CN103184071B - Gasoline desulfurization method - Google Patents
Gasoline desulfurization method Download PDFInfo
- Publication number
- CN103184071B CN103184071B CN201110446629.5A CN201110446629A CN103184071B CN 103184071 B CN103184071 B CN 103184071B CN 201110446629 A CN201110446629 A CN 201110446629A CN 103184071 B CN103184071 B CN 103184071B
- Authority
- CN
- China
- Prior art keywords
- gasoline
- components
- temperature
- enter
- tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000000034 method Methods 0.000 title claims abstract description 35
- 238000006477 desulfuration reaction Methods 0.000 title abstract description 14
- 230000023556 desulfurization Effects 0.000 title abstract description 11
- 230000003197 catalytic effect Effects 0.000 claims abstract description 36
- 238000004821 distillation Methods 0.000 claims abstract description 27
- 230000029936 alkylation Effects 0.000 claims abstract description 26
- 238000005804 alkylation reaction Methods 0.000 claims abstract description 26
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims abstract description 15
- 239000000203 mixture Substances 0.000 claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 5
- 238000006243 chemical reaction Methods 0.000 claims description 25
- 238000000926 separation method Methods 0.000 claims description 16
- 239000005864 Sulphur Substances 0.000 claims description 12
- 239000000470 constituent Substances 0.000 claims description 12
- 239000001257 hydrogen Substances 0.000 claims description 8
- 229910052739 hydrogen Inorganic materials 0.000 claims description 8
- 238000011049 filling Methods 0.000 claims description 7
- 239000002994 raw material Substances 0.000 claims description 5
- 238000003889 chemical engineering Methods 0.000 claims description 4
- 239000007795 chemical reaction product Substances 0.000 claims description 4
- 229910017464 nitrogen compound Inorganic materials 0.000 claims description 4
- 150000002830 nitrogen compounds Chemical class 0.000 claims description 4
- 239000003208 petroleum Substances 0.000 claims description 4
- 238000012827 research and development Methods 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 3
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 1
- 239000003054 catalyst Substances 0.000 abstract description 21
- 150000001336 alkenes Chemical class 0.000 abstract description 13
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 9
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 9
- 229910052717 sulfur Inorganic materials 0.000 abstract description 9
- 239000011593 sulfur Substances 0.000 abstract description 9
- YTPLMLYBLZKORZ-UHFFFAOYSA-N Thiophene Chemical compound C=1C=CSC=1 YTPLMLYBLZKORZ-UHFFFAOYSA-N 0.000 abstract description 8
- 238000002156 mixing Methods 0.000 abstract description 7
- 239000002283 diesel fuel Substances 0.000 abstract description 6
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 abstract description 5
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 4
- 238000005194 fractionation Methods 0.000 abstract description 4
- 229930192474 thiophene Natural products 0.000 abstract description 4
- 230000003009 desulfurizing effect Effects 0.000 abstract description 3
- 238000005406 washing Methods 0.000 abstract description 2
- JBGWMRAMUROVND-UHFFFAOYSA-N 1-sulfanylidenethiophene Chemical class S=S1C=CC=C1 JBGWMRAMUROVND-UHFFFAOYSA-N 0.000 abstract 2
- 150000004767 nitrides Chemical class 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 13
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 8
- 230000002152 alkylating effect Effects 0.000 description 8
- 238000000605 extraction Methods 0.000 description 8
- 238000009835 boiling Methods 0.000 description 7
- 239000000047 product Substances 0.000 description 6
- 239000002904 solvent Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 239000011347 resin Substances 0.000 description 5
- 229920005989 resin Polymers 0.000 description 5
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 239000002808 molecular sieve Substances 0.000 description 4
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 4
- 229910052814 silicon oxide Inorganic materials 0.000 description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- BDHFUVZGWQCTTF-UHFFFAOYSA-M sulfonate Chemical compound [O-]S(=O)=O BDHFUVZGWQCTTF-UHFFFAOYSA-M 0.000 description 4
- 238000004523 catalytic cracking Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 230000033228 biological regulation Effects 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 235000009508 confectionery Nutrition 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 150000001993 dienes Chemical class 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000004706 metal oxides Chemical class 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical class S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000003377 acid catalyst Substances 0.000 description 1
- -1 after reaction Substances 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000011973 solid acid Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 230000019086 sulfide ion homeostasis Effects 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a method for desulfurizing gasoline; mixing gasoline fraction containing a small amount of diesel oil components and hydrogen gas, and feeding the mixture into a pre-hydrogenation reactor; pre-hydrogenated products enter a fractionating tower for fractionation, light components from the top of the fractionating tower are directly used as low-sulfur gasoline blending components, heavy components from the bottom of the fractionating tower enter a water washing tower for removing alkaline nitrides, then enter a group of olefin thiophene alkylation reactors connected in series for increasing the weight of thiophene sulfides in heavy gasoline, gasoline components from the alkylation reactors enter a catalytic distillation tower, the weight of the rest thiophene sulfides is increased under the action of an olefin thiophene alkylation catalyst on the upper part of the catalytic distillation tower, and meanwhile, the gasoline is cut into light components and heavy components; the light component is directly used as a low-sulfur gasoline blending component, and the heavy component is a diesel oil component enriched with sulfide; the method of the invention can greatly reduce the sulfur content in the gasoline and simultaneously reduce the octane number loss brought by the desulfurization process.
Description
Technical field
The present invention relates to the method for the secondary processing of gasoline desulfurization such as a kind of method of gasoline desulfur, particularly catalytically cracked gasoline.
Background technology
In recent years, be protection of the environment, the composition of countries in the world to motor spirit proposes stricter restriction, to reduce the discharge of objectionable impurities.Beijing has carried out motor spirit Beijing provincial standard DB11/238-2007 on January 1st, 2008, and standard regulation vehicle gasoline and sulfur content in vehicle gasoline is not more than 0.005% (m/m), and olefin(e) centent is not more than 30%.Estimate that Beijing will implement state V standard in 2012, regulation vehicle gasoline and sulfur content in vehicle gasoline is not more than 0.001% (m/m), and olefin(e) centent is not more than 25%.In China's motor spirit, the ratio of catalytically cracked gasoline has accounted for more than 80%, is alkene and sulfide main source in gasoline.Therefore, the sulphur content how reducing catalytic gasoline improves the key of China's motor spirit quality.
CN201010616414.9 relates to a kind of catalytic gasoline alkylation desulfuration and device, catalytically cracked gasoline is introduced alkylated reaction tower with volume space velocity 0.5 ~ 6.0h-1 during liquid by the method under pressure 0.2 ~ 1.0MPa after heat exchange is warming up to 50 ~ 110 DEG C, alkylated reaction is carried out under the effect of alkylating and desulfurizing catalyst, after reaction, gasoline alkylate is introduced separation column, be cut into the lighting end (alkylating desulfurization gasoline) of low-sulfur at 175 ~ 185 DEG C of places and be rich in the last running of sulphur, fractionator overhead extraction alkylating desulfurization gasoline, tower reactor extraction last running.Method provided by the invention keeps gasoline octane rating substantially constant while removing the sulfide in gasoline, flow process is simple, plant construction investment is little, process cost is low, operational condition relaxes, sweetening effectiveness is good, and process is easy to control, and the sulphur content of alkylating desulfurization gasoline meets " motor spirit " national standard.
CN101225327A relates to a kind of hydrocarbon recombinant alkylating desulfurization method of catalytically cracked gasoline.The method adopts the pretreater comprising catalytic cracking catalytic gasoline, primary fractionator, single cut alkylation reactor, the device of the composition of separation column again of two cut alkylation reactor and mixture, implement the desulfurization of catalytically cracked gasoline, it is characterized in that comprising following process: with primary fractionator, catalytically cracked gasoline is divided into three fraction section, then the mixture that intermediate boiling fraction adds high boiling fraction with low boiler cut is added two alkylation reactors respectively, alkylated reaction is carried out under the effect of acid catalyst, distill mixing with a certain amount of diesel oil and add separation column again after the mixing of the product of two reactors again, fractionator overhead extraction sweet gasoline again, tower reactor extraction sulfur-containing diesel.
CN200610002377.6 relates to a kind of gasoline alkylation desulfuration method, the method comprises: introduced by the stock oil after preheating in reactor, temperature be 60 ~ 180 DEG C, pressure be 0.1 ~ 2.0MPa, liquid time volume space velocity be the condition of 0.5 ~ 10h-1 under react with catalyst exposure, after reaction, logistics is introduced in separation column, is cut into lighting end product and the last running being enriched sulphur at 100 ~ 200 DEG C of places; When the catalyzer in reactor needs regeneration, switched to by stock oil regenerated solvent or gas to regenerate catalyzer, solvent or gas recovery, recycling after regenerating, after catalyst regeneration, switch to stock oil to proceed reaction.Method flow provided by the invention is simple, operational condition relaxes, desulfuration efficiency is high, loss of octane number is little, and before and after reaction, the hydrocarbon composition of gasoline does not have considerable change, and the side reaction such as olefinic polymerization, alkylating aromatic hydrocarbon is suppressed.
CN200810114387.8 relates to a kind of catalytic distillation method of alkylation desulfurization of gasoline, sour gasoline is added catalytic distillation tower, under the effect of solid acid catalyst, alkene in gasoline and sulfide generation alkylated reaction, generate more high boiling sulfocompound, diesel oil or high boiling point hydrocarbon ils and gasoline are carried out fractionation jointly in a distillation column, and transferred to diesel oil or high boiling hydrocarbon ils from gasoline by high boiling sulfocompound by fractionation, sweet gasoline is from overhead extraction; The working pressure of catalytic distillation tower is 0.1MPa ~ 0.5MPa, reaction zone temperature is 80 DEG C ~ 200 DEG C, and liquid air speed is 0.1h-1 ~ 20h-1, decreases gasoline hydrodesulfurizationmethod device, sulfide in effective elimination gasoline and do not lose octane value, reaches the dual purpose of desulfurization and Olefin decrease; Reaction and separation processes promotes mutually, and can conserve energy, and construction investment is little, and operational condition is gentle, and process is easy to control.
CN200820109556.4 relates to a kind of gasoline alkylation desulfurizing device, and catalytic distillation tower is divided into conversion zone, rectifying section and stripping section; Conversion zone loading catalyst; Rectifying section and the helical packing of stripping section filling stainless steel triangle; Azochlorosulfonate acid resin catalyst is filled out in pre-reactor; FCC gasoline raw material pre-reactor connects, and pre-reactor connects in the middle part of the conversion zone of catalytic distillation tower, and C3 ~ C5 alkene is connected to the conversion zone bottom of catalytic distillation tower; Vapour outlet is connected by complete condenser, and low-sulphur oil extraction mouth is connected with low-sulphur oil extraction mouth connecting tube, and complete condenser is connected with low-sulphur oil extraction mouth connecting tube; The outlet of high-sulfur distillate flow is connected with high-sulfur cut outflow conduit; Regenerated solvent inlet duct is connected with pre-reactor regenerated solvent entrance, and regenerated solvent outlet conduit exports with pre-reactor regenerated solvent and is connected; Suppress aromatic hydrocarbons and alkene generation alkylation and olefinic polyreaction, improve the alkylated reaction selectivity of thiophene-type sulfide, operational condition is gentle, and process is easy to control.
Summary of the invention
The object of the invention is the method for a kind of gasoline desulfur proposed.
The method of gasoline desulfur of the present invention: comprising the gasoline fraction of a small amount of diesel component and hydrogen, to be mixed into pre-hydrogenator by the diene hydrogenation in gasoline be monoolefine, and light mercaptans and thio-ether type compounds are converted into heavy sulfide; Then pre-hydrogenation products enters a separation column and carries out fractionation, from fractionator overhead light constituent out directly as low-sulphur oil blend component, enter a water wash column from Fractionator Bottom heavy constituent out and remove basic nitrogen compound, and then the alkene thiophene alkylation reactor entering one group of series connection makes the thiophene-type sulfide in heavy petrol increase weight.Enter a catalytic distillation tower from alkylation reactor gasoline component out, under the effect of catalytic distillation tower top alkene thiophene alkylation catalyzer, make remaining thiophene-type sulfide increase weight, gasoline is cut into simultaneously light, weigh two components; Light constituent is directly as low-sulphur oil blend component, and heavy constituent is then the diesel component being enriched sulfide.Method of the present invention, can reduce the sulphur content in gasoline significantly, reduces the loss of octane number that sweetening process is brought simultaneously.
Above-mentioned pre-hydrogenator reaction conditions is: hydrogen dividing potential drop 1.0 ~ 4.0Mpa, temperature of reaction 120 ~ 260 DEG C, volume space velocity 2.0 ~ 8.0h
-1, hydrogen to oil volume ratio 10 ~ 200; Catalyst for pre-hydrogenation carrier is the mixture of aluminum oxide, silicon oxide or aluminum oxide and silicon oxide, and active metal is selected from one or more in VIB, VIIIB, and metal oxide content is 10% ~ 60%, and specific surface area of catalyst is 100 ~ 300m
2/ g, pore volume is 0.20 ~ 0.60ml/g;
The operational condition of above-mentioned separation column is: tower top pressure 0.3 ~ 2.0Mpa, feeding temperature 100 ~ 200 DEG C, tower top temperature 70 ~ 120 DEG C, column bottom temperature 200 ~ 280 DEG C;
The condition of abovementioned alkyl reactor is: pressure 0.1 ~ 2.0Mpa, temperature 70 ~ 250 DEG C, air speed 0.5 ~ 5.0h
-1; The catalyzer of alkylation reactor filling is molecular sieve catalysts, sulfonate resin class catalyzer or solid phosphoric acid catalyst;
The operational condition of above-mentioned catalytic distillation tower is: tower top pressure 0.3 ~ 2.0Mpa, feeding temperature 150 ~ 250 DEG C, tower top temperature 120 ~ 200 DEG C, column bottom temperature 220 ~ 300 DEG C; The catalyzer of catalytic distillation tower filling is molecular sieve catalysts, sulfonate resin class catalyzer or solid phosphoric acid catalyst.
Compared with prior art, gasoline desulfating method provided by the invention mainly contains following advantage:
1, relative patent CN201010616414.9, CN101225327A, CN200610002377.6 etc., because present method have employed catalytic distillation technology, can obtain higher reaction conversion ratio.
2, relative patent CN200810114387.8, mainly transforms compared with the sulfide in heavy petrol in the method in alkylation reactor, and catalytic distillation tower is only the assist measure improving transformation efficiency further.
3, relative patent CN200820109556.4 adopts C3 ~ C5 alkene as alkylating reagent, and present method does not introduce new component, but adopts the heavier C6-C9 alkene contained in gasoline as alkylating reagent, more convenient in operation, is also easy to realize.
4, relatively above-mentioned patent, mainly removes compared with the sulfide in light constituent in gasoline component in present method in pre-hydrogenator, removes at alkylation reactor or catalytic distillation tower compared with heavy sulfide.
5, relatively above-mentioned patent, present method has carried out pre-hydrogenation and washing process to gasoline stocks, can the life cycle of significantly extending catalyst.
6, relatively above-mentioned patent, has widened the boiling range of gasoline stocks by the operation of adjustment upstream device in present method, ensure that the yield of gasoline products, also avoided the inactivation or the sulfocompound back-mixing in the product that add the catalyzer that diesel component causes.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of gasoline desulfating method provided by the present invention.
Embodiment
The raw material that this method uses is the wide-cut gasoline component containing part diesel component, and this gasoline component is normally obtained by the petrol and diesel oil cut point improving upstream device such as catalytic cracking fractionating tower;
Wide-cut gasoline raw material and hydrogen are mixed into pre-hydrogenator, under the effect of reactor catalyst for pre-hydrogenation, are monoolefine lightweight sulfide weightening finish simultaneously by the diene hydrogenation in catalytic gasoline; Reaction conditions is: hydrogen dividing potential drop 1.0 ~ 4.0Mpa, temperature of reaction 120 ~ 260 DEG C, volume space velocity 2.0 ~ 8.0h
-1, hydrogen to oil volume ratio 10 ~ 200; Catalyst for pre-hydrogenation carrier is the mixture of aluminum oxide, silicon oxide or aluminum oxide and silicon oxide, and active metal is selected from one or more in VIB, VIIIB, and metal oxide content is 10% ~ 60%, and specific surface area of catalyst is 100 ~ 300m
2/ g, pore volume is 0.20 ~ 0.60ml/g; Pre-hydrogenation products enter separation column be divided into light, weigh two components; The operational condition of separation column is: tower top pressure 0.3 ~ 2.0Mpa, feeding temperature 100 ~ 200 DEG C, tower top temperature 70 ~ 120 DEG C, column bottom temperature 200 ~ 280 DEG C; First enter a water wash column from separation column heavy constituent out and remove alkali nitrogen compound, then the alkylation reactor entering one group of series connection reacts, the catalyzer of alkylation reactor filling is molecular sieve catalysts, sulfonate resin class catalyzer or solid phosphoric acid catalyst, and reaction conditions is: pressure 0.1 ~ 2.0Mpa, temperature 70 ~ 250 DEG C, air speed 0.5 ~ 5.0h
-1; From alkylation reactor reaction product out enter catalytic distillation tower carry out further alkylated reaction charging is divided into simultaneously light, weigh two components; The operational condition of catalytic distillation tower is: tower top pressure 0.3 ~ 2.0Mpa, feeding temperature 150 ~ 250 DEG C, tower top temperature 120 ~ 200 DEG C, column bottom temperature 220 ~ 300 DEG C; The catalyzer of catalytic distillation tower filling is molecular sieve catalysts, sulfonate resin class catalyzer or solid phosphoric acid catalyst;
Gasoline stocks described above is the mixing oil of one or more in catalytically cracked gasoline, catalytic cracking gasoline, coker gasoline and pressure gasoline.
Embodiment 1
With a kind of wide fraction catalytically cracked gasoline for raw material, its character is as shown in table 1.
First wide fraction catalytic gasoline enters a pre-hydrogenator, the GHC-31 catalyzer of Petroleum Chemical Engineering Institute of CNPC research and development is loaded in pre-hydrogenator, catalytic gasoline carries out weighted BMO spaces under the condition of hydrogen dividing potential drop 2.0Mpa, temperature 150 DEG C, air speed 3.0, hydrogen-oil ratio 20: 1, then enter a separation column be divided into light, weigh two components, the condition of separation column is: tower top pressure 0.8MPa, feeding temperature 120 DEG C, tower top temperature 80 DEG C, column bottom temperature 210 DEG C.First enter a water wash column from separation column heavy constituent out and remove alkali nitrogen compound, the alkylation reactor then entering one group of series connection reacts, and reaction conditions is: pressure 0.8Mpa, temperature 160 DEG C, air speed 1.0h
-1; From alkylation reactor reaction product out enter catalytic distillation tower carry out further alkylated reaction charging is divided into simultaneously light, weigh two components; The operational condition of catalytic distillation tower is: tower top pressure 0.5Mpa, feeding temperature 200 DEG C, tower top temperature 170 DEG C, column bottom temperature 240 DEG C; The catalyzer of alkylation reactor and catalytic distillation tower filling is the GHC-41 catalyzer of Petroleum Chemical Engineering Institute of CNPC research and development, from catalytic distillation tower light constituent out directly as low-sulphur oil blend component, heavy constituent is then the diesel component being enriched sulfide.Character is as shown in table 2.
Table 1 wide fraction catalytic gasoline character
Table 2 desulfurization product character
Claims (1)
1. a method for gasoline desulfur, is characterized in that:
With a kind of wide fraction catalytically cracked gasoline for raw material, wide fraction catalytic gasoline character:
First wide fraction catalytic gasoline enters a pre-hydrogenator, the GHC-31 catalyzer of Petroleum Chemical Engineering Institute of CNPC research and development is loaded in pre-hydrogenator, catalytic gasoline carries out weighted BMO spaces under the condition of hydrogen dividing potential drop 2.0Mpa, temperature 150 DEG C, air speed 3.0, hydrogen-oil ratio 20:1, then enter a separation column be divided into light, weigh two components, the condition of separation column is: tower top pressure 0.8MPa, feeding temperature 120 DEG C, tower top temperature 80 DEG C, column bottom temperature 210 DEG C; First enter a water wash column from separation column heavy constituent out and remove alkali nitrogen compound, the alkylation reactor then entering one group of series connection reacts, and reaction conditions is: pressure 0.8Mpa, temperature 160 DEG C, air speed 1.0h
-1; From alkylation reactor reaction product out enter catalytic distillation tower carry out further alkylated reaction charging is divided into simultaneously light, weigh two components; The operational condition of catalytic distillation tower is: tower top pressure 0.5Mpa, feeding temperature 200 DEG C, tower top temperature 170 DEG C, column bottom temperature 240 DEG C; The catalyzer of alkylation reactor and catalytic distillation tower filling is the GHC-41 catalyzer of Petroleum Chemical Engineering Institute of CNPC research and development, from catalytic distillation tower light constituent out directly as low-sulphur oil blend component, heavy constituent is then the diesel component being enriched sulfide.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110446629.5A CN103184071B (en) | 2011-12-28 | 2011-12-28 | Gasoline desulfurization method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110446629.5A CN103184071B (en) | 2011-12-28 | 2011-12-28 | Gasoline desulfurization method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103184071A CN103184071A (en) | 2013-07-03 |
| CN103184071B true CN103184071B (en) | 2015-07-22 |
Family
ID=48675522
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201110446629.5A Active CN103184071B (en) | 2011-12-28 | 2011-12-28 | Gasoline desulfurization method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103184071B (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108018077B (en) * | 2016-10-28 | 2020-10-27 | 中国石油化工股份有限公司 | Method for deep desulfurization of gasoline and equipment for deep desulfurization of gasoline |
| CN108003931B (en) * | 2016-10-28 | 2020-09-22 | 中国石油化工股份有限公司 | Method for deep desulfurization of gasoline and equipment for deep desulfurization of gasoline |
| CN112143518B (en) * | 2019-06-27 | 2024-07-09 | 中国石油化工股份有限公司 | Solid acid alkylation method for producing gasoline |
| CN112143523B (en) * | 2019-06-27 | 2024-06-11 | 中国石油化工股份有限公司 | Pretreatment method of alkylation gasoline raw material |
| CN111892948A (en) * | 2020-06-15 | 2020-11-06 | 新疆寰球工程公司 | Processing method for hydrogenation and octane number loss reduction of catalytically cracked gasoline |
| CN111909726B (en) * | 2020-07-15 | 2023-01-17 | 凯瑞环保科技股份有限公司 | Process for thioalkylation of thiophenes |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1429884A (en) * | 2001-12-30 | 2003-07-16 | 中国石化集团齐鲁石油化工公司 | Desulfurization process of gasoline |
| CN101220295A (en) * | 2008-02-03 | 2008-07-16 | 天津大学 | Device and method for catalytically cracked gasoline and diesel oil coupling desulfurization |
| CN101597510A (en) * | 2008-06-04 | 2009-12-09 | 中国石油天然气股份有限公司 | Catalytic distillation method for gasoline alkylation desulfurization |
| CN102041086A (en) * | 2011-01-17 | 2011-05-04 | 江苏佳誉信实业有限公司 | Selective hydrodesulfurization method for high-sulfur high-olefin catalytic gasoline |
-
2011
- 2011-12-28 CN CN201110446629.5A patent/CN103184071B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1429884A (en) * | 2001-12-30 | 2003-07-16 | 中国石化集团齐鲁石油化工公司 | Desulfurization process of gasoline |
| CN101220295A (en) * | 2008-02-03 | 2008-07-16 | 天津大学 | Device and method for catalytically cracked gasoline and diesel oil coupling desulfurization |
| CN101597510A (en) * | 2008-06-04 | 2009-12-09 | 中国石油天然气股份有限公司 | Catalytic distillation method for gasoline alkylation desulfurization |
| CN102041086A (en) * | 2011-01-17 | 2011-05-04 | 江苏佳誉信实业有限公司 | Selective hydrodesulfurization method for high-sulfur high-olefin catalytic gasoline |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103184071A (en) | 2013-07-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103184071B (en) | Gasoline desulfurization method | |
| CN101597510B (en) | Catalytic distillation method for gasoline alkylation desulfurization | |
| CN104694160B (en) | Combined method for light gasoline alkaline washing desulfurization | |
| CN103571534B (en) | Device and method for producing clean gasoline by combining catalytic cracking and hydrofining | |
| CN103087771B (en) | Hydrogenation method for deeply desulfurizing gasoline | |
| CN101294108B (en) | Combination method of catalytic cracking production separation and hydrogen refining | |
| CN106147844B (en) | A kind of method of hydrotreating for producing super low-sulfur oil | |
| JP4505457B2 (en) | Desulfurization of naphtha gasoline stream derived from fluid catalytic cracker | |
| CN103834439B (en) | A kind of method of deep hydrodesulfurizationof | |
| CN103834438B (en) | A kind of processing method of hydrogenating desulfurization | |
| CN102796556B (en) | A kind of catalysis conversion method of petroleum hydrocarbon | |
| CN102994148B (en) | Deep desulfurization method for gasoline | |
| CN107353934B (en) | Method for reducing octane number loss of gasoline of S Zorb device | |
| CN103059955B (en) | Method for producing clean gasoline from catalytic cracking gasoline | |
| CN104772164A (en) | Catalytic cracking gasoline alkylate desulfurization catalyst and desulfurization technology thereof | |
| CN101519337B (en) | Method for fine desulfurization of high-sulfur C4 of refineries | |
| CN103571536A (en) | Device and method for producing clean gasoline and increasing propylene yield through catalytic cracking and hydrogenation | |
| CN103059954A (en) | Method for reducing catalytic cracking gasoline sulfur content | |
| CN103059951B (en) | Catalytic cracking and catalytic gasoline hydrogenation combined technological method | |
| CN102796558B (en) | A kind of Catalytic conversion method of petroleum hydrocarbon | |
| CN101225327A (en) | Hydrocarbon recombinant alkylating desulfurization method for catalytically cracked gasoline | |
| CN103087770A (en) | Clean gasoline production method through selective hydrogenation and desulfurization of catalytic gasoline | |
| CN103059949A (en) | Catalytic cracking gasoline desulfurization method | |
| CN102533330A (en) | Method for producing low-sulfur gasoline | |
| CN102604672A (en) | Method for producing low-sulfur gasoline |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |