108144318B CN108144318B CN201810102979.1A CN201810102979A CN108144318B CN 108144318 B CN108144318 B CN 108144318B CN 201810102979 A CN201810102979 A CN 201810102979A CN 108144318 B CN108144318 B CN 108144318B
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 115
- 230000023556 desulfurization Effects 0.000 title claims abstract description 115
- 239000007791 liquid phase Substances 0.000 claims abstract description 55
- 239000012071 phase Substances 0.000 claims abstract description 54
- 239000000126 substance Substances 0.000 claims abstract description 45
- 238000000034 method Methods 0.000 claims abstract description 25
- 230000008569 process Effects 0.000 claims abstract description 22
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 21
- 238000005520 cutting process Methods 0.000 claims abstract description 11
- 238000009835 boiling Methods 0.000 claims abstract description 7
- 230000008929 regeneration Effects 0.000 claims description 27
- 238000011069 regeneration method Methods 0.000 claims description 27
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 claims description 23
- 150000001412 amines Chemical class 0.000 claims description 17
- 239000007788 liquid Substances 0.000 claims description 16
- 239000003795 chemical substances by application Substances 0.000 claims description 15
- 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 15
- 239000002808 molecular sieve Substances 0.000 claims description 14
- 239000003463 adsorbent Substances 0.000 claims description 12
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 claims description 12
- 238000010992 reflux Methods 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 10
- UNXNGGMLCSMSLH-UHFFFAOYSA-N dihydrogen phosphate;triethylazanium Chemical compound OP(O)(O)=O.CCN(CC)CC UNXNGGMLCSMSLH-UHFFFAOYSA-N 0.000 claims description 6
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- WQFWCVSIJHRSFG-UHFFFAOYSA-N 2-(2-hydroxyethylamino)ethanol 2-[2-hydroxyethyl(methyl)amino]ethanol Chemical compound N(CCO)CCO.CN(CCO)CCO WQFWCVSIJHRSFG-UHFFFAOYSA-N 0.000 claims 1
- 239000006096 absorbing agent Substances 0.000 claims 1
- 238000002791 soaking Methods 0.000 claims 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 29
- 229910052717 sulfur Inorganic materials 0.000 abstract description 29
- 239000011593 sulfur Substances 0.000 abstract description 29
- 238000009270 solid waste treatment Methods 0.000 abstract description 6
- 239000002699 waste material Substances 0.000 abstract description 4
- 238000002474 experimental method Methods 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 73
- 125000001741 organic sulfur group Chemical group 0.000 description 36
- 238000001179 sorption measurement Methods 0.000 description 31
- 229930195733 hydrocarbon Natural products 0.000 description 24
- 150000002430 hydrocarbons Chemical class 0.000 description 24
- 239000004215 Carbon black (E152) Substances 0.000 description 22
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 15
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 14
- DNJIEGIFACGWOD-UHFFFAOYSA-N ethanethiol Chemical compound CCS DNJIEGIFACGWOD-UHFFFAOYSA-N 0.000 description 14
- JJWKPURADFRFRB-UHFFFAOYSA-N carbonyl sulfide Chemical compound O=C=S JJWKPURADFRFRB-UHFFFAOYSA-N 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 230000000694 effects Effects 0.000 description 8
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 8
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 6
- YTPLMLYBLZKORZ-UHFFFAOYSA-N Thiophene Chemical compound C=1C=CSC=1 YTPLMLYBLZKORZ-UHFFFAOYSA-N 0.000 description 6
- WQAQPCDUOCURKW-UHFFFAOYSA-N butanethiol Chemical compound CCCCS WQAQPCDUOCURKW-UHFFFAOYSA-N 0.000 description 6
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 6
- 239000003921 oil Substances 0.000 description 6
- 239000002910 solid waste Substances 0.000 description 6
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 5
- 150000003568 thioethers Chemical class 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- 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 description 3
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 3
- 125000004432 carbon atom Chemical group C* 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000001282 iso-butane Substances 0.000 description 3
- 229920002521 macromolecule Polymers 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- KOWXKIHEBFTVRU-UHFFFAOYSA-N nga2 glycan Chemical compound CC.CC KOWXKIHEBFTVRU-UHFFFAOYSA-N 0.000 description 3
- 239000001294 propane Substances 0.000 description 3
- 229930192474 thiophene Natural products 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000006757 chemical reactions by type Methods 0.000 description 2
- XTVVROIMIGLXTD-UHFFFAOYSA-N copper(II) nitrate Chemical compound [Cu+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O XTVVROIMIGLXTD-UHFFFAOYSA-N 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 239000006260 foam Substances 0.000 description 2
- VLKZOEOYAKHREP-UHFFFAOYSA-N hexane Substances CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- JPVYNHNXODAKFH-UHFFFAOYSA-N Cu2+ Chemical compound [Cu+2] JPVYNHNXODAKFH-UHFFFAOYSA-N 0.000 description 1
- QMMFVYPAHWMCMS-UHFFFAOYSA-N Dimethyl sulfide Chemical compound CSC QMMFVYPAHWMCMS-UHFFFAOYSA-N 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical group O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 230000003213 activating effect Effects 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000012190 activator Substances 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000013329 compounding Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 229910001431 copper ion Inorganic materials 0.000 description 1
- 150000001924 cycloalkanes Chemical class 0.000 description 1
- 230000009615 deamination Effects 0.000 description 1
- 238000006481 deamination reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical class O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000008595 infiltration Effects 0.000 description 1
- 238000001764 infiltration Methods 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 230000033116 oxidation-reduction process Effects 0.000 description 1
- 238000002161 passivation Methods 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000011218 segmentation Effects 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- ZERULLAPCVRMCO-UHFFFAOYSA-N sulfure de di n-propyle Natural products CCCSCCC ZERULLAPCVRMCO-UHFFFAOYSA-N 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 239000011787 zinc oxide Substances 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
- B01D15/08—Selective adsorption, e.g. chromatography
-
- 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
- B01D53/38—Removing components of undefined structure
- B01D53/44—Organic components
-
- 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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
-
- 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
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a desulfurization system for associated gas, which comprises: the pretreatment system is used for cutting associated gas to be desulfurized into gas-phase substances to be desulfurized and liquid-phase substances to be desulfurized according to the boiling point; the gas-phase desulfurization system is used for desulfurizing the gas-phase substance to be desulfurized obtained after passing through the pretreatment system; and the liquid-phase desulfurization system is used for desulfurizing the liquid-phase substance to be desulfurized obtained after passing through the pretreatment system, wherein the pretreatment system comprises a pretreatment rectifying tower. The pretreatment rectifying tower is adopted to cut into gas phase and liquid phase, and a large amount of sulfur enters the gas phase desulfurization system through the gas phase, so that the treatment load of the liquid phase desulfurization system is small, and the solid waste treatment in the later stage is greatly reduced. Experiments prove that the associated gas desulfurization system reduces the solid waste treatment capacity to only 5-8% per year compared with the single liquid phase desulfurization process, thereby being more environment-friendly and having the lowest three-waste treatment cost.
Description
Technical Field
The invention relates to the technical field of associated gas treatment equipment, in particular to an associated gas desulfurization system.
Background
Associated gas generated in petroleum and natural gas exploitation processes and light hydrocarbon tail gas generated in petrochemical and coal chemical production processes often contain sulfur, the existence form of the sulfur in the gas comprises inorganic sulfur and organic sulfur, the inorganic sulfur is mainly sulfur and hydrogen sulfide, the organic sulfur is mainly mercaptan, thioether, thiophene and carbonyl sulfide with different molecular weights, the difficulty is brought to the comprehensive treatment of the associated gas, desulfurization becomes the primary task of the associated gas treatment, if the desulfurization is not carried out, pipeline corrosion easily occurs in the subsequent processing and using processes, and sulfur-containing tail gas generated by sulfur dioxide generated by combustion pollutes the environment.
At present, domestic associated gas desulfurization mainly comprises dry desulfurization and wet desulfurization:
the dry desulfurization process has simple flow and less equipment, but has more solid wastes, difficult treatment and serious equipment corrosion when the sulfur content is high, so the dry desulfurization process can only be used under the working condition of low sulfur content.
Wet desulfurization mainly includes amine desulfurization and redox desulfurization.
The phenomenon of reverse condensation appears easily in liquid phase amine method desulfurization system in heavy hydrocarbon, can lead to the desulfurization system of later stage to bubble frequently like this, and the oil yield is many, and heavy hydrocarbon is one of the products simultaneously, and the loss of heavy hydrocarbon can bring economic loss in the desulfurization process, and the operation later stage can lead to the incomplete phenomenon of desulfurization simultaneously.
The oxidation-reduction desulfurization has better effect on removing hydrogen sulfide, but the removal of organic sulfur, especially organic sulfur mixed by macromolecules and micromolecules, is difficult (the macromolecule organic sulfur mainly refers to thiophene, butyl mercaptan and organic sulfur with more than four carbon atoms, and the micromolecule organic sulfur mainly refers to organic sulfur with less than two carbon atoms such as methyl mercaptan, ethyl mercaptan and methyl sulfide).
In view of the above-mentioned drawbacks of the prior art desulfurization apparatus, the present inventors have actively studied and innovated based on the years of rich practical experience and expertise in designing and manufacturing such products, and in combination with the application of the theory, in order to create an associated gas desulfurization system, which is more practical. After continuous research and design and repeated sample test and improvement, the invention with practical value is finally created.
Disclosure of Invention
The main purpose of the invention is to overcome the defects of the prior desulfurization device and provide a associated gas desulfurization system, which adopts reasonable segmentation and separation of light hydrocarbon, inorganic sulfur and micromolecular organic sulfur from heavy hydrocarbon and macromolecular organic sulfur to be treated respectively after being separated in advance, and carries out targeted treatment according to the characteristics of the light hydrocarbon, the inorganic sulfur and the micromolecular organic sulfur, thereby being more suitable for practical use and having industrial utilization value.
The aim and the technical problems of the invention are realized by adopting the following technical proposal.
A associated gas desulfurization system comprising:
the pretreatment system is used for cutting associated gas to be desulfurized into gas-phase substances to be desulfurized and liquid-phase substances to be desulfurized according to the boiling point;
the gas-phase desulfurization system is used for desulfurizing the gas-phase substance to be desulfurized obtained after passing through the pretreatment system;
the liquid-phase desulfurization system is used for carrying out desulfurization treatment on the liquid-phase substances to be desulfurized obtained after passing through the pretreatment system;
wherein, the pretreatment system comprises a pretreatment rectifying tower.
As a preferable technical scheme, the absolute pressure in the pretreatment rectifying tower is 300-800KPa, and the tower top temperature is 20-40 ℃.
As a preferable technical scheme, the pretreatment system further comprises a gas-liquid separation reflux tank and a pretreatment rectifying tower top condenser, wherein the gas-liquid separation reflux tank is arranged at the top of the pretreatment rectifying tower and is used for collecting liquid phase substances condensed after the gas phase substances to be desulfurized pass through the pretreatment rectifying tower top condenser and realizing liquid phase total reflux.
As a preferable technical scheme, the pretreatment system further comprises a pretreatment rectifying tower bottom heat exchanger and a pretreatment rectifying tower bottom reboiler which are arranged at the bottom of the pretreatment rectifying tower and used for cooling the liquid-phase substances to be desulfurized output from the pretreatment rectifying tower, and the pretreatment rectifying tower bottom reboiler is responsible for providing heat sources for the rectifying tower.
As a preferable technical scheme, the gas-phase desulfurization system is an amine desulfurization system.
As a preferable technical scheme, the desulfurizing agent in the amine desulfurization system comprises the following components in percentage by mass:
as a preferable technical scheme, the dosage of the desulfurizing agent is as follows: the gas phase is to be desulphurized: the desulfurizing agent=500 to 1400Nm 3 /m 3 。
As a preferred technical scheme, the amine desulfurization system comprises an absorption tower and a regeneration tower, wherein the absolute regeneration pressure of the regeneration tower is 120-250KPa.
The temperature of the top of the regeneration tower is 35-55 ℃, and the temperature of the tower bottom is 105-123 ℃.
As a preferable technical scheme, the liquid-phase desulfurization system is a dry desulfurization system.
As a preferable technical scheme, the adsorption pressure of the dry desulfurization system is 800-1200KPa, the adsorption temperature is 15-45 ℃, and the optimal liquid phase airspeed in the adsorption process is 0.01-0.1m/s;
the adsorbent of the dry desulfurization system is a 13X molecular sieve, and the 13X molecular sieve is subjected to Si (OC 2H 5) 4 infiltration treatment.
By adopting the technical scheme, the following technical effects can be realized:
1) The existing associated gas adopts a single gas-phase desulfurization technology, so that heavy hydrocarbon loss is large, the system is easy to foam, excessive oil phenomenon occurs, the system cannot normally operate in the later period, and meanwhile, the existing associated gas amine desulfurization system is not added with triethylamine phosphate as an enhanced activator, so that the problems of incapability of deeply removing inorganic sulfur, large desulfurization equipment and large circulation amount are solved; the existing associated gas adopts a liquid phase desulfurization technology alone, and comprises direct reaction types and adsorption types, wherein the direct reaction types are iron oxide, zinc oxide and hydrogen sulfide, the generated solid waste is sent out for treatment at a high price at regular intervals, and macromolecule organic sulfur cannot be separated in the reaction process; the invention adopts a pretreatment rectifying tower to reasonably cut and pre-separate light hydrocarbon, inorganic sulfur, small molecular organic sulfur, heavy hydrocarbon and macromolecular organic sulfur, and then respectively treat the light hydrocarbon, the inorganic sulfur and the small molecular organic sulfur, and the pretreatment rectifying tower separates all the inorganic sulfur and the light organic sulfur from a tower top gas phase to a gas phase desulfurization system, so that the phenomenon of heavy hydrocarbon anti-condensation is eliminated in principle, the phenomenon of heavy hydrocarbon oil production is eliminated, and the problems of more oil and high heavy hydrocarbon content in the later stage are solved incompletely in a regeneration tower of the gas phase desulfurization system. The traditional liquid phase desulfurization system is adopted, so that more solid waste is generated and cannot be regenerated, and after the pretreatment rectifying tower is adopted for cutting, a large amount of sulfur enters the gas phase desulfurization system through the gas phase, so that the treatment load of the liquid phase desulfurization system is small, and the solid waste treatment in the later stage is greatly reduced. Experiments prove that the associated gas desulfurization system has the advantages that the solid waste treatment capacity is reduced to only 5-8% per year compared with that of a single liquid phase desulfurization process, so that the associated gas desulfurization system is more environment-friendly, and the three-waste treatment cost is lowest;
according to the invention, a pretreatment tower is adopted, after a large amount of hydrogen sulfide and small molecular organic sulfur are removed by 99% of the optimal amine liquid absorption formula, the residual macromolecular organic sulfur in the system is treated by adopting a modified adsorbent, the total sulfur removal rate of the whole associated gas device is more than or equal to 98%, the desulfurization effect is obvious, the device occupies small area, and the investment is small;
2) Removing a large amount of hydrogen sulfide in an amine desulfurization system, removing a small amount of macromolecular organic sulfur in a dry desulfurization system, completely solving the problems of original wastewater and waste solids, and recycling the liquid phase after adsorption through hot nitrogen regeneration;
3) The invention also discloses a desulfurizing agent, which can remove inorganic sulfur and organic sulfur (H2S, methyl mercaptan and carbonyl sulfur) at one time aiming at the characteristic of high content of inorganic sulfur and organic sulfur, and the total sulfur removal rate is more than 98%. Meanwhile, the method can remove carbon dioxide with a removal rate of more than 97%, is low in regeneration energy consumption, can recycle ammonia liquor, basically does not produce liquid waste, can recycle the ammonia liquor, and is convenient to operate.
4) The modified 13X molecular sieve is adopted for macromolecular organic sulfur (ethanethiol, butanethiol and thioether), so that the selectivity of the macromolecular organic sulfur is enhanced, and the removal efficiency is improved.
Drawings
FIG. 1 is a schematic diagram of a associated gas desulfurization system according to the present invention;
wherein, the device comprises a 1-pretreatment rectifying tower, a 2-pretreatment rectifying tower bottom heat exchanger, a 3-gas-liquid separation reflux tank, a 4-pretreatment rectifying tower top condenser, a 5-gas phase desulfurization system, a 6-liquid phase desulfurization system, 7-associated gas to be desulfurized and an 8-pretreatment rectifying tower bottom reboiler.
Detailed Description
In order to further describe the technical means and effects adopted by the invention to achieve the preset aim, the specific implementation, the characteristics and the effects of the associated gas desulfurization system provided by the invention are described in detail below.
As shown in fig. 1, the present invention discloses a desulfurization system for associated gas, comprising:
the pretreatment system is used for cutting associated gas 7 to be desulfurized into gas-phase substances to be desulfurized and liquid-phase substances to be desulfurized according to boiling points, and as shown in table 1, the associated gas comprises the following components with different boiling points:
TABLE 1 associated gas composition table
As shown in Table 1, the pretreatment system separates by cutting CH4S methyl mercaptan and I-C5 isopentane as demarcation points, because according to the experimental results, ethanethiol can also be treated in gas phase desulfurization, but after ethanethiol is cut, more than five heavy hydrocarbons enter the gas phase desulfurization treatment system for a while, which can cause a series of problems that the gas phase desulfurization system 5 foams seriously and heavy hydrocarbon loss is large, so that CH4S methyl mercaptan and I-C5 isopentane are used as demarcation points for cutting. The associated gas cut by the pretreatment system is divided into gas-phase substances to be desulfurized and liquid-phase substances to be desulfurized, and the gas-phase substances and the liquid-phase substances to be desulfurized respectively enter the gas-phase desulfurization system 5 and the liquid-phase desulfurization system 6 for desulfurization treatment.
The gas-phase desulfurization system 5 is used for desulfurizing the gas-phase substances to be desulfurized obtained after the pretreatment system;
the liquid-phase desulfurization system 6 is used for desulfurizing the liquid-phase to-be-desulfurized substances obtained after the pretreatment system;
the pretreatment system comprises a pretreatment rectifying tower 1, gas-liquid separation of gas-phase substances to be desulfurized is realized through the pretreatment rectifying tower 1, the gas-phase substances to be desulfurized enter a gas-phase desulfurization system 5 through an outlet at the top of the pretreatment rectifying tower 1, and the liquid-phase substances to be desulfurized flow into a liquid-phase desulfurization system 6 through an outlet at the bottom of the pretreatment rectifying tower 1 under the pressurization of a pump.
As a preferable technical scheme, the absolute pressure in the pretreatment rectifying tower 1 is 300-800KPa, the tower top temperature is 20-40 ℃, the tower kettle internal temperature is 95-100 ℃, preferably, the absolute pressure in the pretreatment rectifying tower 1 is 500-600KPa, the tower top temperature is 25-30 ℃, and the tower kettle internal temperature is 98-100 ℃. Under the pressure and temperature conditions, the pretreatment rectifying tower 1 separates inorganic sulfur and light organic sulfur from the top gas phase to the gas phase desulfurization system 5, so that the phenomenon of heavy hydrocarbon anti-condensation is eliminated in principle, the phenomenon of heavy hydrocarbon oil production is eliminated, and the problems of more oil in the later stage, high heavy hydrocarbon content, incomplete analysis in the regeneration tower of the gas phase desulfurization system 5 and the like are solved. The traditional liquid phase desulfurization system 6 alone is adopted, so that solid waste is more and cannot be regenerated, and after the pretreatment rectifying tower 1 is adopted for cutting, a large amount of sulfur enters the gas phase desulfurization system 5 through the gas phase, so that the treatment load of the liquid phase desulfurization system 6 is small, and the solid waste treatment in the later stage is also greatly reduced. Experiments prove that the associated gas desulfurization system reduces the solid waste treatment capacity to only 5-8% per year compared with the single liquid phase desulfurization process, thereby being more environment-friendly and having the lowest three-waste treatment cost.
As a preferable technical scheme, the pretreatment system further comprises a gas-liquid separation reflux tank 3 and a pretreatment rectifying tower top condenser 4, wherein the gas-liquid separation reflux tank 3 is arranged at the top of the pretreatment rectifying tower 1, and the gas-liquid separation reflux tank 3 is used for collecting liquid phase substances condensed after gas phase substances to be desulfurized pass through the pretreatment rectifying tower top condenser 4.
As a preferred technical scheme, the pretreatment system further comprises a pretreatment rectifying tower bottom heat exchanger 2 arranged at the bottom of the pretreatment rectifying tower 1 and used for cooling the high-temperature liquid phase to-be-desulfurized substance output from the pretreatment rectifying tower 1.
As a preferred technical scheme, the pretreatment system further comprises a reboiler 8 arranged at the bottom of the pretreatment rectifying tower 1 and responsible for providing heat source for the pretreatment rectifying tower 1.
As a preferable technical scheme, the gas-phase desulfurization system 5 is an amine desulfurization system, and specifically, the desulfurizing agent in the amine desulfurization system comprises the following components in percentage by mass:
30-40% of Methyldiethanolamine (MDEA)
Diethanolamine (DEA) 2-10%
Sulfolane 10-25%
Triethylamine phosphate 1-3%
The balance of water.
Preferably, the desulfurizing agent in the amine desulfurization system comprises the following components in percentage by mass:
the MDEA and DEA are used for removing inorganic sulfur, and triethylamine phosphate is added as an activating agent, so that the removal efficiency is improved, in the desulfurization process, hydrogen sulfide is in a gas phase, the desulfurization effect is poor if the hydrogen sulfide cannot enter a liquid phase, and after DEA is subjected to enhanced activation by compounding the triethylamine phosphate, the hydrogen sulfide can break through a gas film more easily to enter a liquid film to react with the amine liquid, and in addition, small-molecule organic sulfur can be effectively removed through sulfolane.
As a preferable technical scheme, the dosage of the desulfurizing agent is as follows: gas phase to-be-desulfurized substance: desulfurizing agent=500 to 1400Nm 3 /m 3 Preferably, the desulfurizing agent is used in the following amount: desulfurizing agent=800-900 Nm of gas phase to-be-desulfurized substance 3 /m 3 。
As a preferable technical scheme, the amine desulfurization system comprises an absorption tower and a regeneration tower, wherein the absolute regeneration pressure of the regeneration tower is 120-250KPa, the optimal absolute regeneration pressure is 130-150KPa, and the full regeneration analysis of inorganic sulfur and organic sulfur can be ensured under the pressure value.
The top temperature of the regeneration tower is 35-55 ℃, preferably 40-45 ℃, all condensate is refluxed at the temperature, noncondensable gas is hydrogen sulfide and small molecular organic sulfur which are discharged outside, and the temperature of the tower bottom is 105-123 ℃, preferably 108-115 ℃.
As a preferred embodiment, the liquid-phase desulfurization system 6 is a dry desulfurization system. Heavy hydrocarbons with less than five carbon atoms and macromolecular organic sulfur are removed by the pretreatment system through a dry adsorption desulfurization technology, and a large amount of hydrogen sulfide in associated gas is separated through gas phase, so that only a small amount of macromolecular organic sulfur is removed, the operation period of the dry desulfurization system is long, and the solid waste is less. The dry adsorption desulfurization adopts modified zeolite adsorption, because thiophene and more than five organic sulfur than other cyclic organic sulfur and carbon are difficult to remove in the process, and meanwhile, the organic sulfur is difficult to react with strong alkali.
The high pressure is favorable for adsorption, but the effect is not increased after the pressure exceeds a certain amount of data, and the adsorption pressure of the dry desulfurization system is preferably 800-1200KPa, and the adsorption temperature is preferably 15-45 ℃. The lower the adsorption temperature is in the adsorption process, the better the adsorption effect is, and the higher the temperature of the liquid phase to be desulfurized matters flowing out of the pretreatment rectifying tower 1 is, the higher the temperature is than the optimal adsorption temperature, so that the bottom of the pretreatment rectifying tower is provided with the heat exchanger 2 at the bottom of the tower, and the liquid phase to be desulfurized enters the adsorber after being cooled.
The adsorbent is used in the adsorption process in an amount of 5-15 wt% and the adsorption capacity is optimal in an amount of 8-10 wt%, i.e. the raw material contains 8g of organic sulfur, and more than 100g of adsorbent is needed to be prepared.
The optimal liquid space velocity in the adsorption process is 0.01-0.1m/s, preferably 0.01-0.03m/s (space velocity is the ratio of the liquid volume flow divided by the interfacial surface, and the area is the diameter area of the adsorber, regardless of the condition of filling the adsorbent). The nitrogen with the temperature of 200 ℃ is adopted for regeneration, the flow rate of the nitrogen in the regeneration process is controlled to be 6-8m/s, the regeneration pressure is 120-150KPa, after 3.5 hours of regeneration, the temperature of the adsorption system is reduced by adopting normal-temperature nitrogen, and the temperature is reduced for 0.5 hour to be switched to the next adsorption period.
Because the heavy hydrocarbon is various alkane, alkene, cycloalkane and other substances, all are hydrocarbon, the heavy hydrocarbon is a weak polar or nonpolar compound, all organic sulfur, whether oxygen-containing organic sulfur and oxygen-free organic sulfur, can lead to very strong polarity of the substances, in order to make the adsorption process selective, the invention creatively carries out modification and passivation on the basis of the traditional 13X molecular sieve, so that the adsorption capacity for sulfur and oxygen after modification is stronger, the adsorption capacity for nonpolar and weak polar substances is basically not realized, preferably, the adsorbent of the dry desulfurization system is the 13X molecular sieve, and the 13X molecular sieve is soaked in Si (OC 2H 5) 4 for 15 hours, specifically, the 13X molecular sieve is soaked in 8 percent Si (OC 2H 5) 4 for 15 hours, then is dried at 120 ℃, is soaked in 10 percent copper nitrate for 12 hours, is dried at normal temperature, and finally is baked at 450 ℃ for 2 hours, and the finished product is prepared. The method modifies the silicon dioxide groups in the molecular sieve and attaches copper ions, so that the adsorption efficiency of the molecular sieve is improved.
For further explanation of the present invention, the associated gas desulfurization system provided by the present invention is described in detail below with reference to specific examples, but should not be construed as limiting the scope of the present invention.
Example 1
Desulfurization treatment of associated gas to be desulfurized shown in Table 2 was performed by using the associated gas desulfurization system of the present invention, wherein the associated gas flow rate was 150Nm 3 And/h, pressure 580KPa:
table 2 example 1 associated gas composition table to be desulphurised
| Component (A) | Content (mass ratio) |
| Hydrogen sulfide | 0.0018 |
| Carbon dioxide | 0.0005 |
| Methane | 0.0921 |
| Ethane (ethane) | 0.0962 |
| Propane | 0.388 |
| Isobutane | 0.102 |
| N-butane | 0.211 |
| Isopentane | 0.045 |
| N-pentane | 0.028 |
| N-hexane | 0.035 |
| Methyl mercaptan | 0.0002 |
| Ethanethiol | 100ppm |
| Butanethiol | 37ppm |
| Thioether compounds | 160ppm |
| Carbonyl sulfide | 0.0001 |
Specifically, the operation pressure of the associated gas in the pretreatment rectifying tower 1 is 530KPa, the tower top temperature is 20 ℃, the liquid phase total reflux is carried out, the tower bottom temperature is 97.6 ℃, the gas phase to-be-desulfurized substances are obtained from the tower top of the pretreatment rectifying tower 1 and are shown in the table 3, and the liquid phase to-be-desulfurized substances are shown in the table 4:
TABLE 3 Table 1 composition of the gas phase to be desulfurized obtained by cutting and separating in the pretreatment rectifying column
| Component (A) | Content (mass ratio) |
| Hydrogen sulfide | 0.0020 |
| Carbon dioxide | 0.0006 |
| Methane | 0.1033 |
| Ethane (ethane) | 0.1079 |
| Propane | 0.435 |
| Isobutane | 0.1144 |
| N-butane | 0.2366 |
| Carbonyl sulfide | 0.0001 |
| Methyl mercaptan | 0.0002 |
After the gas-phase substance to be desulfurized passes through the pretreatment tower, the yield of the methyl mercaptan after the cutting of the components is 99.8 percent by weight, and the rest components are heavy hydrocarbon in the tower kettle liquid phase and macromolecular organic sulfur.
The gas phase to-be-desulfurized substances obtained at the top of the pretreatment rectifying tower 1 are shown in table 4:
table 4 example 1 composition table of liquid phase to be desulfurized obtained by cutting and separating in pretreatment rectifying column
| Component (A) | Content (mass ratio) |
| Isopentane | 0.4158 |
| N-pentane | 0.2587 |
| More than six carbon components | 0.3234 |
| Ethanethiol | 0.0009 |
| Butanethiol | 0.0003 |
| Thioether compounds | 0.0009 |
The liquid phase to-be-desulfurized substance obtained is adopted for 10 kg, the liquid phase to-be-desulfurized substance is cooled to 30 ℃ by adopting a heat exchanger and is pressurized to 900KPa by adopting a pump, the adsorbent dosage in the adsorption process is 300 g of modified 13X molecular sieve adsorbent according to the mass ratio of organic sulfur, the adsorption capacity is filled according to 10% by weight, the space velocity of the liquid phase in the adsorption process is 0.02m/s (the space velocity is the ratio of the volume flow of liquid divided by the interfacial meter, the area is the diameter area of the adsorber and the condition of filling the adsorbent is not considered), specifically, the adsorber is a 304-material stainless steel pipe with the diameter of 10mm, the bulk density of the modified molecular sieve is 0.6g/ml, and 500ml of adsorbent is stacked. The nitrogen with the temperature of 200 ℃ is adopted for regeneration, the flow rate of the nitrogen in the regeneration process is controlled to be 6m/s, the regeneration pressure is 150KPa, after 3.5 hours of regeneration, the nitrogen at normal temperature is adopted for cooling the adsorption system, and the cooling time is 0.5 hour, and then the next adsorption period is switched. In the adsorption process, the total sulfur outlet is 15ppm after adsorption, and the total sulfur removal rate is more than or equal to 98%.
The preparation steps of the modified 13X molecular sieve are as follows: 100g of 13X molecular sieve was separated in 8% Si (OC 2 H 5 ) 4 The mixture is immersed for 15 hours, reacted for 1-2 hours at the temperature of 51 ℃, then dried at the temperature of 120 ℃, immersed for 12 hours in 10% copper nitrate, reacted at normal temperature, dried at the temperature of 200 ℃ and finally roasted for 2 hours at the temperature of 450 ℃ to obtain the modified adsorbent finished product.
Example 2
Desulfurization treatment of associated gas to be desulfurized shown in Table 5 was carried out by using the associated gas desulfurization system of the present invention, wherein the associated gas flow rate was 100Nm 3 And/h, the pressure is 600KPa:
table 5 example 2 associated gas composition table to be desulphurised
| Component (A) | Content (mass ratio) |
| Hydrogen sulfide | 0.0022 |
| Carbon dioxide | 0.0003 |
| Methane | 0.0395 |
| Ethane (ethane) | 0.0681 |
| Propane | 0.4007 |
| Isobutane | 0.0984 |
| N-butane | 0.2424 |
| Isopentane | 0.0687 |
| N-pentane | 0.0654 |
| N-hexane | 0.0138 |
| Methyl mercaptan | 0.0002 |
| Ethanethiol | 120ppm |
| Butanethiol | 50ppm |
| Thioether compounds | 220ppm |
| Carbonyl sulfide | 0.0001 |
Specifically, the operation pressure of the associated gas in the pretreatment rectifying tower 1 is 550KPa, the tower top temperature is 21 ℃, the liquid phase is in total reflux, the tower bottom temperature is 96.5 ℃, the tower top gas phase is in total deamination desulfurization system, the absorption tower pressure is 520KPa, and the desulfurizing agent comprises: MDEA 35% (mass percent for all below); DEA 8%; sulfolane 25%; 1.5% of triethylamine phosphate and 30.5% of water; the circulating absorbent flow rate was 850Nm 3 Associated gas/m 3 The pressure of the amine liquid and the regeneration tower is 150KPa, the temperature of the top of the regeneration tower is 42 ℃, the temperature of the tower kettle is 121 ℃, and the liquid phase is totally refluxed. The components with boiling point more than or equal to methyl mercaptan are absorbedThe purified associated gas generated after the tower recovery treatment contains 2ppm of hydrogen sulfide and 11ppm of methyl mercaptan and does not contain other sulfur-containing components.
From the above examples 1 and 2, it is known that the pretreatment system is adopted to divide the associated gas to be desulfurized according to the boiling point, and then the gas phase and the liquid phase are desulfurized respectively, so that the sulfur-containing substances in the purified associated gas are greatly reduced, and the operation period of the dry desulfurization system and the produced solid waste are reduced.
The present invention is not limited to the above-mentioned embodiments, but is not limited to the above-mentioned embodiments, and any simple modification, equivalent changes and modification made to the above-mentioned embodiments according to the technical matters of the present invention can be made by those skilled in the art without departing from the scope of the present invention.
Claims (7)
1. A associated gas desulfurization system, comprising:
the pretreatment system is used for cutting associated gas (7) to be desulfurized into gas-phase substances to be desulfurized and liquid-phase substances to be desulfurized according to the boiling point;
a gas phase desulfurization system (5) for desulfurizing the gas phase to-be-desulfurized substance obtained after passing through the pretreatment system;
a liquid-phase desulfurization system (6) for desulfurizing the liquid-phase substance to be desulfurized obtained after passing through the pretreatment system;
wherein the pretreatment system comprises a pretreatment rectifying tower (1); the gas-phase desulfurization system (5) is an amine desulfurization system; the liquid-phase desulfurization system (6) is a dry desulfurization system; the pretreatment system separates according to the cut methyl mercaptan and isopentane as demarcation points;
the absolute pressure in the pretreatment rectifying tower (1) is 300-800KPa, and the tower top temperature is 20-40 ℃.
2. The associated gas desulfurization system according to claim 1, wherein the pretreatment system further comprises a gas-liquid separation reflux tank (3) and a pretreatment rectification tower top condenser (4) which are arranged at the top of the pretreatment rectification tower (1), and the gas-liquid separation reflux tank (3) is used for collecting liquid phase substances condensed after the gas phase substances to be desulfurized pass through the pretreatment rectification tower top condenser (4) and realizing liquid phase total reflux.
3. The associated gas desulfurization system according to claim 1, characterized in that the pretreatment system further comprises a pretreatment rectification column bottom heat exchanger (2) and a pretreatment rectification column bottom reboiler (8) arranged at the bottom of the pretreatment rectification column (1) for cooling the liquid phase to be desulfurized substance outputted from the pretreatment rectification column (1), the pretreatment rectification column bottom reboiler (8) being responsible for providing a heat source for the rectification column.
4. The associated gas desulfurization system of claim 1, wherein the desulfurizing agent in the amine desulfurization system comprises the following components in percentage by mass:
30-40% of methyl diethanolamine
Diethanolamine 2-10%
Sulfolane 10-25%
Triethylamine phosphate 1-3%
The balance of water.
5. The associated gas desulfurization system of claim 4, wherein the desulfurizing agent is used in an amount of: the desulfurizing agent is used for treating 500-1400 standard cubic meters of the gas-phase substances to be desulfurized.
6. The associated gas desulfurization system of claim 1, wherein the amine process desulfurization system comprises an absorber tower and a regeneration tower, wherein the regeneration tower has a regeneration absolute pressure of 120-250KPa.
7. The associated gas desulfurization system of claim 1, wherein the adsorbent of the dry desulfurization system is a 13X molecular sieve, and the 13X molecular sieve is subjected to Si (OC 2 H 5 ) 4 And (5) soaking treatment.
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Citations (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0446993A (en) * | 1990-06-15 | 1992-02-17 | Jgc Corp | Process for desulfurizing gas oil |
| CN101264413A (en) * | 2008-04-30 | 2008-09-17 | 王胜利 | Total sulfides removing solvent and preparation thereof |
| CN101343562A (en) * | 2007-07-09 | 2009-01-14 | 中国石油化工股份有限公司 | Hydrodesulphurization, olefin reduction method for gasoline |
| CN201280527Y (en) * | 2008-10-09 | 2009-07-29 | 山东齐旺达集团海仲化工科技有限公司 | Aromatic hydrocarbon production equipment |
| CN101829541A (en) * | 2010-06-08 | 2010-09-15 | 上海交通大学 | Mesoporous molecular sieve base nano metallic oxide and preparation method of desulfurizer thereof |
| CN102580470A (en) * | 2012-02-20 | 2012-07-18 | 西南石油大学 | Desulfurizing agent for purifying natural gas and petrochemical gas |
| CN103771347A (en) * | 2012-10-22 | 2014-05-07 | 中国石油化工股份有限公司 | Method for converting hydrogen sulfide into crystalline sulfur by using anhydrous solvent |
| CN104031708A (en) * | 2013-03-06 | 2014-09-10 | 中国石油天然气股份有限公司 | Ionic liquid formula solution for desulfurization of natural gas with high sulfur content |
| CN104789290A (en) * | 2015-03-25 | 2015-07-22 | 湖北华邦化学有限公司 | Method for deep desulfurization of liquefied petroleum gas |
| WO2016123859A1 (en) * | 2015-02-04 | 2016-08-11 | 中国石油大学(北京) | Desulfurization adsorbent for petrol and petrol desulfurization method |
| WO2016123860A1 (en) * | 2015-02-04 | 2016-08-11 | 中国石油大学(北京) | Gasoline deep desulfurization method |
| CN106731578A (en) * | 2017-01-05 | 2017-05-31 | 南京英斯派工程技术有限公司 | A kind of continuous desulfurization production system and its sulfur removal technology |
| CN106730967A (en) * | 2017-01-11 | 2017-05-31 | 河北美邦工程科技股份有限公司 | A kind of utilization top gaseous phase cut condenses the system and method for thermal rectification |
| CN207980460U (en) * | 2018-02-01 | 2018-10-19 | 南京英斯派工程技术有限公司 | A kind of associated gas desulphurization system |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2002040617A1 (en) * | 2000-11-17 | 2002-05-23 | Jgc Corporaton | Method of desulfurizing gas oil fraction, desulfurized gas oil, and desulfurizer for gas oil fraction |
| CN103495340B (en) * | 2013-10-15 | 2015-11-18 | 北京博源恒升高科技有限公司 | The method of SOx in compound alcamines solution removal gas |
-
2018
- 2018-02-01 CN CN201810102979.1A patent/CN108144318B/en active Active
Patent Citations (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0446993A (en) * | 1990-06-15 | 1992-02-17 | Jgc Corp | Process for desulfurizing gas oil |
| CN101343562A (en) * | 2007-07-09 | 2009-01-14 | 中国石油化工股份有限公司 | Hydrodesulphurization, olefin reduction method for gasoline |
| CN101264413A (en) * | 2008-04-30 | 2008-09-17 | 王胜利 | Total sulfides removing solvent and preparation thereof |
| CN201280527Y (en) * | 2008-10-09 | 2009-07-29 | 山东齐旺达集团海仲化工科技有限公司 | Aromatic hydrocarbon production equipment |
| CN101829541A (en) * | 2010-06-08 | 2010-09-15 | 上海交通大学 | Mesoporous molecular sieve base nano metallic oxide and preparation method of desulfurizer thereof |
| CN102580470A (en) * | 2012-02-20 | 2012-07-18 | 西南石油大学 | Desulfurizing agent for purifying natural gas and petrochemical gas |
| CN103771347A (en) * | 2012-10-22 | 2014-05-07 | 中国石油化工股份有限公司 | Method for converting hydrogen sulfide into crystalline sulfur by using anhydrous solvent |
| CN104031708A (en) * | 2013-03-06 | 2014-09-10 | 中国石油天然气股份有限公司 | Ionic liquid formula solution for desulfurization of natural gas with high sulfur content |
| WO2016123859A1 (en) * | 2015-02-04 | 2016-08-11 | 中国石油大学(北京) | Desulfurization adsorbent for petrol and petrol desulfurization method |
| WO2016123860A1 (en) * | 2015-02-04 | 2016-08-11 | 中国石油大学(北京) | Gasoline deep desulfurization method |
| CN104789290A (en) * | 2015-03-25 | 2015-07-22 | 湖北华邦化学有限公司 | Method for deep desulfurization of liquefied petroleum gas |
| CN106731578A (en) * | 2017-01-05 | 2017-05-31 | 南京英斯派工程技术有限公司 | A kind of continuous desulfurization production system and its sulfur removal technology |
| CN106730967A (en) * | 2017-01-11 | 2017-05-31 | 河北美邦工程科技股份有限公司 | A kind of utilization top gaseous phase cut condenses the system and method for thermal rectification |
| CN207980460U (en) * | 2018-02-01 | 2018-10-19 | 南京英斯派工程技术有限公司 | A kind of associated gas desulphurization system |
Non-Patent Citations (1)
| Title |
|---|
| 上海交通大学.《机电词典》.机械工业出版社,1991,第1224页. * |
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