CN103396833A - Method of producing gasoline for car from synthetic naphtha - Google Patents
Method of producing gasoline for car from synthetic naphtha Download PDFInfo
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- CN103396833A CN103396833A CN201310370081XA CN201310370081A CN103396833A CN 103396833 A CN103396833 A CN 103396833A CN 201310370081X A CN201310370081X A CN 201310370081XA CN 201310370081 A CN201310370081 A CN 201310370081A CN 103396833 A CN103396833 A CN 103396833A
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Abstract
The invention discloses a method of producing gasoline for a car from naphtha. The method comprises the following steps: feeding the naphtha which is synthesized by a coal indirect liquefaction process into a fractionating tower for fractioning, wherein C5-C6 which is fractioned out by a tower line I is fed to a normal paraffin hydro-isomerization process for being treated; and feeding fraction which is not lower than 80 DEG C and obtained at the tower bottom to a fixed-bed catalytic reforming process for being treated; and mixing and feeding the oil, which is obtained by the normal paraffin hydro-isomerization process and the fixed-bed catalytic reforming process, into a degassing tower for degassing to obtain a car gasoline component at the tower bottom. According to the method of producing gasoline for a car from naphtha disclosed by the invention, the fixed-bed catalytic reforming process is adopted for converting C7-C9 alkane not lower than 80 DEG C in the synthetic naphtha into aromatic hydrocarbon; and the normal paraffin hydro-isomerization process is adopted for realizing the hydrocarbon isomerization of the C5-C6 normal paraffin in the synthetic naphtha. And therefore, the octane value of the synthetic naphtha is effectively improved, and the car gasoline with indexes reaching National Gasoline Quality Standard-VI is produced.
Description
One, technical field
The invention belongs to the motor spirit production technical field, be specifically related to a kind of method of producing motor spirit with the synthetic petroleum naphtha of ICL for Indirect Coal Liquefaction technique.
Two, background technology
In China's ICL for Indirect Coal Liquefaction production technology, synthetic naphtha is the synthetic product of cold-trap oil after hydrogenation technique, is that one of main products in synthetic oil is produced in gelatin liquefaction, and its output accounts for 22% of product coal synthetic oil total recovery.Owing in coal oil-producing technique process, having generated a large amount of single diolefins, this part alkene is changing into normal paraffin after hydrogenation is saturated, and in the product synthetic naphtha, normal paraffin content is generally in 85% left and right.The octane value of normal paraffin is lower, and the octane value of nC6 (RON) is that the octane value (RON) of 26, nC7 is 0.The octane value that a large amount of existence of normal paraffin affect synthetic naphtha, lower than 40, can't dispatch from the factory as gasoline products, and manufacturing enterprise has produced negative impact to the coal liquefaction.Do not have at present ripe production technique can solve the too low problem of synthetic naphtha octane value both at home and abroad.The synthetic naphtha octane value is too low can not, as the motor spirit composition problems, become the bottleneck that coal liquefaction enterprise produces.Objectively the existing coal liquefaction of China enterprise mostly concentrates the remote districts that are based upon rich coal resources, and communications and transportation difficulty, petrochemical complex derived product scarce capacity can not be given prominence to as this negative issue of motor spirit component is more aobvious synthetic naphtha.
Three, summary of the invention
The purpose of this invention is to provide a kind of method for preparing motor spirit with ICL for Indirect Coal Liquefaction technique synthetic naphtha, adopt the method can effectively improve the octane value of synthetic naphtha, solve the too low problem of synthetic naphtha octane value, produce the motor spirit that index reaches " national gasoline quality standard-VI ", solve coal liquefaction enterprise production technology bottleneck problem, improve coal liquefaction enterprise whole economic efficiency.
For achieving the above object, the technical solution used in the present invention is: the method comprises the steps: ICL for Indirect Coal Liquefaction technique synthetic naphtha is sent into to the separation column fractionation, and tower top deviates from≤component of C4; The C5-C6 that tower one line fractionates out sends into normal paraffin hydro-isomerization metallization processes and processes; At the bottom of tower, obtain >=80 ℃ of cuts send into the fixed-bed catalytic reforming process and process; After the generation oil that finally normal paraffin hydro-isomerization metallization processes and fixed-bed catalytic reforming process is obtained mixes, send into degassing tower degassed, at the bottom of tower, obtain the motor spirit component.
The inventive method improves the octane value of synthetic naphtha, is in the situation that carbon number distribution constant realization the substantially.Adopt the fixed-bed catalytic reforming process by in synthetic naphtha >=the C7-C9 alkane of 80 ℃ changes into aromatic hydrocarbons; Adopt normal paraffin hydro-isomerization metallization processes to realize the hydrocarbon isomerization of the C5-C6 normal paraffin in synthetic naphtha.Effectively improve the octane value of synthetic naphtha, produce the motor spirit that index reaches " national gasoline quality standard-VI ", solve coal liquefaction enterprise production technology bottleneck problem, improve coal liquefaction enterprise whole economic efficiency.
The present invention has following features:
1, adopted front fractionation process first synthetic naphtha to be isolated to C5-C6 cut and >=80 ℃ of cuts, and normal paraffin hydro-isomerization metallization processes and fixed-bed catalytic reformation combination process have been adopted targetedly, respectively C5-C6 cut and >=80 ℃ of cuts are carried out to normal alkane isomerization and catalytic reforming aromatization, the octane value active principle is kept simultaneously in making synthetic naphtha, conflicting composition is changed into respectively to the component that corresponding octane value is higher, thereby the whole octane value of synthetic naphtha is improved, reaches the motor spirit quality standard.
2, the inventive method adopts the selectivity isomerization technique for the nC5-nC6 cut; not only solve nC5-nC6 and affected the problem that octane value is low; and due to isomerization gasoline susceptibility little (RON and MON only differ 1.5 units usually), the octane value that adopts normal paraffin hydro-isomerization metallization processes to improve gasoline has realistic meaning to strengthen environmental protection.
4, due to present reforming reaction, can only improve the quality of 80-180 ℃ of part petroleum naphtha, and normal paraffin hysomer process adjustments front end≤80 ℃ gasoline component octane values, the generation oil of catalytic reforming and isomerization combination process, the gasoline boiling range is had more reasonably and distribute, thereby improve petrolic startability and improve active power.
5, ICL for Indirect Coal Liquefaction technique synthetic naphtha further is reduced through processing rear impurity content, and oil quality all reaches state's IV gasoline standard requirement.
Four, embodiment
The present embodiment adopts main physico-chemical property such as the following table of ICL for Indirect Coal Liquefaction technique synthetic naphtha:
The concrete steps of the inventive method are as follows
1. raw material pretreatment process:
ICL for Indirect Coal Liquefaction technique synthetic naphtha is sent into to separation column, and tower top deviates from≤component of C4, and tower one line fractionates out the C5-C6 cut as normal paraffin normal paraffin hysomer process feeds, at the bottom of tower, obtain >=80 ℃ of cuts are as the charging of fixed bed reforming process.
2. normal paraffin hydro-isomerization metallization processes:
The C5-C6 cut that tower one line is fractionated out and hydrogen Hybrid Heating, after 250-270 ℃ of temperature of reaction, enter the fixed bed isomerization reactor and under catalyst action, carry out isomerization reaction, obtain generating oil.
The catalyzer that above-mentioned normal paraffin hydro-isomerization metallization processes adopts is domestic FI-15 alkane isomerization catalyst.This catalyzer is take molecular sieve as support of the catalyst, and the Ni-Mo metal is Primary Catalysts and promotor.The catalyzer Main Function is the isomerization that realizes the nC5-nC6 normal paraffin, for prevent from having cracking side-reaction in conversion process, occurs, and reaction process need to be carried out facing under the hydrogen state, and because the hydrogen dividing potential drop does not need too highly, the reactive hydrogen oil ratio requires lower.
Above-mentioned normal paraffin hysomer technological reaction condition is:
Temperature (℃): 250-270 pressure (MPa): 1.5-2.0
Air speed (H
-1): 0.2-1.8 hydrogen-oil ratio (v/v): (1.5-5)/1
3. fixed-bed catalytic reforming process:
By at the bottom of tower, obtaining >=after 80 ℃ of cuts are heated to 470-520 ℃ of temperature of reaction and the hot hydrogen of relevant temperature mix, enter one section fixed-bed catalytic reforming reactor and carry out catalytic reforming reaction, after one section reforming reaction product of gained and hydrogen mixture heating, enter two sections fixed-bed catalytic reforming reactors and carry out the second segment catalytic reforming reaction, after two sections reformates of gained and hydrogen mixture heating, enter again the three-section fixed-bed catalytic reforming reactor and carry out reforming reaction, above-mentioned reaction all moves under catalyst action, finally obtain generating oil.
Above-mentioned fixed-bed catalytic reforming reactor quantity is four, three reactor operation during normal production run, and one is used during for catalyst regeneration.
Above-mentioned fixed-bed catalytic reforming process process is the strong endothermic reaction process, in reaction process because of endothermic heat of reaction, temperature drop by a relatively large margin occurs, the capacity scale of reactor is subject to the temperature drop impact can not be excessive, between each fixed-bed catalytic reforming reactor, heating facility to be set, guaranteed that heat supply is sufficient flexible with the reactor inlet temperature adjustment, meets each reactor catalyst bed temperature all moves under required state demand.
The catalyzer that above-mentioned fixed-bed catalytic reforming process adopts is domestic PS-VI precious metal reforming catalyst, and this catalyzer is take the 5A molecular sieve as carrier, and platinum, iridium precious metal are Primary Catalysts and the promotor of reactive behavior.
The reaction conditions of above-mentioned fixed-bed catalytic reforming process is:
Temperature (℃): 470-520 pressure (MPa): 0.3-1.3
Air speed (H
-1): 1-3.5 hydrogen-oil ratio (v/v): (800-1300)/1
4. generate oily degasification technique:
Normal paraffin hydro-isomerization metallization processes and fixed-bed catalytic reforming process generate after oil mixes and enter the degassing tower middle part, owing in catalytic reforming and isomerization reaction, with scission reaction, occurring, in tower, by top, deviate from non-condensable gas and solution gas, the motor spirit component carrying device at the bottom of tower after degassed.
Reaction generates physico-chemical property such as the following table of oil:
Reaction generates oil and contrasts as following table with " national gasoline quality standard-VI " leading indicator:
As can be known from the above table, indirect liquefaction technique synthetic naphtha is after normal paraffin hydro-isomerization metallization processes and the reaction of fixed-bed catalytic reforming process, foreign matter content reduces, octane value is improved significantly, quality product has reached " national gasoline quality standard-VI " gasoline main standard index, the gasoline component octane value susceptibility that particularly passes through normal paraffin hydro-isomerization metallization processes is little, the gasoline of producing is more reasonable on fraction distribution, can improve the startability of engine.
Claims (7)
1. a synthetic naphtha is produced the method for motor spirit, and the method comprises the steps: ICL for Indirect Coal Liquefaction technique synthetic naphtha is sent into to the separation column fractionation, and tower top deviates from≤component of C4; The C5-C6 that tower one line fractionates out sends into normal paraffin hydro-isomerization metallization processes and processes; At the bottom of tower, obtain >=80 ℃ of cuts send into the fixed-bed catalytic reforming process and process; After the generation oil that finally normal paraffin hydro-isomerization metallization processes and fixed-bed catalytic reforming process is obtained mixes, send into degassing tower degassed, at the bottom of tower, obtain the motor spirit component.
2. a kind of synthetic naphtha according to claim 1 is produced the method for motor spirit, and it is characterized in that: the concrete steps of the method are:
1. raw material pretreatment process:
ICL for Indirect Coal Liquefaction technique synthetic naphtha is sent into to separation column, and tower top deviates from≤component of C4, and tower one line fractionates out the C5-C6 cut as normal paraffin normal paraffin hysomer process feeds, at the bottom of tower, obtain >=80 ℃ of cuts are as the charging of fixed bed reforming process;
2. normal paraffin hydro-isomerization metallization processes:
The C5-C6 cut that tower one line is fractionated out and hydrogen Hybrid Heating, after 250-270 ℃ of temperature of reaction, enter the fixed bed isomerization reactor and under catalyst action, carry out isomerization reaction, obtain generating oil;
3. fixed-bed catalytic reforming process:
By at the bottom of tower, obtaining >=after 80 ℃ of cuts are heated to 470-520 ℃ of temperature of reaction and the hot hydrogen of relevant temperature mix, enter one section fixed-bed catalytic reforming reactor and carry out catalytic reforming reaction, after one section reforming reaction product of gained and hydrogen mixture heating, enter two sections fixed-bed catalytic reforming reactors and carry out the second segment catalytic reforming reaction, after two sections reformates of gained and hydrogen mixture heating, enter again the three-section fixed-bed catalytic reforming reactor and carry out reforming reaction, above-mentioned reaction all moves under catalyst action, finally obtain generating oil;
4. generate oily degasification technique:
Normal paraffin hydro-isomerization metallization processes and fixed-bed catalytic reforming process generate after oil mixes and enter the degassing tower middle part, owing in catalytic reforming and isomerization reaction, with scission reaction, occurring, in tower, by top, deviate from non-condensable gas and solution gas, the motor spirit component carrying device at the bottom of tower after degassed.
3. a kind of synthetic naphtha according to claim 1 and 2 is produced the method for motor spirit, and it is characterized in that: the catalyzer that described normal paraffin hydro-isomerization metallization processes adopts is the FI-15 alkane isomerization catalyst.
4. a kind of synthetic naphtha according to claim 1 and 2 is produced the method for motor spirit, and it is characterized in that: described normal paraffin hysomer technological reaction condition is:
Temperature (℃): 250-270 pressure (MPa): 1.5-2.0
Air speed (H
-1): 0.2-1.8 hydrogen-oil ratio (v/v): (1.5-5)/1.
5. a kind of synthetic naphtha according to claim 1 and 2 is produced the method for motor spirit, it is characterized in that: the catalyzer that described fixed-bed catalytic reforming process adopts is PS-VI precious metal reforming catalyst.
6. a kind of synthetic naphtha according to claim 1 and 2 is produced the method for motor spirit, and it is characterized in that: the reaction conditions of described fixed-bed catalytic reforming process is:
Temperature (℃): 470-520 pressure (MPa): 0.3-1.3
Air speed (H
-1): 1-3.5 hydrogen-oil ratio (v/v): (800-1300)/1.
7. a kind of synthetic naphtha according to claim 2 is produced the method for motor spirit, it is characterized in that: step 3. in fixed-bed catalytic reforming reactor quantity be four, three reactor operation during normal production run, one is used during for catalyst regeneration.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104711017A (en) * | 2013-12-17 | 2015-06-17 | Ifp新能源公司 | Catalytic reforming process |
| CN105861043A (en) * | 2016-06-14 | 2016-08-17 | 洛阳市科创石化科技开发有限公司 | Technological method for producing high-octane gasoline through naphtha |
| CN111925822A (en) * | 2020-07-17 | 2020-11-13 | 中科合成油工程有限公司 | Method for preparing high-octane gasoline and device for implementing method |
| CN113234471A (en) * | 2021-06-24 | 2021-08-10 | 中国石油化工股份有限公司 | Naphtha reforming processing optimization process |
| CN113956900A (en) * | 2021-11-04 | 2022-01-21 | 辽宁北方华锦五洲化工工程设计有限公司 | Based on C5C6Naphtha deep processing method and device for isomerization device |
| CN115717088A (en) * | 2021-08-27 | 2023-02-28 | 中国石油化工股份有限公司 | No. 75 coal-based aviation gasoline composition and preparation method thereof |
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| US4747933A (en) * | 1987-03-27 | 1988-05-31 | Uop Inc. | Isomerization unit with integrated feed and product separation facilities |
| CN101397230A (en) * | 2007-09-28 | 2009-04-01 | 中国石油化工股份有限公司 | C5 and/or C6 alkane isomerization process |
| CN101570698A (en) * | 2008-04-29 | 2009-11-04 | 中国石油化工股份有限公司 | Method for catalyzing and transforming naphtha |
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2013
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| US4747933A (en) * | 1987-03-27 | 1988-05-31 | Uop Inc. | Isomerization unit with integrated feed and product separation facilities |
| CN101397230A (en) * | 2007-09-28 | 2009-04-01 | 中国石油化工股份有限公司 | C5 and/or C6 alkane isomerization process |
| CN101570698A (en) * | 2008-04-29 | 2009-11-04 | 中国石油化工股份有限公司 | Method for catalyzing and transforming naphtha |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104711017A (en) * | 2013-12-17 | 2015-06-17 | Ifp新能源公司 | Catalytic reforming process |
| CN104711017B (en) * | 2013-12-17 | 2018-10-19 | Ifp 新能源公司 | Catforming |
| CN105861043A (en) * | 2016-06-14 | 2016-08-17 | 洛阳市科创石化科技开发有限公司 | Technological method for producing high-octane gasoline through naphtha |
| CN111925822A (en) * | 2020-07-17 | 2020-11-13 | 中科合成油工程有限公司 | Method for preparing high-octane gasoline and device for implementing method |
| CN113234471A (en) * | 2021-06-24 | 2021-08-10 | 中国石油化工股份有限公司 | Naphtha reforming processing optimization process |
| CN115717088A (en) * | 2021-08-27 | 2023-02-28 | 中国石油化工股份有限公司 | No. 75 coal-based aviation gasoline composition and preparation method thereof |
| CN115717088B (en) * | 2021-08-27 | 2024-05-17 | 中国石油化工股份有限公司 | No. 75 coal-based aviation gasoline composition and preparation method thereof |
| CN113956900A (en) * | 2021-11-04 | 2022-01-21 | 辽宁北方华锦五洲化工工程设计有限公司 | Based on C5C6Naphtha deep processing method and device for isomerization device |
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