CN110759802B - Simultaneous production process of 2-methyl-butene-1 and 2-methyl-butene-2 - Google Patents
Simultaneous production process of 2-methyl-butene-1 and 2-methyl-butene-2 Download PDFInfo
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Abstract
A process for simultaneously producing 2-methyl-butene-1 and 2-methyl-butene-2, belonging to the technical field of fine chemical intermediates. The method is characterized in that pure isoprene is used as a raw material, a fixed bed reactor and a rectifying tower are combined, the selectivity and the reaction depth of selective hydrogenation reaction are improved by means of QSH-06 catalyst matched with measures for controlling isoprene conversion rate, reaction conditions and hydrogen-diene ratio, 2-methyl-1-butene is prevented from being isomerized and generated, reacted materials enter the rectifying tower, and the unreacted isoprene and the mixture of 2-methyl-1-butene and 2-methyl-2-butene are extracted from the side line of the rectifying tower. The 2-methyl-2-butylene product and the 2-methyl-1-butylene product with higher purity can be obtained simultaneously after rectification.
Description
Technical Field
A process for simultaneously producing 2-methyl-butene-1 and 2-methyl-butene-2, belonging to the technical field of fine chemical intermediates.
Background
Tert-pentene is a colorless, volatile liquid with an unpleasant odor, and is usually a mixture of 2-methyl-1-butene and 2-methyl-2-butene. Today, the demand for green chemicals is rapidly increasing. Wherein the refinery catalytically cracked C5 fraction contains about 8% of tertiary pentenes and the cracked C5 fraction also contains small amounts of tertiary pentenes.
The tertiary amylene product is a mixture of 2-methyl-1-butene and 2-methyl-2-butene, the production of the tertiary amylene in the industry at present generally adopts mixed carbon five components to etherify to generate TAME, then the methyl tertiary amyl ether is cracked at high temperature, methanol contained in the cracked product is removed by washing, and the high-purity tertiary amylene is obtained after rectification. Since there is a demand for 2-methyl-butene-1 and 2-methyl-2-butene products having higher purity, respectively, on the market, 2-methyl-1-butene is produced by willey Organics inc. U.S. Biddle Sawyer Co. And Willey Organics Inc. produce 2-methyl-2-butene. In China, only Shanghai Shiziji, zibo Co-carbon and other companies produce 2-methyl-2-butene. The traditional process route is as follows: preparing TAME by etherification of five carbon components, high temperature decomposition, washing with water to remove methanol, rectification and separation, 2-methyl-butene-1 and 2-methyl-2-butene are respectively obtained. Has the defects of long process flow, complex process, high energy consumption and the like.
China CN20121036394 provides a selective hydrogenation method of crude isoamylene, which is to carry out hydrogenation reaction on a crude isoamylene fraction material through a fixed bed catalyst bed layer in the presence of a mixed gas of nitrogen and hydrogen. The hourly space velocity of the liquid is controlled to be 4.0 to 12.0 h -1 Controlling the system pressure to be 0.5 to 2.0 MPa, controlling the reactant feeding temperature to be 30 to 80 ℃, and controlling the molar ratio of hydrogen to isoprene in the crude isoamylene fraction to be 1 to 1.5:1, the volume percentage of the nitrogen in the mixed gas of the nitrogen and the hydrogen is 70 to 95 percent. According to the method, pure hydrogen is changed into mixed gas of nitrogen and hydrogen during hydrogenation, isoprene in the crude isoamylene fraction is converted into isoamylene under the premise that other hydrogenation conditions are not changed, the isomerization reaction of 1-pentene is effectively inhibited, and the content of 1-pentene in the hydrogenated crude isoamylene is increased.
In summary, the current industrial production and the production of the tert-pentene product in various documents generally adopt the process flow of C5 etherification-ether hydrolysis-water washing of methanol-rectification-isomerization, have the defects of long process flow, complex reaction process, difficult obtainment of high-purity (generally about 94% in the current industry) 2-methyl-2-butene product and 2-methyl-1-butene product, and the like, and are difficult to meet the requirements of industrial production.
Disclosure of Invention
The technical problem to be solved by the invention is as follows: overcomes the defects of the prior art and provides a process for simultaneously producing 2-methyl-butene-1 and 2-methyl-butene-2 with simple process flow and high product purity.
The technical scheme adopted by the invention for solving the technical problems is as follows: the process for simultaneously producing 2-methyl-butene-1 and 2-methyl-butene-2 is characterized by comprising the following preparation steps:
1) Hydrogen and isoprene the ratio of diene/diene is 1.07 to 1.12:1, then entering a fixed bed hydrogenation reactor, carrying out selective hydrogenation reaction on isoprene under the action of QSH-06 catalyst, the pressure in the fixed bed hydrogenation reactor is 0.4 to 0.7MPa, the inlet temperature is 40 to 50 ℃, and the space velocity for adding the isoprene material is 0.7 to 0.9h -1 The selective hydrogenation reaction of isoprene is carried out under the action of QSH-06 catalyst, the conversion rate of isoprene in a fixed bed hydrogenation reactor is 60% -80%, and the ratio of 2-methyl-butene-1 to 2-methyl-butene-2 is 4~5:1,
2) And (2) feeding the reacted material into a rectifying tower, extracting unreacted isoprene and a mixture of 2-methyl-1-butene and 2-methyl-2-butene from a rectifying tower side line, directly returning the mixture to an inlet of a fixed bed hydrogenation reactor for diluting the concentration of the isoprene, wherein the dilution ratio is 20 to 50, the 2-methyl-butene-1 with the purity of more than 99.5% is obtained at the top of the rectifying tower under the conditions that the pressure in the rectifying tower is 0.37 to 0.43MPa and the reflux ratio is 8.2 to 9.7, and a 2-methyl-butene-2 product with the purity of more than 99.5% is obtained at the bottom of the rectifying tower.
The invention takes pure isoprene as raw material, adopts a process flow combining a fixed bed reactor and a rectifying tower, adopts a measure of selecting specific catalyst to control the isoprene conversion rate, reaction conditions and hydrogen-diene ratio, the selectivity and the reaction depth of the selective hydrogenation reaction are improved, and the isomerization of the 2-methyl-1-butene is prevented, so that the 2-methyl-butene-2 product and the 2-methyl-butene-1 product with higher purity can be obtained simultaneously after rectification.
Preferably, the hydrogen and the isoprene in the step 1) are mixed according to a hydrogen/diene ratio of 1.09 to 1.11. The preferred hydrogen/diolefin ratio optimizes the selectivity and reaction depth of the selective hydrogenation reaction.
Preferably, the pressure in the fixed bed hydrogenation reactor in the step 1) is 0.5 to 0.6MPa, and the inlet temperature is 44 to 46 ℃. The reaction rate can be controlled by the optimized reaction conditions in the fixed bed hydrogenation reactor, the reaction selectivity is improved, the ratio of 2-methyl-butene-1 to 2-methyl-butene-2 in the product is further controlled, and the purity of the final product is ensured.
Preferably, the space velocity for adding the isoprene material in the step 1) is 0.75 to 0.85h -1 . The preferable addition rate of the isoprene material can better ensure that the catalyst can fully play a catalytic role and ensure the reaction efficiency.
Preferably, the conversion rate of isoprene in the fixed bed hydrogenation reactor in the step 1) is 66-71%, and the ratio of 2-methyl-butene-1 to 2-methyl-butene-2 is 4.3-4.5: 1. the invention realizes the control of the selectivity of the reaction by utilizing the coordination control of a specific catalyst and the conversion rate. The optimal conversion rate control is the optimal control condition of the method, and the purity of the 2-methyl-1-butene and the 2-methyl-2-butene products obtained from the tower bottom of the rectifying tower can be greatly improved.
Preferably, the dilution ratio of the isoprene at the inlet of the fixed bed hydrogenation reactor in the step 2) is 35 to 39. The optimized dilution ratio of the isoprene material can better ensure that the catalyst can fully play a catalytic role and ensure the reaction efficiency.
Preferably, the pressure in the rectifying tower in the step 2) is 0.39 to 0.41MPa, and the reflux ratio is 8.6 to 9.3. The preferred run-off conditions of the rectification column apparatus are matched with the preferred conditions of the fixed bed reactor to better match the reaction rates before and after. Thereby improving the preparation efficiency.
Preferably, the device comprises a fixed hydrogenation bed reactor and a rectifying tower, wherein the top of the fixed hydrogenation bed reactor is connected with an isoprene feeding pipeline and a hydrogen feeding pipeline, the bottom of the top of the fixed hydrogenation bed reactor is connected to a material inlet in the middle of the rectifying tower through a rectifying tower feeding pipeline, and a lateral line connecting port at the upper part of the rectifying tower is connected to an isoprene feeding pipeline connected to the top of the fixed hydrogenation bed reactor through a lateral line reflux pipeline; the top of the rectifying tower is connected with a 2-methyl-1-butene collecting pipeline, and the bottom of the rectifying tower is connected with a 2-methyl-butene collecting pipeline.
Compared with the prior art, the invention has the beneficial effects that: the inventors have found that the QSH-06 catalyst produces 2-methyl-1-butene in the presence of isoprene which is substantially free of 2-methyl-2-butene isomerization during the hydrogenation reaction. QSH-06 is a commercial catalyst produced by Zilliac limited, and QSH-06 is mainly used in MTO carbon four selective hydrogenation process. The invention is applied to the process for preparing the tertiary amylene by the selective hydrogenation of the isoprene to realize the simultaneous production of the 2-methyl-1-butene and the 2-methyl-2-butene. The reacted material enters a rectifying tower, and the unreacted isoprene and the mixture of 2-methyl-1-butene and 2-methyl-2-butene are extracted from the side line of the rectifying tower and directly return to the inlet of the fixed bed hydrogenation reactor for diluting the concentration of the isoprene.
Drawings
FIG. 1 is a schematic diagram of the connection of the apparatus used in the process for producing 2-methyl-1-butene and 2-methyl-2-butene according to the present invention.
The device comprises a fixed hydrogenation bed reactor 1, a fixed hydrogenation bed reactor 2, a rectifying tower 3, an isoprene feeding pipeline 4, a hydrogen feeding pipeline 5, a rectifying tower feeding pipeline 6, a lateral line return pipeline 7, a tower top material pipeline 8, an unreacted material return pipeline 9 and a 2-methyl-1-butylene collecting pipeline.
Detailed Description
The invention is further illustrated by the following specific examples, of which example 1 is the best mode of practice.
Referring to figure 1: the device for the production process of 2-methyl-1-butene and 2-methyl-2-butene comprises a fixed hydrogenation bed reactor 1 and a rectifying tower 2, wherein the top of the fixed hydrogenation bed reactor 1 is connected with an isoprene feeding pipeline 3 and a hydrogen feeding pipeline 4, the bottom of the top of the fixed hydrogenation bed reactor 1 is connected to a material inlet in the middle of the rectifying tower 2 through a rectifying tower feeding pipeline 5, and a lateral line connecting port at the upper part of the rectifying tower 2 is connected to the isoprene feeding pipeline 3 connected to the top of the fixed hydrogenation bed reactor 1 through a lateral line reflux pipeline 6; the top of the rectifying tower 2 is connected with a tower top material pipeline 7, the tower top material pipeline 7 is respectively connected with an unreacted material return pipeline 8 and a 2-methyl-1-butene collecting pipeline 9 through three parts, and the unreacted material return pipeline 8 is connected to the upper part of the rectifying tower 2; the bottom of the rectifying tower 2 is connected with a 2-methyl-butene collecting pipeline.
Example 1
Referring to the process flow shown in FIG. 1, 1) hydrogen and isoprene are mixed according to a hydrogen/diene ratio (mol) of 1.10 and then enter a fixed bed hydrogenation reactor, and a selective hydrogenation reaction of isoprene occurs under the action of a QSH-06 catalyst, wherein the pressure in the fixed bed hydrogenation reactor is 0.55MPa, the inlet temperature is 45 ℃, and the space velocity for adding isoprene material is 0.82h -1 And under the action of a QSH-06 catalyst, carrying out selective hydrogenation reaction on isoprene, wherein the conversion rate of the isoprene in the fixed bed hydrogenation reactor is 69%, and the ratio of 2-methyl-1-butene to 2-methyl-2-butene is 4.4:1,
2) And (3) feeding the reacted material into a rectifying tower, extracting unreacted isoprene and a mixture of 2-methyl-1-butene and 2-methyl-2-butene from a side line of the rectifying tower, directly returning the mixture to an inlet of a fixed bed hydrogenation reactor for diluting the concentration of the isoprene, wherein the dilution ratio is 37, under the conditions that the pressure in the rectifying tower is 0.40MPa and the reflux ratio is 8.9, the 2-methyl-butene-1 with the purity of 99.7% is obtained at the top of the rectifying tower, and the 2-methyl-2-butene product with the purity of 99.7% is obtained at the bottom of the rectifying tower.
Example 2
Referring to the process flow shown in FIG. 1, 1) hydrogen and isoprene are mixed according to a hydrogen/diene ratio (mol) of 1.11 and then enter a fixed bed hydrogenation reactor, and a selective hydrogenation reaction of isoprene occurs under the action of a QSH-06 catalyst, wherein the pressure in the fixed bed hydrogenation reactor is 0.5MPa, the inlet temperature is 44 ℃, and the space velocity for adding isoprene material is 0.75h -1 And the selective hydrogenation reaction of isoprene is carried out under the action of a QSH-06 catalyst, the conversion rate of isoprene in the fixed bed hydrogenation reactor is 71%, and the ratio of 2-methyl-1-butene to 2-methyl-2-butene is 4.5:1,
2) And (3) feeding the reacted material into a rectifying tower, extracting unreacted isoprene and a mixture of 2-methyl-1-butene and 2-methyl-2-butene from a side line of the rectifying tower, directly returning the mixture to an inlet of a fixed bed hydrogenation reactor for diluting the concentration of the isoprene, wherein the dilution ratio is 39, under the conditions that the pressure in the rectifying tower is 0.41MPa and the reflux ratio is 8.6, the 2-methyl-butene-1 with the purity of 99.6% is obtained at the top of the rectifying tower, and the 2-methyl-2-butene product with the purity of 99.6% is obtained at the bottom of the rectifying tower.
Example 3
Referring to the process flow shown in FIG. 1, 1) hydrogen and isoprene are mixed according to a hydrogen/diene ratio (mol) of 1.09 and then enter a fixed bed hydrogenation reactor, and a selective hydrogenation reaction of isoprene occurs under the action of a QSH-06 catalyst, wherein the pressure in the fixed bed hydrogenation reactor is 0.6MPa, the inlet temperature is 46 ℃, and the space velocity for adding isoprene material is 0.85h -1 And under the action of a QSH-06 catalyst, carrying out selective hydrogenation reaction on isoprene, wherein the conversion rate of the isoprene in the fixed bed hydrogenation reactor is 66%, and the ratio of 2-methyl-1-butene to 2-methyl-2-butene is 4.3:1,
2) The reacted material enters a rectifying tower, the unreacted isoprene and the mixture of 2-methyl-1-butene and 2-methyl-2-butene are extracted from the side line of the rectifying tower and directly return to the inlet of a fixed bed hydrogenation reactor for diluting the concentration of isoprene, the dilution ratio is 35, 2-methyl-butene-1 with the purity of 99.6 percent is obtained at the top of the rectifying tower under the conditions that the pressure in the rectifying tower is 0.39MPa and the reflux ratio is 9.3, and the 2-methyl-2-butene product with the purity of 99.6 percent is obtained at the bottom of the rectifying tower.
Example 4
Referring to the process flow shown in FIG. 1, 1) hydrogen and isoprene are mixed according to a hydrogen/diene ratio (mol) of 1.07 and then enter a fixed bed hydrogenation reactor, and a selective hydrogenation reaction of isoprene occurs under the action of a QSH-06 catalyst, wherein the pressure in the fixed bed hydrogenation reactor is 0.4MPa, the inlet temperature is 40 ℃, and the space velocity for adding isoprene material is 0.7h -1 And under the action of a QSH-06 catalyst, carrying out selective hydrogenation reaction on isoprene, wherein the conversion rate of the isoprene in the fixed bed hydrogenation reactor is 60%, and the ratio of 2-methyl-1-butene to 2-methyl-2-butene is 4:1,
2) The reacted material enters a rectifying tower, the unreacted isoprene and the mixture of 2-methyl-1-butene and 2-methyl-2-butene are extracted from the side line of the rectifying tower and directly return to the inlet of a fixed bed hydrogenation reactor for diluting the concentration of isoprene, the dilution ratio is 20, 2-methyl-butene-1 with the purity of 99.5 percent is obtained at the top of the rectifying tower under the conditions that the pressure in the rectifying tower is 0.37MPa and the reflux ratio is 8.2, and the 2-methyl-2-butene product with the purity of 99.5 percent is obtained at the bottom of the rectifying tower.
Example 5
Referring to the process flow shown in fig. 1, 1) hydrogen and isoprene are mixed according to a hydrogen/diene ratio (mol) of 1.12 and then enter a fixed bed hydrogenation reactor, and a selective hydrogenation reaction of isoprene is carried out under the action of QSH-06 catalyst, wherein the pressure in the fixed bed hydrogenation reactor is 0.7MPa, the inlet temperature is 50 ℃, and the space velocity for adding isoprene material is 0.9h -1 And under the action of QSH-06 catalyst, the selective hydrogenation reaction of isoprene occurs, the conversion rate of isoprene in the fixed bed hydrogenation reactor is 80%, and the ratio of 2-methyl-1-butene to 2-methyl-2-butene is 5:1,
2) The reacted material enters a rectifying tower, the unreacted isoprene and the mixture of 2-methyl-1-butene and 2-methyl-2-butene are extracted from the side line of the rectifying tower and directly return to the inlet of a fixed bed hydrogenation reactor for diluting the concentration of isoprene, under the conditions that the dilution ratio is 50, the pressure in the rectifying tower is 0.43MPa and the reflux ratio is 9.7, the 2-methyl-butene-1 with the purity of 99.5 percent is obtained at the top of the rectifying tower, and the 2-methyl-2-butene product with the purity of 99.5 percent is obtained at the bottom of the rectifying tower.
Comparative example 1
The process flow and the process conditions are the same as those of the example 1, except that the pressure in the fixed bed hydrogenation reactor is 0.55MPa, the inlet temperature is 45 ℃ and the space velocity for adding the isoprene material is 0.82h -1 (ii) a The internal reflux ratio of the rectifying tower is 2.5, the purity of the 2-methyl-butene-1 obtained at the top of the rectifying tower is 97.8 percent, and the purity of the 2-methyl-2-butene product obtained at the bottom of the rectifying tower is 69.3 percent.
Comparative example 1
The procedure and process conditions were the same as in example 1, except that the catalyst used was QSH-05 catalyst. A small amount of 2-methyl-butene-1 is obtained at the top of the rectifying tower, and the purity of the 2-methyl-2-butene product obtained at the bottom of the rectifying tower is 89.3 percent.
The foregoing is directed to preferred embodiments of the present invention, other and further embodiments of the invention may be devised without departing from the basic scope thereof, and the scope thereof is determined by the claims that follow. However, any simple modification, equivalent change and modification of the above embodiments according to the technical essence of the present invention are within the protection scope of the technical solution of the present invention.
Claims (7)
1. A process for the simultaneous production of 2-methyl-butene-1 and 2-methyl-butene-2, characterized in that the preparation steps comprise:
1) The molar ratio of hydrogen to isoprene is 1.07 to 1.12:1, mixing the mixture, putting the mixture into a fixed bed hydrogenation reactor, and carrying out selective hydrogenation reaction on isoprene under the action of QSH-06 catalyst, wherein the pressure in the fixed bed hydrogenation reactor is 0.4 to 0.7MPa, the inlet temperature is 40 to 50 ℃, and the space velocity for adding isoprene material is 0.7 to 0.9h -1 The selective hydrogenation reaction of isoprene is carried out under the action of a QSH-06 catalyst, the conversion rate of isoprene in a fixed bed hydrogenation reactor is 66 to 71 percent, and the ratio of 2-methyl-butene-1 to 2-methyl-butene-2 is 4.3 to 4.5:1;
2) And (2) feeding the reacted material into a rectifying tower, extracting unreacted isoprene and a mixture of 2-methyl-1-butene and 2-methyl-2-butene from a rectifying tower side line, directly returning the mixture to an inlet of a fixed bed hydrogenation reactor for diluting the concentration of the isoprene, wherein the dilution ratio is 20 to 50, the 2-methyl-butene-1 with the purity of more than 99.5% is obtained at the top of the rectifying tower under the conditions that the pressure in the rectifying tower is 0.37 to 0.43MPa and the reflux ratio is 8.2 to 9.7, and a 2-methyl-butene-2 product with the purity of more than 99.5% is obtained at the bottom of the rectifying tower.
2. The process for the simultaneous production of 2-methyl-butene-1 and 2-methyl-butene-2 according to claim 1, characterized in that: the molar ratio of hydrogen to isoprene in the step 1) is 1.09 to 1.11:1 and mixing.
3. The process for the simultaneous production of 2-methyl-butene-1 and 2-methyl-butene-2 according to claim 1, characterized in that: the pressure in the fixed bed hydrogenation reactor in the step 1) is 0.5-0.6 MPa, and the inlet temperature is 44-46 ℃.
4. The process for the simultaneous production of 2-methyl-butene-1 and 2-methyl-butene-2 according to claim 1, characterized in that: the space velocity for adding the isoprene material in the step 1) is 0.75 to 0.85h -1 。
5. The process for the simultaneous production of 2-methyl-butene-1 and 2-methyl-butene-2 according to claim 1, characterized in that: the dilution ratio of the isoprene at the inlet of the fixed bed hydrogenation reactor in the step 2) is 35 to 39.
6. The process for the simultaneous production of 2-methyl-butene-1 and 2-methyl-butene-2 according to claim 1, characterized in that: the pressure in the rectifying tower in the step 2) is 0.39 to 0.41MPa, and the reflux ratio is 8.6 to 9.3.
7. The process for the simultaneous production of 2-methyl-butene-1 and 2-methyl-butene-2 according to claim 1, characterized in that: the device comprises a fixed hydrogenation bed reactor (1) and a rectifying tower (2), wherein the top of the fixed hydrogenation bed reactor (1) is connected with an isoprene feeding pipeline (3) and a hydrogen feeding pipeline (4), the bottom of the top of the fixed hydrogenation bed reactor (1) is connected to a material inlet in the middle of the rectifying tower (2) through a rectifying tower feeding pipeline (5), and a lateral line connecting port at the upper part of the rectifying tower (2) is connected to the isoprene feeding pipeline (3) connected to the top of the fixed hydrogenation bed reactor (1) through a lateral line reflux pipeline (6); the top of the rectifying tower (2) is connected with a 2-methyl-1-butene collecting pipeline (9), and the bottom of the rectifying tower (2) is connected with a 2-methyl-butene collecting pipeline.
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62108827A (en) * | 1985-11-07 | 1987-05-20 | Mitsubishi Chem Ind Ltd | Production of 3-methylbutene-1 |
| EP0556025A1 (en) * | 1992-02-10 | 1993-08-18 | Chemical Research & Licensing Company | Selective hydrogenation of C5 streams |
| US5689013A (en) * | 1995-09-12 | 1997-11-18 | Neste Ot | Process for preparing tertiary alkyl ethers from an olefinic hydrocarbon feedstock |
| CN1490286A (en) * | 2002-10-16 | 2004-04-21 | 中国石油化工股份有限公司 | Separating method for cracking C5-fraction |
| CN1810743A (en) * | 2005-01-28 | 2006-08-02 | 中国石油化工股份有限公司 | Method of utilizing cracked, C5 fraction |
| CN101108782A (en) * | 2007-07-19 | 2008-01-23 | 中国石油化工集团公司 | Separation method of diene hydrocarbon in five fractions of petroleum cracked carbon |
| CN101679145A (en) * | 2007-06-08 | 2010-03-24 | 弗纳技术股份有限公司 | Dehydrogenation and polymerization process |
| CN103333042A (en) * | 2013-07-24 | 2013-10-02 | 上海派尔科化工材料有限公司 | Method for preparing pentene |
-
2018
- 2018-07-27 CN CN201810844301.0A patent/CN110759802B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62108827A (en) * | 1985-11-07 | 1987-05-20 | Mitsubishi Chem Ind Ltd | Production of 3-methylbutene-1 |
| EP0556025A1 (en) * | 1992-02-10 | 1993-08-18 | Chemical Research & Licensing Company | Selective hydrogenation of C5 streams |
| US5689013A (en) * | 1995-09-12 | 1997-11-18 | Neste Ot | Process for preparing tertiary alkyl ethers from an olefinic hydrocarbon feedstock |
| CN1490286A (en) * | 2002-10-16 | 2004-04-21 | 中国石油化工股份有限公司 | Separating method for cracking C5-fraction |
| CN1810743A (en) * | 2005-01-28 | 2006-08-02 | 中国石油化工股份有限公司 | Method of utilizing cracked, C5 fraction |
| CN101679145A (en) * | 2007-06-08 | 2010-03-24 | 弗纳技术股份有限公司 | Dehydrogenation and polymerization process |
| CN101108782A (en) * | 2007-07-19 | 2008-01-23 | 中国石油化工集团公司 | Separation method of diene hydrocarbon in five fractions of petroleum cracked carbon |
| CN103333042A (en) * | 2013-07-24 | 2013-10-02 | 上海派尔科化工材料有限公司 | Method for preparing pentene |
Non-Patent Citations (2)
| Title |
|---|
| 粗异戊烯选择加氢过程中2MB1的异构化;张蕊等;《化学工程师》;20090825;第23卷(第08期);第58-59+76页 * |
| 龚剑平编.侧线塔.《精馏塔的自动调节》.化学工业出版社,1984,第201-202页. * |
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