CN107137948B - Method for removing dicyclopentadiene from ethylene cracking carbon nine fraction - Google Patents
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Abstract
The invention provides a method for removing dicyclopentadiene from ethylene cracking carbon-nine fraction, which comprises the steps of adding a selective solvent into the ethylene cracking carbon-nine fraction for vacuum rectification, selectively removing dicyclopentadiene from the carbon-nine fraction which has extremely complex components and a boiling point close to that of the dicyclopentadiene and is difficult to separate by using a common rectification method, further treating the removed dicyclopentadiene fraction containing the selective solvent, and recycling the separated selective solvent for reuse to obtain high-purity dicyclopentadiene. The invention utilizes the high selectivity of the selective solvent to the dicyclopentadiene, can reduce the dicyclopentadiene content in the carbon nine fraction to below 1 percent, and solves the influence of the residue of the dicyclopentadiene on the quality of the subsequent petroleum resin; the method avoids the problem that active components are easy to explode and gather in a high-temperature cracking method so as to block equipment, avoids potential safety hazards caused by frequent cleaning, reduces the production cost, and realizes long-period, continuous and stable production.
Description
Technical Field
The invention belongs to the technical field of chemical separation, and particularly relates to a method for removing dicyclopentadiene from carbon nine fraction in ethylene cracking.
Background
The by-product C9 aromatic hydrocarbon fraction (cracked C9 for short) of ethylene plant is the residual fraction after extracting and separating C5 fraction and C6-C8 fraction (BTX is produced by hydrogenation) from cracked gasoline, which accounts for 10-20% of total yield of ethylene, and for the by-product C9 and C9+ components of ethylene, the by-product C9 petroleum resin is mainly characterized by being rich in diolefin and vinyl aromatic hydrocarbon, high in reaction activity, and widely used in chemical industries such as paint, printing ink, coating and adhesive, and is an important raw material of fine chemical engineering, except for producing solvent oil, extracting heavy aromatic hydrocarbon components and increasing yield of light aromatic hydrocarbon.
The cracked C9 fraction has extremely complicated composition, more than 150 kinds, and can be divided into three types according to the chemical structure and the reactivity of active components in the cracked C9 fraction: styrene and its derivatives of the first class, such as styrene, vinyl toluene, and the like; indene of the second kind and its derivatives, such as indene, methylindene, etc.; a third category of dicyclopentadiene and cyclopentadiene produced after decomposition thereof.
The third component in the ethylene cracking C9 fraction, especially dicyclopentadiene (DCPD), has high activity, is a main factor influencing the hue of the resin, has strict requirements on the resin abroad, and generally has no more than 2%, while the DCPD content in the C9 fraction in China is generally higher than 15%, so that the C9 petroleum resin grades in China are few, the color is deep, no uniform quality index exists, the application is not wide, and meanwhile, the application in high-grade paint is influenced, and the ethylene cracking C9 fraction also has some applications in tire additives, low-grade ink and adhesives in rubber shoe factories.
The boiling points of DPCD and methyl styrene which affect the quality of C9 petroleum resin are only 0.6 ℃, the composition of cracked C9 fraction is extremely complex, the boiling points are extremely close, DCPD cannot be removed by adopting a common distillation method, therefore, the existing production method and the published patent adopt a cracking chemical method of liquid phase depolymerization or gas phase depolymerization, the C9 fraction is heated to 380 ℃ by a heating furnace, dicyclopentadiene in the C9 fraction is depolymerized, then the mixture diene monomer is obtained at the tower top through rectification by a rectifying tower, and the cracked gasoline fraction is obtained at the tower bottom; however, because of reversibility of depolymerization and polymerization of dicyclopentadiene, dicyclopentadiene remaining in carbon nine fraction in a cracking method is generally about 3-5%, and is extremely difficult to reach a level below 1%.
Disclosure of Invention
In view of the above, the present invention aims to overcome the defects of the removal of dicyclopentadiene by the high temperature cracking method, and provides a novel method for removing dicyclopentadiene from the carbon-nine fraction obtained by ethylene cracking, wherein dicyclopentadiene is selectively removed from the carbon-nine fraction which has extremely complicated components and has a component boiling point close to that of the carbon-nine fraction and is difficult to separate by a common distillation method by adding a selective solvent into the carbon-nine fraction obtained by ethylene cracking and carrying out reduced pressure distillation, and meanwhile, high-purity dicyclopentadiene is prepared by using the removed dicyclopentadiene fraction containing the selective solvent.
In order to achieve the purpose, the technical scheme of the invention is realized as follows:
a method for removing dicyclopentadiene from carbon-nine fraction generated by ethylene cracking is characterized by adding selective solvent of dicyclopentadiene into carbon-nine fraction generated by ethylene cracking and rectifying under reduced pressure to remove dicyclopentadiene. Further, the desorption rectifying tower adopts a plate distillation tower or a packed tower.
Further, the selective solvent is benzaldehyde or furfural, and the operating pressure of the vacuum rectification is less than or equal to 30 KPa.
Further, the method also comprises a process for purifying and refining the removed dicyclopentadiene containing the selective solvent, which comprises the following steps: (1) removing the selective solvent in the dicyclopentadiene containing the selective solvent by adopting an extraction and rectification mode to obtain crude dicyclopentadiene and a selective solvent mixture containing an extracting agent; (2) and carrying out reduced pressure rectification on the crude dicyclopentadiene fraction to remove light component impurities in the crude dicyclopentadiene fraction to obtain a refined dicyclopentadiene fraction.
Further, the extracting agent is N-methyl pyrrolidone, and the operation pressure of the extraction and rectification is less than or equal to 50 KPa.
Further, the method also comprises a process for recovering the selective solvent mixture containing the extracting agent, and comprises the following steps: (1) adding water with the same mass as the extractant into the mixture, and after layering, taking the upper layer as a selective solvent and the lower layer as an extractant aqueous solution; (2) directly recovering the upper selective solvent, and recovering the lower extractant aqueous solution after dehydration.
Further, the recovered selective solvent is returned to ethylene cracking carbon nine fraction to remove a dicyclopentadiene system; the recovered extractant returns to dicyclopentadiene containing the selective solvent to remove the selective solvent system.
Further, a plate distillation tower or a packed tower is adopted as an operation tower for removing the dicyclopentadiene.
Further, a plate distillation column or a packed column is used as an operation column for purifying and refining dicyclopentadiene.
Furthermore, the dicyclopentadiene containing the selective solvent enters from the tower kettle of the operation tower, the extractant enters from the middle upper part of the tower, the crude dicyclopentadiene is extracted from the tower top, and the selective solvent containing the extractant is extracted from the tower kettle.
Compared with the prior art, the method for removing dicyclopentadiene from the carbon nine fraction in ethylene cracking has the following advantages:
(1) the method adopts a selective solvent reduced pressure distillation method to remove dicyclopentadiene in the carbon nine fraction, utilizes the high selectivity of the selective solvent to the dicyclopentadiene, can reduce the content of the dicyclopentadiene in the carbon nine fraction to a level below 1 percent, thoroughly solves the influence of the residue of the dicyclopentadiene on the subsequent production quality of the carbon nine petroleum resin, simultaneously adopts the reduced pressure distillation method, avoids the occurrence of the problem that active components are easy to implode in a high temperature cracking method so as to block equipment, stops the potential safety hazard caused by frequent cleaning, simultaneously reduces the production cost, and realizes long-period, continuous and stable production;
(2) the carbon nine fraction treated by the method of the invention basically has no residue of dicyclopentadiene, downstream petroleum resin production does not need multistage polymerization, the quality is high and stable, the carbon nine fraction is purer than the carbon nine fraction treated by the traditional method, and pure and high-quality petroleum resin can be obtained without adding special catalyst, so the production cost of the petroleum resin is further reduced;
(3) the method for preparing high-purity dicyclopentadiene directly treats dicyclopentadiene fraction containing selective solvent separated by vacuum distillation, has simple post-treatment process, can ensure that the purity of the dicyclopentadiene after treatment can reach more than 98 percent, can return the separated selective solvent to a dicyclopentadiene removal system for continuous use after treatment, and has no wastewater environmental protection problem.
(4) The method has advanced process flow, utilizes the high selectivity of the selective solvent to the dicyclopentadiene, and reduces the energy consumption for removing the dicyclopentadiene by more than 50 percent compared with the prior art.
Detailed Description
Unless defined otherwise, technical terms used in the following examples have the same meanings as commonly understood by one of ordinary skill in the art to which the present invention belongs. The test reagents used in the following examples, unless otherwise specified, are all conventional biochemical reagents; the experimental methods are conventional methods unless otherwise specified.
The invention will be described in detail with reference to the following examples.
The ethylene cracking carbon nine-fraction raw material adopted in the following examples is from Guangzhou Xinhuayue petrochemical company Limited, wherein the raw material comprises the following components in percentage by mass: 27.9 percent of dicyclopentadiene, 37.84 percent of styrene segment (styrene and homologues thereof) and 34.26 percent of indene segment (indene and homologues thereof).
Example 1
In the first step, dicyclopentadiene in the carbon nine fraction of ethylene cracking is removed (a glass rectifying tower with the diameter of 30mm and the height of 1.5m is selected as an operation tower):
adding 200ml of ethylene cracking carbon nine fraction and 200ml of benzaldehyde into a tower kettle, controlling the operation pressure in the tower to be 30kpa, heating to reflux, controlling the kettle temperature to be 83.4 ℃ and the top temperature to be 62.8 ℃, and pumping the ethylene cracking carbon nine fraction and the benzaldehyde from the middle part of the tower, wherein the feeding rate of the ethylene cracking carbon nine fraction is 150ml/hr, the feeding rate of the benzaldehyde is 60ml/hr, the reflux ratio at the top of the tower is 10:1, the fraction extracted at the top of the tower is dicyclopentadiene containing 48% of benzaldehyde, and the residue of the dicyclopentadiene in the tower kettle liquid is 0.56%;
and the second step, removing benzaldehyde from the fraction at the top of the tower (selecting a glass rectifying tower with the diameter of 30mm and the height of 1.5m as an operation tower):
adding 1000ml of dicyclopentadiene fraction containing 48% of benzaldehyde into a tower kettle, controlling the operation pressure in the tower to be 30kpa, heating to reflux, wherein the temperature of the tower is 76.2 ℃, the top temperature is 64.5 ℃, pumping N-methyl pyrrolidone from a position 1.2m away from the tower kettle, the feeding rate is 150ml/hr, the reflux ratio at the top of the tower is 10:1, the fraction extracted at the top of the tower is crude dicyclopentadiene fraction containing 0.16% of benzaldehyde, and the mixture of benzaldehyde and N-methyl pyrrolidone is extracted at the tower kettle;
thirdly, refining the crude dicyclopentadiene (selecting a glass rectifying tower with the diameter of 30mm and the height of 1.5m as an operation tower): wherein, the content (mass fraction) of each component in the crude dicyclopentadiene fraction is respectively as follows: 56.23% of dicyclopentadiene, 1.22% of methyl styrene and 42.55% of other light component impurities;
adding 500ml of crude dicyclopentadiene fraction into a tower kettle, controlling the operation pressure in the tower to be 20kpa, heating until reflux, wherein the kettle temperature is 110.3 ℃, the top temperature is 82.8 ℃, total reflux is carried out for 10min, the reflux ratio at the top of the tower is 5:1, after 61% of light component is removed, the dicyclopentadiene content in the distillate at the bottom of the tower kettle is 98.11%, and the recovery rate of dicyclopentadiene with the recovery rate being more than 98% is 72.86%;
fourthly, recovering a mixture of benzaldehyde and N-methyl pyrrolidone: adding water with the same mass as N-methyl pyrrolidone into the mixture, layering, returning the upper layer to the first step for reuse after direct recovery, and returning the lower layer to the second step for reuse after dehydration.
Example 2
In the first step, dicyclopentadiene in the carbon nine fraction of ethylene cracking is removed (a glass rectifying tower with the diameter of 30mm and the height of 1.5m is selected as an operation tower):
adding 200ml of ethylene cracking carbon nine fraction and 200ml of benzaldehyde into a tower kettle, controlling the operation pressure in the tower to be 30kpa, heating to reflux, controlling the kettle temperature to be 83.4 ℃ and the top temperature to be 62.8 ℃, and pumping the ethylene cracking carbon nine fraction and the benzaldehyde from the middle part of the tower, wherein the feeding rate of the ethylene cracking carbon nine fraction is 150ml/hr, the feeding rate of the benzaldehyde is 60ml/hr, the reflux ratio at the top of the tower is 3:1, the fraction extracted from the top of the tower is dicyclopentadiene containing 51% of benzaldehyde, and the residue of the dicyclopentadiene in the tower kettle liquid is 0.48%;
and the second step, removing benzaldehyde from the fraction at the top of the tower (selecting a glass rectifying tower with the diameter of 30mm and the height of 1.5m as an operation tower):
adding 1000ml of dicyclopentadiene fraction containing 51% of benzaldehyde into a tower kettle, controlling the operation pressure in the tower to be 30kpa, heating to reflux, wherein the temperature of the tower is 76.2 ℃, the top temperature is 64.5 ℃, pumping N-methyl pyrrolidone from a position 1.2m away from the tower kettle, the feeding rate is 150ml/hr, the reflux ratio at the top of the tower is 3:1, the fraction extracted at the top of the tower is crude dicyclopentadiene fraction containing 0.21% of benzaldehyde, and the mixture of benzaldehyde and N-methyl pyrrolidone is extracted at the tower kettle;
thirdly, refining the crude dicyclopentadiene (selecting a glass rectifying tower with the diameter of 30mm and the height of 1.5m as an operation tower): wherein, the content (mass fraction) of each component in the crude dicyclopentadiene fraction is respectively as follows: 57.35% of dicyclopentadiene, 1.08% of methyl styrene and 41.57% of other light component impurities;
adding 500ml of crude dicyclopentadiene fraction into a tower kettle, controlling the operation pressure in the tower to be 20kpa, heating until reflux, wherein the kettle temperature is 110.3 ℃, the top temperature is 82.8 ℃, total reflux is carried out for 10min, the reflux ratio at the top of the tower is 3:1, after 59% of light component removal is extracted, the dicyclopentadiene content in the fraction at the tower kettle is 98.02%, and the dicyclopentadiene recovery rate of more than 98% is 73.43%;
fourthly, recovering a mixture of benzaldehyde and N-methyl pyrrolidone: adding water with the same mass as N-methyl pyrrolidone into the mixture, layering, returning the upper layer to the first step for reuse after direct recovery, and returning the lower layer to the second step for reuse after dehydration.
Example 3
In the first step, dicyclopentadiene in the carbon nine fraction of ethylene cracking is removed (a glass rectifying tower with the diameter of 30mm and the height of 1.5m is selected as an operation tower):
adding 200ml of ethylene cracking carbon nine fraction and 200ml of furfural into a tower kettle, controlling the operation pressure in the tower to be 30kpa, heating to reflux, wherein the kettle temperature is 83.4 ℃, the top temperature is 62.8 ℃, and pumping the ethylene cracking carbon nine fraction and the furfural from the middle part of the tower, wherein the feeding rate of the ethylene cracking carbon nine fraction is 150ml/hr, the feeding rate of the furfural is 60ml/hr, the reflux ratio of the tower top is 3:1, the fraction extracted from the tower top is dicyclopentadiene containing 50.36% of the furfural, and the residue content of the dicyclopentadiene in the tower kettle liquid is 0.48%;
and the second step, removing benzaldehyde from the fraction at the top of the tower (selecting a glass rectifying tower with the diameter of 30mm and the height of 1.5m as an operation tower):
adding 1000ml of dicyclopentadiene fraction containing 50.36% of furfural into a tower kettle, controlling the operation pressure in the tower to be 30kpa, heating until reflux, controlling the kettle temperature to be 76.2 ℃ and the top temperature to be 64.5 ℃, pumping N-methyl pyrrolidone from a position 1.2m away from the tower kettle, wherein the feeding rate is 150ml/hr, the reflux ratio at the top of the tower is 3:1, the fraction extracted at the top of the tower is crude dicyclopentadiene fraction containing 0.2% of furfural, and the mixture of furfural and N-methyl pyrrolidone is extracted at the tower kettle;
thirdly, refining the crude dicyclopentadiene (selecting a glass rectifying tower with the diameter of 30mm and the height of 1.5m as an operation tower): wherein, the content (mass fraction) of each component in the crude dicyclopentadiene fraction is respectively as follows: 55.66% of dicyclopentadiene, 1% of methyl styrene and 43.34% of other light component impurities;
adding 500ml of crude dicyclopentadiene fraction into a tower kettle, controlling the operation pressure in the tower to be 20kpa, heating until reflux, wherein the kettle temperature is 110.3 ℃, the top temperature is 82.8 ℃, total reflux is carried out for 10min, the reflux ratio at the top of the tower is 3:1, 60.3% of light component removal is carried out, the dicyclopentadiene content in the distillate at the bottom of the tower kettle is 98.15%, and the recovery rate of dicyclopentadiene with the recovery rate being more than 98% is 70.64%;
fourthly, recovering a mixture of furfural and N-methyl pyrrolidone: adding water with the same mass as N-methyl pyrrolidone into the mixture, layering, wherein the upper layer is a selective solvent layer, directly recovering the solvent layer, returning to the first step for use, and the lower layer is an N-methyl pyrrolidone aqueous solution, dehydrating, and returning to the second step for use.
The embodiment shows that the method for removing dicyclopentadiene in the carbon nine fraction by adopting the selective solvent vacuum rectification method can reduce the content of dicyclopentadiene in the carbon nine fraction to a level below 1 percent, thoroughly solves the influence of the residue of dicyclopentadiene on the subsequent production quality of the carbon nine petroleum resin, and solves the serious problems of equipment blockage, difficult continuous production and the like caused by high-temperature cracking treatment of dicyclopentadiene;
further processing the removed dicyclopentadiene fraction containing the selective solvent to obtain a dicyclopentadiene product with the purity of more than 98 percent; the treated selective solvent can be further recycled, no waste liquid is generated, and the method is safe and environment-friendly; meanwhile, due to the high selectivity of the selective solvent, the energy consumption for removing the dicyclopentadiene can be reduced by more than 50 percent compared with the prior art.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and should not be taken as limiting the invention, so that any modifications, equivalents, improvements and the like, which are within the spirit and principle of the present invention, should be included in the scope of the present invention.
Claims (7)
1. A method for removing dicyclopentadiene from carbon nine fraction in ethylene cracking is characterized in that: adding a selective solvent of dicyclopentadiene into the ethylene cracking carbon nine fraction and removing the dicyclopentadiene in a vacuum rectification mode; the selective solvent is benzaldehyde or furfural; the operating pressure of the vacuum rectification is less than or equal to 30 KPa; a plate distillation tower or a packed tower is used as an operation tower for removing dicyclopentadiene, and dicyclopentadiene and the selective solvent are simultaneously extracted from the top of the tower.
2. The method for removing dicyclopentadiene from carbon nine fraction for ethylene cracking as claimed in claim 1, wherein: also comprises a process for purifying and refining the removed dicyclopentadiene containing the selective solvent, which comprises the following steps: (1) removing the selective solvent in the dicyclopentadiene containing the selective solvent by adopting an extraction and rectification mode to obtain crude dicyclopentadiene and a selective solvent mixture containing an extracting agent; (2) and carrying out reduced pressure rectification on the crude dicyclopentadiene fraction to remove light component impurities in the crude dicyclopentadiene fraction to obtain a refined dicyclopentadiene fraction.
3. The method for removing dicyclopentadiene from carbon nine fraction of ethylene cracking as claimed in claim 2, wherein: the extracting agent is N-methyl pyrrolidone, and the operation pressure of the extraction and the rectification is less than or equal to 50 KPa.
4. The method for removing dicyclopentadiene from carbon nine fraction for ethylene cracking as claimed in claim 2 or 3, wherein: also includes a process for recovering the selective solvent mixture containing the extractant, comprising the steps of: (1) adding water with the same mass as the extractant into the mixture, and after layering, taking the upper layer as a selective solvent and the lower layer as an extractant aqueous solution; (2) directly recovering the upper selective solvent, and recovering the lower extractant aqueous solution after dehydration.
5. The method for removing dicyclopentadiene from carbon nine fraction obtained by ethylene cracking according to claim 4, wherein: the recovered selective solvent is returned to ethylene cracking carbon nine fraction to remove the dicyclopentadiene system; the recovered extractant returns to dicyclopentadiene containing the selective solvent to remove the selective solvent system.
6. The method for removing dicyclopentadiene from carbon nine fraction for ethylene cracking as claimed in claim 2 or 3, wherein: a plate distillation tower or a packed tower is adopted as an operation tower for purifying and refining the dicyclopentadiene.
7. The method for removing dicyclopentadiene from carbon nine fraction obtained by ethylene cracking according to claim 6, wherein: the dicyclopentadiene containing the selective solvent enters from the tower kettle of the operation tower, the extractant enters from the middle upper part of the tower, the crude dicyclopentadiene is extracted from the tower top, and the selective solvent containing the extractant is extracted from the tower kettle.
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Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10158208A (en) * | 1996-11-25 | 1998-06-16 | Maruzen Petrochem Co Ltd | Separation and recovery of cyclohexyl vinyl ether |
| CN101063042A (en) * | 2006-04-27 | 2007-10-31 | 中国石油化工股份有限公司 | Light-end products oxidation desulfurizing and deodorizing method |
| CN101104573A (en) * | 2007-07-19 | 2008-01-16 | 中国石油化工集团公司 | Method for separating isoprene by combined rectification |
| CN101583582A (en) * | 2006-09-08 | 2009-11-18 | 纳幕尔杜邦公司 | Azeotrope compositions comprising 1,1,1,2,3-pentafluoropropene and hydrogen fluoride and uses thereof |
| CN101824336A (en) * | 2010-04-22 | 2010-09-08 | 中国寰球工程公司辽宁分公司 | Technique for producing terphenyl, indane and aromatics solvent oil by cracking C9 fraction and hydrogenation |
| CN102795957A (en) * | 2011-05-27 | 2012-11-28 | 中国石油化工股份有限公司 | Method for separating m-ethyltoluene and p-ethyltoluene by extractive distillation |
| CN103068773A (en) * | 2010-08-10 | 2013-04-24 | Amt国际股份有限公司 | Novel methods for regeneration of solvents for extractive processes |
| CN104703951A (en) * | 2012-09-20 | 2015-06-10 | 鲁姆斯科技公司 | Butadiene extraction pre-absorber |
| CN105709451A (en) * | 2014-12-23 | 2016-06-29 | 坎普利斯公司 | Process system for separating chemicals, distillation column arrangement, and method of separating chemicals |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FI117633B (en) * | 2000-12-29 | 2006-12-29 | Chempolis Oy | Recovery and manufacture of chemicals in mass production |
-
2017
- 2017-05-27 CN CN201710393400.7A patent/CN107137948B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10158208A (en) * | 1996-11-25 | 1998-06-16 | Maruzen Petrochem Co Ltd | Separation and recovery of cyclohexyl vinyl ether |
| CN101063042A (en) * | 2006-04-27 | 2007-10-31 | 中国石油化工股份有限公司 | Light-end products oxidation desulfurizing and deodorizing method |
| CN101583582A (en) * | 2006-09-08 | 2009-11-18 | 纳幕尔杜邦公司 | Azeotrope compositions comprising 1,1,1,2,3-pentafluoropropene and hydrogen fluoride and uses thereof |
| CN101104573A (en) * | 2007-07-19 | 2008-01-16 | 中国石油化工集团公司 | Method for separating isoprene by combined rectification |
| CN101824336A (en) * | 2010-04-22 | 2010-09-08 | 中国寰球工程公司辽宁分公司 | Technique for producing terphenyl, indane and aromatics solvent oil by cracking C9 fraction and hydrogenation |
| CN103068773A (en) * | 2010-08-10 | 2013-04-24 | Amt国际股份有限公司 | Novel methods for regeneration of solvents for extractive processes |
| CN102795957A (en) * | 2011-05-27 | 2012-11-28 | 中国石油化工股份有限公司 | Method for separating m-ethyltoluene and p-ethyltoluene by extractive distillation |
| CN104703951A (en) * | 2012-09-20 | 2015-06-10 | 鲁姆斯科技公司 | Butadiene extraction pre-absorber |
| CN105709451A (en) * | 2014-12-23 | 2016-06-29 | 坎普利斯公司 | Process system for separating chemicals, distillation column arrangement, and method of separating chemicals |
Non-Patent Citations (2)
| Title |
|---|
| 汪翩翩.萃取精馏提取裂解碳九芳烃中双环戊二烯的研究.《中国优秀硕士学位论文全文数据库工程科技Ⅰ辑》.2015,(第1期),第41-42页. * |
| 萃取精馏提取裂解碳九芳烃中双环戊二烯的研究;汪翩翩;《中国优秀硕士学位论文全文数据库工程科技Ⅰ辑》;20150115(第1期);第41-42页 * |
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