CN103524287A - Processing method for ethylene cracking C5 - Google Patents
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Abstract
The invention discloses a processing method for ethylene cracking C5. The method comprises the following steps: removing below-C4 light-dydrocarbon fractions in ethylene cracking C5 so as to obtain a material subjected to below-C4 light-dydrocarbon fraction removal; under the condition of dimerization, carrying out dimerization on the material subjected to below-C4 light-dydrocarbon fraction removal so as to obtain a material subjected to dimerization; carrying out de-weighting on the material subjected to dimerization so as to obtain a material subjected to de-weighting; under the condition of primary rectification, feeding the material subjected to de-weighting into a primary rectifying tower to separate, so that concentrated isoprene is obtained from the top of the primary rectifying tower, and concentrated pentadiene is obtained in a tower kettle; under the condition of secondary rectification, feeding the concentrated isoprene into a secondary rectifying tower to separate, so that coarse isoprene is obtained from the top of the secondary rectifying tower. According to the method disclosed by the invention, the quality of coarse isoprene extracted and rectified in the next step is ensured, and the quantity of extracted and rectified coarse isoprene is increased, so that the total recovery rate of coarse isoprene is improved, therefore, the method has great industrial application value.
Description
Technical field
The present invention relates to the treatment process of a kind of cracking of ethylene C5.
Background technology
Cracking of ethylene C5(is called for short C 5 fraction conventionally) be the by product of preparing ethylene by steam cracking device, be generally about 10～20 % by weight of ethylene yield, conventionally contain tens kinds of components such as alkane, alkene, diolefin, alkynes of 4～6 carbon atoms.What wherein content was more is isoprene, cyclopentadiene and m-pentadiene, and its content is respectively in 15～25 % by weight, 12～15 % by weight, 14～20 % by weight left and right, and three accounts for 40～60 % by weight of cracking of ethylene C5.These diolefins due to have special molecular structure, chemical property active, can synthesize many important high value added products, be the precious resources of chemical utilization, take that they can produce multiple petrochemical complex and the fine chemical products such as polyisoprene rubber, specialty elastomer, petroleum resin, SIS thermoplastic elastomer, agricultural chemicals, spices, solidifying agent, fire retardant, energy-saving and smoke-removing agent, quick-acting disinfectant, medicine as raw material.
Along with the fast-developing of ethylene industry and the demand increase to synthetic rubber and synthetic resins, cracking of ethylene C 5 fraction is as a kind of important industrial chemicals, and its extraction and application has been subject to the generally attention of countries in the world day by day.At present, industrialized cracking of ethylene C5 separating technology mainly contains following several:
Acetonitrile (ACN) extraction process: acetonitrile extraction process is external one of the most widely used C 5 fraction separation method, is used the U.S. ESSO company that mainly contains, U.S. Atlantic Richfield company, the Japan SYnthetic Rubber Co. Ltd of this technology.Its know-why is divided into three steps, the first step, C 5 fraction generates dicyclopentadiene by hot dimerization reaction by the cyclopentadiene polymerization in raw material, by rectifying, cyclopentadiene and m-pentadiene are separated and obtained thick isoprene, second step, adopt the acetonitriles of moisture 5 about % by weight or the mixed solvent of acetonitrile-vinyl cyanide-acetone and water through two-stage solvent extraction rectifying separation, to remove the hydrocarbon impurities such as monoolefine in thick isoprene, alkane, alkynes, then obtain half refining isoprene through washing except the solvent acetonitrile of deentrainment; The 3rd step, half refining isoprene is by the de-polymerization grade isoprene product that obtains purity 99.5% after light, de-heavy of two-stage conventional distillation.The total recovery of isoprene be in extracting rectifying charging isoprene 90～95%.
Dimethyl formamide (DMF) extraction process: dimethyl formamide extraction process You Cheng GPIFa，You Nippon Zeon Co., Ltd. succeeded in developing and built up full scale plant in 1971.Domestic built C5 separation industries device all adopts this technology at present.Its know-why is that first C 5 fraction generates dicyclopentadiene by dipolymer reactor by cyclopentadiene polymerization in raw material, by de-heavy and rectifying separation, goes out cyclopentadiene and m-pentadiene obtains thick isoprene; Then to adopt dimethyl formamide be solvent removes the hydrocarbon impurities such as monoolefine in thick isoprene, alkane, alkynes and obtains half refining isoprene through two-stage solvent extraction rectifying separation, then by two-stage conventional distillation, half refining isoprene is purified to 99.5% polymerization grade isoprene product.The total recovery of isoprene be in extracting rectifying charging isoprene 90～95%.
N-methyl pyrrolidone (NMP) method: N-methyl pyrrolidone method is developed the earliest by German BASF AG, after improve again, be characterized in adopting the mode of the solvent extraction of N-methyl pyrrolidone and hydrogenation to remove cyclopentadiene, m-pentadiene and alkynes, rather than adopting hot dimerization to remove dicyclopentadiene, isoprene yield is compared with Gao Keda more than 97%.Its know-why is that first C 5 fraction enters extraction tower, and the side line extraction that the nmp solvent with moisture 3～10% extracts the diolefine in C 5 fraction by tower enters rectifying tower, and rectifying tower top obtains purity and is about 97% isoprene; At the bottom of tower, the mixture of dicyclopentadiene, m-pentadiene, alkynes and saturated solvent returns to extraction tower bottom again, and extracts out and enter hydrogenator from bottom, by m-pentadiene hydrocracking, is amylene and pentane, and dicyclopentadiene is converted into cyclopentenes and pentamethylene; Monoolefine after hydrogenation and alkane turn back to ，You top, extraction tower top again and deviate from.Although the yield of the comparatively simple isoprene of this technique is also higher, the purity of isoprene does not reach the requirement of polymerization-grade far away, and this technique is larger to chemical resource destruction potential in C5, and therefore domestic do not have enterprise to adopt the method.
Hence one can see that, the method that adopts C 5 fraction separation to prepare polymerization grade isoprene at present mainly contains acetonitrile extraction process and dimethyl formamide extraction process, and acetonitrile extraction process and dimethyl formamide extraction process separation of C 5 cuts all mainly comprise pre-treatment and the thick large step of isoprene extracting rectifying two of C 5 fraction, wherein, the pre-treatment of C 5 fraction mainly comprises: separated several steps of the removing of the following cut of C4, the hot dimerization of cyclopentadiene and de-heavy, isoprene and m-pentadiene; The main purpose of extracting rectifying is thick isoprene process solvent extraction rectifying and the conventional distillation that pre-treatment is obtained, and removes monoolefine, alkane and alkynes wherein, the polymerization grade isoprene that then de-light, de-recuperation is greater than 99.5% to purity.In order to guarantee that extracting rectifying can finally obtain the polymerization grade isoprene that m-pentadiene content is less than 50ppm, in the thick isoprene that pre-separation obtains, m-pentadiene concentration must be less than 10ppm.With the separating technology of current C 5 fraction, isoprene monomer is with respect to the yield of isoprene in C5 total raw material lower (being only generally 60% left and right).The rate of recovery that improves isoprene monomer has two approach, one is the rate of recovery that further improves extracting rectifying workshop section isoprene, and one is to improve by improving pre-separation technique the rate of recovery that improves isoprene into the isoprene total amount of extracting rectifying workshop section.The technical study of extracting rectifying is comparatively ripe at present, extracting rectifying workshop section isoprene total recovery generally can reach more than 92%, through de-frivolous heavy post polymerization grade isoprene, with respect to the isoprene yield in the thick isoprene of extracting rectifying charging, can reach 85% left and right (can produce a small amount of chemical industry grade isoprene), the space of isoprene yield of further improving extracting rectifying and rear centrifugal station is very limited; It is a new bright spot that thereby the improvement by pre-separating system improves the rate of recovery that improves isoprene monomer in whole C 5 fraction separating technology into the isoprene amount of extracting rectifying.When in current C5 pretreatment technology, isoprene and m-pentadiene adopt a rectifying separation, for the so a part of isoprene of quality (be m-pentadiene concentration is controlled at 10ppm following) that guarantees tower top isoprene, cut in the m-pentadiene product material at the bottom of tower (its concentration is about 15%) and produce and mix C 5 petroleum resin, but caused like this loss of isoprene monomer.
CN200710122227.3 discloses the method for the one-section abstraction separating cracked carbon 5 fraction that utilizes reactive distillation, belong to cracked, C 5 fraction separation method, the long flow path existing in order to solve prior art, the problems such as complicacy that energy consumption is high and selection hydrogenation unit is brought, a kind of method that does not need to select the one-section abstraction separating cracked carbon 5 fraction of hydrogenation has been proposed, comprise step: (1) cracking c_5 raw material is isolated the light constituents such as carbon four and alkynes in pre-lightness-removing column 1, then in pre-weight-removing column 2, through reactive distillation processes, make cyclopentadiene two be polymerized to dicyclopentadiene, and obtain the logistics that comprises isoprene, (2) logistics that comprises isoprene, through extraction tower 3 and Analytic Tower 4, obtains isoprene logistics, (3) isoprene logistics obtains polymerization grade isoprene product through reactive distillation processes in weight-removing column 5.
In recent years along with polyisoprene rubber and other adopt isoprene monomer as the thermoplastic elastic body of raw material as the developing rapidly of isoprene-isobutylene rubber, SIS etc., the economic worth of isoprene monomer is using value as other industrial chemicals higher than it more and more significantly.How on the basis of existing technology the pre-treatment of C 5 fraction to be improved to improve the yield of thick isoprene in preprocessing process, also guarantee that the separated thick isoprene obtaining meets the requirement as extracting rectifying feed preparation polymerization grade isoprene raw material simultaneously, there is industrial realistic meaning.
Polymerization grade isoprene is as a kind of raw material that has industrial application value, and its final recovery yield is the emphasis that those skilled in the art pay close attention to always.In extracting rectifying process, the most enterprises of the yield of isoprene can both reach more than 92% at present, the space of further improving its yield is less, as previously mentioned, than extracting rectifying process, the preprocessing process of cracking of ethylene C 5 fraction has larger raising space, but how to improve this preprocessing process, it is a technological difficulties, because this process not only needs to guarantee the yield of thick isoprene, and must guarantee that the thick isoprene obtaining after processing can meet the requirement as the raw material of extracting rectifying feed preparation polymerization grade isoprene.The at present pre-treatment of C 5 fraction mainly comprises: separated several steps of the removing of the following cut of C4, hot dimerization and de-weight, isoprene and m-pentadiene, and the separated of isoprene and m-pentadiene is all to carry out separation to produce thick isoprene by a step rectifying, in order to control the content of the m-pentadiene in thick isoprene, be less than 10ppm and using and meet the requirement of preparing polymerization grade isoprene raw material as extracting rectifying, adopt at present the method for single stage method rectifying separation isoprene and m-pentadiene to produce the yield of thick isoprene still limited.
Summary of the invention
The present invention relates to a kind ofly can improve thick isoprene yield, and obtain meeting the treatment process as the cracking of ethylene C 5 fraction of the thick isoprene of extracting rectifying feed preparation polymerization grade isoprene ingredient requirement.
To achieve these goals, the invention provides a kind for the treatment of process of cracking of ethylene C 5 fraction, cracking of ethylene C 5 fraction is removing the following cut of C4 first, then by removing material after the following cut of C4, be added to dipolymer reactor and react, cyclopentadiene polymerization in raw material is generated to dicyclopentadiene, and reacted material is by de-weight and rectifying separation goes out cyclopentadiene and m-pentadiene obtains thick isoprene; Then by separation of extractive distillation, remove monoolefine, alkane, the alkynes impurity in thick isoprene, and the final polymerization grade isoprene that obtains of purifying, it is characterized in that after dipolymer reactor reaction, reacted material is sent into weight-removing column, remove the above hydrocarbon-fraction of C6, comprise that the light constituent of isoprene, pentane, amylene, m-pentadiene is from overhead extraction, in de-material after heavy, the content of the above hydrocarbon-fraction of C6 is 0.01～0.03 % by weight, and m-pentadiene content is 10～20 % by weight; Described de-material after heavy is sent in the first rectifying tower and carried out rectifying separation, and tower top obtains concentrated isoprene, and tower reactor obtains concentrated m-pentadiene; In concentrated m-pentadiene, isoprene content is lower than 0.6 % by weight; To concentrate isoprene and send in Second distillation column and carry out rectifying separation, and from the tower top of Second distillation column, obtain thick isoprene, in thick isoprene, the weight content of m-pentadiene is lower than 10ppm.
In the present invention, cracking of ethylene C 5 fraction is the by product of preparing ethylene by steam cracking device, more preferably cracking of ethylene C 5 fraction contains isoprene 15～28 % by weight, m-pentadiene 12～24 % by weight, cyclopentadiene 10～28 % by weight, following light ends fractionation 5～18 % by weight of C4, above hydrocarbon-fraction 8～20 % by weight of C6.
In the present invention, optional a wider range of rectifying condition of the first rectifying tower, only need meet the condition of requirement of the present invention, specifically can form and select according to handled raw material, for the present invention, preferably described the first rectifying condition comprises: total stage number or theoretical plate number are 60～120, are preferably 70～100; Tower reactor temperature is 70～110 ℃, is preferably 80～100 ℃; Tower top temperature is 35～70 ℃, is preferably 40～65 ℃; Reflux ratio is 4～10, is preferably 5～8.
In the present invention, optional a wider range of rectifying condition of Second distillation column, specifically can form and select according to handled raw material, for the present invention, preferably described the second rectifying condition comprises: total stage number or theoretical plate number are 60～120, are preferably 70～100; Tower reactor temperature is 60～105 ℃, is preferably 65～100 ℃; Tower top temperature is 30～65 ℃, is preferably 40～60 ℃; Reflux ratio is 12～18, is preferably 13～16.
For the condition of the second rectifying is easily controlled, for the present invention, it is more than 65 % by weight that preferred described the first rectifying condition makes the content of m-pentadiene in described concentrated m-pentadiene.
In the thick isoprene that guarantee to adopt treatment process of the present invention to obtain, the amount of m-pentadiene can meet under the prerequisite of requirement of extracting rectifying, and preferably described the second rectifying condition makes in described Second distillation column still isoprene content lower than 20 % by weight.
In the present invention, the method that the following light ends fractionation of C4 in institute's cracking of ethylene C 5 fraction is removed, is not specially limited, and adopts prior art, preferably removes in the material after the following light ends fractionation of C4, and the content of the following light ends fractionation of C4 is 0.01～0.03 % by weight.
Remove optional a wider range of rectifying condition of the following light ends fractionation of C4, can select according to the composition of the raw material of handled cracking of ethylene C5, for the present invention, preferred described rectifying condition comprises: total stage number of rectifying tower or theoretical plate number are 20～50, the temperature of tower bottom of rectifying tower is 80～120 ℃, tower top temperature.
In the present invention, removing the process for dimerization that material after the following light ends fractionation of C4 carries out cyclopentadiene can carry out with reference to prior art, the present invention is not specially limited, and cyclopentadiene 90 % by weight that remove described in preferably making after dimerization in the material of the following light ends fractionation of C4 are converted above.
In the present invention, the material after dimerization takes off heavy method can carry out with reference to prior art, and the present invention is not specially limited.Generally speaking, the material after dimerization takes off heavy main purpose and is to remove the above component of C6 containing in the dicyclopentadiene that obtains after dimerization and all the other cracking of ethylene C5.
For the present invention, preferably de-heavy rectifying condition is drawn together: total stage number of weight-removing column or theoretical plate number are 20～50, and the temperature of tower reactor is 100～140 ℃, and tower top temperature is 30～60 ℃, and reflux ratio is 1～5.
Adopt the concentration of the thick middle m-pentadiene of thick isoprene obtaining in the present invention in 10ppm, can meet the requirement of preparing the raw material of polymerization grade isoprene as extracting rectifying, can remove monoolefine, alkane, the alkynes impurity in thick isoprene by conventional separation of extractive distillation, and the final polymerization grade isoprene that obtains of purifying.
The present invention is by isoprene and m-pentadiene rectifying, first the content that guarantees the yield relieving tower top m-pentadiene of isoprene is controlled, as far as possible isoprene is first separated by tower top, in making at the bottom of tower, the content of isoprene is reduced to below 0.6% by current tens percent, and then the concentrated isoprene containing 1～2% m-pentadiene concentration of having an appointment that can't meet extracting rectifying charging that tower top is obtained carries out separated again, make it reach the requirement meeting as extracting rectifying feed preparation polymerization grade isoprene raw material, the yield that so just can guarantee thick isoprene in this process maximizes, and the whole yield that improves polymerization grade isoprene in cracking of ethylene C5 separation thus.
Method than prior art, use the rate of recovery of the thick isoprene that disposal methods of the present invention obtains greatly to improve and (improve up to 24%, that is to say that the isoprene amount that can make in extracting rectifying charging improves 24%, by the extracting rectifying workshop section isoprene rate of recovery 92%, approximately can make cracking of ethylene C5 prepare the isoprene rate of recovery and improve 22 percentage points, by polymerization grade isoprene yield 85%, can make cracking of ethylene C5 prepare polymerization grade isoprene yield and improve 20 percentage points), and in the thick isoprene that treatment process of the present invention obtains, the concentration of m-pentadiene is in 10ppm, can meet the requirement of preparing the raw material of polymerization grade isoprene as extracting rectifying.As can be seen here, method of the present invention had both guaranteed the quality of thick isoprene, had improved again the rate of recovery of thick isoprene, thereby can improve total isoprene rate of recovery.
Method of the present invention has not only improved the yield of thick isoprene than prior art, and guaranteed the precision as the thick isoprene of follow-up extracting rectifying raw material, adopt method of the present invention can (only have on a small quantity separated materials at bottom of tower again by isoprene is almost completely separated with m-pentadiene in the preprocessing process of cracking of ethylene C5, can be used as the raw material of petroleum resin), thereby improved the total recovery of isoprene, and the concentration that has simultaneously improved m-pentadiene has improved its quality.As can be seen here, treatment process of the present invention only increases than prior art the maximization that a rectifying tower can realize the thick isoprene yield of cracking of ethylene C5 preprocessing process, and construction and cost of investment are little, and processing condition are simple, easily control, there is high industrial application value.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of the treatment process of cracking of ethylene C5 of the present invention.
Wherein, T1-decarburization four towers, R1-dipolymer reactor, T2-weight-removing column, T3-the first rectifying tower, T4-Second distillation column.
1-carbon Wuyuan material, the following cut of 2-C4, the rear material of 3-decarburization four, C5 and heavy constituent after 4-dimerization reaction, the de-heavy rear material of 5-, the above cut of 6-C6,7-concentrates isoprene, and 8-concentrates m-pentadiene, the thick isoprene of 9-, 10-the second rectifying residuum.
Embodiment
Below in conjunction with accompanying drawing, a kind of embodiment for the treatment of process provided by the present invention is further detailed, all the other are various can realize method of the present invention all similarly, and the present invention repeats no more.
As shown in Figure 1, method provided by the invention comprises the following steps:
(1) cracking of ethylene C5 is sent in de-C4 tower T1 to remove a small amount of following light ends fractionation of C4 in cracking of ethylene C5 raw material, tower top obtains the following light ends fractionation of C4, and tower reactor obtains removing the material of the following light ends fractionation of C4;
(2) material that removes the following light ends fractionation of C4 step (1) being obtained is sent into the dimerization (preferably the transformation efficiency of cyclopentadiene is not less than 90%) of carrying out cyclopentadiene in dipolymer reactor R1 and is obtained the material after dimerization;
(3) material after dimerization step (2) being obtained is sent in weight-removing column T2 to remove the above cut of C6, wherein the above cut of C6 distillates from tower reactor, removes the material that C6 comprises isoprene, m-pentadiene cut above (also claiming de-material after heavy) and distillates from tower top;
(4) step (3) is obtained de-heavy after material send in the first rectifying tower T3 and carry out rectifying separation, from the tower top of rectifying tower T3, obtain concentrated isoprene, tower reactor obtains concentrated m-pentadiene;
(5) concentrated isoprene step (4) being obtained is sent in Second distillation column T4 and is carried out rectifying separation, from the tower top of rectifying tower T4, obtains separated thick isoprene again, and tower reactor obtains the second rectifying residuum.
Embodiment 1
(1) Lanzhou Petrochemical chemical industry residue cracking c5 (material forms in Table 1) (flow is 400kg/hr) is sent in de-C4 tower T1 and carried out removing of the following light ends fractionation of C4, tower top obtains the following light ends fractionation 2(of C4 material and forms in Table 1), the material 3(material composition that tower reactor obtains removing the following light ends fractionation of C4 is in Table 1), wherein, the interior operating parameters of tower is in Table 2;
(2) material that removes the following light ends fractionation of C4 3 step (1) being obtained is sent into the material 4(material that the dimerization of carrying out cyclopentadiene in dipolymer reactor R1 obtains after dimerization and is formed in Table 1), wherein, dimerization condition is in Table 2;
(3) material 4 after dimerization step (2) being obtained is sent in weight-removing column T2 to remove the above cut of C6, wherein the above cut 6(of C6 material forms in Table 1) from tower reactor, distillate, the material 5(that removes the above cut of C6 also claims de-material after heavy) (material forms in Table 1) distillate from tower top, wherein, the interior operational condition of tower is in Table 2;
(4) step (3) is obtained de-heavy after material 5 send in the first rectifying tower T3 and carry out rectifying separation, from the tower top of rectifying tower T3, obtain concentrated isoprene material 7(material composition in Table 1), tower reactor obtains concentrated m-pentadiene 8(material and forms in Table 1), wherein the interior operational condition of tower is in Table 2;
(5) the concentrated isoprene material 7 step (4) being obtained is sent into and in Second distillation column T4, is carried out rectifying separation, from the tower top of rectifying tower T4, be extracted the thick isoprene 9(of rectifying charging material composition in Table 1), tower reactor obtains the second rectifying residuum 10(material and forms in Table 1), wherein the interior operational condition of tower is in Table 2.
Embodiment 2-3
According to the disposal methods cracking of ethylene C5 of embodiment 1, different, step (4) changes with the operational condition in step (5), and specifically in Table 2, all the other conditions are all identical.
Comparative example 1
According to the method for embodiment 1, process cracking of ethylene C5, different, there is no step (4), all the other conditions are in Table 2.
Table 1
Table 1 is continuous
Table 2
Note: the 1. ratio of the amount of pure isoprene in the amount of pure isoprene and raw material C5 in the thick isoprene material of isoprene yield fingering extracting rectifying in table.
2. in table, first three embodiment increases isoprene three kinds of different operating floor datas of improvement technique of knockout tower again, the 4th comparative example be existing technique (there is no isoprene separating technology again) in order to guarantee that the concentration of m-pentadiene in thick isoprene meets the requirement that extracting rectifying charging is less than 10ppm, the yield of isoprene loses greatly.
In table, data can be found out, method than prior art, adopt the rate of recovery of the thick isoprene (being reconcentration isoprene) that disposal methods of the present invention obtains greatly to improve (improving more than 20%), and in the thick isoprene that treatment process of the present invention obtains, the concentration of m-pentadiene, in 10ppm, can meet the requirement of preparing the raw material of polymerization grade isoprene as extracting rectifying.As can be seen here, method of the present invention had both guaranteed the quality of thick isoprene, had improved again the rate of recovery of thick isoprene, thereby can improve total isoprene rate of recovery, had good industrial application value.
Claims (9)
1. the treatment process of a cracking of ethylene C 5 fraction, cracking of ethylene C 5 fraction is removing the following cut of C4 first, then by removing material after the following cut of C4, be added to dipolymer reactor and react, cyclopentadiene polymerization in raw material is generated to dicyclopentadiene, and reacted material is by de-weight and rectifying separation goes out cyclopentadiene and m-pentadiene obtains thick isoprene; Then by separation of extractive distillation, remove monoolefine, alkane, the alkynes impurity in thick isoprene, and the final polymerization grade isoprene that obtains of purifying, it is characterized in that after dipolymer reactor reaction, reacted material is sent into weight-removing column, remove the above hydrocarbon-fraction of C6, comprise that the light constituent of isoprene, pentane, amylene, m-pentadiene is from overhead extraction, in de-material after heavy, the content of the above hydrocarbon-fraction of C6 is 0.01～0.03 % by weight, and m-pentadiene content is 10～20 % by weight; Described de-material after heavy is sent in the first rectifying tower and carried out rectifying separation, and tower top obtains concentrated isoprene, and tower reactor obtains concentrated m-pentadiene, and in concentrated m-pentadiene, isoprene content is lower than 0.6 % by weight; To concentrate isoprene and send in Second distillation column and carry out rectifying separation, and from the tower top of Second distillation column, obtain thick isoprene, in thick isoprene, the weight content of m-pentadiene is lower than 10ppm.
2. treatment process according to claim 1, is characterized in that the content of m-pentadiene in concentrated m-pentadiene is more than 65 % by weight.
3. treatment process according to claim 1, is characterized in that in Second distillation column tower reactor that isoprene content is lower than 20 % by weight.
4. treatment process according to claim 1, is characterized in that its rectifying condition of the first rectifying tower comprises: theoretical plate number is 60～120, and tower reactor temperature is 70～110 ℃, and tower top temperature is 35～70 ℃, and reflux ratio is 4～10.
5. according to the treatment process described in any one in claim 1 or 3, it is characterized in that its rectifying condition of Second distillation column comprises: theoretical plate number is 60～120, and tower reactor temperature is 60～105 ℃, and tower top temperature is 30～65 ℃, and reflux ratio is 12～18.
6. treatment process according to claim 1, rectifying condition when the following light ends fractionation of C4 in cracking of ethylene C5 removes that it is characterized in that comprises: the theoretical plate number of rectifying tower is 20～50, the temperature of tower bottom of rectifying tower is 80～120 ℃, and tower top temperature is 30～60 ℃, and reflux ratio is 8～15.
7. treatment process according to claim 1, it is characterized in that reacted material sends into weight-removing column, remove the above hydrocarbon-fraction of C6, the rectifying condition of weight-removing column comprises: the theoretical plate number of weight-removing column is 20～50, the temperature of tower reactor is 100～140 ℃, tower top temperature is 30～60 ℃, and reflux ratio is 1～5.
8. treatment process according to claim 1, is characterized in that removing material after the following cut of C4 and is added to dipolymer reactor and reacts, and cyclopentadiene 90 % by weight in material are converted above.
9. treatment process according to claim 1, it is characterized in that cracking of ethylene C 5 fraction contains isoprene 15～28 % by weight, m-pentadiene 12～24 % by weight, cyclopentadiene 10～28 % by weight, following light ends fractionation 5～18 % by weight of C4, above hydrocarbon-fraction 8～20 % by weight of C6.
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Non-Patent Citations (3)
| Title |
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| 吕世军: "C5馏分分离新工艺的基础研究和萃取剂的选择与优化研究", 《中国博士学位论文全文数据库 工程科技I辑》 * |
| 唐保良等: "萃取法分离异戊二烯工艺分析", 《甘肃科技》 * |
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Application publication date: 20140122 |