WO2010073841A1 - ジシクロペンタジエンの精製方法 - Google Patents
ジシクロペンタジエンの精製方法 Download PDFInfo
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- WO2010073841A1 WO2010073841A1 PCT/JP2009/069210 JP2009069210W WO2010073841A1 WO 2010073841 A1 WO2010073841 A1 WO 2010073841A1 JP 2009069210 W JP2009069210 W JP 2009069210W WO 2010073841 A1 WO2010073841 A1 WO 2010073841A1
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- dicyclopentadiene
- fraction
- distillation
- purifying
- crude
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
- C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/343—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances the substance being a gas
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G50/00—Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2603/00—Systems containing at least three condensed rings
- C07C2603/56—Ring systems containing bridged rings
- C07C2603/58—Ring systems containing bridged rings containing three rings
- C07C2603/60—Ring systems containing bridged rings containing three rings containing at least one ring with less than six members
- C07C2603/66—Ring systems containing bridged rings containing three rings containing at least one ring with less than six members containing five-membered rings
- C07C2603/68—Dicyclopentadienes; Hydrogenated dicyclopentadienes
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/104—Light gasoline having a boiling range of about 20 - 100 °C
Definitions
- the present invention relates to a method for purifying dicyclopentadiene.
- DCPD Dicyclopentadiene
- ethylidene norbornene and cycloolefin polymers are widely used as a starting material for producing compounds such as, for example, ethylidene norbornene and cycloolefin polymers.
- purified high-purity DCPD is required. It may be said.
- DCPD is industrially manufactured by dimerizing cyclopentadiene contained in the C5 fraction in the thermal decomposition product of naphtha. In this case, a process for separating the C5 fraction from the thermal decomposition product, a dedicated facility for dimerizing the C5 fraction, and the like are required.
- dicyclopentadiene is produced by thermally decomposing a C8 or higher fraction from an LPG cracking unit and dimerizing high-purity cyclopentadiene obtained from the decomposition product.
- a method has been proposed.
- Patent Documents 1 and 2 also require great capital investment and operation costs in order to carry out thermal decomposition and dimerization.
- high-purity DCPD when used, it is generally required that not only the purity but also the hue are good.
- the economics in the production of dicyclopentadiene it is desirable that the number of distillation steps be small.
- no method has been studied for improving the hue.
- the present invention has been made in view of the above circumstances, and provides a method for purifying dicyclopentadiene, which is capable of obtaining high-purity dicyclopentadiene and is advantageous in terms of equipment cost and operation cost as compared with conventional ones.
- the purpose is to provide.
- Another object of the present invention is to provide a method for purifying dicyclopentadiene that can improve the hue of a dicyclopentadiene-containing fraction that has been purified by distillation.
- the present inventors have found that high-purity dicyclopentadiene can be separated and recovered by distillation from a specific crude dicyclopentadiene derived from a reaction product obtained by a dimerization reaction of cracked gasoline. Furthermore, the present inventors examined a method for obtaining high-purity dicyclopentadiene from a distillate containing dicyclopentadiene by a single distillation, and the colored fraction separated by distillation from the top of the distillation column. It has been found that the color can be removed by bringing a specific gas into contact with the dicyclopentadiene having an excellent hue. And the present inventors came to complete this invention based on these knowledge.
- the present invention removes the C5 fraction and the BTX fraction from the reaction product of the dimerization reaction of cracked gasoline produced as a by-product in an ethylene plant using the C2, C3, and C4 fractions as raw materials.
- a first dicyclopentadiene purification method is provided, in which dicyclopentadiene is separated and recovered by distillation of dicyclopentadiene containing dicyclopentadiene.
- cracked gasoline means a C5 to C9 fraction that is a byproduct of the ethylene unit.
- the BTX fraction means a C6 to C8 fraction such as benzene, toluene, xylene and the like.
- the first method for purifying dicyclopentadiene of the present invention it is possible to obtain high-purity purified dicyclopentadiene in one distillation column by using the specific crude dicyclopentadiene as a distillate. Become. Moreover, the crude dicyclopentadiene can be supplied as a product obtained after separation and recovery of a useful BTX fraction, which can be advantageous in terms of raw material costs.
- the first method for purifying dicyclopentadiene according to the present invention can contribute to effective utilization of crude dicyclopentadiene, which is a by-product of BTX using cracked gasoline as a raw material.
- the crude dicyclopentadiene contains 10 to 40% by mass of methyl dicyclopentadiene, and the content of methyl dicyclopentadiene in the dicyclopentadiene separated and recovered
- the crude dicyclopentadiene is preferably distilled so that the amount is less than 1.0% by mass.
- methyldicyclopentadiene refers to a compound represented by the following structural formula.
- the reaction product obtained by dimerization of cracked gasoline contains a large amount of methyldicyclopentadiene as a by-product, but in the purification of dicyclopentadiene, a large amount of methyldicyclopentadiene must be removed. Is required.
- the purified dicyclopentadiene obtained by the above purification method can be particularly useful for the production of ethylidene norbornene and cycloolefin polymers.
- the content of dicyclopentadiene in the crude dicyclopentadiene is 40 to 90% by mass, and the purity of dicyclopentadiene separated and recovered is 93% by mass.
- the crude dicyclopentadiene is preferably distilled so as to achieve the above.
- the crude dicyclopentadiene is reduced to 130 ° C. or less. It is preferable to distill at
- the present invention also provides a second method for purifying dicyclopentadiene, wherein a dicyclopentadiene-containing fraction purified by distillation is contacted with an inert gas or a hydrocarbon gas having 1 to 3 carbon atoms.
- the hue of a dicyclopentadiene-containing fraction that has been purified by distillation can be improved, and dicyclopentadiene having an excellent hue can be obtained.
- the second method of purifying dicyclopentadiene according to the present invention can obtain a sufficient hue improvement effect with equipment such as a gas-liquid contact device, it is operated in comparison with the method using an adsorbent or crystallization. This is advantageous in terms of cost and equipment cost.
- the dicyclopentadiene-containing fraction purified by distillation it is preferable to bring the dicyclopentadiene-containing fraction purified by distillation into contact with nitrogen or methane.
- nitrogen or methane gases are preferable in that they are easily available and handled in petroleum refining and petrochemical factories and are inexpensive.
- the dicyclopentadiene-containing fraction purified by distillation is distilled and purified from a distillate derived from a reaction product by a dimerization reaction of cracked gasoline.
- cracked gasoline means a C5 to C9 fraction that is a by-product of the ethylene unit.
- the cracked gasoline is preferably cracked gasoline by-produced in an ethylene plant using C2, C3 and C4 fractions as raw materials. Also in this case, it is possible to improve the hue of the dicyclopentadiene-containing fraction that has been purified by distillation, and it is possible to obtain more dicyclopentadiene with high added value from the reaction product resulting from the dimerization reaction of cracked gasoline more economically. .
- the dicyclopentadiene-containing fraction purified by distillation contains 85 to 99% by mass of dicyclopentadiene, and the total of cyclopentadiene and methylcyclopentadiene is 0. It is preferable to contain 1 to 10% by mass.
- dicyclopentadiene excellent in hue can be obtained from such fractions by sufficiently removing light impurities such as cyclopentadiene and methylcyclopentadiene.
- useful dicyclopentadiene can be efficiently recovered from the remaining fraction from which higher-purity dicyclopentadiene is taken out, and the economics in the production of dicyclopentadiene can be further improved.
- the hue of the dicyclopentadiene-containing fraction purified by distillation can exceed 100 in APHA, and the hue can be reduced to 100 or less in APHA.
- a high-purity dicyclopentadiene can be obtained, and a dicyclopentadiene purification method that is advantageous in terms of equipment cost and operation cost as compared with the prior art can be provided.
- purification method of dicyclopentadiene which can improve the hue of the dicyclopentadiene containing fraction refine
- FIG. 1 is a flow diagram showing an example of a dicyclopentadiene purification apparatus in which the first dicyclopentadiene purification method of the present invention is carried out.
- a purification apparatus 100 shown in FIG. 1 includes a distillation column 10 for distilling a specific crude dicyclopentadiene according to the first method for purifying dicyclopentadiene of the present invention.
- the distillation column 10 is connected to a recovery line L2 for recovering dicyclopentadiene separated by distillation and a recovery line L3 for extracting a fraction at the bottom of the column.
- the specific crude dicyclopentadiene according to the first method for purifying dicyclopentadiene of the present invention supplied to the distillation column 10 was by-produced in an ethylene plant using C2, C3 and C4 fractions as raw materials.
- C5 fraction and BTX fraction are removed from the reaction product of the dimerization reaction of cracked gasoline.
- the ethylene plant which uses a C2 fraction, a C3 fraction, and a C4 fraction as a raw material may be called an LPG cracker.
- the cracked gasoline may contain a C5 to C9 fraction, but in order to reduce impurities similar to dicyclopentadiene, the sum of the contents of isoprene and piperylene is 2 minutes relative to the content of cyclopentadiene. Those of 1 or less are preferable.
- reaction product for example, a product obtained by dimerizing the cracked gasoline under a liquid phase reaction condition where the reaction temperature is 75 ° C. to 200 ° C. can be used.
- the unreacted C5 fraction is removed from the reaction product by distillation, and the residue obtained by removing the BTX fraction by distillation can be used as it is as the crude dicyclopentadiene according to the present invention.
- the unreacted C5 fraction can be removed by ordinary distillation purification.
- the BTX fraction can be removed by ordinary distillation purification.
- the total content of isopropenyl norbornene (IPNB) and propenyl norbornene (PNB) is in order to increase the purity of the obtained product dicyclopentadiene to 93% by mass or more.
- the ratio is preferably less than 4% by mass relative to dicyclopentadiene, and more preferably less than 3% by mass.
- the crude dicyclopentadiene may contain methyltetrahydroindene (MeTHI), methyldicyclopentadiene (MeDCPD), etc. in addition to isopropenyl norbornene (IPNB) and propenyl norbornene (PNB).
- MeTHI methyltetrahydroindene
- MeDCPD methyldicyclopentadiene
- IPNB isopropenyl norbornene
- PPB propenyl norbornene
- the distillation column 10 a known distillation column can be used.
- the crude dicyclopentadiene is mixed with, for example, a first fraction containing dicyclopentadiene at a high concentration (a fraction having a boiling point of 160 to 170 ° C. at normal pressure), and heavy impurities such as MeTHI and MeDCPD.
- a first fraction containing dicyclopentadiene at a high concentration a fraction having a boiling point of 160 to 170 ° C. at normal pressure
- heavy impurities such as MeTHI and MeDCPD.
- the first fraction is recovered as purified dicyclopentadiene through a recovery line L2.
- the second fraction is recovered from the bottom of the tower through the recovery line L3, and can be used for, for example, liquid fuel.
- a light fraction that is lighter than the first fraction and contains light impurities such as cyclopentadiene (CPD) and methylcyclopentadiene (MeCPD) can be collected separately, and preferably through a purification method described later. Therefore, it can be used as a recovery source of dicyclopentadiene or a gaseous fuel.
- CPD cyclopentadiene
- MeCPD methylcyclopentadiene
- the number of theoretical plates of the distillation column 10 can be 30 to 60, and preferably 40 to 50 from the viewpoint of optimizing the relationship between the reflux ratio and the number of distillation steps. However, since the optimum number of stages differs depending on the composition, it can be appropriately changed.
- the distillation in the distillation column 10 is preferably performed at a temperature of 130 ° C. or lower from the viewpoint of suppressing the decomposition of dicyclopentadiene and increasing the recovery rate of dicyclopentadiene relative to the crude dicyclopentadiene.
- the temperature here refers to the temperature at the bottom of the tower.
- distillation in the distillation column 10 is carried out under conditions of a pressure of 10 to 15 kPaA at the top of the column, a temperature of 90 to 105 ° C. at the top of the column, and a temperature of 120 to 135 ° C. at the bottom of the column. It is preferable to implement as 7 times.
- a crude dicyclopentadiene containing 40 to 90% by mass of dicyclopentadiene is prepared, and the crude dicyclopentadiene is used so that the first fraction contains 93% by mass or more of DCPD. It is preferable to carry out distillation, and it is more preferred to carry out distillation so as to contain 95% by mass or more. Such distillation can be performed, for example, by adjusting the reflux ratio of the distillation column 10 and the recovery rate of dicyclopentadiene in the distillation column 10.
- the content of methyl dicyclopentadiene in the first fraction is less than 1.0% by mass.
- the crude dicyclopentadiene is preferably distilled. Such distillation can be performed, for example, by adjusting the reflux ratio of the distillation column 10 and the recovery rate of dicyclopentadiene in the distillation column 10.
- the crude dicyclopentadiene can be distilled under the condition of side-cutting from an arbitrary position from the top of the column to the feed stage, and the first fraction can be obtained from the side of the distillation column.
- the above crude dicyclopentadiene is distilled under the condition of side-cutting from 3 to 10 stages below the top of the column to obtain the first fraction from the side of the distillation column. Is preferred.
- the content of DCPD in the first fraction can be further improved, and the hue of the first fraction can be further improved.
- a light fraction obtained from the top and containing light impurities such as cyclopentadiene (CPD) and methylcyclopentadiene (MeCPD) can be recovered.
- CPD cyclopentadiene
- MeCPD methylcyclopentadiene
- it can be used as a recovery source of dicyclopentadiene or a gaseous fuel through a purification method described later.
- FIG. 2 is a flowchart showing an example of a method for obtaining the first fraction from the side of the distillation column in the first method for purifying dicyclopentadiene of the present invention.
- L22 is a line for extracting the first fraction from the side of the distillation column 10
- L21 is a line for extracting the light fraction from the top of the column.
- FIG. 3 is a flow diagram showing an example of a dicyclopentadiene purification apparatus in which the second dicyclopentadiene purification method of the present invention is carried out.
- a purification apparatus 120 shown in FIG. 3 includes a distillation column 10 for distilling a distillate containing dicyclopentadiene, a light fraction containing dicyclopentadiene purified by distillation in the distillation column 10, and an inert gas or carbon.
- a distillation column 20 is provided in contact with the hydrocarbon gas of several to three.
- the distillation column 10 is connected to a supply line L1 for supplying a distillate containing dicyclopentadiene to the distillation column 10.
- the distillation column 10 and the distillation column 20 are connected by a transfer line L21, and a light fraction containing dicyclopentadiene distilled and purified by the distillation column 10 is supplied to the distillation column 20 through the transfer line L21. . Further, the distillation column 10 is connected to a recovery line L22 for taking out a first fraction containing dicyclopentadiene distilled and purified in the distillation column 10.
- the distillation column 20 includes a supply line L4 for supplying an inert gas or a hydrocarbon gas having 1 to 3 carbon atoms to the distillation column 20, and a dicyclopentadiene-containing liquid having an improved hue from the distillation column 20.
- a recovery line L5 to be taken out and a recovery line L6 to take out light components from the distillation column 20 are connected. And in the distillation column 20, the 2nd dicyclopentadiene purification method of this invention is implemented.
- the distillate containing dicyclopentadiene supplied from L1 is a lighter fraction than dicyclopentadiene, such as those derived from the reaction product of dimerization reaction of cracked gasoline, cyclopentadiene and methylcyclopentadiene.
- a dicyclopentadiene-containing liquid contained as an impurity can be used.
- the product to be distilled is preferably derived from a reaction product obtained by dimerization reaction of cracked gasoline.
- cracked gasoline means a C5 to C9 fraction that is a by-product of the ethylene unit.
- the cracked gasoline is preferably obtained from an LPG cracker.
- the LPG cracker refers to an ethylene apparatus using C2 fraction, C3 fraction and C4 fraction as raw materials.
- the product obtained by removing the unreacted C5 fraction and BTX fraction from the reaction product of the LPG cracker cracked gasoline dimerization reaction is supplied to the distillation column 10. Is preferred. Unreacted C5 fraction and BTX fraction can be removed by ordinary distillation purification.
- the total content of isopropenyl norbornene (IPNB) and propenyl norbornene (PNB) is preferably less than 4% by mass with respect to dicyclopentadiene.
- distillate derived from the reaction product may contain methyltetrahydroindene (MeTHI), methyldicyclopentadiene (MeDCPD), etc. in addition to isopropenyl norbornene (IPNB) and propenyl norbornene (PNB). is there.
- MeTHI methyltetrahydroindene
- MeDCPD methyldicyclopentadiene
- IPNB isopropenyl norbornene
- PNB propenyl norbornene
- the distillate is a light fraction containing light impurities such as cyclopentadiene (CPD) and methylcyclopentadiene (MeCPD) and dicyclopentadiene, and a first containing dicyclopentadiene at a high concentration.
- a second fraction containing heavy impurities such as MeTHI and MeDCPD (fraction having a boiling point of 172 ° C. or higher at normal pressure).
- Light fractions containing light impurities such as CPD and MeCPD and dicyclopentadiene are transferred to distillation column 20 through transfer line L21, and the first fraction containing dicyclopentadiene at a high concentration is product through recovery line L22. As recovered.
- the number of theoretical plates of the distillation column 10 can be 30 to 60, and preferably 40 to 50 from the viewpoint of optimizing the relationship between the reflux ratio and the number of distillation steps. However, since the optimum number of stages differs depending on the composition, it can be appropriately changed.
- the distillation in the distillation column 10 is carried out under conditions of a pressure of 10 to 15 kPaA at the top of the column, a temperature of 90 to 105 ° C. at the top of the column, and a temperature of 120 to 135 ° C. at the bottom of the column. It is preferable to implement as 7 times.
- the distillate is distilled so that the light fraction contains 80 to 99% by mass of DCPD, and more preferably 85 to 95% by mass.
- the said to-be-distilled material is distilled on the conditions which side-cut from the arbitrary places from a tower top to a feed stage, and a 1st fraction is acquired from the side of a distillation tower.
- the above-mentioned distillate can be distilled under conditions of side-cutting from 3 to 10 stages below the top of the column to obtain the first fraction from the side of the distillation column.
- distillation may be performed so that the content of dicyclopentadiene in the first fraction containing dicyclopentadiene at a high concentration is 93% by mass or more and the content of MeDCPD is less than 1.0% by mass. preferable.
- the color of the first fraction obtained as a high-purity DCPD product can be made more excellent, and from the light fraction, DCPD improved in hue by the second purification method of the present invention. You can get enough.
- the hue of the light fraction is usually more than 100 in APHA, but may be 200 or more.
- APHA is measured by the color measuring method prescribed
- the second dicyclopentadiene purification method of the present invention is carried out.
- a distillation column which is a packed column is used, but any vessel can be used without particular limitation as long as it is capable of gas-liquid contact and can take out a predetermined liquid.
- the distillation column which is a plate column is mentioned.
- the number of theoretical plates of the distillation column 20 is preferably 10 to 30 plates, more preferably 15 to 25 plates, from the viewpoint of efficient separation. However, since the optimum number of stages differs depending on the composition, it can be appropriately changed.
- the light fraction can be supplied from the top of the distillation column 20, and the inert gas or the hydrocarbon gas having 1 to 3 carbon atoms can be supplied from the bottom of the distillation column 20.
- nitrogen, argon, carbon dioxide can be used.
- hydrocarbon gas having 1 to 3 carbon atoms methane, ethane, and propane can be used.
- nitrogen, methane, and ethane are preferable, and nitrogen and methane are more preferable in terms of easy availability and handling.
- the contact between the light fraction and the inert gas or the hydrocarbon gas having 1 to 3 carbon atoms can be carried out at normal temperature and normal pressure, but it is light in terms of more efficiently removing light impurities such as CPD and MeCPD. It is preferable that the fraction is preheated to 60 to 90 ° C. and then fed to the distillation column 20.
- the flow rate of the light fraction to the distillation column 20 and the flow rate of the inert gas or the hydrocarbon gas having 1 to 3 carbon atoms are set so that the gas has a volume ratio of 50 to 200 times that of the light fraction. It is preferable to do.
- the hue is improved from the distillation column 20, and a dicyclopentadiene-containing liquid containing high-purity dicyclopentadiene is recovered through the recovery line L5.
- the hue of the dicyclopentadiene-containing liquid is preferably 100 or less, more preferably 60 or less in terms of APHA.
- FIG. 4 is a flowchart showing another example of a dicyclopentadiene purification apparatus in which the second dicyclopentadiene purification method of the present invention is carried out.
- the dicyclopentadiene purification apparatus 130 shown in FIG. 4 has the same configuration as the dicyclopentadiene purification apparatus 120 except that the recovery line L22 in the dicyclopentadiene purification apparatus 120 is not provided.
- a fraction containing dicyclopentadiene distilled and purified in the distillation column 10 is purified in the distillation column 20 by the second dicyclopentadiene purification method of the present invention.
- dicyclopentadiene can be purified under the same conditions as the dicyclopentadiene purification apparatus 120 except that the acquisition of the first fraction is omitted.
- Distillation in the distillation column 10 is performed under the conditions of a pressure of 10 to 15 kPaA at the top of the column, a temperature of 90 to 105 ° C. at the top of the column, and a temperature of 120 to 135 ° C. at the bottom of the column, and the reflux ratio is 4 to 8 times, preferably 6 to 7 times. It is preferable to implement as.
- the distillate supplied through L1 is preferably distilled so that the fraction containing dicyclopentadiene taken out from L21 contains 80 to 99% by mass of DCPD, preferably 85 to 95. It is more preferable to distill so as to contain the mass%.
- a DCPD product having high purity and excellent hue can be efficiently obtained by purification and distillation purification according to the second purification method of the present invention in the distillation column 20.
- the hue of the fraction containing dicyclopentadiene extracted from the L21 is usually more than 100 in APHA, but may be 200 or more. Even in this case, a DCPD product having high purity and excellent hue can be efficiently obtained by the purification and distillation purification according to the second purification method of the present invention in the distillation column 20.
- the purification method of dicyclopentadiene of the present invention by preparing a specific crude dicyclopentadiene, high-purity dicyclopentadiene can be obtained by a single distillation using a normal distillation facility.
- the present invention can also provide an industrially advantageous method for producing dicyclopentadiene which obtains high-purity dicyclopentadiene from LPG. That is, the method for producing dicyclopentadiene includes a first step of preparing cracked gasoline by-produced in an ethylene plant using C2, C3 and C4 fractions as raw materials, and cracked gasoline prepared in the first step.
- the second to fourth steps can be performed under the conditions described above.
- the method for purifying dicyclopentadiene according to the present invention comprising the step of bringing the dicyclopentadiene-containing fraction purified by distillation into contact with an inert gas or a hydrocarbon gas having 1 to 3 carbon atoms includes, for example, a trace amount of light It can be used as a method for improving the hue of dicyclopentadiene-containing fractions colored due to impurities or a method for removing light impurities from dicyclopentadiene-containing fractions in which light impurities are not completely separated and removed.
- Example 1 Crude dicyclopentadiene having the composition shown in Table 2 obtained by removing the C5 fraction and BTX fraction from the reaction product of the dimerization reaction of cracked gasoline by-produced by the LPG cracker was prepared.
- the above-mentioned crude dicyclopentadiene heated in advance to 80 ° C. at a flow rate of 40 g / min is supplied to a distillation column (theoretical plate number: 40) having a configuration similar to that of the purification apparatus 100 shown in FIG.
- the pressure was 12.5 kPaA and the reflux ratio was 8.
- recovered from the tower top was 25 g / min, and the hue was APHA200 +.
- the second fraction was recovered from the tower bottom at a flow rate of 15 g / min. At this time, the column top temperature was 99 ° C., and the column bottom temperature was 118 ° C.
- Table 2 shows the compositions of the first fraction and the second fraction obtained.
- the composition analysis was performed by a gas chromatograph.
- Example 2 The above-mentioned crude dicyclopentadiene previously heated to 80 ° C. is supplied at a flow rate of 100 g / min to a distillation column (20 theoretical plates) having the same configuration as the purification device 110 shown in FIG.
- the pressure was 12.5 kPaA and the reflux ratio was 40.
- the first fraction was extracted as a side cut at the fifth stage position from the top of the tower and collected at a flow rate of 66 g / min.
- the light fraction recovered from the top of the tower was recovered at a flow rate of 8 g / min, and the second fraction was recovered from the bottom of the tower at a flow rate of 26 g / min.
- the column top temperature was 103 ° C.
- the column bottom temperature was 124 ° C.
- the content of dicyclopentadiene in the first fraction was 93.3% by mass.
- the hue of the 1st fraction was 60 by APHA.
- Example 3 A dicyclopentadiene-containing fraction having the composition shown in Table 3 was prepared by distillation purification from a fraction obtained by removing the C5 fraction and the BTX fraction from the reaction product obtained by dimerization of cracked gasoline by-produced by the LPG cracker. .
- the hue of this dicyclopentadiene-containing fraction was 200+ with APHA.
- the dicyclopentadiene-containing fraction heated at 65 ° C. is supplied from the top of the column to a distillation column having a theoretical plate number of 10 at a flow rate of 200 ml / min, and nitrogen is supplied from the bottom of the column at a flow rate of 2.6 L / h. Then, gas-liquid contact was performed. A recovered fraction was obtained at a flow rate of 198 ml / min. The hue of this recovered fraction was about 50 by APHA. Further, as shown in Table 3, it was confirmed that the content of CPD and MeCPD was reduced in the recovered fraction while maintaining the DCPD content sufficiently.
- the composition analysis was performed by a gas chromatograph.
- Example 4 Dicyclopentadiene-containing fractions having the compositions shown in Table 4 were prepared from the same distillate as in Example 3 by distillation. The hue of this dicyclopentadiene-containing fraction was 200+ with APHA.
- the dicyclopentadiene-containing fraction heated in advance at 90 ° C. is supplied from the top of the column to a distillation column having a theoretical plate number of 20 at a flow rate of 310 L / h, and methane is supplied from the bottom of the column at a flow rate of 35 kg / h. Gas-liquid contact was performed. A recovered fraction was obtained at a flow rate of 300 L / h. The hue of this recovered fraction was 50 by APHA. Further, as shown in Table 4, the recovered fraction had a large DCPD content, and it was confirmed that the contents of CPD and MeCPD were reduced.
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Abstract
Description
LPGクラッカーで副生した分解ガソリンの二量化反応による反応生成物からC5留分及びBTX留分を除去することにより得られた表2に示す組成を有する粗ジシクロペンタジエンを用意した。
図2に示す精製装置110と同様の構成を有する装置の蒸留塔(理論段数20段)に、予め80℃に加熱した上記の粗ジシクロペンタジエンを100g/minの流量で供給し、塔頂における圧力12.5kPaA及び還流比40とした。第1の留分は塔頂から5段目の位置でサイドカット抜き出しとし、流量66g/minで回収した。また、塔頂からの軽質留分の回収量は8g/min、塔底からは第2の留分を26g/minの流量で回収した。このときの塔頂温度は103℃、塔底温度は124℃であった。第1の留分におけるジシクロペンタジエンの含有量は、93.3質量%であった。また、第1の留分の色相は、APHAで60であった。
LPGクラッカーで副生した分解ガソリンの二量化反応による反応生成物からC5留分及びBTX留分を除去した留分から、蒸留精製され、表3に示す組成を有するジシクロペンタジエン含有留分を用意した。このジシクロペンタジエン含有留分の色相は、APHAで200+であった。
実施例3と同様の被蒸留物から蒸留により、表4に示す組成を有するジシクロペンタジエン含有留分を用意した。このジシクロペンタジエン含有留分の色相は、APHAで200+であった。
Claims (10)
- C2留分、C3留分及びC4留分を原料とするエチレンプラントで副生した分解ガソリンの二量化反応による反応生成物からC5留分及びBTX留分を除去してなる、ジシクロペンタジエンを含む粗ジシクロペンタジエン、を蒸留することによりジシクロペンタジエンを分離回収する、ジシクロペンタジエンの精製方法。
- 前記粗ジシクロペンタジエンが、メチルジシクロペンタジエンを10~40質量%含有するものであり、
分離回収されたジシクロペンタジエンにおけるメチルジシクロペンタジエンの含有量が1.0質量%未満となるように前記粗ジシクロペンタジエンを蒸留する、請求項1に記載のジシクロペンタジエンの精製方法。 - 前記粗ジシクロペンタジエンにおけるジシクロペンタジエンの含有量が40~90質量%であり、
分離回収されたジシクロペンタジエンの純度が93質量%以上となるように前記粗ジシクロペンタジエンを蒸留する、請求項1又は2に記載のジシクロペンタジエンの精製方法。 - 前記粗ジシクロペンタジエンを130℃以下で蒸留する、請求項1~3のいずれか一項に記載のジシクロペンタジエンの精製方法。
- 蒸留精製されたジシクロペンタジエン含有留分を、不活性ガス又は炭素数1~3の炭化水素ガスと接触させる、ジシクロペンタジエンの精製方法。
- 前記蒸留精製されたジシクロペンタジエン含有留分を、窒素又はメタンと接触させる、請求項5に記載のジシクロペンタジエンの精製方法。
- 前記蒸留精製されたジシクロペンタジエン含有留分が、分解ガソリンの二量化反応による反応生成物由来の被蒸留物から蒸留精製されたものである、請求項5又は6に記載のジシクロペンタジエンの精製方法。
- 前記分解ガソリンが、C2留分、C3留分及びC4留分を原料とするエチレンプラントで副生した分解ガソリンである、請求項7に記載のジシクロペンタジエンの精製方法。
- 前記蒸留精製されたジシクロペンタジエン含有留分が、ジシクロペンタジエンを85~99質量%含み、シクロペンタジエン及びメチルシクロペンタジエンを合計で0.1~10質量%含む、請求項5~8のいずれか一項に記載のジシクロペンタジエンの精製方法。
- 前記蒸留精製されたジシクロペンタジエン含有留分の色相がAPHAで100を超え、その色相をAPHAで100以下にする、請求項5~9のいずれか一項に記載のジシクロペンタジエンの精製方法。
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CA2748247C (en) | 2008-12-26 | 2019-04-02 | Jx Nippon Oil & Energy Corporation | Method for refining dicyclopentadiene |
CZ2010823A3 (cs) * | 2010-11-11 | 2012-05-23 | Unipetrol Rpa, S.R.O. | Zpusob výroby technického dicyklopentadienu |
CA2873228A1 (en) * | 2012-05-22 | 2013-11-28 | Dow Global Technologies Llc | Process for treating a dicyclopentadiene monomer |
CN109665930A (zh) * | 2017-10-16 | 2019-04-23 | 中国石油化工股份有限公司 | 一种由碳五馏分制备高纯度双环戊二烯的方法 |
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