CN1654602A - Etherification method for alkene contained light gasoline - Google Patents
Etherification method for alkene contained light gasoline Download PDFInfo
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- CN1654602A CN1654602A CN 200410003406 CN200410003406A CN1654602A CN 1654602 A CN1654602 A CN 1654602A CN 200410003406 CN200410003406 CN 200410003406 CN 200410003406 A CN200410003406 A CN 200410003406A CN 1654602 A CN1654602 A CN 1654602A
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Abstract
The olefin containing light gasoline etherifying process of the present invention has short technological process, less apparatus adopted, convenient operation, no noble metal in use and sulfur poisoning. The technological scheme is that the olefin containing light gasoline etherifying process includes eliminating diolefin, eliminating alkali and nitrogen and hydroetherifying, and features the first section of selective hydrogenation reaction with double functional non-noble catalyst for eliminating diolefin, eliminating alkali and nitrogen, and the second section of hydroetherifying reaction between isomeric active olefin and methanol to produce etherified gasoline.
Description
Technical field
The present invention relates to the etherified gasoline production technique, particularly a kind of alkene petroleum naphtha etherification method that contains.
Background technology
Along with the environmental regulation standard is more and more stricter, the production of clean gasoline more and more is subject to people's attention, and wherein the etherificate of olefine contained gasoline is one of its important method.
Etherification reaction generally uses strong acid cation exchange resin catalyst, and the use molecular sieve catalyst of only a few is as USP5609654.Olefine contained gasoline contains a small amount of diene and alkali nitrogen, and the former can gather on catalyzer, and the latter understands the acidity of catalyst neutralisation, and they all have grievous injury to the performance of resin catalyst.Therefore, before carrying out etherification reaction, need to remove diene and alkali nitrogen.
Remove diene and adopt the selective hydrogenation method, when removing diene, requirement can not reduce the content of the isomeric olefine of tool etherification activity, the catalyzer that uses in the prior art is loaded noble metal catalyst normally, (for example also precious metal directly can be loaded on the catalyst for etherification, Iguatius etc., HydrocarbonProcessing, 1995,74 (2): 51; USP5609654; CN1048722A; CN1046549A; Wang Haiyan etc.; Ion-exchange and absorption, 2002,18 (3): 249; Hu Jingmin etc., petrochemical complex, 1999,28 (6): 354), catalyzer cost height not only, and exist precious metal to run off easily and the technological deficiency of sulfur poisoning, catalyst life is not long.
The method of removing alkali nitrogen generally has solvent extration, chemical extraction method and absorption method.The solvent that solvent extration uses mainly is a water, also uses acid solvent such as arbon dioxide solution and acetic acid solution (USP5847230 for example; Ma Jun etc., Fusun PetroleumCollege's journal, 2001,21 (1): 20; Brock HL etc., Hydrocarbon Processing, 1991,70 (9): 133; Li Ji, Shenyang chemical industry, 1997,26 (3): 26; Xie Ying etc., lubricating oil, 2000,15 (4): 52), extraction process is at industrial extraction tower and the back extraction tower of needing, and equipment is huge, the energy consumption height, water resources is relatively wasted, and brings environmental issue.Chemical extraction method is to utilize the acid complex compound contain transition metal and nitrogen complexing with dealkalize nitrogen, except that the existence shortcoming identical with conventional extraction process, production cost also higher (as Wei Yi etc., Fusun PetroleumCollege's journal, 2002,22 (2): 1; Yue Kunxia etc., Fusun PetroleumCollege's journal, 1998,18 (1): 12).Comparatively speaking, though absorption method is fairly simple, have equally that equipment is big, the deficiency of long flow path; Though at present people are inclined to employing, do not have universally recognized high-quality sorbent material (as Ma Jun etc., petrochemical complex Journal of Chinese Universities, 2001,14 (2): 11; Chen Wenyi etc., oil refining design, 2001,31 (1): 52; Luan Xilin etc., petrochemical complex Journal of Chinese Universities, 1999,12 (2): 15).
In a word, what contain in the prior art that the etherification method of alkene petroleum naphtha adopts is three sections etherification technologies, is respectively and removes alkali nitrogen section, removes the diene section and carry out the etherification reaction of hydro-refining section.Obviously, three sections etherification technologies exist technical process length, many, the unhandy technical deficiencies of production unit and carried noble metal and promptly carry the technological deficiency that palladium type catalyzer exists easy loss of precious metal and sulfur poisoning.
Summary of the invention
The present invention is directed to the above-mentioned technical deficiency and the defective that exist in the prior art, a kind of shortened process greatly is provided, thereby reduce production unit and bring operation to contain alkene petroleum naphtha etherification method easily, this method does not adopt noble metal catalyst, thereby does not have the technological deficiency of precious metal loss and easy sulfur poisoning.
Technical scheme of the present invention is as follows:
Contain alkene petroleum naphtha etherification method, comprise and remove diene, remove alkali nitrogen and carry out etherification reaction of hydro-refining containing the alkene petroleum naphtha, it is characterized in that: first section is combined into one section and carries out selective hydrogenation by adopting difunctional non-precious metal catalyst will remove diene and removing alkali nitrogen, second section is heterogeneous activity alkene and methyl alcohol carries out etherification reaction of hydro-refining, produces etherified gasoline.
Described difunctional non-precious metal catalyst is a copper-base composite oxidate.
Described copper-base composite oxidate catalyzer can make the section of winning selective hydrogenation remove diene and reach more than 98% (weight ratio) and more than the dealkalize nitrogen 80% (weight ratio).
Described copper-base composite oxidate catalyzer without reduction or sulfidizing, is participated in first section directly and is carried out selective hydrogenation.
The described alkene petroleum naphtha that contains is catalytic cracking petroleum naphtha or light coker naphtha or the thermo-cracking petroleum naphtha of doing less than 80 ℃.
Described first section selective hydrogenation is identical with described second section reaction process condition that etherification reaction of hydro-refining adopted.
Described identical reaction process condition is: 30～100 ℃ of temperature of reaction, pressure 0.5～2.0MPa, liquid air speed 1.0～4.0h
-1, hydrogen to oil volume ratio 50～500.
Described identical reaction process condition is preferably: 40～80 ℃ of temperature of reaction, pressure 0.8～1.5MPa, liquid air speed 1.5～3.0h
-1, hydrogen to oil volume ratio 80～300.
The described alkene petroleum naphtha that contains is through behind described first section selective hydrogenation, and diene content is less than 0.1% (weight ratio), and the alkali nitrogen content is less than 0.2ppm, and the isomeric olefine of tool etherification activity increases by 0.38～2.91% (weight ratio) simultaneously; In second section, use the sulfonic acid type strong acid cation exchange resin catalyst, through after first section processing contain alkene petroleum naphtha and methanol mixed after carry out etherification reaction of hydro-refining, C5 activity isomerism olefin conversion is greater than 55% (weight ratio) in the etherified gasoline that produces, C6 activity isomerism olefin conversion is greater than 25% (weight ratio), and the ether massfraction is greater than 15%.
Technique effect of the present invention is as follows:
Compared with prior art, because the present invention contains alkene petroleum naphtha etherification method, two technological processs of hydrogenation respectively being taken off diene and removing alkali nitrogen are combined into one section, thereby shortened whole flow process, make conventional three sections etherification technologies become two sections, promptly first section is combined into one section and carries out selective hydrogenation by adopting difunctional non-precious metal catalyst will remove diene and removing alkali nitrogen, second section is heterogeneous activity alkene and methyl alcohol carries out etherification reaction of hydro-refining, produce etherified gasoline, like this, just shortened technical process greatly, thereby reduced production unit and bring operation convenient.This method does not adopt noble metal catalyst, thereby has solved the technological deficiency of easy loss of precious metal and sulfur poisoning.
With of the prior art year palladium type catalyzer was that noble metal catalyst is compared, the base metal copper-based catalysts not only has bifunctional technique effect, not only takes off diene but also remove alkali nitrogen, and greatly reduce production cost, and the isomeric olefine of tool etherification activity does not reduce, even increases to some extent.So containing the direct etherified gasoline octane value that obtains of alkene petroleum naphtha etherification method by the present invention does not reduce.
Because containing the alkene petroleum naphtha is catalytic cracking petroleum naphtha or light coker naphtha or the thermo-cracking petroleum naphtha of doing less than 80 ℃, this just can give prominence to and manifest advantage and the practical function of the present invention in suitability for industrialized production.In actual use, through check and test, be 47 ℃ in temperature of reaction, reaction pressure is 1.1MPa, the liquid air speed is 2.0h
-1, hydrogen to oil volume ratio is under 130 the normal condition, behind the successive reaction 100h, does not still contain diene from be filled with the product that comes out through the selective hydrogenation device of the non-precious metal catalyst that reduction is handled, isomeric olefine increases by 2.17%.Outstanding and the technical progress that this shows technique effect is significantly.
Because first section selective hydrogenation is identical with second section reaction process condition that etherification reaction of hydro-refining adopted, this equilibrium distribution for energy source and power in the suitability for industrialized production and relevant device brings great convenience, and helps enforcement of the present invention.
Owing to determined reaction process condition with data mode, promptly a plurality of related process parameters are implemented technical solution of the present invention and obtain the corresponding techniques effect to provide a great convenience for concrete.
Owing to put down in writing the component content technical characterictic of the product that obtains behind first section selective hydrogenation, also put down in writing the component content technical characterictic that second section olefine contained gasoline after using the sulfonic acid type strong acid cation exchange resin catalyst to first section processing carries out product that etherification reaction of hydro-refining obtains, like this, just can further show technique effect of the present invention from these component content technical characterictics.
Description of drawings
Accompanying drawing contains the process flow diagram of alkene petroleum naphtha etherification method for the present invention.
Mark lists as follows among the figure:
1. hydrogen; 2. contain the alkene petroleum naphtha; 3. first transferpump; 4. first mixing tank; 5. selective hydrogenation device; 6. methyl alcohol; 7. second transferpump; 8. second mixing tank; 9. etherification reaction of hydro-refining device; 10. condenser; 11. holding tank.
Embodiment
The present invention is described in further detail below in conjunction with drawings and Examples.Should be pointed out that following embodiment is described further a kind of alkene petroleum naphtha etherification method that contains provided by the invention, so that those skilled in the art understand the present invention, but not thereby limiting the invention.
As shown in the figure, hydrogen 1 and olefine contained gasoline 2 enter first mixing tank 4 behind first transferpump 3, enter the selective hydrogenation device 5 that non-precious metal catalyst is housed then, carry out hydrogenation and remove diene and the reaction of dealkalize nitrogen, i.e. first section selective hydrogenation; Mixture comes out afterwards and the methyl alcohol 6 through second transferpump 7 mixes in second mixing tank 8, enters etherification reaction of hydro-refining device 9 again, i.e. the subordinate phase etherification reaction of hydro-refining; Through condenser 10, enter holding tank 11 at last afterwards.Hydrogen returns and recycles, and the etherified gasoline that obtains from holding tank 11 can reconcile into the clean gasoline of standard with other distillate.Accompanying drawing only is a reference drawing, and wherein selective hydrogenation device 5 and etherification reaction of hydro-refining device 9 are not limited only to fixed-bed reactor, also can be expanded bed reactor, and feeding manner also is not limited to the downstream formula, can be the upstream formula.
The invention is characterized in and adopt a kind of difunctional non-precious metal catalyst, diene and alkali nitrogen in the while selectively removing olefine contained gasoline, two technological processs of existing hydrogenation respectively being taken off diene and removing alkali nitrogen are combined into one section, thereby shortened whole flow process, make conventional three sections etherification technologies become two sections, not only can greatly save and build the facility investment expense, and greatly save the production operation expense.
Difunctional non-precious metal catalyst is non-noble metal copper-base composite oxidate among the present invention.
Use after difunctional copper-based catalysts can reduce among the present invention, also can directly use without reduction or sulfidizing.
The excellent properties that difunctional non-precious metal catalyst had among the present invention is applied in and contains in the alkene petroleum naphtha etherification procedure, it is identical with ether hydro-etherification two-stage reaction processing condition that hydrogenation dealkalize nitrogen takes off diene, the required hydrogen of etherification reaction of hydro-refining process section is from the hydrogen of one section reaction process, thereby having made things convenient for whole technological operation, production cost is low.
In etherification reaction technology section of the present invention, the hydrogen of ether hydro-etherification is exactly the hydrogen from one section reaction process.
Reaction process condition gentleness of the present invention.The temperature of first section reaction process section is 30-100 ℃, is preferably 40-80 ℃; Reaction pressure is 0.5-2.0MPa, is preferably 0.8-1.5MPa; The liquid air speed is 1.0-4.0h
-1, be preferably 1.5-3.0h
-1Hydrogen to oil volume ratio is 50-500, is preferably 80-300.Second section reaction process condition that etherification reaction of hydro-refining adopted with first section the reaction process condition that selective hydrogenation adopted is identical or basic identical or gap is little.
Contain the gasoline that the alkene petroleum naphtha can be a different sources among the present invention, as catalytically cracked gasoline, coker gasoline and pyrolysis gasoline.
Among the embodiment, not marked per-cent is weight percentage.
Embodiments of the invention are as follows:
Embodiment 1:
The light fractions of FCC naphtha (＜75 ℃) that will contain 2.66% isoprene with enter selective hydrogenation device 5 in the accompanying drawing after hydrogen mixes, the non-precious metal catalyst that filling is handled through reduction in the selective hydrogenation device 5, temperature of reaction is 47 ℃, reaction pressure is 1.1MPa, and the liquid air speed is 2.0h
-1, hydrogen to oil volume ratio is 130, does not contain diene from the product that selective hydrogenation device 5 comes out, isomeric olefine increases by 2.91%.
Embodiment 2:
The light fractions of FCC naphtha (＜75 ℃) that will contain 2.66% isoprene with enter selective hydrogenation device 5 in the accompanying drawing after hydrogen mixes, the non-precious metal catalyst that filling is handled through reduction in the selective hydrogenation device 5, temperature of reaction is 64 ℃, reaction pressure is 1.1MPa, and the liquid air speed is 2.0h
-1, hydrogen to oil volume ratio is 130, does not contain diene from the product that selective hydrogenation device 5 comes out, isomeric olefine increases by 0.66%.
Embodiment 3:
The light fractions of FCC naphtha (＜75 ℃) that will contain 2.66% isoprene with enter selective hydrogenation device 5 in the accompanying drawing after hydrogen mixes, the non-precious metal catalyst that filling is handled through reduction in the selective hydrogenation device 5, temperature of reaction is 78 ℃, reaction pressure is 1.1MPa, and the liquid air speed is 2.0h
-1, hydrogen to oil volume ratio is 130, does not contain diene from the product that selective hydrogenation device 5 comes out, isomeric olefine increases by 0.78%.
Embodiment 4:
The light fractions of FCC naphtha (＜75 ℃) that will contain 2.66% isoprene with enter selective hydrogenation device 5 in the accompanying drawing after hydrogen mixes, the non-precious metal catalyst that filling is handled through reduction in the selective hydrogenation device 5, temperature of reaction is 85 ℃, reaction pressure is 1.1MPa, and the liquid air speed is 2.0h
-1, hydrogen to oil volume ratio is 130, does not contain diene from the product that selective hydrogenation device 5 comes out, isomeric olefine increases by 0.38%.
Embodiment 5:
The light fractions of FCC naphtha (＜75 ℃) that will contain 2.66% isoprene with enter selective hydrogenation device 5 in the accompanying drawing after hydrogen mixes, the non-precious metal catalyst that filling is handled through reduction in the selective hydrogenation device 5, temperature of reaction is 47 ℃, reaction pressure is 1.4MPa, and the liquid air speed is 2.0h
-1, hydrogen to oil volume ratio is 130, does not contain diene from the product that selective hydrogenation device 5 comes out, isomeric olefine increases by 2.12%.
Embodiment 6:
The light fractions of FCC naphtha (＜75 ℃) that will contain 2.66% isoprene with enter selective hydrogenation device 5 in the accompanying drawing after hydrogen mixes, the non-precious metal catalyst that filling is handled through reduction in the selective hydrogenation device 5, temperature of reaction is 47 ℃, reaction pressure is 0.8MPa, and the liquid air speed is 2.0h
-1, hydrogen to oil volume ratio is 130, does not contain diene from the product that selective hydrogenation device 5 comes out, isomeric olefine increases by 2.53%.
Embodiment 7:
The light fractions of FCC naphtha (＜75 ℃) that will contain 2.66% isoprene with enter selective hydrogenation device 5 in the accompanying drawing after hydrogen mixes, the non-precious metal catalyst that filling is handled through reduction in the selective hydrogenation device 5, temperature of reaction is 47 ℃, reaction pressure is 1.1MPa, and the liquid air speed is 2.5h
-1, hydrogen to oil volume ratio is 130, does not contain diene from the product that selective hydrogenation device 5 comes out, isomeric olefine increases by 2.30%.
Embodiment 8:
The light fractions of FCC naphtha (＜75 ℃) that will contain 2.66% isoprene with enter selective hydrogenation device 5 in the accompanying drawing after hydrogen mixes, the non-precious metal catalyst that filling is handled through reduction in the selective hydrogenation device 5, temperature of reaction is 47 ℃, reaction pressure is 1.1MPa, and the liquid air speed is 3.0h
-1, hydrogen to oil volume ratio is 130, does not contain diene from the product that selective hydrogenation device 5 comes out, isomeric olefine increases by 1.31%.
Embodiment 9:
The light fractions of FCC naphtha (＜75 ℃) that will contain 2.66% isoprene with enter selective hydrogenation device 5 in the accompanying drawing after hydrogen mixes, the non-precious metal catalyst that filling is handled through reduction in the selective hydrogenation device 5, temperature of reaction is 47 ℃, reaction pressure is 1.1MPa, and the liquid air speed is 2.0h
-1, hydrogen to oil volume ratio is 85, does not contain diene from the product that selective hydrogenation device 5 comes out, isomeric olefine increases by 2.11%.
Embodiment 10:
The light fractions of FCC naphtha (＜75 ℃) that will contain 2.66% isoprene with enter selective hydrogenation device 5 in the accompanying drawing after hydrogen mixes, the non-precious metal catalyst that filling is handled through reduction in the selective hydrogenation device 5, temperature of reaction is 47 ℃, reaction pressure is 1.1MPa, and the liquid air speed is 2.0h
-1, hydrogen to oil volume ratio is 200, does not contain diene from the product that selective hydrogenation device 5 comes out, isomeric olefine increases by 2.50%.
Embodiment 11:
The light fractions of FCC naphtha (＜75 ℃) that will contain 2.66% isoprene with enter selective hydrogenation device 5 in the accompanying drawing after hydrogen mixes, the non-precious metal catalyst that filling is handled through reduction in the selective hydrogenation device 5, temperature of reaction is 47 ℃, reaction pressure is 1.1MPa, and the liquid air speed is 2.0h
-1, hydrogen to oil volume ratio is 130, behind the successive reaction 100h, does not still contain diene from the product that selective hydrogenation device 5 comes out, isomeric olefine increases by 2.17%.
Embodiment 12:
The light fractions of FCC naphtha (＜75 ℃) that will contain 2.66% isoprene with enter selective hydrogenation device 5 in the accompanying drawing after hydrogen mixes, the non-precious metal catalyst that filling is handled through reduction in the selective hydrogenation device 5, temperature of reaction is 47 ℃, reaction pressure is 1.1MPa, and the liquid air speed is 2.0h
-1, hydrogen to oil volume ratio is 130, the 1.4ppm of alkali nitrogen from raw material reduces to 0.2ppm from the product that selective hydrogenation device 5 comes out.
Embodiment 13:
The light fractions of FCC naphtha (＜75 ℃) that will contain 2.66% isoprene with enter selective hydrogenation device 5 in the accompanying drawing after hydrogen mixes, the non-precious metal catalyst that filling is handled without reduction in the selective hydrogenation device 5, temperature of reaction is 47 ℃, reaction pressure is 1.1MPa, and the liquid air speed is 2.0h
-1, hydrogen to oil volume ratio is 130, does not contain diene from the product that selective hydrogenation device 5 comes out, isomeric olefine increases by 2.15%.
Embodiment 14:
The coker gasoline lighting end (＜75 ℃) that will contain 2.66% isoprene with enter selective hydrogenation device 5 in the accompanying drawing after hydrogen mixes, the non-precious metal catalyst that filling is handled without reduction in the selective hydrogenation device 5, temperature of reaction is 47 ℃, reaction pressure is 1.1MPa, and the liquid air speed is 2.0h
-1, hydrogen to oil volume ratio is 130, does not contain diene from the product that selective hydrogenation device 5 comes out, and isomeric olefine increases by 2.10%, and the alkali nitrogen content is 0.18ppm.
Embodiment 15:
The product that first section reaction process comes out with enter etherification reaction of hydro-refining device 9 in the accompanying drawing after methyl alcohol mixed in by volume 7: 1, filling sulfonic acid type strong acid cation exchange resin catalyst in the etherification reaction of hydro-refining device 9, temperature of reaction is 60 ℃, other condition is with the first segment process condition, contain ether 18.0% in the etherified gasoline product that produces, C5 isomeric olefine transformation efficiency is 58.0%, and C6 isomeric olefine transformation efficiency is 28.0%, and the productive rate of tert amyl methyl ether(TAME) is 54.8%.
Embodiment 16:
The pyrolysis gasoline lighting end (＜75 ℃) that will contain 3% isoprene with enter selective hydrogenation device 5 in the accompanying drawing after hydrogen mixes, the non-precious metal catalyst that filling is handled without reduction in the selective hydrogenation device 5, temperature of reaction is 47 ℃, reaction pressure is 1.1MPa, and the liquid air speed is 2.0h
-1, hydrogen to oil volume ratio is 130, does not contain diene from the product that selective hydrogenation device 5 comes out, and isomeric olefine increases by 2.9%, and the alkali nitrogen content is 0.18ppm.
Embodiment 17:
The pyrolysis gasoline lighting end (＜75 ℃) that will contain 1.5% isoprene with enter selective hydrogenation device 5 in the accompanying drawing after hydrogen mixes, the non-precious metal catalyst that filling is handled without reduction in the selective hydrogenation device 5, temperature of reaction is 47 ℃, reaction pressure is 1.1MPa, and the liquid air speed is 2.0h
-1, hydrogen to oil volume ratio is 130, does not contain diene from the product that selective hydrogenation device 5 comes out, and isomeric olefine increases by 1.1%, and the alkali nitrogen content is 0.19ppm.
Claims (9)
1. contain alkene petroleum naphtha etherification method, comprise and remove diene, remove alkali nitrogen and carry out etherification reaction of hydro-refining containing the alkene petroleum naphtha, it is characterized in that: first section is combined into one section and carries out selective hydrogenation by adopting difunctional non-precious metal catalyst will remove diene and removing alkali nitrogen, second section is heterogeneous activity alkene and methyl alcohol carries out etherification reaction of hydro-refining, produces etherified gasoline.
2. the alkene petroleum naphtha etherification method that contains according to claim 1, it is characterized in that: described difunctional non-precious metal catalyst is a copper-base composite oxidate.
3. the alkene petroleum naphtha etherification method that contains according to claim 2 is characterized in that: described copper-base composite oxidate catalyzer can make the section of winning selective hydrogenation remove diene and reach more than 98% (weight ratio) and more than the dealkalize nitrogen 80% (weight ratio).
4. the alkene petroleum naphtha etherification method that contains according to claim 2 is characterized in that: described copper-base composite oxidate catalyzer, and without reduction or sulfidizing, participate in first section directly and carry out selective hydrogenation.
5. the described alkene petroleum naphtha that contains is catalytic cracking petroleum naphtha or light coker naphtha or the thermo-cracking petroleum naphtha of doing less than 80 ℃.
6. the alkene petroleum naphtha etherification method that contains according to claim 1 and 2 is characterized in that: described first section selective hydrogenation is identical with described second section reaction process condition that etherification reaction of hydro-refining adopted.
7. the alkene petroleum naphtha etherification method that contains according to claim 6, it is characterized in that: described identical reaction process condition is: 30～100 ℃ of temperature of reaction, pressure 0.5～2.0Mpa, liquid air speed 1.0～4.0h
-1, hydrogen to oil volume ratio 50～500.
8. the alkene petroleum naphtha etherification method that contains according to claim 7, it is characterized in that: described identical reaction process condition is: 40～80 ℃ of temperature of reaction, pressure 0.8～1.5Mpa, liquid air speed 1.5～3.0h
-1, hydrogen to oil volume ratio 80～300.
9. the alkene petroleum naphtha etherification method that contains according to claim 8, it is characterized in that: the described alkene petroleum naphtha that contains is through behind described first section selective hydrogenation, diene content is less than 0.1% (weight ratio), the alkali nitrogen content is less than 0.2ppm, and the isomeric olefine of tool etherification activity increases by 0.38～2.91% simultaneously; In second section, use the sulfonic acid type strong acid cation exchange resin catalyst, through after first section processing contain alkene petroleum naphtha and methanol mixed after carry out etherification reaction of hydro-refining, C5 activity isomerism olefin conversion is greater than 55% (weight ratio) in the etherified gasoline that produces, C6 activity isomerism olefin conversion is greater than 25% (weight ratio), and the ether massfraction is greater than 15%.
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| CN 200410003406 CN1654602A (en) | 2004-02-13 | 2004-02-13 | Etherification method for alkene contained light gasoline |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102618329A (en) * | 2011-01-31 | 2012-08-01 | 北京安耐吉能源工程技术有限公司 | Gasoline processing method |
| CN108949228A (en) * | 2017-05-19 | 2018-12-07 | 中国石油化工股份有限公司 | Produce the method and system of clean gasoline |
| CN108949229A (en) * | 2017-05-19 | 2018-12-07 | 中国石油化工股份有限公司 | Produce the method and system of clean gasoline |
| CN108949226A (en) * | 2017-05-19 | 2018-12-07 | 中国石油化工股份有限公司 | Produce the method and system of clean gasoline |
-
2004
- 2004-02-13 CN CN 200410003406 patent/CN1654602A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102618329A (en) * | 2011-01-31 | 2012-08-01 | 北京安耐吉能源工程技术有限公司 | Gasoline processing method |
| CN108949228A (en) * | 2017-05-19 | 2018-12-07 | 中国石油化工股份有限公司 | Produce the method and system of clean gasoline |
| CN108949229A (en) * | 2017-05-19 | 2018-12-07 | 中国石油化工股份有限公司 | Produce the method and system of clean gasoline |
| CN108949226A (en) * | 2017-05-19 | 2018-12-07 | 中国石油化工股份有限公司 | Produce the method and system of clean gasoline |
| CN108949226B (en) * | 2017-05-19 | 2020-10-27 | 中国石油化工股份有限公司 | Method and system for producing clean gasoline |
| CN108949229B (en) * | 2017-05-19 | 2020-10-27 | 中国石油化工股份有限公司 | Method and system for producing clean gasoline |
| CN108949228B (en) * | 2017-05-19 | 2020-10-27 | 中国石油化工股份有限公司 | Method and system for producing clean gasoline |
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