CN1160035A - Method for separation of petroleum cracking C5 fraction by liquid phase feeding extraction rectification - Google Patents
Method for separation of petroleum cracking C5 fraction by liquid phase feeding extraction rectification Download PDFInfo
- Publication number
- CN1160035A CN1160035A CN 96116289 CN96116289A CN1160035A CN 1160035 A CN1160035 A CN 1160035A CN 96116289 CN96116289 CN 96116289 CN 96116289 A CN96116289 A CN 96116289A CN 1160035 A CN1160035 A CN 1160035A
- Authority
- CN
- China
- Prior art keywords
- tower
- solvent
- column
- extractive distillation
- enters
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A process for preparing C5 diolefin such as isoprene by means of extractive rectification method using DMF as solvent to separate C5 fraction obtained by cracking petroleum includes thermal dimerization to remove bicycloprene, the first extractive rectification, removing heavy components, the second extractive rectification and removing light components, and features use of liquid-phase feeding operation for the first and second extractive rectifications, resulting in no self-collection of C5 diolefin in vaporizator, no need of periodical cleaning of vaporizator and no reduction of yield of C5 diolefin. In addition, its mixer has simpler structure and smaller size than vaporizator, so decreasing investment in apparatus.
Description
The present invention relates to a kind of method of separating the petroleum cracking C 5 fraction with extraction fractional distillation.
The a considerable amount of C 5 fractions of by-product are rich in diolefins such as isoprene, cyclopentadiene and m-pentadiene in the process of petroleum cracking system ethene in the C 5 fraction.These diolefin chemical property are active, are the valuable sources of chemical utilization.With the difference on petroleum hydrocarbon cracking raw materials, cracking severity and the separation degree, diolefin content in the C 5 fraction can be different, total but content at least between 40～60%.Therefore, separate and utilize C 5 fraction for the economic benefit that improves ethylene unit, the comprehensive utilization petroleum resources have far reaching significance.
C 5 fraction is close by more than 20 kinds of boiling points, and the component that easily forms azeotrope is each other again formed, and therefrom isolates the higher C 5 diene of comprehensive utilization added value, and its technology is very complicated.In order to produce the high C 5 diene of purity, more employing in the prior art be extraction fractional distillation.Selective solvent commonly used has dimethyl formamide (DMF) and acetonitrile, and has produced some representative commercial runs therefrom, as patent J63101338, J74019245, J74039644, US3, and 510,405, US3,535,260 is disclosed.Plurality of advantages such as wherein the DMF method is easy to separate with carbon five because the DMF solvent is good to the selectivity of C 5 diene, solubleness is big, and the low and toxicity of corrodibility is little and as if more people accept.As U.S. Pat 3,510,405 described be exactly a kind of typical case and comparatively ideal DMF method technology.
Existing DMF method is separated C 5 fraction and is generally comprised following process:
The material carbon 5 distillate is through hot dimerization reaction and therefrom isolate dicyclopentadiene; With DMF is that solvent carries out extracting rectifying in the presence of stopper, and solvent is by a stripping tower recycling use; Material carries out rectifying through a weight-removing column, therefrom separates the heavy component that contains cyclopentadiene and m-pentadiene; With DMF is solvent further extracting rectifying in the presence of stopper, and solvent reclaims by stripping tower and uses; Material obtains highly purified isoprene product after a lightness-removing column carries out rectifying.
Since in three kinds of C 5 dienes the isoprene market development early and be widely used, so general C 5 fraction separation process scheme is only separated utilization isoprene wherein.Along with petrochemical complex, the particularly development of fine chemistry industry, the applied research of m-pentadiene and dicyclopentadiene is also quite successful, and its market requirement increases day by day, and therefore the technology of exploitation obtains m-pentadiene and cyclopentadiene product with the further rectifying separation of heavy component material that removes in the flow process recently.
In DMF method C 5 fraction separation process, first and second extracting rectifying is a critical step comparatively, it all can produce very big influence for the treatment capacity of ultimate yield, product purity and even the whole device of C 5 diene, so the design of this part Processes and apparatus is very important.In the prior art, usually, all adopt the mode of C 5 fraction gas-phase feed to operate in order to make rectifying section and stripping section in the extractive distillation column keep close solvent strength in order to the separating of component.On stream, be provided with respectively before first extractive distillation column and second extractive distillation column vaporizer with C 5 fraction all vaporize the back charging.But because C 5 fraction (about 60～100 ℃) under vaporization temperature, very easily polymerization of C 5 diene wherein is even also be like this under the situation that has stopper to exist.Therefore usually need to be provided with and be equipped with platform and switch and use, with regular removing polymkeric substance, and in order to reduce the accumulation of stopper and polymkeric substance in the vaporizer as far as possible, the vaporizer bottom needs continuous and quantitative to extract partial material out, and this has just influenced the yield of diolefin.For second extracting rectifying, because isoprene purity has reached about 98% in the feed carbon 5 distillate, polymerism and cause the loss of isoprene even more serious.
The purpose of this invention is to provide a kind of improved DMF method C 5 fraction separation method, phase when it passes through to change the charging of extractive distillation column C 5 fraction material, and take a series of relative measures, overcome the above-mentioned shortcoming that exists in the existing DMF method C 5 fraction separation method effectively.
Method provided by the invention mainly comprises following process: 1) the material carbon 5 distillate carries out hot dimerization reaction in hot dipolymer reactor, so that the most of cyclopentadiene dimerization in the C 5 fraction generates dicyclopentadiene, temperature of reaction is 60～150 ℃, reaction pressure is 1.0～1.5MPa, and reactant removes dicyclopentadiene and heavy component through fractionation by distillation then; 2) material that is obtained by said process enters first extractive distillation column with the middle part that liquid phase enters after a mixing tank and the DMF solvent by tower, another part solvent is then entered by the top of tower, entering the DMF solvent temperature by cat head is 40～70 ℃, the DMF solvent temperature that enters mixing tank is 100～140 ℃, entering the DMF solvent of mixing tank and the throughput ratio of material is 0.7～1.5, the tower internal pressure is 0.1～0.3, MPa, 100～140 ℃ of tower still temperature, the trim the top of column ratio is 4～10, in the presence of stopper, carry out extracting rectifying, must be rich in the solvent material of C 5 dienes such as isoprene by the tower still; 3) above-mentioned tower still material enters first stripping tower by the top of tower, stripping Tata still obtains reclaiming solvent and returns first extractive distillation column and recycle, and its cat head material enters a weight-removing column and carries out rectifying separation to isolate cyclopentadiene, m-pentadiene and other heavy component; 4) weight-removing column cat head material enters second extractive distillation column with the bottom that liquid phase enters after a mixing tank and the DMF solvent by tower, another part solvent is then entered by the top of tower, the DMF solvent temperature that is entered by cat head is 40～70 ℃, the DMF solvent temperature that enters mixing tank is 100～140 ℃, entering the DMF solvent of mixing tank and the throughput ratio of material is 0.7～1.5, the tower internal pressure is 0.1～0.3MPa, tower still temperature is 100～150 ℃, the trim the top of column ratio is 4～8, carries out extracting rectifying in the presence of stopper.The tower still material that contains a small amount of cyclopentadiene and other alkene and alkynes enters second stripping tower, and the recovery solvent that obtains returns second extractive distillation column and recycles after further handling; 5) the cat head material of second extractive distillation column enters lightness-removing column and carries out rectifying separation to remove light component from the bottom, gets highly purified isoprene product by tower still side line.
Stopper in first extracting rectifying and the employing of the second extracting rectifying process can be ONP, oil of mirbane, furfural, NMP, thanomin or NaNO2 etc.
By the dicyclopentadiene heavy component material of separation removal behind the hot dimerization reaction and the tower still material of weight-removing column, can remove processes such as carbon six hydrocarbon components by other carbon five hydrocarbon components of rectifying separation, rectifying again, obtain highly purified m-pentadiene and dicyclopentadiene product.
Wherein the charging at first extractive distillation column and second extractive distillation column changes liquid-phase operation into, be the feature place that the present invention makes improvements prior art, this can be avoided gas-phase feed this drawback that operates in that the material vaporization time causes in the C 5 fraction diolefin polymerization so that vaporizer often stops up and final diolefin yield descends.
Yet the liquid phase feeding operation will bring the stripping section load of extractive distillation column to increase and problems such as interior stripping section of tower and rectifying section solvent strength skewness.Therefore, taked that in the present invention solvent is divided into two portions and added and has mixed during with the material charging this measure of adding from cat head respectively.This can make the solvent strength distribution in the tower be tending towards even first, second since with mixing of materials be the solvent of relatively-high temperature, this makes material partly vaporize with dissolving after solvent contacts or be partially dissolved in the solvent and obtain heat at mixing tank, thereby reduce the load of extractive distillation column stripping section, improve the treatment capacity of extractive distillation column.
Design of Mixer should be considered in principle that material and solvent can produce to mix fully and avoid the material bumping to vibrate, and mixing the back material, to be heated that vaporization have these two factors of enough spaces, contriver to think to be provided with the columnar structured of a solvent jet pipe at the center be a kind of comparatively ideal designs scheme.High-temperature solvent is entered by the mixing tank bottom, sprays in mixing tank from jet pipe, and the C 5 fraction material is then entered by mixing tank bottom sides tangential direction, then the high-temperature solvent thorough mixing that shape rises and jet pipe sprays in the shape of a spiral.Outlet is arranged at the top of mixing tank.Resistance should be lacked and reduce to this segment pipe of opening for feed from mixing tank to extractive distillation column as much as possible, to prevent that gas-liquid is separated and C 5 diene overstand and cause polymerization in pipeline.Certainly, this moment C 5 diene owing to exist when solvent and stopper are arranged, the possibility of its autohemagglutination reduces greatly.
In addition, also can adopt the mixing equipment of venturi mixer or other kind.
Sneak into flow by wishing in feed rate, temperature of charge, solvent self-temperature and the extractive distillation column of carbon five materials that the factors of controlling such as solvent strength are determined with the hot solvent that carbon five mixing of materials are required.It should be that solvent strength that the concentration of mixing liquid phase part solvent in the gas-liquid mixture that the back generates and extractive distillation column feed plate place will be controlled is identical that best hot solvent is sneaked into flow.The inventor thinks the flow-ratio control of the solvent that enters mixing tank and material 0.7～1.5th, and is suitable.
With the solvent phase of carbon five mixing of materials for the solvent that adds from the extracting rectifying column overhead, be the pyritous solvent, this be for make material before entering tower the part vaporization with the load of reduction stripping section.Therefore, the temperature of solvent is higher more favourable to vaporization, but the too high diolefin autohemagglutination that easily causes C 5 fraction of temperature.And low excessively temperature will cause solvent to have bigger mixed volume can have enough heats to make material reach certain evaporating capacity, and this has increased the power consumption of extractive distillation column stripping section and rectifying section liquid phase load and delivery solvent on the contrary again.According to diolefin content in the C 5 fraction and the stopper performance that is adopted, the contriver advises that the temperature of solvent should be controlled between 100～140 ℃.Certainly, this also is the solvent that can obtain this temperature in the flow process easily in order to consider simultaneously.
Compared with prior art, the present invention is owing to change gas-phase feed into liquid phase feeding operation, solved the problem that gas-phase feed operates in the easy autohemagglutination of C 5 diene in the vaporizer effectively.In addition, the mixing tank that will adopt among the present invention is with respect to vaporizer, and its structure, volume are all much smaller.Therefore, the investment of equipment can correspondingly reduce.And the regular switching cleaning of having avoided gasifier must carry out because of polymer plugging reaches the environmental pollution that therefore causes, and the generation of polymkeric substance causes, and degradation then is the main embodiment of positively effect of the present invention under the C 5 diene final yield.
Accompanying drawing 1 is the process flow sheet of the embodiment of the invention;
Accompanying drawing 2 is carbon five materials that adopt in the embodiment of the invention, the structural representation of high-temperature solvent mixer.
Embodiment:
Shown in accompanying drawing 1, the material carbon 5 distillate at first enters hot dipolymer reactor 1 and carries out hot dimerization reaction, and temperature of reaction is controlled at 60～150 ℃, and reaction pressure is controlled at 1.0～1.5MPa.Reactant enters pre-weight-removing column 2 to isolate dicyclopentadiene and other heavy component, i.e. tower still material W1.The stage number of pre-weight-removing column is 30～50, and opening for feed is between the 15th～20 block of column plate, and its processing parameter is: tower internal pressure 0.05～0.10MPa, and 80～110 ℃ of tower still temperature, trim the top of column is than 1～4.
The cat head material of pre-weight-removing column 2 enters mixing tank 3 with liquid phase, and from first stripping tower, 5 tower stills and enter first extractive distillation column 4 after the DMF of heat exchange solvent, carries out extracting rectifying in the presence of the stopper thanomin.Another part solvent is then entered by the first stripping Tata still direct top from first extractive distillation column after heat exchange, cooling, and temperature is controlled at 40～50 ℃.The high-temperature solvent temperature that enters mixing tank is controlled at 100～140 ℃, and entering the high-temperature solvent of mixing tank and the throughput ratio of carbon five materials is 0.7～1.5.The stage number of first extractive distillation column is 90～140, and opening for feed is between the 50th～60 block of column plate, and its processing parameter is: tower internal pressure 0.1～0.3MPa, and 100～140 ℃ of tower still temperature, trim the top of column is than 4～10.
The tower still material of first extractive distillation column enters first stripping tower 5, obtains reclaiming solvent by the tower still and returns first extractive distillation column and recycle.The stage number of first stripping tower is 30～50, and opening for feed is between the 20th～25 block of column plate, and its processing parameter is: tower internal pressure 0.01～0.04MPa, and 100～170 ℃ of tower still temperature, trim the top of column is than 1～3.
The cat head material of first stripping tower enters weight-removing column 6, is isolated the material W2 of dicyclopentadiene, m-pentadiene and other heavy component by the tower still.The stage number of weight-removing column is 1 20～160, and opening for feed is between the 50th～60 block of column plate.Its processing parameter is: tower internal pressure 0.1～0.4MPa, and 50～100 ℃ of tower still temperature, trim the top of column is than 30～50.
After the cat head material condensation of weight-removing column with liquid phase enter mixing tank 7 with from the 3rd stripping tower 11 tower stills and after the DMF of heat exchange solvent, enter second extractive distillation column 8, in the presence of the stopper thanomin, carry out extracting rectifying.Another part solvent is then directly entered by the top of second extractive distillation column after heat exchange, cooling by the tower still of the 3rd stripping tower 11, its temperature is controlled at 40～50 ℃, the solvent temperature that enters mixing tank is controlled at 100～140 ℃, and entering the high-temperature solvent of mixing tank and the throughput ratio of carbon five materials is 0.7～1.5.The stage number of second extractive distillation column is 132～182, and opening for feed is between the 100th～120 block of column plate.Its processing parameter is: tower internal pressure 0.1～0.3MPa, and 100～140 ℃ of tower still temperature, trim the top of column is than 4～8.Be admitted to second stripping tower 10 after the solvent that contains a small amount of cyclopentadiene and other alkene and alkynes is discharged by the tower still and reclaim solvents.
The cat head material of second extractive distillation column enters lightness-removing column 9 removing light component, and getting purity by tower still side line is isoprene product more than 99.3%.The stage number of lightness-removing column is 75～130, and opening for feed is between the 30th～40 block of column plate.Its processing parameter is: tower internal pressure 0.1～0.3MPa, and 40～80 ℃ of tower still temperature, trim the top of column is than 100～600.
Second stripping tower 10 is an atmospheric operation, and tower still temperature is controlled at 100～170 ℃, and the trim the top of column ratio is 1～3, and its stage number is 35～50, and opening for feed is between the 10th～20 block of column plate.The tower still material of second stripping tower enters the 3rd stripping tower 11 further removing cyclopentadiene and the alkynes in the circulating solvent, but its cat head material is sent the solvent treatment part except that the extraction unit that refluxes, and refining solvent send the second extraction tower rectifying tower to recycle.
The 3rd stripping tower 11 is a decompression operation, and the tower internal pressure is 0.01～0.03MPa, and tower still temperature is controlled at 80～120 ℃, and the trim the top of column ratio is 70～90, and its stage number is 30～50, and opening for feed is between the 5th～10 block of column plate.
The tower still material W2 that tower still material W1 that is obtained by pre-weight-removing column 2 and weight-removing column 6 obtain, again through rectifying separation remove other carbon five hydrocarbon components, rectifying removes processes such as carbon six hydrocarbon components, highly purified m-pentadiene and dicyclopentadiene product.This part equipment can not put into main flow.
The major ingredient of the tower still material W3 of lightness-removing column is an isoprene, and it is reclaimed suitable position in the Returning process.
Carbon five materials and the high-temperature solvent that adopt among the embodiment carry out the blended mixer structure as shown in Figure 2.Be provided with a solvent jet pipe 13 at the center of columnar mixer tube 12, the first half tube wall of jet pipe has some solvent spray orifices 14.Jet pipe connects with the import 15 of solvent, and the annular space that forms between cylindrical shell 12 and the jet pipe 13 is the vaporizing chamber of mixing section and carbon five materials.Carbon five material inlets 16 are opened in the cylindrical shell bottom sides with tangential direction.
Claims (3)
1. one kind is separated the method produce C 5 dienes such as isoprene by petroleum cracking system ethylene by-product C 5 fraction, comprises following process:
The material carbon 5 distillate carries out hot dimerization reaction in hot dipolymer reactor, make the most of cyclopentenes dimerization in the C 5 fraction generate dicyclopentadiene, temperature of reaction is 60～150 ℃, and reaction pressure is 1.0～1.5MPa, and reactant removes dicyclopentadiene and heavy component through fractionation by distillation then;
The material that is obtained by said process enters first extractive distillation column by the middle part of tower, with DMF is that solvent carries out extracting rectifying in the presence of stopper, the tower internal pressure is 0.1～0.3MPa, tower still temperature is 100～140 ℃, the trim the top of column ratio is 4～10, must be rich in the solvent material of C 5 dienes such as isoprene by the tower still;
Above-mentioned tower still material enters first stripping tower by the top of tower, stripping Tata still must reclaim solvent and return first extractive distillation column and recycle, its cat head material enters a weight-removing column and carries out rectifying separation, to isolate dicyclopentadiene, m-pentadiene and other heavy component;
Weight-removing column cat head material enters second extractive distillation column by the tower middle part, with DMF is that solvent carries out extracting rectifying in the presence of stopper, the tower internal pressure is 0.1～0.3MPa, tower still temperature is 100～150 ℃, the trim the top of column ratio is 4～8, its tower still material that contains a small amount of cyclopentadiene and other alkene and alkynes enters follow-up stripping tower, and the recovery solvent that obtains returns second extractive distillation column and recycles;
The cat head material of second extractive distillation column enters lightness-removing column to carry out rectifying separation and takes off to remove light component from the bottom, gets highly purified isoprene product by tower still side line,
It is characterized in that first extractive distillation column and second extractive distillation column are all with liquid phase feeding, and the DMF solvent is divided into two portions respectively by cat head and entering in the tower outside tower with after carbon five materials mix in a mixing tank, the DMF solvent temperature that is entered by cat head is 40～70 ℃, the DMF solvent temperature that enters mixing tank is 100～140 ℃, and the solvent that enters mixing tank is 0.7～1.5 with the mass flow ratio.
2. separate the method for producing C 5 dienes such as isoprene according to the described C 5 fraction of claim 1, it is characterized in that described by the dicyclopentadiene heavy component material of separation removal behind the hot dimerization reaction and the tower still material of weight-removing column, remove processes such as carbon six hydrocarbon components by other carbon five hydrocarbon components of rectifying separation, rectifying, obtain highly purified m-pentadiene and dicyclopentadiene product.
3. separate the method for producing C 5 dienes such as isoprene according to claim 1 or 2 described C 5 fractions, it is characterized in that the stopper that described first extracting rectifying and the second extracting rectifying process adopt is ONP, oil of mirbane, furfural, NMP, thanomin or NaNO2 etc.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96116289A CN1055281C (en) | 1996-03-20 | 1996-03-20 | Method for separation of petroleum cracking C5 fraction by liquid phase feeding extraction rectification |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96116289A CN1055281C (en) | 1996-03-20 | 1996-03-20 | Method for separation of petroleum cracking C5 fraction by liquid phase feeding extraction rectification |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1160035A true CN1160035A (en) | 1997-09-24 |
| CN1055281C CN1055281C (en) | 2000-08-09 |
Family
ID=5123407
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN96116289A Expired - Lifetime CN1055281C (en) | 1996-03-20 | 1996-03-20 | Method for separation of petroleum cracking C5 fraction by liquid phase feeding extraction rectification |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1055281C (en) |
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1077561C (en) * | 1998-11-09 | 2002-01-09 | 化学工业部北京化工研究院 | Process for separating diolefin from C5 fraction |
| CN101805631A (en) * | 2010-05-07 | 2010-08-18 | 天津大学 | Variable pressure steam stripping method of C5 fraction extraction solvent |
| CN101209948B (en) * | 2006-12-31 | 2010-10-06 | 淄博鲁华泓锦化工股份有限公司 | Method for modifying heat dimerization effect of cyclopentadiene |
| CN101100412B (en) * | 2007-07-19 | 2011-03-23 | 中国石油化工集团公司 | Postheating dimerization method for separating C5 diene |
| CN101544534B (en) * | 2009-04-16 | 2012-04-25 | 中国石油兰州石油化工公司 | Method for directly separating and purifying cyclopentene from C5 raw material adopting extraction and distillation technology |
| CN101289360B (en) * | 2007-04-19 | 2012-10-24 | 中国石化上海石油化工股份有限公司 | Process for preparing 2-amylene by separating C5 distillate of petroleum |
| CN101289361B (en) * | 2007-04-19 | 2012-10-24 | 中国石化上海石油化工股份有限公司 | Process for preparing 2-amylene by separating C5 distillate of petroleum |
| CN101289362B (en) * | 2007-04-19 | 2012-10-24 | 中国石化上海石油化工股份有限公司 | Process for preparing 1-amylene by separating C5 distillate of petroleum |
| CN101544533B (en) * | 2009-05-06 | 2012-11-21 | 南京工业大学 | Method for depredating acetylene hydrocarbon in cracked carbon-5 distillate by acetylene hydrocarbon post-depredation process |
| CN102951987A (en) * | 2011-08-17 | 2013-03-06 | 中国石油化工股份有限公司 | Method for separation of C5 fraction and preparation of dicyclopentadiene |
| CN102951988A (en) * | 2011-08-17 | 2013-03-06 | 中国石油化工股份有限公司 | Separation method of C5 fraction |
| CN101289363B (en) * | 2007-04-19 | 2013-06-19 | 中国石化上海石油化工股份有限公司 | Process for preparing 1-amylene by separating C5 distillate of petroleum |
| CN103570487A (en) * | 2012-07-27 | 2014-02-12 | 青岛伊科思技术工程有限公司 | Control method for separating cyclopentadiene from C5 fraction by utilizing dimerization method |
| CN110950732A (en) * | 2019-12-31 | 2020-04-03 | 淄博鲁华同方化工有限公司 | Large-scale carbon five separation method |
| US11203556B2 (en) | 2018-06-04 | 2021-12-21 | Sabic Global Technologies B.V. | Dimerization of cyclopentadiene using reactive jet mixing |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104591948B (en) * | 2013-10-30 | 2018-04-24 | 中石化上海工程有限公司 | It is a kind of to reduce the method that pentadiene process energy consumption is separated from petroleum cracking C5 fractions |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DD94614A (en) * | ||||
| DE1183071B (en) * | 1962-12-22 | 1964-12-10 | Erdoelchemie Gmbh | Process for the recovery of ioprene from C fractions |
| GB1113279A (en) * | 1965-10-18 | 1968-05-08 | Exxon Research Engineering Co | Isoprene purification process |
-
1996
- 1996-03-20 CN CN96116289A patent/CN1055281C/en not_active Expired - Lifetime
Cited By (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1077561C (en) * | 1998-11-09 | 2002-01-09 | 化学工业部北京化工研究院 | Process for separating diolefin from C5 fraction |
| CN101209948B (en) * | 2006-12-31 | 2010-10-06 | 淄博鲁华泓锦化工股份有限公司 | Method for modifying heat dimerization effect of cyclopentadiene |
| CN101289363B (en) * | 2007-04-19 | 2013-06-19 | 中国石化上海石油化工股份有限公司 | Process for preparing 1-amylene by separating C5 distillate of petroleum |
| CN101289360B (en) * | 2007-04-19 | 2012-10-24 | 中国石化上海石油化工股份有限公司 | Process for preparing 2-amylene by separating C5 distillate of petroleum |
| CN101289361B (en) * | 2007-04-19 | 2012-10-24 | 中国石化上海石油化工股份有限公司 | Process for preparing 2-amylene by separating C5 distillate of petroleum |
| CN101289362B (en) * | 2007-04-19 | 2012-10-24 | 中国石化上海石油化工股份有限公司 | Process for preparing 1-amylene by separating C5 distillate of petroleum |
| CN101100412B (en) * | 2007-07-19 | 2011-03-23 | 中国石油化工集团公司 | Postheating dimerization method for separating C5 diene |
| CN101544534B (en) * | 2009-04-16 | 2012-04-25 | 中国石油兰州石油化工公司 | Method for directly separating and purifying cyclopentene from C5 raw material adopting extraction and distillation technology |
| CN101544533B (en) * | 2009-05-06 | 2012-11-21 | 南京工业大学 | Method for depredating acetylene hydrocarbon in cracked carbon-5 distillate by acetylene hydrocarbon post-depredation process |
| CN101805631A (en) * | 2010-05-07 | 2010-08-18 | 天津大学 | Variable pressure steam stripping method of C5 fraction extraction solvent |
| CN101805631B (en) * | 2010-05-07 | 2013-06-26 | 天津大学 | Variable pressure steam stripping method of C5 fraction extraction solvent |
| CN102951987A (en) * | 2011-08-17 | 2013-03-06 | 中国石油化工股份有限公司 | Method for separation of C5 fraction and preparation of dicyclopentadiene |
| CN102951988A (en) * | 2011-08-17 | 2013-03-06 | 中国石油化工股份有限公司 | Separation method of C5 fraction |
| CN102951987B (en) * | 2011-08-17 | 2016-06-22 | 中国石油化工股份有限公司 | Separate C5 fraction the method producing dicyclopentadiene |
| CN102951988B (en) * | 2011-08-17 | 2016-06-29 | 中国石油化工股份有限公司 | A kind of method separating C5 fraction |
| CN103570487A (en) * | 2012-07-27 | 2014-02-12 | 青岛伊科思技术工程有限公司 | Control method for separating cyclopentadiene from C5 fraction by utilizing dimerization method |
| US11203556B2 (en) | 2018-06-04 | 2021-12-21 | Sabic Global Technologies B.V. | Dimerization of cyclopentadiene using reactive jet mixing |
| CN110950732A (en) * | 2019-12-31 | 2020-04-03 | 淄博鲁华同方化工有限公司 | Large-scale carbon five separation method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1055281C (en) | 2000-08-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1055281C (en) | Method for separation of petroleum cracking C5 fraction by liquid phase feeding extraction rectification | |
| CN101821361B (en) | Process for 1,3-butadiene separation from crude C4 stream with acetylene converter | |
| CN1172886C (en) | Process for composite solvent for separating arylhydrocarbon by extraction and distillation | |
| CN101244974B (en) | Method for one-section abstraction distillation separation cracking carbon 5-cut fraction | |
| CN111954654B (en) | Method for separating aromatic hydrocarbon by extractive distillation | |
| CN105585411A (en) | Hydrogenation method of butadiene extraction tail gas | |
| CN103086823B (en) | Method and device for separating n-hexane, isohexane and benzene | |
| CN101450885A (en) | Method for separating carbon 5 fraction by one-stage extraction and rectification | |
| CN1085646C (en) | Method for separating arene from hydrocarbons mixture by use of extraction and rectification | |
| EP1359989B1 (en) | Quench water pretreat process | |
| CN101081993B (en) | Method for recovering aromatic hydrocarbons from hydrocarbons mixture with high content of aromatic hydrocarbons | |
| CN1272408C (en) | Composite solvent in use for extracting, rectifying and separating arene and method of application | |
| CN1125008C (en) | Process for recovering arylhydrocarbon by combination of extracting distillation with liquid-liquid extraction | |
| CN101244975B (en) | Method for producing polymerization level isoprene with one-section abstraction combined azeotropy distillation | |
| CN102485708B (en) | C5 fraction separation method employing hypergravity extractive distillation apparatus | |
| US4761222A (en) | Method for separating normally liquid organic compounds | |
| CN1083819C (en) | Method for separating arene by using extraction and rectification | |
| CN1077561C (en) | Process for separating diolefin from C5 fraction | |
| CN100460373C (en) | Method for extracting rectifying and separating benzene | |
| CN1093527C (en) | Preparation method of high-purity cyclopentadiene | |
| CN101955410A (en) | Reclaim cinnamic method and system from containing cinnamic raw material | |
| CN101397261B (en) | Regeneration method of dimethylformamide as extracting solvent for cracking carbon 5 and use thereof | |
| KR100517898B1 (en) | Downflow type catalytic cracking reaction apparatus and method for producing gasoline and light oil using waste synthetic resins using the same | |
| CN103566608A (en) | Regeneration system and regeneration method for solvent of cracked C5 separation device | |
| JPH0552353B2 (en) |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20000809 |
|
| EXPY | Termination of patent right or utility model | ||
| DD01 | Delivery of document by public notice |
Addressee: Sinopec Beijing Petrochemical Engineering Company Document name: Notification of Expiration of Patent Right Duration |