CN102634370B - Gasoline hydro-upgrading method - Google Patents
Gasoline hydro-upgrading method Download PDFInfo
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- CN102634370B CN102634370B CN201110035565.XA CN201110035565A CN102634370B CN 102634370 B CN102634370 B CN 102634370B CN 201110035565 A CN201110035565 A CN 201110035565A CN 102634370 B CN102634370 B CN 102634370B
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- 238000000034 method Methods 0.000 title claims abstract description 30
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 43
- 239000001257 hydrogen Substances 0.000 claims abstract description 43
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 30
- 238000006243 chemical reaction Methods 0.000 claims abstract description 28
- 230000023556 desulfurization Effects 0.000 claims abstract description 28
- 230000003197 catalytic effect Effects 0.000 claims abstract description 27
- 150000001336 alkenes Chemical class 0.000 claims abstract description 21
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 19
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 claims abstract description 19
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 18
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims abstract description 18
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000004821 distillation Methods 0.000 claims abstract description 17
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000002994 raw material Substances 0.000 claims abstract description 6
- 150000002431 hydrogen Chemical class 0.000 claims description 23
- 239000005864 Sulphur Substances 0.000 claims description 9
- 239000003208 petroleum Substances 0.000 claims description 7
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical class S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 5
- 238000009835 boiling Methods 0.000 claims description 3
- 238000006317 isomerization reaction Methods 0.000 abstract description 9
- 239000007788 liquid Substances 0.000 abstract description 7
- 230000004048 modification Effects 0.000 abstract description 7
- 238000012986 modification Methods 0.000 abstract description 7
- 238000005899 aromatization reaction Methods 0.000 abstract description 5
- 238000007670 refining Methods 0.000 abstract description 5
- 238000000926 separation method Methods 0.000 abstract description 4
- 150000001993 dienes Chemical class 0.000 abstract description 3
- 239000007791 liquid phase Substances 0.000 abstract description 3
- 239000000463 material Substances 0.000 abstract description 3
- 238000002156 mixing Methods 0.000 abstract description 3
- 229910052717 sulfur Inorganic materials 0.000 abstract description 3
- 239000011593 sulfur Substances 0.000 abstract description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 abstract description 2
- 239000003054 catalyst Substances 0.000 description 22
- 239000000047 product Substances 0.000 description 20
- 239000003921 oil Substances 0.000 description 17
- 239000000203 mixture Substances 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 8
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 5
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 5
- 229920006395 saturated elastomer Polymers 0.000 description 5
- 229910052814 silicon oxide Inorganic materials 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 3
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 229910044991 metal oxide Inorganic materials 0.000 description 3
- 150000004706 metal oxides Chemical class 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 2
- 238000002715 modification method Methods 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- 241000269350 Anura Species 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- KWKAKUADMBZCLK-UHFFFAOYSA-N methyl heptene Natural products CCCCCCC=C KWKAKUADMBZCLK-UHFFFAOYSA-N 0.000 description 1
- 238000006011 modification reaction Methods 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 238000007493 shaping process Methods 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a method for gasoline hydrogenation modification; gasoline raw materials are firstly mixed with hydrogen and enter a catalytic distillation tower to remove diene, and then gasoline is cut into light and heavy gasoline components; the light gasoline coming out of the top of the catalytic distillation tower is directly used as a clean gasoline blending component, the heavy gasoline coming out of the bottom of the catalytic distillation tower firstly enters a hydro-upgrading reactor for aromatization, isomerization and other reactions, then enters a hydro-desulfurization reactor for supplementary refining, the material coming out of the hydro-desulfurization reactor is cooled and then enters a product separator for gas-liquid separation, the hydrogen coming out of the gas-liquid separator is recycled after desulfurization treatment, and the liquid phase product enters a desulfurization alcohol tower for further reducing the mercaptan content of the gasoline and then is mixed with the light gasoline to obtain a hydro-upgrading gasoline product; the method provided by the invention can not only greatly reduce the contents of sulfur and olefin in the gasoline, but also reduce the octane number loss brought by the modification process.
Description
Technical field
The present invention relates to a kind of method of the secondary processing of gasoline hydro-upgradings such as hydrogenation modification method of inferior patrol, particularly catalytically cracked gasoline.
Background technology
In recent years, be protection of the environment, countries in the world have proposed stricter restriction to the composition of motor spirit, to reduce the discharge of objectionable impurities.Beijing has carried out the provincial standard DB11/238-2007 of motor spirit Beijing 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 that, how to reduce catalytic gasoline is to improve the key of China's motor spirit quality.
Catalyzed gasoline hydrogenation desulfurization technology is mainly divided two large classes both at home and abroad at present.One class is selective hydrodesulfurization technology: by catalyst modification, suppress the olefin saturated activity of catalyzer, avoid alkene by too much saturated in hydrogenating desulfurization, reduce the loss of octane number of hydrogenation process.Another kind of technology is catalytic gasoline modification technology: conventional hydrogenation catalyst is used in hydrogenating desulfurization, then by isomerization, aromizing, cracking reaction, hydrogenating desulfurization gasoline is processed, improved the octane value of gasoline to make up the loss of octane number in hydrodesulfurization process.
ZL200410020932 patent discloses a kind of hydrogenation modification method of inferior patrol.The method is the processing method that alkene falls in a kind of full cut FCC gasoline hydrodesulfurizationmethod.Under the condition that hydrogen exists and temperature raises gradually, contact with three kinds of catalyzer, form three reaction zones.The first reaction zone temperature is lower, uses Hydrobon catalyst, mainly removes the diolefin in gasoline; Second, third reaction zone temperature is high, and gasoline reforming catalyst is used in second reaction zone, comprises the upgrading reaction of aromizing, isomerization and benzene alkylation reaction, improves the octane value of gasoline, improves quality product; Catalyst for selectively hydrodesulfurizing is used in the 3rd reaction zone, removes to greatest extent organic sulfide in oil.It is charging that the method adopts full cut catalytic gasoline, and loss of octane number is larger.
ZL200410060574 patent discloses a kind of inferior patrol hydrogenation modifying process.Its technological process is: feed gasoline is cut into lighting end and last running at 60～90 ℃, wherein last running elder generation and hydrogen mix, again with Hydrobon catalyst contact reacts, reacted effluent contacts and carries out aromatization modification reaction with aromatization modification catalyzer again, obtains high-octane rating low-sulphur oil cut; Heavy naphtha after upgrading mixes with lighting end or through the pretreated lighting end of mercaptan removal again, obtains product gasoline.This patent need to adopt the method for soda finishing mercaptan removal, can cause the discharge of the disagreeableness alkaline residue of environment.
ZL200510090501 patent discloses a kind of method of gasoline hydrogenation modifying.Gasoline stocks is cut into light gasoline fraction and heavy naphtha, and light gasoline fraction removes mercaptan wherein through alkali cleaning refining desulfurization alcohol; Heavy gasoline cut contacts with catalyst for hydro-upgrading together and carries out hydrogenating desulfurization and hydro-upgrading reaction with hydrogen, and described catalyst for hydro-upgrading is a kind of catalyzer by zeolite and alumina composite shaping carrier load non-noble metal components.The method is used a kind of catalyst for hydro-upgrading, and the functions such as isomerization, cracking, desulfurization, denitrogenation, olefin saturated complete on same catalyzer.This patent also needs to adopt the method for soda finishing mercaptan removal, can cause the discharge of the disagreeableness alkaline residue of environment.
ZL200410102818 patent discloses a kind of gasoline modifying method.Comprise the following steps: a) under isomerisation of olefin processing condition, gasoline fraction oil is contacted with olefin skeletal isomerization catalyzer; B), under hydrodesulfurization condition, step reaction effluent a) is contacted with Hydrobon catalyst.This method mainly adopts the method for isomerization upgrading, and liquid product yield is lower.
US5411658 discloses a kind of method of gasoline upgrading, and the method, by after catalytic gasoline hydrofining, directly enters second segment reactor and carries out octane value recovering.This patent hydrofining adopts traditional Hydrobon catalyst, and loss of octane number is larger.
Summary of the invention
The object of the invention is to provide on the basis of existing technology a kind of method of inferior patrol hydro-upgrading.
Gasoline stocks mix with hydrogen first enter a catalytic distillation tower remove diolefine and by gasoline cut into gently, two components of heavy petrol.From catalytic distillation column overhead petroleum naphtha out, directly as clean gasoline blend component, from heavy petrol out at the bottom of tower and hydrogen mix, be introduced into a hydro-upgrading reactor, and then enter a hydrodesulphurisatioreactors reactors and carry out post-refining.From hydrodesulphurisatioreactors reactors material is out cooling, enters product separator and carry out gas-liquid separation.From gas-liquid separator hydrogen out, after desulfurization is processed, recycle, liquid-phase product enters after mercaptan removal tower reduces the mercaptans content in gasoline and is mixed to get reformulated gasoline product with petroleum naphtha.
The reaction conditions of above-mentioned catalytic distillation tower is: tower top pressure 0.5～2.0Mpa, 120～180 ℃ of feeding temperatures, 60～120 ℃ of tower top temperatures, 160～220 ℃ of column bottom temperatures, hydrogen to oil volume ratio 10～200.The support of the catalyst of catalytic distillation tower filling is the mixture of aluminum oxide, silicon oxide or aluminum oxide and silicon oxide, active metal is selected from one or more in VIB or VIIIB, metal oxide weight is 10%～70%, specific surface area of catalyst is 100～300m2/g, and pore volume is 0.20～0.60ml/g.
The reaction conditions of above-mentioned hydro-upgrading reactor is: hydrogen dividing potential drop 1.0～4.0Mpa, 280～450 ℃ of temperature of reaction, volume space velocity 1.0～4.0h
-1, hydrogen to oil volume ratio 100～600.Catalyst for hydro-upgrading carrier is ZSM-5, Beta, SAPO molecular sieve or its mixture, by catalyst weight 100%, molecular sieve weight is 60%～90%, and metal oxide weight is 1%～10%, active metal is selected from one or more in VIB or VIIIB, and surplus is binding agent.Specific surface area of catalyst is 200～500m
2/ g, pore volume is 0.20～0.50ml/g.
The reaction conditions of above-mentioned hydrodesulphurisatioreactors reactors is: hydrogen dividing potential drop 1.0～4.0Mpa, 200～350 ℃ of temperature of reaction, volume space velocity 2.0～8.0h
-1, hydrogen to oil volume ratio 100～600.Hydrodesulfurization catalyst support is the mixture of aluminum oxide, silicon oxide or aluminum oxide and silicon oxide, active metal is selected from one or more in VIB or VIIIB, by catalyst weight 100%, metal oxide weight is 10%～30%, and specific surface area of catalyst is 100～300m
2/ g, pore volume is 0.20～0.80ml/g.
The reaction conditions of above-mentioned mercaptan removal tower is: hydrogen dividing potential drop 0.5～2.0Mpa, feeding temperature 200-300 ℃, tower top temperature 180-280 ℃, column bottom temperature 250-350 ℃, hydrogen to oil volume ratio 5～50.Mercaptan-eliminating catalyst is aluminum oxide, silicon oxide or its mixture or without hydrogen exchange na-pretreated zeolite.
Gasoline hydrogenation modifying process provided by the invention mainly contains following advantage:
1, the flow process that the present invention adopts, not only reduced the olefin(e) centent in gasoline, also significantly reduce the mercaptans content in gasoline, substituted soda finishing mercaptan removal operation in patent ZL200410060574, ZL200510090501, avoided the discharge of the disagreeableness alkaline residue of environment.
2, the present invention mainly adopts aromatization modification technology, the isomerization modification technology that patent ZL200410102818 adopts relatively, and loss of octane number is little, and liquid is received high.
3, the present invention has adopted the flow process of first upgrading back end hydrogenation, and with respect to the flow process of upgrading after the first hydrogenation of the employings such as patent ZL200410060574, product aromatization rate is high, and loss of octane number is little.
4, the refining catalyst for selectively hydrodesulfurizing that adopts after the present invention, for the Hydrobon catalyst of patent ZL200510090501, US5411658 use, the loss of octane number that hydrogenation process is brought is less.
Accompanying drawing explanation
Fig. 1 is the principle flow chart of gasoline hydrogenation modifying method provided by the present invention.
Embodiment
Technical process of the present invention is: will after gasoline stocks and hydrogen mixing, enter a catalytic distillation tower, under tower top pressure 0.5～2.0Mpa, 120～180 ℃ of feeding temperatures, 60～120 ℃ of tower top temperatures, 160～220 ℃ of column bottom temperatures, hydrogen to oil volume ratio 10～200 conditions, carry out hydrogenation reaction, by the diene in catalytic gasoline saturated and by gasoline be divided into light, weigh two components.Heavy petrol enters hydro-upgrading reactor after mixing with hydrogen, at hydrogen dividing potential drop 1.0～4.0Mpa, 280～450 ℃ of temperature of reaction, volume space velocity 1.0～4.0h
-1, under hydrogen to oil volume ratio 100～500 conditions, there is aromizing, isomerization reaction, follow the reactions such as desulfurization, olefin saturated simultaneously.By hydro-upgrading, olefin(e) centent, sulphur content in gasoline significantly reduce.Then hydro-upgrading reaction product enters hydrodesulphurisatioreactors reactors and carries out post-refining, at hydrogen dividing potential drop 1.0～4.0Mpa, 200～350 ℃ of temperature of reaction, volume space velocity 2.0～8.0h
-1, under hydrogen to oil volume ratio 100～500 conditions, further reduce olefin(e) centent and sulfide content in gasoline.After hydrogenating desulfurization product is cooling, enters product separator separation and carry out gas-liquid separation.From gas-liquid separator hydrogen out, after processing, desulfurization recycles, liquid-phase product enters mercaptan removal tower, after hydrogen dividing potential drop 0.5～2.0Mpa, feeding temperature 200-300 ℃, tower top temperature 180-280 ℃, column bottom temperature 250-350 ℃ reaction conditions first remove the mercaptan in gasoline with fractionator overhead out petroleum naphtha be mixed to get reformulated gasoline product.
The present invention is applicable to the hydro-upgrading of inferior patrol, is mainly used in the hydro-upgrading of the secondary processing of gasoline such as catalytically cracked gasoline, catalytic cracking gasoline, coker gasoline and pressure gasoline.
Gasoline upgrading technique of the present invention, is characterized in that adopting full distillation gasoline pre-treatment, then light, heavy petrol is separated, heavy petrol adopts the technical process of first hydro-upgrading back end hydrogenation desulfurization.
Comparative example
Take a kind of catalytically cracked gasoline as raw material, and its character is as shown in table 1.First catalytic gasoline enters catalytic distillation tower, under tower top pressure 0.75Mpa, 145 ℃ of feeding temperatures, 90 ℃ of tower top temperatures, 205 ℃ of conditions of column bottom temperature, reacts, and is cut into two components of weight gasoline simultaneously, and heavy naphtha accounts for 65% of raw material.First heavy petrol be mixed into hydrodesulphurisatioreactors reactors with hydrogen, under hydrogen dividing potential drop 1.8MPa, 252 ℃ of conditions, carries out hydrogenating desulfurization.Then enter hydro-upgrading reactor and carry out hydro-upgrading under the reaction conditions of 385 ℃ of hydrogen dividing potential drop 2.0MPa, temperature of reaction.Hydro-upgrading product is mixed to get clean gasoline product with petroleum naphtha after stabilizer tower is stable.Processing condition and generation oil nature are in Table 2.As can be seen from Table 2, product sulphur content is 66ppm, desulfurization degree 81.5%, and olefin(e) centent drops to 27.8%, octane value (RON) loss 1.1Ge unit from 48.5%.
Embodiment 1
The stock oil that embodiment 1 is used is identical with comparative example.First catalytic gasoline enters catalytic distillation tower, under tower top pressure 0.75Mpa, 145 ℃ of feeding temperatures, 90 ℃ of tower top temperatures, 205 ℃ of conditions of column bottom temperature, reacts, and is cut into two components of weight gasoline simultaneously, and heavy naphtha accounts for 65% of raw material.First heavy petrol be mixed into hydro-upgrading reactor with hydrogen, under the reaction conditions of 385 ℃ of hydrogen dividing potential drop 2.0MPa, temperature of reaction, carries out hydro-upgrading, then enters hydrodesulphurisatioreactors reactors and carry out hydrogenating desulfurization under hydrogen dividing potential drop 1.8MPa, 252 ℃ of conditions.After desulfurization, then product enters mercaptan removal tower, under hydrogen dividing potential drop 1.8Mpa, 300 ℃ of feeding temperatures, 260 ℃ of tower top temperatures, 350 ℃ of column bottom temperatures, hydrogen to oil volume ratio 50 conditions, further reduce after the mercaptans content of gasoline with fractionator overhead out petroleum naphtha be mixed to get reformulated gasoline product.Processing condition and generation oil nature are in Table 2.As can be seen from Table 2, product sulphur content is 45ppm, desulfurization degree 87.4%, and olefin(e) centent drops to 29.5%, octane value (RON) loss 0.5Ge unit from 48.5%.
Embodiment 2
The stock oil that embodiment 2 is used is identical with comparative example.First catalytic gasoline enters catalytic distillation tower and reacts under tower top pressure 0.75Mpa, 145 ℃ of feeding temperatures, 90 ℃ of tower top temperatures, 205 ℃ of conditions of column bottom temperature, is cut into two components of weight gasoline simultaneously, and heavy naphtha accounts for 65% of raw material.First heavy petrol be mixed into hydro-upgrading reactor with hydrogen, under the reaction conditions of 385 ℃ of hydrogen dividing potential drop 2.0MPa, temperature of reaction, carries out hydro-upgrading, then enters hydrodesulphurisatioreactors reactors and carry out hydrogenating desulfurization under hydrogen dividing potential drop 1.8MPa, 265 ℃ of conditions.Product introduction mercaptan removal tower after desulfurization, under hydrogen dividing potential drop 1.8Mpa, 300 ℃ of feeding temperatures, 260 ℃ of tower top temperatures, 350 ℃ of column bottom temperatures, hydrogen to oil volume ratio 50 conditions, further reduce after the mercaptans content of gasoline with fractionator overhead out petroleum naphtha be mixed to get reformulated gasoline product.Processing condition and generation oil nature are in Table 2.As can be seen from Table 2, in product, sulphur content is 20ppm, desulfurization degree 94.4%, and olefin(e) centent drops to 28.1%, octane value (RON) loss 1.1Ge unit from 48.5%.
Table 1
| Material name | Catalytic gasoline |
| Density (20 ℃), g/cm 3 | 0.721 |
| Sulphur, ppm | 356 |
| Olefin(e) centent, volume % | 48.5 |
| Boiling range, ℃ | |
| Initial boiling point | 36 |
| 10％ | 52 |
| 50％ | 96 |
| Do | 197 |
| Octane value (RON) | 92 |
Table 2
| Comparative example 1 | Embodiment 1 | Embodiment 2 | |
| Processing condition | |||
| Catalytic distillation tower tower top pressure, MPa | 0.75 | 0.75 | 0.75 |
| Catalytic distillation tower feeding temperature, ℃ | 145 | 145 | 145 |
| Catalytic distillation tower tower top temperature, ℃ | 90 | 90 | 90 |
| Catalytic distillation tower column bottom temperature, ℃ | 205 | 205 | 205 |
| Pre-hydrogenation temperature, ℃ | 160 | 160 | 90 |
| Hydro-upgrading pressure, MPa | 2.0 | 2.0 | 205 |
| Hydro-upgrading temperature, ℃ | 385 | 385 | 385 |
| Hydrogenating desulfurization pressure, MPa | 1.8 | 1.8 | 1.8 |
| Hydrogenating desulfurization temperature, ℃ | 252 | 252 | 265 |
| Mercaptan removal column overhead pressure, MPa | 1.8 | 1.8 | |
| Mercaptan removal tower feeding temperature, ℃ | 300 | 300 | |
| Mercaptan removal column overhead temperature, ℃ | 260 | 260 | |
| Mercaptan removal tower column bottom temperature, ℃ | 350 | 350 | |
| Product property | |||
| Density, (20 ℃), g/cm 3 | 0.713 | 0.715 | 0.712 |
| Sulphur content, ppm | 66 | 45 | 20 |
| Olefin(e) centent, volume % | 27.8 | 29.5 | 28.1 |
| Octane value (RON) | 90.9 | 91.5 | 90.9 |
| Loss of octane number | 1.1 | 0.5 | 1.1 |
| Desulfurization degree % | 81.5 | 87.4 | 94.4 |
Claims (1)
1. a method for gasoline hydrogenation modifying, is characterized in that:
First catalytic gasoline enters catalytic distillation tower, under tower top pressure 0.75Mpa, 145 ℃ of feeding temperatures, 90 ℃ of tower top temperatures, 205 ℃ of conditions of column bottom temperature, reacts, and is cut into two components of weight gasoline simultaneously, and heavy naphtha accounts for 65% of raw material; First heavy petrol be mixed into hydro-upgrading reactor with hydrogen, under the reaction conditions of 385 ℃ of hydrogen dividing potential drop 2.0MPa, temperature of reaction, carries out hydro-upgrading, then enters hydrodesulphurisatioreactors reactors and carry out hydrogenating desulfurization under hydrogen dividing potential drop 1.8MPa, 252 ℃ of conditions; After desulfurization, then product enters mercaptan removal tower, under hydrogen dividing potential drop 1.8Mpa, 300 ℃ of feeding temperatures, 260 ℃ of tower top temperatures, 350 ℃ of column bottom temperatures, hydrogen to oil volume ratio 50 conditions, further reduce after the mercaptans content of gasoline with fractionator overhead out petroleum naphtha be mixed to get reformulated gasoline product; Product sulphur content is 45ppm, desulfurization degree 87.4%, and olefin(e) centent drops to 29.5% from 48.5%, and octane value RON loses 0.5Ge unit;
The character of described catalytic gasoline is: 20 ℃ of density 0.721g/cm
3, S35 6ppm, olefin(e) centent 48.5v%, 36 ℃ of initial boiling points, 10% heats up in a steamer a little 52 ℃, and 50% heats up in a steamer a little 96 ℃, does 197 ℃, and octane value RON is 92.
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| SG11201903082QA (en) * | 2016-10-21 | 2019-05-30 | China Petroleum & Chem Corp | Process for treating gasoline |
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| US5411658A (en) * | 1991-08-15 | 1995-05-02 | Mobil Oil Corporation | Gasoline upgrading process |
| EP0949314B1 (en) * | 1998-03-20 | 2006-06-14 | China Petrochemical Corporation | Hydrodesulfurisation of hydrocarbon oils |
| CN1283761C (en) * | 2004-10-18 | 2006-11-08 | 中国石油化工集团公司 | Hydrogenation modification process for low grade gasoline |
| CN101161791B (en) * | 2006-10-12 | 2012-01-25 | 中国石油化工股份有限公司 | Method for producing clean gasoline |
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|---|---|---|---|---|
| CN1718688A (en) * | 2004-07-06 | 2006-01-11 | 中国石油化工股份有限公司 | Hydrogenation modification method of faulty gasoline |
| CN101307254A (en) * | 2007-05-18 | 2008-11-19 | 中国石油化工股份有限公司 | Process for producing cleaning gasoline from poor-quality gasoline |
| CN101845322A (en) * | 2010-05-12 | 2010-09-29 | 中国石油天然气股份有限公司 | Production method for reducing sulfur and olefin content in gasoline |
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