CN101475836A - Hydrogenation adsorption desulphurization and catalytic hydro-dearomatization cascade reaction process - Google Patents
Hydrogenation adsorption desulphurization and catalytic hydro-dearomatization cascade reaction process Download PDFInfo
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- CN101475836A CN101475836A CN 200910073684 CN200910073684A CN101475836A CN 101475836 A CN101475836 A CN 101475836A CN 200910073684 CN200910073684 CN 200910073684 CN 200910073684 A CN200910073684 A CN 200910073684A CN 101475836 A CN101475836 A CN 101475836A
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- hydrogenation
- cascade reaction
- sulfide
- hydrogen
- catalyst
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 99
- 238000001179 sorption measurement Methods 0.000 title claims abstract description 25
- 238000010523 cascade reaction Methods 0.000 title claims abstract description 13
- 230000003197 catalytic effect Effects 0.000 title claims description 18
- 238000000034 method Methods 0.000 title abstract description 12
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims abstract description 44
- 239000003054 catalyst Substances 0.000 claims abstract description 35
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000002994 raw material Substances 0.000 claims abstract description 24
- 239000001257 hydrogen Substances 0.000 claims description 25
- 229910052739 hydrogen Inorganic materials 0.000 claims description 25
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 22
- 241001120493 Arene Species 0.000 claims description 17
- 239000003795 chemical substances by application Substances 0.000 claims description 17
- 230000000274 adsorptive effect Effects 0.000 claims description 16
- 238000005516 engineering process Methods 0.000 claims description 15
- 229910018879 Pt—Pd Inorganic materials 0.000 claims description 8
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 6
- 229910052759 nickel Inorganic materials 0.000 claims description 5
- 229910052763 palladium Inorganic materials 0.000 claims description 5
- 229910052697 platinum Inorganic materials 0.000 claims description 5
- 239000003208 petroleum Substances 0.000 claims description 4
- 239000002283 diesel fuel Substances 0.000 claims description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 abstract description 16
- 229910000037 hydrogen sulfide Inorganic materials 0.000 abstract description 16
- 238000006477 desulfuration reaction Methods 0.000 abstract description 4
- 230000023556 desulfurization Effects 0.000 abstract description 4
- 239000003921 oil Substances 0.000 description 22
- 238000006243 chemical reaction Methods 0.000 description 19
- 239000000047 product Substances 0.000 description 15
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 10
- 150000001336 alkenes Chemical class 0.000 description 8
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- 239000005864 Sulphur Substances 0.000 description 6
- 239000002904 solvent Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- 230000002779 inactivation Effects 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 229910003296 Ni-Mo Inorganic materials 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 125000003118 aryl group Chemical group 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 3
- 125000001741 organic sulfur group Chemical group 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 231100000614 poison Toxicity 0.000 description 2
- 230000007096 poisonous effect Effects 0.000 description 2
- 238000004904 shortening Methods 0.000 description 2
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000006254 arylation reaction Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000008157 edible vegetable oil Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000004073 vulcanization Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
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Abstract
The invention discloses a cascade reaction process for hydrogenation adsorption desulfurization and hydro-dearomatization. A hydrogenation adsorption catalyst and a hydro-dearomatization catalyst are directly and serially filled, and a raw material is removed with sulfide through the hydrogenation adsorption catalyst under the condition of hydrogenation adsorption, and then is removed with aromatic hydrocarbon through the hydro-dearomatization catalyst under the condition of hydro-dearomatization. The process has the advantages that no hydrogen sulfide is generated in a first reactor, and the content of the sulfide in a product is lower, thereby prolonging the using period of a second hydro-dearomatization catalyst, reducing operation cost, reducing equipment, and saving the investment.
Description
Technical field
The invention belongs to a kind of hydrogenation adsorption desulfurize and hydrogenation aromatics-removing cascade reaction technology.
Background technology
Extracting is used to edible oil 6 along with country
#The raising of solvent oil specification of quality, 6
#Aromaticity content index in the solvent oil is reduced to 0.1%, present industrial production 6 from 1%
#The solvent oil technology reaches this index certain difficulty.Produce 6
#The raw material of solvent oil generally is that aromatic hydrocarbons is raffinated oil, straight-run spirit or field condensate, the solvent that present industrial extracting aromatic hydrocarbons uses is the sulfide tetramethylene sulfone, contain a certain amount of organic sulfide during aromatic hydrocarbons is raffinated oil inevitably, also have organic sulfide to exist in straight-run spirit and the field condensate.Because the hydrogen of hydrogenation generally also contains the inorganic sulfur of 0.5ppm, these sulfide all are the poisonous substances that deep hydrogenation removes the arenes catalytic agent, there are these sulfide to exist the agent of hydrogenation and removing arenes catalytic can not keep stable aromatic hydrogenation activity, remove 6 by shortening
#Aromatic hydrocarbons in the solvent oil becomes a difficult problem.Traditional Hydrobon catalyst is such as Ni-Mo (W)/Al
2O
3, Co-Mo/Al
2O
3Be that organosulfur hydrogenation in the raw material is produced hydrogen sulfide, the product behind the hydrogenation is cooled to liquid and passes through stripper plant again the hydrogen sulfide stripping that produces.Also contain a large amount of gas vulcanization hydrogen in the hydrogen that recycles, also need to carry out adsorbing and removing hydrogen sulfide.And the hydrogen sulfide in the product might be further generates mercaptan with olefine reaction, and the product organic sulfur content behind the hydrogenation is difficult to be lower than 0.5ppm.Because these remove the existence of hydrogen sulfide device, desulphurization reactor can not directly be connected with taking off the aromatic hydrocarbons reactor, enter two sections remove the aromatic hydrocarbons reactor before raw material and hydrogen need reheat, wasted a large amount of energy.
Ni/ZnO is a good sulfide hydrogenation adsorptive catalyst, its catalysis absorption principle is, by the Ni on the catalyzer sulfide is carried out hydrogenation and destroy its structure, sulphur atom in the sulfide is transferred on the support of the catalyst ZnO, there is not hydrogen sulfide to generate so add the product of hydrogen adsorption through Ni/ZnO, sulphur content can be lower than 0.03ppm in the product, and the elementary sulfur loading capacity can reach more than 20% of catalyst body quality.Also just need not traditional Ni-Mo (W)/Al
2O
3, Co-Mo/Al
2O
3Remove the operation of hydrogen sulfide after the hydrogenating desulfurization.
Ni, Pt, Pd or Pt-Pd load on Al
2O
3Or SiO
2The hydrogenation and removing aromatic hydrocarbons activity of last catalyzer is very high, can make the aromaticity content in the raw material be lower than 0.1% by shortening under appropriate reaction conditions.If reaction raw materials contains 0.5ppm sulfide, above-mentioned catalyzer will reduce so that inactivation, and the speed of catalyst activity reduction or inactivation is relevant with the sulphur content in the raw material.The high inactivation of sulphur content is just fast, and the low inactivation of sulphur content is just slow.In a word, the sulphur content in the raw material is the main poisonous substance of Ni, Pt, Pd or the agent of Pt-Pd hydrogenation and removing arenes catalytic, and a certain amount of sulfide is arranged in the raw material, and above-mentioned catalyzer just can not keep aromatic hydrogenation activity steadily in the long term.In order to make the agent of hydrogenation and removing arenes catalytic that long life-span be arranged, must at first reduce the sulphur content in the raw material as far as possible and could realize this target.
Summary of the invention
The object of the invention provides a kind of hydrogenation adsorption desulfurize and hydrogenation aromatics-removing cascade reaction technology of hydrogenation and removing arenes catalytic agent long service life.
Technology of the present invention is to adopt hydrogenation adsorptive catalyst and the agent of the hydrogenation and removing arenes catalytic filling of directly connecting, raw material removes sulfide by the hydrogenation adsorptive catalyst earlier under the hydrogenation adsorption conditions after, agent removes aromatic hydrocarbons under hydrogenation and removing aromatic hydrocarbons condition through the hydrogenation and removing arenes catalytic again.
Petrol and diesel oil cuts such as aforesaid raw material can be petroleum naphtha, raffinate oil, field condensate.
Aforesaid hydrogenation adsorptive catalyst is Ni/ZnO.
The hydrogenation adsorption conditions of aforesaid hydrogenation adsorptive catalyst is: at 270-330 ℃, 1.3-2.5MPa, 1.0-3.5h
-1, hydrogen to oil volume ratio 200-600 reaction conditions under carry out hydrogenation adsorption desulfurize.
The agent of hydrogenation and removing arenes catalytic can be that Ni, Pt, Pd or Pt-Pd load on Al as mentioned above
2O
3Or SiO
2On catalyzer, concrete catalyzer comprises but is not limited to following catalyzer,
Pt/Al
2O
3" Bulletin of Chinese Academy of Sciences ", 1999, (04)
Ni/Al
2O
3Chinese invention patent 200410092428
Pd/Al
2O
3Chinese invention patent 97118845.9
Ni/SiO
2Catalyzer "
Petroleum journal (refining of petroleum)",
2005 02 phases)
Pt-Pd/Al
2O
3Hydrogenation catalyst "
Chemical science and technology market",
2006 06 phases
The hydrogenation and removing aromatic hydrocarbons condition of hydrogenation and removing arenes catalytic agent as mentioned above: 130-240 ℃, 1.3-2.5MPa, 1-4h
-1, hydrogen to oil volume ratio 200-600.
The present invention is a cascade reaction technology, and filling Ni/ZnO hydrogenation adsorptive catalyst in first reactor for the sulfide hydrocracking in the stock oil, and is adsorbed on elementary sulfur on the catalyst body.Because this process does not produce hydrogen sulfide, just do not need reaction product is cooled to liquid, do not need reaction product and Hydrogen Separation yet, the product of first reactor directly can be added the reaction of carrying out hydrogenation and removing aromatic hydrocarbons in second reactor.What load in second reactor is that Ni, Pt, Pd or Pt-Pd load on Al
2O
3Or SiO
2Aromatic hydrocarbon hydrogenation catalyst, these catalyzer all have very high hydrogenation and removing aromatic hydrocarbons ability, if but the ability that contains sulfide catalyst hydrogenation and removing aromatic hydrocarbons in the raw material is very fast forfeiture, it is closely related to we can say that these catalyst hydrogenations remove the activity and the sulfide content in the raw material of aromatic hydrocarbons.High more through the sulfide content in the catalyzer raw material, it is short more that catalyst hydrogenation removes the work-ing life of aromatic hydrocarbons.Ni/ZnO hydrogenation adsorptive catalyst can make that sulfide content is lower than 0.03ppm in the product, is more conducive to the agent of hydrogenation and removing arenes catalytic and keeps active for a long time.If use traditional Ni-Mo (W)/Al
2O
3, Co-Mo/Al
2O
3Hydrobon catalyst, sulfide in the raw material produces hydrogen sulfide through catalyst hydrogenation, product need be cooled to liquid and pass through gas-liquid separation again, and hydrogen and product will remove respectively to reheat behind the hydrogen sulfide and just can enter second reactor and carry out the reaction of hydrogenation and removing aromatic hydrocarbons.Because this process produces a large amount of hydrogen sulfide, hydrogen sulfide can generate mercaptan with the olefine reaction in the product, and the content of sulfide is difficult to be lower than 0.5ppm in this process liquid product.With use Ni/ZnO hydrogenation adsorptive catalyst to remove sulfide to compare, the sulfide that not only enters in the hydrogenation and removing aromatic hydrocarbons reactor has increased more than 10 times, but also has increased refrigerated separation equipment and hydrogen sulfide stripping equipment, operates also loaded down with trivial detailsly, has wasted the energy.
The advantage of method that the present invention narrates is not produce in first reactor hydrogen sulfide, and sulfide content is lower in the product, played the life cycle that has prolonged the agent of second hydrogenation and removing arenes catalytic, reduced running cost, guaranteed steadily carrying out of hydrogenation reaction, avoided the energy of waste because cooling is heated.And the equipment that reduces, saved investment.
Description of drawings
Fig. 1 is a process flow sheet of the present invention
Fig. 2 is traditional desulfurization, take off fragrant machinery process flow sheet.
As shown in the figure: the 1st, interchanger opening for feed, the 2nd, desulphurization reactor, the 3rd takes off aromatic hydrocarbons reactor, the 4th, hydrogen feed mouth, the 5th, material inlet, the 6th, outlet for product, the 7th, rectifying tower, the 8th, vapour liquid separator, the 9th, pump, the 10th, sulfide hydrogen hydrogen outlet, the 11st, arylation reaction device hydrogen inlet, the 13rd is taken off in isolated hydrogen sulfide outlet, the 12nd in the liquid phase, desulfurization reaction product heavy constituent outlet.
Embodiment
Embodiment 1:
It (mainly is C that raw material takes from that CONTINUOUS REFORMER raffinates oil as the by product of the aromatic extraction unit of raw material
6, C
7Hydrocarbon), olefin(e) centent 6.42%, total aromaticity content 2.12% (benzene 0.20%, toluene 0.81, dimethylbenzene 1.11%), organic sulfur content 5.0ppm (being equivalent to the 20ppm tetramethylene sulfone).Filling Ni/ZnO hydrogenation adsorptive catalyst in first reactor is at 270 ℃, 1.3MPa, 1.5h
-1, hydrogen to oil volume ratio 200 reaction conditions under carry out hydrogenation adsorption desulfurize.Second reactor charge Ni/Al
2O
3, reaction conditions is 130 ℃, 1.3MPa, 2h
-1, hydrogen to oil volume ratio 200.Hydrogenation postcure thing and alkene the results are shown in Table 1, and aromatic hydrocarbons the results are shown in Table 2.
Embodiment 2:
Raw material and filling method are with embodiment 1, and hydrogenation adsorptive catalyst reaction conditions is at 330 ℃, 2.5MPa, 3.5h
-1, hydrogen to oil volume ratio 600 carries out hydrogenation adsorption desulfurize.Second reactor charge Pt/Al
2O
3, reaction conditions is 220 ℃, 2.5MPa, 3.0h
-1, hydrogen to oil volume ratio 600.Hydrogenation postcure thing and alkene the results are shown in Table 1, and aromatic hydrocarbons the results are shown in Table 2.
Embodiment 3:
Raw material and filling method are with embodiment 1, and hydrogenation adsorptive catalyst reaction conditions is at 300 ℃, 2.0MPa, 2.5h
-1, hydrogen to oil volume ratio 400 carries out hydrogenation adsorption desulfurize.The agent of hydrogenation and removing arenes catalytic changes to Pd/Al
2O
3, reaction conditions is 240 ℃, 2.0MPa, 2.5h
-1, hydrogen to oil volume ratio 400.Hydrogenation postcure thing and alkene the results are shown in Table 1, and aromatic hydrocarbons the results are shown in Table 2.
Embodiment 4:
Raw material and filling method are with embodiment 1, and hydrogenation adsorptive catalyst reaction conditions is at 290 ℃, 1.5MPa, 1.5h
-1, hydrogen to oil volume ratio 300 carries out hydrogenation adsorption desulfurize.The agent of hydrogenation and removing arenes catalytic changes to Pt-Pd/Al
2O
3, reaction conditions is 230 ℃, 1.5MPa, 1.5h
-1, hydrogen to oil volume ratio 300.Hydrogenation postcure thing and alkene the results are shown in Table 1, and aromatic hydrocarbons the results are shown in Table 2.
Embodiment 5:
Raw material (mainly is C from field condensate
6, C
7Hydrocarbon), olefin(e) centent 0.42%, benzene 3.28%, organic sulfur content 50.6ppm, loading catalyst is with embodiment 1.Hydrogenation adsorptive catalyst reaction conditions is at 270 ℃, 1.8MPa, 1.0h
-1, hydrogen to oil volume ratio 200.Hydrogenation dearomatization catalyst changes Ni/SiO into
2, reaction conditions is 150 ℃, 1.8MPa, 1.0h
-1, hydrogen to oil volume ratio 200.Hydrogenation postcure thing and alkene the results are shown in Table 1, and aromatic hydrocarbons the results are shown in Table 2.
Product olefin(e) centent behind table 1 hydrogenation
* in this reaction process through after the reaction of hydrogenation adsorbing and removing sulfide, the sulfide content in the product has and is lower than 0.03ppm (lower bound of Instrument measuring), so sulfide content will not listed in table.
Product aromaticity content behind table 2 hydrogenation
Claims (7)
1, a kind of hydrogenation adsorption desulfurize and hydrogenation aromatics-removing cascade reaction technology, it is characterized in that hydrogenation adsorptive catalyst and the agent of the hydrogenation and removing arenes catalytic filling of directly connecting, raw material removes sulfide by the hydrogenation adsorptive catalyst earlier under the hydrogenation adsorption conditions after, agent removes aromatic hydrocarbons under hydrogenation and removing aromatic hydrocarbons condition through the hydrogenation and removing arenes catalytic again.
2, a kind of hydrogenation adsorption desulfurize as claimed in claim 1 and hydrogenation aromatics-removing cascade reaction technology, it is characterized in that described raw material be petroleum naphtha, raffinate oil, field condensate or petrol and diesel oil cut.
3, a kind of hydrogenation adsorption desulfurize as claimed in claim 1 and hydrogenation aromatics-removing cascade reaction technology is characterized in that described hydrogenation adsorptive catalyst is Ni/ZnO.
4, a kind of hydrogenation adsorption desulfurize as claimed in claim 1 and hydrogenation aromatics-removing cascade reaction technology is characterized in that described hydrogenation adsorption conditions is: at 270-330 ℃, 1.3-2.5MPa, 1.0-3.5h
-1, hydrogen to oil volume ratio 200-600.
5, a kind of hydrogenation adsorption desulfurize as claimed in claim 1 and hydrogenation aromatics-removing cascade reaction technology is characterized in that the agent of described hydrogenation and removing arenes catalytic is that Ni, Pt, Pd or Pt-Pd load on Al
2O
3Or SiO
2On catalyzer.
6, a kind of hydrogenation adsorption desulfurize as claimed in claim 5 and hydrogenation aromatics-removing cascade reaction technology is characterized in that the agent of described hydrogenation and removing arenes catalytic is Pt/Al
2O
3, Ni/Al
2O
3, Pd/Al
2O
3, Ni/SiO
2Or Pt-Pd/Al
2O
3
7, a kind of hydrogenation adsorption desulfurize as claimed in claim 1 and hydrogenation aromatics-removing cascade reaction technology is characterized in that described hydrogenation and removing aromatic hydrocarbons condition is 130-240 ℃, 1.3-2.5MPa, 1-4h
-1, hydrogen to oil volume ratio 200-600.
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|---|---|---|---|
| CN 200910073684 CN101475836B (en) | 2009-01-19 | 2009-01-19 | Hydrogenation adsorption desulphurization and catalytic hydro-dearomatization cascade reaction process |
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|---|---|---|---|
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| Publication Number | Publication Date |
|---|---|
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| CN101475836B CN101475836B (en) | 2012-12-26 |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101942330A (en) * | 2009-07-09 | 2011-01-12 | 中国石油化工股份有限公司抚顺石油化工研究院 | Method for deep hydrogenation, sulfur removal and aromatics removal of diesel oil |
| CN101475836B (en) * | 2009-01-19 | 2012-12-26 | 中国科学院山西煤炭化学研究所 | Hydrogenation adsorption desulphurization and catalytic hydro-dearomatization cascade reaction process |
| CN103059975A (en) * | 2011-10-18 | 2013-04-24 | 中国石油化工股份有限公司 | Hydrotreatment method for producing solvent naphtha in flexible mode |
| CN103102973A (en) * | 2011-11-14 | 2013-05-15 | 李清会 | Hydrogenated decomposition and separation system for intermediate composition oil of petroleum |
| CN104877077A (en) * | 2015-06-24 | 2015-09-02 | 大连理工大学 | Method for preparing hydrogenated C9 petroleum resin |
| CN105296001A (en) * | 2015-11-16 | 2016-02-03 | 西北大学 | System for preparing aromatic hydrocarbons through hydrogenation catalytic reforming of coal tar and method |
| CN107541248A (en) * | 2017-08-30 | 2018-01-05 | 中国石油化工股份有限公司 | A kind of environmentally-frierubber rubber filling oil and preparation method thereof |
| CN108504385A (en) * | 2018-03-30 | 2018-09-07 | 中海油天津化工研究设计院有限公司 | A method of cleaning diesel oil liquid phase circulation hydrogenation dearomatization |
| CN109395740A (en) * | 2017-08-18 | 2019-03-01 | 中国石油化工股份有限公司 | Polycyclic aromatic hydrocarbon selective hydrocatalyst |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101475836B (en) * | 2009-01-19 | 2012-12-26 | 中国科学院山西煤炭化学研究所 | Hydrogenation adsorption desulphurization and catalytic hydro-dearomatization cascade reaction process |
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2009
- 2009-01-19 CN CN 200910073684 patent/CN101475836B/en not_active Expired - Fee Related
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101475836B (en) * | 2009-01-19 | 2012-12-26 | 中国科学院山西煤炭化学研究所 | Hydrogenation adsorption desulphurization and catalytic hydro-dearomatization cascade reaction process |
| CN101942330A (en) * | 2009-07-09 | 2011-01-12 | 中国石油化工股份有限公司抚顺石油化工研究院 | Method for deep hydrogenation, sulfur removal and aromatics removal of diesel oil |
| CN101942330B (en) * | 2009-07-09 | 2013-06-19 | 中国石油化工股份有限公司 | Method for deep hydrogenation, sulfur removal and aromatics removal of diesel oil |
| CN103059975B (en) * | 2011-10-18 | 2015-11-25 | 中国石油化工股份有限公司 | A kind of hydroprocessing process of flexible production solvent oil |
| CN103059975A (en) * | 2011-10-18 | 2013-04-24 | 中国石油化工股份有限公司 | Hydrotreatment method for producing solvent naphtha in flexible mode |
| CN103102973A (en) * | 2011-11-14 | 2013-05-15 | 李清会 | Hydrogenated decomposition and separation system for intermediate composition oil of petroleum |
| CN104877077A (en) * | 2015-06-24 | 2015-09-02 | 大连理工大学 | Method for preparing hydrogenated C9 petroleum resin |
| CN104877077B (en) * | 2015-06-24 | 2018-02-16 | 大连理工大学 | A kind of method for preparing hydrogenation C9 Petropols |
| CN105296001A (en) * | 2015-11-16 | 2016-02-03 | 西北大学 | System for preparing aromatic hydrocarbons through hydrogenation catalytic reforming of coal tar and method |
| CN105296001B (en) * | 2015-11-16 | 2017-06-30 | 西北大学 | A kind of coal tar hydrogenating catalytic reforming prepares the system and method for aromatic hydrocarbons |
| CN109395740A (en) * | 2017-08-18 | 2019-03-01 | 中国石油化工股份有限公司 | Polycyclic aromatic hydrocarbon selective hydrocatalyst |
| CN109395740B (en) * | 2017-08-18 | 2021-10-01 | 中国石油化工股份有限公司 | Polycyclic aromatic hydrocarbon selective hydrogenation catalyst |
| CN107541248A (en) * | 2017-08-30 | 2018-01-05 | 中国石油化工股份有限公司 | A kind of environmentally-frierubber rubber filling oil and preparation method thereof |
| CN108504385A (en) * | 2018-03-30 | 2018-09-07 | 中海油天津化工研究设计院有限公司 | A method of cleaning diesel oil liquid phase circulation hydrogenation dearomatization |
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|---|---|
| CN101475836B (en) | 2012-12-26 |
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