WO2001034540A1 - Procede de production continue d'un compose tetracyclododecene - Google Patents
Procede de production continue d'un compose tetracyclododecene Download PDFInfo
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- WO2001034540A1 WO2001034540A1 PCT/JP2000/007934 JP0007934W WO0134540A1 WO 2001034540 A1 WO2001034540 A1 WO 2001034540A1 JP 0007934 W JP0007934 W JP 0007934W WO 0134540 A1 WO0134540 A1 WO 0134540A1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C13/00—Cyclic hydrocarbons containing rings other than, or in addition to, six-membered aromatic rings
- C07C13/28—Polycyclic hydrocarbons or acyclic hydrocarbon derivatives thereof
- C07C13/32—Polycyclic hydrocarbons or acyclic hydrocarbon derivatives thereof with condensed rings
- C07C13/62—Polycyclic hydrocarbons or acyclic hydrocarbon derivatives thereof with condensed rings with more than three condensed rings
- C07C13/66—Polycyclic hydrocarbons or acyclic hydrocarbon derivatives thereof with condensed rings with more than three condensed rings the condensed ring system contains only four rings
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/02—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons
- C07C2/50—Diels-Alder conversion
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- 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
- C07C2603/86—Ring systems containing bridged rings containing four rings
Definitions
- the present invention relates to a method for continuously producing tetracyclododecanes, and more particularly, to a cyclone having excellent optical properties, high transparency, heat resistance, and oil absorption.
- High-purity tetracyclodecene (hereinafter sometimes referred to as TCD), which is a raw material for fin (co) polymer, can be used for a long period of time, even when inexpensive crude DCPD is used. It relates to a method that can be manufactured continuously and stably.
- Cycloolefin (CO) polymers are attracting attention as a polymer having excellent optical properties, high transparency, heat resistance, and oil absorption, and are used as raw materials for such polymers.
- cyclohexene dicyclopentadiene (hereinafter sometimes referred to as DCPD)
- norbornanes norbornanes
- tetracyclodecenes Cyclic offers are useful.
- cyclic olefins are polymerized using an organometallic complex catalyst.
- the polymerization method can be roughly classified into two. In other words, homopolymerization of the cyclic olefin at the olefin site or copolymerization with the lower ⁇ -methyl olefin requires the use of a Ziegler catalyst or a metallocene catalyst. Polymerization proceeds with and. As the other polymerization method, metathesis polymerization using a carbene-type complex is known.
- TCDs can be produced using cyclopentene (hereinafter sometimes referred to as CPD), DCPD, or a mixture of these.
- CPD cyclopentene
- DCPD DCPD
- Diels-Alder Die 1 s -A 1 der
- a typical method is to produce a reaction mixture containing norbornane, and to recover and circulate 2-norbornene in the reaction mixture.
- Japanese Patent Application Laid-Open No. Hei 6-94437 discloses a method for producing tetradecane-dodecane, which is used to recover and recycle and regenerate such production 2-norbornane. Are known.
- An object of the present invention is to provide a method for stably and continuously producing high-purity tetracyclododecenes using inexpensive crude DCPD as a raw material.
- the first aspect of the present invention is to provide the olefin represented by the general formula (1), the crude cyclopentagene, the Z or dicyclopentagene, and the general formula (1).
- the norbornanes represented by the formula (2) are continuously supplied to the reactor to cause a heating reaction, and the norbornenes contained in the reaction mixture from the reactor and the pen-opening pen.
- Disoprene amount 1 to 100 000 mass P P m with respect to the total weight of cyclopentene and dicyclopentene
- Piperylene amount 1 to: 100,000 mass P P m based on the total weight of cyclopentene and dicyclopentene
- R t and R 2 represent the same or different groups. Each represents a hydrogen atom, a methyl group or an ethyl group.
- a second aspect of the present invention includes the following steps 1) to 5), and isoprene and piperylene in the raw material introduced into the reactor, represented by the general formula (4).
- a general formula (3) characterized in that it is produced by maintaining one, two or any two of these 2-methylnorbornenes in the following range. )), And relates to a continuous production method for tetracyclododecene.
- Disoprene amount 1 to 100 000 mass P P m based on the total weight of cyclopentene and zinc pentagene
- Piperylene amount 1 to 100,000 mass P P m based on the total weight of cyclopentene and dicyclopentene
- 1-methyl-2-norbornane represented by the general formula (4): 1 to 1 with respect to the total amount of cyclopentagen and dicyclopentagen
- R i and R 2 represent the same or different groups, and each represents a hydrogen atom, a methyl group, or an ethyl group.
- step 2 a step of separating dicyclopentadiene from the reaction mixture by distillation;
- step 5 a step of separating tetracyclododecens from the reaction mixture by distillation.
- the third aspect of the present invention is the first or second aspect of the present invention, wherein the reaction mixture When dicyclopentagen is separated from the product by a distillation column, the temperature and pressure conditions at the top and bottom of the distillation column are 50 to 12 ° C and 30 KPa or less, respectively.
- a dicyclopentadiene is extracted from the top of the distillation column under the conditions of 80 to 200 ° C and 80 KPa or less. It concerns a continuous manufacturing method.
- the fourth aspect of the present invention relates to the first or second aspect of the present invention, wherein the olefin, the crude cyclopentane, the Z or dicyclopentane, and the The reaction was carried out at a reaction temperature of 100 to 400 ° C, a reaction pressure of 0.5 to 40 MPa, a residence time of 0.1 to 360 minutes, and the number of moles of the dichloride pentagene ( Cyclopentene is converted to dicyclopentene), and the olefin is 0.1 to 50 times mol and the norbornane is 1 mol.
- the present invention relates to a method for continuously producing tetracyclododecene, which is supplied to a reactor at a molar ratio of about 50 times and reacted.
- a high-purity tetracyclododecene compound can be stably and continuously produced over a long period of time while using crude DCPD as a raw material.
- the orphans represented by the above general formula (1) used in the present invention are those containing 2 to 4 carbon atoms.
- Examples of typical orchid are ethylene, propylene, 1—butene, trans 2—butene, cis-1 2—butene, etc. In any case, it is desirable to use a polymerization grade.
- crude DCPPD is used as a diced mouth pentagene which is a raw material to be supplied.
- Crude DCPD is recovered from by-product oil obtained by thermal cracking or catalytic cracking of light hydrocarbons such as naphtha for the production of lower-grade oils such as ethylene. This is advantageous because it can be obtained in large quantities and is inexpensive.
- a crude disc-opening pentangen it is possible to use a crude disc-opening pengen of 70% by mass or more. As long as impurities are contained, higher purity products, for example, those having a purity of about 90 to 95% by mass or more can be used.
- impurities in dicyclopentenegen are as follows: isopropioninolenonorbornene, propionylnorbornene, and byurnorbornene. ⁇ Tetrahydromethylen dendene also includes methylcyclopentagen, and their content is naturally However, depending on the purity of dicyclopentene, it may contain up to 10% by mass.
- Cyclopentene is industrially obtained by pyrolysis of zinc cyclopentene, but pyrolysis of crude dicyclopentene is performed. Then, in response to the fact that it contains impurities, CPD also contains impurities.
- the raw material of the present invention advantageously contains such a crude CPD. Further, since CPD is easily dimerized into DCPD, a raw material which is a mixture of CPD and DCPD is also included in the raw material of the present invention. In the case of a CPD / DCPD mixture, the above purity refers to the sum of CPD and DCPD.
- Alkyl norebornane is prepared from olefins and cyclopentenes and Z or dicyclopentenes as a reaction temperature.
- the reaction pressure is 0.1 to 4 OMPa.
- the alkyl tetracycline can be obtained by coexisting the olefin and the dicyclopentagen and the Z or cyclopentagen.
- Alkyl nonolepollene can be produced at the same time that dodecene is produced.
- alkyl norbornane In order to synthesize tetradecane-dodecenes efficiently, it is essential that alkyl norbornane coexist in the reaction system.
- the alkylnorbornene separated from the mixture is recycled and reused as the reaction raw material. Since alkylnorbornane is a compound that is difficult to obtain industrially, in the production process of the present invention, the amount of alkylnorbornene in the reactor after the reaction is smaller than the amount of alkylnorbornene consumed in the reactor. It is important for the cyclic use of alkyl norporene to select conditions that do not result in a large or at least a small amount of alkyl norbornane produced. this Such conditions can be achieved, for example, by adjusting the molar ratio of each raw material.
- the norpolpinenes which are the raw materials of the present invention, are norbornanes represented by the above general formula (2) (hereinafter, may be referred to as alkylnorbornenes).
- R represents an alkyl group having 2 or less carbon atoms or a hydrogen atom, and specifically, 2—norbornene, 5—methyl-2-norbornene (methynorenol) (Ponorenene) ⁇ 5 — Ethanol 1 2-Nornovorenolene (Ethyl Nornovorenolen), 5, 6-Dimethylinol 2 — Nonolbornane (dimethyl) Norbonolene).
- the configuration of these substituents is arbitrary, and any isomer can be used.
- Tetracyclododecenes which are the target compounds of the method of the present invention, are tetracyclododenes represented by the above-mentioned general formula (3) (alkyltetracyclodextrins).
- R represents an alkyl group having 2 or less carbon atoms or a hydrogen atom, and specifically, 1, 4, 5, 8-di- Metanos 1, 2, 3, 4, 4a, 5, 8, 8a — ⁇ ⁇ ⁇ ⁇ ⁇ ⁇ ⁇ ⁇ ), 2 — methyl 1, 4, 4, 5, 8 — dimethyl 1, 2, 4, 4, 4a, 5, 8, 8, 8a — octahydronaphtha (Methyl dicyclodecane), 2—ethyl 1,4,5,8—dimethano 1,2,3,4,4a, 5,8,8 a — year old (Ethyl tetracyclodene), 2, 3 — dimethyl 1, 4, 5, 8 — dimethyl 1, 2, 3, 4, 4, 4a
- steric chemistries are arbitrary, and the steric structure of the substituent and the steric structure of the ring (end 0 — en do body, endo-exo body, exo-endo body, exo-exo body) are also completely arbitrary.
- FIG. 1 is a process flow showing one embodiment of the present invention.
- the supply line of alkyl norbornane at the start of the reaction is omitted.
- 1 indicates a solvent tank.
- 2 H) to prevent solidification of Circulation 2-Norbornane. Therefore, it is preferable that the solvent used has a boiling point close to that of 2-norbornene.
- an aromatic or aliphatic hydrocarbon having 6 to 8 carbon atoms is suitable.
- Alicyclic hydrocarbons and branched aliphatic hydrocarbons are more preferred because of their safety to the human body and the environment. Specifically, isohexane, isoheptane, and isooctane , Cyclohexan, methylcyclohexane, dimethylcyclohexane, ethylcyclopentane.
- isohexane, isoheptane, and isooctane are hexane, heptane, octane, etc., and are compounds having a branch more than a methyl group. It can be used regardless of its substitution position, isomer, etc., specifically, 2-methylpentane, 3-methylpentan, 2,3-dimethyl Nolebutane, 2-methylhexane, 3-methylhexane , 2,3-dimethylpentan, 2,4,1 dimethylpentan, 2,2,3-trimethylbutane, 2-methylheptan, 3-methylhepta , 4 — methylheptan, 2, 3 — dimethylhexane, 2,4 dimethylhexane, 2, 5 — dimethylhexane, 2, 2,, 3 — Trimethyltilpentan, 2, 2, 4 1 Trimethyltilpentan, 2, 3, 4 — Trimethyltilpentan, 2, 3, 3 — Trimethyltilpentane,
- Dimethylcyclohexane for example, 1,2—Dimethylcyclohexane, 1,3—Dimethylcyclohexane, 1,4-Dimethylcyclohexane Can be used, and the relative positions of the two methyl groups can be used immediately.
- branched aliphatic and alicyclic hydrocarbons close to the boiling point of norbornane 95 as described above are preferred, and these are used as a mixture with norbornane by distillation. It is preferable because it allows stable recovery at the same time and solves the problem of clogging of the distillation recovery line.
- water can be used to cool the distillation capacitor (not shown), and water and seawater can be used. Is preferably used.
- the temperature of the refrigerant ranges from 0 to 95, depending on the type and amount of the solvent used. In addition, since the boiling point of norpolunene is 95 ° C, there is a possibility that norbornane may be lost in the exhaust gas depending on the distillation pressure.
- the pressure is preferably 10 to 200 KPa, more preferably 10 to 100 kPa:
- the temperature of the refrigerant is 0 to 100 kPa, depending on the type and amount of the solvent used. 80 is appropriate.
- the solvent and the like lost in the exhaust gas during distillation can be added to the raw material tank as appropriate and replenished.
- alkyl norbornane is liquid at room temperature. Therefore, there is no necessity to use a solvent to prevent solidification as in 2-norbornene.
- the solvent can be recovered at the same time as the components to be recycled, i.e., olefin or alkylnorbornene, and more preferably simultaneously with the alkylnorbornene. I prefer it. Therefore, it is preferable to use a solvent having a boiling point close to that of alkyl norbornane, and in most cases, a solvent having the same carbon number may be used.
- Reference numeral 2 in FIG. 1 denotes a tank of the crude synchropentagen.
- the dipentic pentagenes are decomposed into the penic dipentapentanes.
- Reference numeral 3 in Fig. 1 is a tank of the Orefin. Specifically, they are ethylene, propylene, 1-butene, trans-1-butene, and si-1-2-butene.
- the amount of olefin used is determined by the number of moles of dicyclopentene (converted to dicyclopentene). When it is set to 1, the molar ratio is from 0 to 20 times, preferably from 0.2 to; I 5 times, more preferably from 0.5 to 15 times.
- the molar ratio of olefin to DCPD is less than 0.1, the amount of alkylnorbornane produced is small, and the amount of alkylnorbornene used in the synthesis of alkyltetrachlorododecene is low. It is not preferable because the amount increases and the amount of alkylnorbornane used in circulation decreases. Also, the addition of a large excess of olefin is not preferable because it consumes a large amount of energy at the time of collecting the olefin.
- the cyclopentagen and z or zinc cyclopentagen are introduced into the reactor 5 by the transfer pump 4.
- the olefin, particularly ethylene is pressurized by a booster (not shown) or the like and introduced into the reactor 5.
- the amount of alkynolenonorbornene to be supplied is 1 in terms of the number of moles of dicyclopentane (cyclopentene is converted to dicyclopentene).
- the amount supplied is 1 to 50 times mol, preferably 1 to 30 times mol, and more preferably 1 to 20 times mol. If the amount of alkyl norbornane is large, the reaction yields relatively low heavy fractions, but it requires a large amount of circulating water and requires a large amount of energy for distillation, so this is a very good solution. is not. Dicyclopen Even Jen and
- an alkyltetracyclodecene is synthesized in a reactor 5.
- Reactor 5 can use either a complete mixing type or a piston flow type.
- Commercial products of the piston-type mouth type 1 reactor include “Noritatake Power 21 Co., Ltd.” “Static Mixer” and Sumitomo Heavy Industries Co., Ltd. “Sruza Kazumi”. Kisa ”and“ Skamiki Kizaichi ”manufactured by Sakura Seisakusho Co., Ltd.
- the reactor 5 may have a single-stage structure or a multi-stage structure of two or more stages. Completely mixed reactors or piston-flow type 1 reactors can be used in series or in parallel.
- the residence time is 0.1 to 360 minutes, preferably 2 to 240 minutes. If the residence time is less than 0.1 minute, unreacted substances will increase and this is inappropriate.
- the reaction pressure is 0. It is 5 to 40 MPa, preferably l to 30 MPa.
- the reaction temperature is from 100 to 400 ° C, preferably from 150 to 300 ° C. In particular, when dicyclopentagen is used as a raw material, if the reaction temperature is 100 ° C or higher, the dicyclopentene can be easily transferred to the dicyclopentene. It is preferable because it is decomposed into.
- the olefin having a low boiling point in the reactor 5 is an anolyl-nor-norbornene-cyclopentagene and a dicyclopentane. It is preferred that it be fully dissolved in Gen. When a solvent is used, it is preferable that it be sufficiently dissolved in the solvent.
- Such a state depends on the molar mixing ratio of the alkyl norbornane, the dichloride pen and the cyclopentagen, and the olefin.
- Bruno Rubo Le when molar mixing ratio of the solvent ne on / / di emissions click b pen data
- Jefferies emissions Z et Chi les emission 8 1 1, approximately 2 in the case of temperature 1 8 0 ° C. 5 MP a more Pressure is required.
- isoprene, piperylene, and the compound of the general formula (4) are used because crude DCPD is used as a raw material.
- 1-methyl-2-norbornene, any one or two of them, or three of these (hereinafter, isoprene, piperylene and 1-methyl 1—Norbornene) is produced in the reactor.
- the produced 1-methyl-2-norbornane is distilled together with norbornene to be recycled and reused, and isoprene and piperylene are recycled and reused equally. Distill with unreacted CPD.
- isoprene, piperylene, and the like with respect to the sum of dicyclopentene and cyclopentene in the reaction raw material flowing into the reactor are described. Any one or any two or any one of the 1-methyl-2-norbornanes as the compound of the general formula (4) is within a certain range. It will be maintained.
- the total amount of DCPD and CPD means the total amount of pure DCPD and pure CPD analyzed by gas chromatography or the like.
- the range of the amount of isoprene maintained is determined by the total amount of cyclopentagen and dicyclopentane in the raw materials introduced into the reactor. 1 to 100 000 mass p pm, preferably 1 to 700 mass PP m.
- the amount of piperylene to be maintained is the total amount of cyclopentene and dicyclobenzene in the raw materials introduced into the reactor. 1 to 1000 mass p Pm, preferably 1 to 700 mass PP m (11).
- the maintained amount of 1-methyl-2-norbornane is controlled by adding cyclopentane and dicyclope in the raw material introduced into the reactor. 1 to 7 0 0 0 based on the total amount of the engine
- the amount of disoprene, amount of piperylene and amount of 1-methyl-2-norbornene can be maintained at any one, at any one of the two conditions, or at the same time.
- the conditions are maintained at the same time. Preferably, any two or more conditions are retained. If the amount of isoprene, the amount of pyrylene and the amount of 1-methyl-2-norbornane exceeds this range, the target substance is the target substance, alkyltrate cyclodode.
- the amount of by-products having a boiling point close to that of selenium is rapidly increased, resulting in a decrease in the purity of the product alkyl decylcyclodecane, which is not desirable. It is not preferable because side reactions such as generation of rubber-like polymer of isoprene-piperylene occur inside the apparatus and blockage of pipes.
- the amounts of isoprene, piperylene and 1.1-methyl-2-norporene in the raw materials are maintained and adjusted within the above-mentioned ranges.
- alkyltetracyclodecene can be produced with high purity.
- isoprene, piperylene, 1-methyl-2-norbornene is caused by impurities in crude DCPD
- adjustment of the amount is performed, for example, by using crude crude supplied to the reactor.
- the amount of circulating norbornene and the amount of unreacted CPD may be adjusted as appropriate. It can also be adjusted by adjusting the reaction temperature and other reaction conditions. Of course, it is adjusted within the range of conditions such as the above-mentioned molar ratio of raw materials, reaction temperature range and the like.
- 1-methyl-2-norbornene of the general formula (4) is represented by the following formula: It is methyl 1-norbornene, but when propylene or butene-11 is used as an olefin, 1-methyl-12-no of the above general formula (4) is used.
- Lebornanes are 1,5-dimethyl-1,2-norbornane, 1,6-dimethyl-2-norbornane, and 1-methyl-5-ethyl, respectively.
- the reaction mixture continuously withdrawn from the reactor 5 is then led to a distillation step.
- the reaction mixture from the reactor 5 is introduced into the first distillation column 6, and the pressure is adjusted to 0.1 to 1 MPa.
- unreacted olefins and cyclopentene are mainly separated from the top of the tower.
- the distillation conditions are as follows: distillation at the top: pressure 100-: L 000 KPa, temperature 25-45 ° C; pressure at the bottom 100-: L 000 KPa, temperature 25-100. Arbitrarily selected from the range of C.
- pressure 100-: L 000 KPa, temperature 25-45 ° C
- ethylene by setting the pressure slightly higher than normal pressure, it becomes possible to condense the overhead gas with inexpensive seawater or industrial water.
- the unreacted oil and cyclopentadiene separated from the top of the first distillation column 6 are recovered and used as raw materials for effective use of the unreacted raw materials. At least a part of it is circulated to the reactor 5 via the line 11 and reused. At that time, the ethylene or the like is pressurized by a pressure booster (not shown) and introduced into the reactor 5 as necessary. In addition, it can be returned to the reference tank 3 via the line 12 and used for circulation and use.
- the distillation conditions of the second distillation column 7 are 0.1 to 200 KPa at the top of the distillation column 7, preferably 1 to L00 KPa, at a temperature of 35 to 96 ° C, and at the bottom at the bottom. Pressure 0.1 to 200 KPa, preferably 1 to: L 0 0 KPa, temperature 40 to 190 ° C.
- the distillation column can be filled with various packing materials or refluxed to increase the separation efficiency.
- the number of theoretical plates in each distillation column is 1 to 100, preferably 2 to 50, and more preferably 3 to 30.
- the reflux ratio can be determined by checking the separation state of each distillation column, and usually 1 to 50 is appropriate.
- Alkyl norbornane is separated and recovered from the top of the second distillation column 7, and at least a part thereof is circulated to the reactor 5 via the line 10 and reused.
- This alkylnorporene fraction may contain cyclopentagen in some cases.
- a solvent is used in the reaction, one of the purposes of the solvent is to prevent solidification of norbornane, and it is preferable to distill the solvent together with the alkylnorbornane here.
- the recycled alkyl norbornene alone or a mixture of the recycled alkyl norbornene and the solvent used as needed passes through the recycled line 10 and reacts for reuse as a raw material. Circulate to vessel 5 As appropriate, it is mixed with the solvent or crude dicyclopentadiene supplied from the solvent tank 1 and the crude dicyclopentagentank 2 and led to the liquid feed (transfer) pump 4. Introduced into reactor 5.
- the unreacted olefin, cyclopentadiene, alkylnorbornene and, if necessary, the solvent used are separated and recovered in one distillation step. It is also possible to carry out the distillation in a column, and it is possible to withdraw these fractions at the same time from the top of the column, and to circulate at least a part of each to the reactor. it can.
- the alkyl borane fraction distilled off from the top of the second distillation column 7 is further distilled by another distillation column (not shown), so that the alkyl borane fraction at the top of the column is removed. High-purity alkylnorbornene can be extracted from the ruborene fraction.
- the reaction mixture extracted from the bottom of the second distillation column 7 is sent to the third distillation column 8 to separate dicyclopentenegen from the top of the column.
- the distillation conditions at this time are as follows: temperature and pressure conditions at the top and bottom of the distillation column are respectively 50 to: L 20 ° C, 30 KPa or less, 80 to 200 ° C, 80 KP a is preferably less than or equal to.
- the recovered fraction can be reused as a dicyclopentene raw material as appropriate.
- the desired product the alkyl silicate outlet dodecene
- the desired product is extracted from the top of the column, and heavy substances having a higher boiling point are extracted from the bottom of the column.
- the operating condition of the fourth distillation column 9 is that the pressure at the bottom of the column is 30 KPa or less, Preferably, the temperature is below 200 ° C.
- cyclopentadene and alkylnorbornane which have boiling points close to each other, are included as components to be mixed in by distillation and recovery.
- Alkyl methylcyclohexene due to the reaction of quinone with isoprene, and xenium compound at the mouth of the alkyl thiocyanate due to the reaction of olefin and butadiene have been confirmed.
- no addition reaction occurs with the pentopenthazine, and that it is not synthesized from olefin and isoprene. Therefore, these compounds have no effect even if they are mixed into the recycled raw materials to be recycled.
- an antioxidant and a polymerization inhibitor can be added.
- hydridoquinone, 2,6-di-t-butylphenol, 2,6-di-t-butyl-P-cresole, 4-methoxyphenol Hydroxylamines such as N-N-dimethylmethylhydroxylamine, N, N-dimethylhydroxylamine, N-N-dimethylmethylhydroxylamine Min compounds and the like are suitably added.
- the amount added is usually in the range of 10 to 1000 mass ppm, preferably 50 to 500 ppm by mass, based on the total amount of the reactants supplied into the reactor. You.
- it can be preferably added to the product tetracyclodecen compound in the range of 50 to 500,000 mass ppm.
- FIG. 1 is a process flow showing one embodiment of the present invention.
- 1 is a solvent tank
- 2 is a crude dicyclopentadiene tank
- 3 is an ortho-fin tank
- 4 is a pump for sending liquid
- 5 is a pump for sending liquid.
- 6 is the first distillation column
- 7 is the second distillation column
- 8 is the third distillation column
- 9 is the fourth distillation column.
- Reservoir, 1 ⁇ indicates 2-norbornane circulation line
- 11 and 12 indicate unreacted olefin circulation line.
- Norbornane Z-methylcyclohexane was mixed at a mass ratio of 85 to 15, and the crude dichloride-opened benzene and ethylene were continuously introduced into the reactor 5.
- the purity of the raw materials was norbornane (99.7% by mass), dicyclopentene benzene (73.7% by mass), and ethylene (99.9% by mass).
- Norbornane Z dicyclopentene evening ethylene has a molar ratio of 4.5 / 1/1, and crude dicyclopentagen is a crude dicyclopentagen that is not subjected to purity conversion.
- the amount of Clopentagen 1332 g was 1 mol (the same applies to the following Examples and Comparative Examples).
- Reactor 5 was maintained at 5 MPa. Based on the mixture of norbornane and methylcyclohexane, the residence time was 15 minutes, and the reaction temperature in the reactor 5 was 230 ° C.
- the reaction mixture from the reactor 5 was introduced into the first distillation column 6.
- the first distillation column 6 has 20 theoretical stages, and by operating at 400 KPa, a mixture of ethylene and cyclopentenegen is continuously separated from the top of the column to obtain a line. And then circulated to reactor 5 via
- the reaction mixture extracted from the bottom of the first distillation column 6 is then sent to the second distillation column 7, which has 30 theoretical plates, at 20 KPa and a top temperature of 43 ° C.
- norbornane and methylcyclohexane were recovered at the same time.
- the mixture extracted from the bottom of the second distillation column 7 is guided to the third distillation column 8 having 25 theoretical plates, and the unreacted distillate is obtained from the top of the column at 1 ° KPa and a top temperature of 84 ° C.
- the pentagon was separated.
- the reaction mixture extracted from the bottom of this column is guided to the fourth distillation column 9 with 25 theoretical plates, and the target substance is tetrac from the top at 3 KPa and a top temperature of 89 ° C.
- Rhodedecene was obtained.
- Heavy substances having a boiling point higher than TCD were extracted from the bottom of the tower.
- Norbornene Z dicyclopentagen Z moles of ethylene! : 8/1 Z 1 in a dagger continuously reacting, operating the first distillation column 6 at 200 KPa, discarding the separated ethylene, and The reaction conditions described in Example 1 were used except that the operating conditions in 30 were 30 KPa, the overhead temperature was 47 ° C, and norbornene and methylcyclohexane were simultaneously recovered. Continuous operation was performed.
- samples were withdrawn from the inlet of the reactor 5 where all the raw materials flowed in over time, and the pure cycle port pentagen and pure dicyclopentaner contained in each sample were extracted.
- the amounts of isoprene, piperylene, and 1-methyl-1-nonoleporene relative to the total amount of gen were measured, they were 13000 mass PPm, 1200 mass PPm, It was stable at 38,000 mass PPm, and the purity of tetracyclodecene was 94.7 mass%, which was stable and continuous operation was possible without any change with high purity.
- a continuous reaction was carried out under the same reaction conditions as in Example 1 except that the monolayer of norbornane / dicyclopentadiene / ethylene was changed to 2 / ⁇ / ⁇ .
- the reaction mixture from the reactor 5 was introduced into the first distillation column 6.
- the first distillation column 6 has 20 theoretical plates. By operating at 100 KPa, 1-butene is continuously separated from the top of the column, and the lines 11 and 1 are separated. The solution was returned to butan tank 3 via 2, and was recycled to reactor 5.
- the mixed liquid extracted from the bottom of the first distillation column 6 is sent to the second distillation column 7, which has 30 theoretical plates, and the temperature is 13 KPa, and the top temperature is 77 to 83 ° C. Chill 2-norbornene was recovered and recycled to reactor 5 through line 10.
- the mixed liquid extracted from the bottom of the second distillation column 7 is guided to the third distillation column 8 having 25 theoretical plates, and the unreacted distillate is obtained from the top at 10 KPa and a top temperature of 90 ° C.
- the cyclopentagen was separated.
- the mixed liquid extracted from the bottom of this column is subjected to fourth distillation with 25 theoretical plates
- the mixture was led to tower 9, where the desired product, ethyltetrachlorddecene, was obtained at 3 KPa from the top and at a temperature of 118 ° C. From the bottom of the column, heavy substances having a boiling point higher than that of ethyl tetracyclododecene were extracted.
- the reactor 5 was maintained at 5.0 MPa, and the reaction temperature in the reactor 5 was 230 ° C. with a residence time of 30 minutes.
- the reaction mixture from the reactor 5 was introduced into the first distillation column 6.
- the first distillation column 6 has 20 theoretical stages, and by operating at 150 KPa, propylene is continuously separated from the top of the column, and lines 11 and After returning to propylene tank 3 via 1 2, it was recycled to reactor 5.
- the mixed liquid extracted from the bottom of the first distillation column 6 is sent to the second distillation column 7, which has 30 theoretical plates, and has 20 KPa and a top methyl temperature of 51 to 81 ° C.
- 1-Norbornane was recovered and recycled to reactor 5 via line 10.
- the mixed liquid extracted from the bottom of the second distillation column 7 is led to the third distillation column 8 having 25 theoretical plates, and the unreacted distillate is obtained from the top at 10 KPa and a top temperature of 90 ° C. Clopentergen was isolated.
- the mixed liquid extracted from the bottom of this column is led to the fourth distillation column 9 having 25 theoretical plates, where 3 KPa from the top and a top temperature of 107 ° C, methyl tetramethyl Cyclododecene was obtained. From the bottom of the tower, Heavy substances having a boiling point higher than that of dodecene were extracted.
- samples were withdrawn from the inlet of the reactor 5 every time, and the total of the pure cycle mouth pen and the pure dicyclopentagen contained in each sample
- the total amount of 1,6-dimethyl-2-norbornane and 1,5-dimethyl-2-norbornane, isoprene, and piperylene were measured. At this time, they were 8.1000 mass PPm, 1900 mass PPm and 21000 mass PPm, respectively, and the purity of the product methyl tetralan chloride decene was 8%. It had a low purity of 7.8 mass 0 Zo.
- crude DCPD which is a low-purity dicyclopentagen can be used as a raw material, and Isoprene, piperylene, and the above-mentioned general formula (4) based on the total amount of the shrink-open pen and the dicyclopentane in the raw material introduced into the vessel.
- 1-methyl-2-norporenes represented by the following formulas: high power, one power, or one or two powers, or by setting these three quantities within a certain range Since it is possible to produce high-purity dicyclopentagens stably over a long period of time, its industrial utility value is extremely large.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US09/869,776 US6441259B1 (en) | 1999-11-10 | 2000-11-10 | Process for the continuous preparation of tetracyclododecens |
EP00974908A EP1151982B1 (en) | 1999-11-10 | 2000-11-10 | Process for continuously producing tetracyclododecene compound |
JP2001536491A JP4503901B2 (ja) | 1999-11-10 | 2000-11-10 | テトラシクロドデセン類の連続的製造方法 |
TW090109688A TWI256947B (en) | 1999-11-10 | 2001-04-23 | A process for the continuous preparation of tetracyclododecenes |
Applications Claiming Priority (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP11/319714 | 1999-11-10 | ||
JP11/319711 | 1999-11-10 | ||
JP11/319710 | 1999-11-10 | ||
JP31971499 | 1999-11-10 | ||
JP31971199 | 1999-11-10 | ||
JP31971099 | 1999-11-10 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2001034540A1 true WO2001034540A1 (fr) | 2001-05-17 |
Family
ID=27339746
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2000/007934 WO2001034540A1 (fr) | 1999-11-10 | 2000-11-10 | Procede de production continue d'un compose tetracyclododecene |
Country Status (5)
Country | Link |
---|---|
US (1) | US6441259B1 (ja) |
EP (1) | EP1151982B1 (ja) |
JP (1) | JP4503901B2 (ja) |
TW (1) | TWI256947B (ja) |
WO (1) | WO2001034540A1 (ja) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2001139500A (ja) * | 1999-11-10 | 2001-05-22 | Nippon Petrochem Co Ltd | ノルボルネンおよび高純度テトラシクロドデセンの同時製造方法 |
KR101053507B1 (ko) | 2009-09-28 | 2011-08-03 | 코오롱인더스트리 주식회사 | 테트라시클로도데센 유도체의 제조방법 |
WO2019026664A1 (ja) * | 2017-07-31 | 2019-02-07 | 三井化学株式会社 | シアノノルボルネンの製造方法 |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4320239A (en) * | 1981-02-13 | 1982-03-16 | The B. F. Goodrich Company | Reaction products of an olefin, a norbornene and a cyclopentadiene |
JPH03128333A (ja) * | 1989-07-10 | 1991-05-31 | Mitsui Petrochem Ind Ltd | テトラシクロドデセンの製造方法 |
JPH069437A (ja) * | 1992-06-22 | 1994-01-18 | Mitsui Petrochem Ind Ltd | テトラシクロドデセンの製造方法 |
JPH10287592A (ja) * | 1997-04-10 | 1998-10-27 | Nippon Zeon Co Ltd | 粗製テトラシクロドデセン混合物およびその製造方法、精製されたテトラシクロドデセンの製造方法およびその製造装置 |
WO2000001742A1 (fr) * | 1998-07-02 | 2000-01-13 | Nippon Petrochemicals Company, Limited | Compositions tetracyclododecene et procede de fabrication correspondant |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP3113428B2 (ja) * | 1992-06-22 | 2000-11-27 | 三井化学株式会社 | テトラシクロドデセン類の製造方法 |
-
2000
- 2000-11-10 EP EP00974908A patent/EP1151982B1/en not_active Expired - Lifetime
- 2000-11-10 US US09/869,776 patent/US6441259B1/en not_active Expired - Lifetime
- 2000-11-10 JP JP2001536491A patent/JP4503901B2/ja not_active Expired - Fee Related
- 2000-11-10 WO PCT/JP2000/007934 patent/WO2001034540A1/ja active Application Filing
-
2001
- 2001-04-23 TW TW090109688A patent/TWI256947B/zh not_active IP Right Cessation
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4320239A (en) * | 1981-02-13 | 1982-03-16 | The B. F. Goodrich Company | Reaction products of an olefin, a norbornene and a cyclopentadiene |
JPH03128333A (ja) * | 1989-07-10 | 1991-05-31 | Mitsui Petrochem Ind Ltd | テトラシクロドデセンの製造方法 |
JPH069437A (ja) * | 1992-06-22 | 1994-01-18 | Mitsui Petrochem Ind Ltd | テトラシクロドデセンの製造方法 |
JPH10287592A (ja) * | 1997-04-10 | 1998-10-27 | Nippon Zeon Co Ltd | 粗製テトラシクロドデセン混合物およびその製造方法、精製されたテトラシクロドデセンの製造方法およびその製造装置 |
WO2000001742A1 (fr) * | 1998-07-02 | 2000-01-13 | Nippon Petrochemicals Company, Limited | Compositions tetracyclododecene et procede de fabrication correspondant |
Non-Patent Citations (1)
Title |
---|
See also references of EP1151982A4 * |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2001139500A (ja) * | 1999-11-10 | 2001-05-22 | Nippon Petrochem Co Ltd | ノルボルネンおよび高純度テトラシクロドデセンの同時製造方法 |
KR101053507B1 (ko) | 2009-09-28 | 2011-08-03 | 코오롱인더스트리 주식회사 | 테트라시클로도데센 유도체의 제조방법 |
WO2019026664A1 (ja) * | 2017-07-31 | 2019-02-07 | 三井化学株式会社 | シアノノルボルネンの製造方法 |
US10774038B2 (en) | 2017-07-31 | 2020-09-15 | Mitsui Chemicals, Inc. | Process for producing cyanonorbornene |
Also Published As
Publication number | Publication date |
---|---|
EP1151982A1 (en) | 2001-11-07 |
EP1151982B1 (en) | 2012-03-28 |
US6441259B1 (en) | 2002-08-27 |
JP4503901B2 (ja) | 2010-07-14 |
TWI256947B (en) | 2006-06-21 |
EP1151982A4 (en) | 2004-12-15 |
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