WO1998040448A1 - Procede de preparation de diene conjugue purifie - Google Patents
Procede de preparation de diene conjugue purifie Download PDFInfo
- Publication number
- WO1998040448A1 WO1998040448A1 PCT/JP1998/001011 JP9801011W WO9840448A1 WO 1998040448 A1 WO1998040448 A1 WO 1998040448A1 JP 9801011 W JP9801011 W JP 9801011W WO 9840448 A1 WO9840448 A1 WO 9840448A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- extractive distillation
- extraction solvent
- distillation column
- supplied
- conjugated gen
- Prior art date
Links
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- 239000011593 sulfur Substances 0.000 description 1
- IFLREYGFSNHWGE-UHFFFAOYSA-N tetracene Chemical compound C1=CC=CC2=CC3=CC4=CC=CC=C4C=C3C=C21 IFLREYGFSNHWGE-UHFFFAOYSA-N 0.000 description 1
- 238000011282 treatment Methods 0.000 description 1
- FEONEKOZSGPOFN-UHFFFAOYSA-K tribromoiron Chemical compound Br[Fe](Br)Br FEONEKOZSGPOFN-UHFFFAOYSA-K 0.000 description 1
- 238000003809 water extraction Methods 0.000 description 1
Classifications
-
- 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
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/08—Azeotropic or extractive distillation
Definitions
- the present invention relates to a method for producing a purified conjugated gen, comprising a step of separating a conjugated gen from a petroleum fraction containing a conjugated gen such as a C4 hydrocarbon fraction / C5 hydrocarbon fraction by extractive distillation. More specifically, when separating and purifying conjugated gens such as high-purity isoprene-butadiene from petroleum oil fractions, while suppressing the production of polymers inside the refinery, The present invention relates to a method for producing a purified conjugated gen.
- the manufacturing method of this invention in the separation-refining process of the conjugated gen from the petroleum fraction, the polymerization of the conjugated gen is prevented.
- the generation of polymer is suppressed, the dirt of the distillation tower and the heat exchanger is prevented, and further, the clogging of the pipe and the decrease in thermal efficiency are less likely to occur.
- 1,3—Conjugated gens such as butadiene, isoprene, and macroplane are accidentally porous insoluble polymers (so-called popcorn) in both the liquid and gaseous phases.
- Polymer or a rubbery polymer.
- polymerization such as appropriate operating temperature, high monomer purity, coexistence of gas and liquid phases, mixing of water, and the presence of iron oxide are considered. Conditions that are likely to occur are available o
- the porous insoluble polymer is a crosslinked solvent insoluble polymer, It is called a popcorn polymer because of its appearance. Once produced, this popcorn polymer, as a seed, self-proliferates exponentially in the presence of conjugated diene vapors and liquids. Quickly clog parts. Since the popcorn polymer is a tough crosslinked polymer, it is insoluble in known solvents and does not melt when heated. Therefore, the popcorn polymer is extremely difficult to remove.
- conjugated gens such as 1,3-butadiene and isoprene are generally obtained from petroleum fractions containing conjugated genes such as C4 hydrocarbon fraction and C5 hydrocarbon fraction. It is separated and purified by a series of distillation operations including extractive distillation. Since a petroleum fraction containing conjugated gen contains a large number of hydrocarbons having similar boiling points, conjugated gen cannot be separated and purified only by distillation using a boiling point difference. Therefore, in the process of separating and purifying conjugated gens from petroleum fractions, a process for separating conjugated gens by extractive distillation utilizing the difference in solubility in solvents is arranged.
- Japanese Patent Publication No. 47-41323 and Japanese Patent Publication No. 45-196682 contain a conjugated gen.
- a method of extracting and distilling the resulting hydrocarbon mixture using an extraction solvent to which a polymerization inhibitor or a chain transfer agent has been added is disclosed.
- Japanese Patent Application Laid-Open No. 56-81526 and Japanese Patent Publication No. 43-220281 disclose a petroleum fraction containing a conjugated gen, furfural and furfural weight.
- a method of performing extractive distillation using an extraction solvent to which a condensate has been added is disclosed.
- An object of the present invention is to provide a method for producing a purified conjugated gen which includes a step of separating conjugated gen from a petroleum fraction containing conjugated gen by extractive distillation for a long time.
- An object of the present invention is to provide a production method capable of suppressing generation of a polymer or a rubbery polymer.
- an object of the present invention is to prevent the polymerization of conjugated gens in an extractive distillation apparatus, thereby suppressing the formation of polymers, dirt in the apparatus, clogging of pipes, and a decrease in thermal efficiency.
- An object of the present invention is to provide a method for producing a purified conjugated gen.
- a purified conjugated gene comprising a step of separating a conjugated gene from a petroleum fraction containing the conjugated gene by extractive distillation.
- an amide compound is used as an extraction solvent, and water is present in a specific ratio in an extraction solvent composed of the amide compound, whereby the conjugated It has been found that polymerization of the polymer can be prevented.
- the production of a popcorn polymer or a rubbery polymer can be suppressed even during a long-term operation, so that dirt and clogging of the device can be prevented. Moreover, in the method of the present invention, since the water concentration in the extraction solvent is adjusted within a specific range, corrosion of the apparatus is not promoted. The present invention has been completed based on these findings.
- a method for producing a purified conjugated gen which includes a step of separating the conjugated gen from a petroleum fraction containing the conjugate by extractive distillation,
- FIG. 1 is a schematic diagram of an example of a separation and purification apparatus used in a method for producing purified butadiene, which includes a step of separating butadiene from a C4 hydrocarbon fraction by extractive distillation.
- the petroleum fraction containing a conjugated gen used in the present invention may be any hydrocarbon mixture containing a conjugated gen, and its composition is not particularly limited.
- Representative examples of such a petroleum fraction include a C4 hydrocarbon fraction containing 1,3-butadiene and a C5 hydrocarbon fraction containing isoprene. You.
- Such petroleum fractions are usually those obtained by cracking naphtha and separating C2 and C3 hydrocarbons such as ethylene and propylene. More preferably, the concentration of the conjugated gen in these petroleum fractions is increased by extractive distillation or the like.
- the production method of the present invention is particularly suitably used for a petroleum fraction containing 1,3-butadiene.
- the oil fraction containing the conjugated gen is usually fed to the middle stage of the extractive distillation column.
- a method for producing a purified conjugated gen which includes a step of separating conjugated gen by extraction distillation from a petroleum fraction containing conjugated gen, includes an extraction distillation step using an extraction solvent, and a distillation step using a boiling point difference.
- a typical method is a distillation operation that combines the above. Therefore, a specific example will be described.
- C4 hydrocarbon fractions such as naphtha cracked oils generally include propane, propylene, isobutene, arene, n-butane, isobutene, 1-butene, Trans 1-butene, cis 1-2-butene, 1,3-butadiene, methyl acetylene, 1,2-butadiene, vinyl acetylene ing.
- a distillation process using an extraction distillation process and a boiling point difference is usually used. And a separation and purification process combining the above.
- C5 hydrocarbon When producing ethylene by steam cracking and other high temperature treatments of hydrocarbons, a C5 hydrocarbon fraction is by-produced.
- C5 hydrocarbon In general, n-pentane, isopentane, 1-pentene, 2-methyl-1-butene, trans-2-pentene, cis-12-pent 2-, methyl-2--butene, isoprene, trans-1-1,31-pentagen, cis-1,3-penta-gen, 1,4-pentadiene, 2- Contains butyne, isopropenyl acetylene, isopropyl acetylene, cyclopentane, cyclopentene, cyclopentagen, and others.
- Methods for recovering high-grade isoprene of polymerization grade from the C5 hydrocarbon fraction include, for example, (1) pentanes, pentenes, etc. from the C5 hydrocarbon fraction in the first extractive distillation step. (2) The isoprene extracted in the first extraction distillation step was removed as a raffinate to remove substances (solubility-soluble hydrocarbons) with lower solubility in the solvent than isoprene. Most of cyclopentagen is obtained from an extract containing a substance having a higher solubility in a solvent (easily soluble hydrocarbon) than isoprene by a high-boiling-point removal distillation process.
- a two-stage extractive distillation process consisting of a first extractive distillation process for the purpose of removing hydrogen and a second extractive distillation process for the purpose of removing readily soluble hydrocarbons; and During or after the extractive distillation step, a distillation step utilizing the boiling point difference is appropriately arranged. Separation of conjugated gens from hydrocarbon mixtures is performed by extractive distillation, and the distillation process is used for further purification. Is arranged.
- such a separation / purification process involves additional steps such as separation, recovery, purification, and reflux of the extraction solvent.
- a separation and purification process may include a step of removing a polymerization inhibitor such as acetylene by a chemical reaction.
- Figure 1 shows an example of the process and equipment for producing 1,3—butadiene by separating and recovering 1,3—butadiene from a C 4 hydrocarbon fraction containing 1,3—butadiene. Is shown.
- the gasified C4 hydrocarbon fraction is supplied from tube 1 to the middle stage of the first extractive distillation column A, and the extraction solvent such as N, N-dimethylformamide is supplied from tube 2. Then, the bottom is heated by a reboiler 8 through a pipe 7 to perform the first stage extractive distillation.
- hydrocarbons with lower solubility in the extraction solvent than 1,3-butadiene (propane, propylene, isobutene, arene, n-butadiene) , Isobutene, 1-butene, trans-1—butene, cis-1—butene, etc.), from the top, tube 3, condenser 4. Removed via tube 6.
- the main components of raffinate are butenes. However, the gas from the top is condensed by the condenser 4 and a part of the condensate is returned to the top of the extractive distillation column A via the pipe 5.
- the pressure in the first distillation column A is usually 1 to 10 atm, and the bottom temperature is usually 100 to 160 ° C.
- the number of stages of the extractive distillation column A can be set as appropriate, but it is usually about 100 to 300, and in most cases about 100 to 200.
- hydrocarbons methylacetylene, 1,2-butadiene having higher solubility in extraction solvents than 1,3-butadiene and 1,3-butadiene , Vinyl acetylene, etc.
- the extracted liquid is taken out and supplied via pipe 9 to the top of the first stripping tower B. Heated by a reboiler 19 via a pipe 18 at the lower part of the stripping tower B, the hydrocarbon is evaporated and separated from the solvent.
- the pressure in the stripping tower B is usually 1 to 2 atm, and the bottom temperature is the boiling point at that pressure.
- Butadiene and acetylene are taken out from the top of the stripping tower B, liquefied in the cooler 11 through the pipe 10, and separated into gas and liquid. Part of the liquid is returned to the top of the stripping tower B via pipes 12 and 13, and the remainder is sent to the washing tower F via pipe 14.
- the extraction solvent is taken out through the pipe 20 and is pumped by the pump 21 through the pipe 22, the pipe 23, the cooler 24, and the pipe 25. It is circulated to the first extractive distillation column A via the tube 2 or supplied to the second extractive distillation column C via the tubes 25 and 26.
- the gas exiting the cooler 11 is led to a compressor 16 via a pipe 15, compressed there, and then supplied to an intermediate stage of the second extractive distillation column C via a pipe 17. .
- the extraction solvent is supplied to the second extractive distillation column C from a tube 26.
- the mixture is heated by a reboiler 33 via a pipe 32 to perform second-stage extractive distillation.
- the second extractive distillation column C is mainly supplied with 1,3-butadiene and hydrocarbons having a higher solubility in the extraction solvent than 1,3-butadiene.
- the gas at the top of the second extractive distillation column C is 1,3-butadiene containing a small amount of impurities, which is condensed in the condenser 28 via the pipe 27 and returned to the top via the pipe 29 The remaining part is sent to the first distillation column G via a pipe 30.
- a liquid mainly composed of a solvent at the bottom of the second extractive distillation column C is sent to an intermediate stage of the butadiene recovery column D via a pipe 34.
- the distillate taken out from the top of the recovery tower D is sent to the compressor 16 via the pipe 35.
- Collection The discharge from the bottom of the tower D is supplied to the top of the second stripping tower E via a pipe 38, a pump 39, and a pipe 40.
- a reboiler 37 is arranged via 36.
- the extraction solvent is recovered from the bottom of the second stripping tower E, and then passed through pipes 48, 49, 50, etc., from pipe 2 to the first extraction tower A, or from pipe 26 to the second extraction tower A. Reflux to extractive distillation column C.
- the distillate taken out from the top of the stripping tower E passes through the pipe 41 and liquefies in the condenser 42.
- the water is returned to the stripping tower E via 4 3 and 4 4, and the remainder is supplied to the intermediate stage of the washing tower F via the pipe 45.
- the second stripping tower E At the bottom of the second stripping tower E, it can be heated by a reboiler 47 through a pipe 46.
- the operating conditions for the second extractive distillation column C and the second stripper E are the same as those for the first extractive distillation column A and the first stripper B, respectively.
- Water is supplied from the pipe 52 to the top of the washing tower F, and the extraction solvent is washed with water and purified.
- the purified extraction solvent passes through the pipe 55, the pump 56, the pipe 57, etc., joins with the extraction solvent flowing from the pipe 23, and then from the pipe 2 to the first extractive distillation column A. From the pipe 26, the water is refluxed to the second extractive distillation column.
- the amount of water in the extraction solvent withdrawn from the bottom of the washing tower F so that the amount of water in the extraction solvent in the tubes 2 and 26 is within the range of 50 to 100 ppm.
- a method of adjusting the amount of water for example, there is a method of adding water to a purified extraction solvent.
- a reboiler 54 is arranged via a pipe 53.
- the gas extracted from the top of the second extractive distillation column C is condensed by the condenser 28, and a part of the condensate is returned from the pipe 28 to the top of the second extractive distillation column C, and the remainder is It is fed from the pipe 30 to the top of the first distillation column G.
- impurities having a boiling point lower than that of 1,3-butadiene are removed.
- the distillate from the top of the first distillation column G is passed through a condenser (not shown) Condensed, a part of the condensed liquid is returned to the first distillation column G, and the remainder is discharged from the pipe 58 and incinerated as boiler fuel or by freezing.
- the product discharged from the bottom of the first distillation column G is supplied to the second distillation column H via a pipe 59.
- the distillate discharged from the top of the second distillation column H is condensed by a condenser (not shown), a part of the condensed liquid is returned to the second distillation column H, and the remainder is connected to a pipe 60. Extracted as high-purity 1,3-butadiene products.
- the stream at the bottom of the second distillation column H is discharged from the pipe 61.
- the operating conditions of each of the distillation columns G and H can be controlled such that the pressure in the column is 1 to 15 atm and the temperature in the column is the boiling point at that pressure.
- the number of stages in the distillation column can be set as appropriate, but is usually 50 to 200 stages, and in many cases, about 100 stages.
- the conjugated gen-containing oil fraction is subjected to extractive distillation by an extractive distillation column using an extraction solvent comprising an amide compound, and
- the method is characterized in that the extraction solvent in the extraction solvent supply stage is adjusted so that a specific amount of water is present. This prevents polymerization of the conjugated gen in the separation and purification process. Therefore, the present invention can also be referred to as a method for preventing polymerization of conjugated gen.
- the amount of water in the extraction solvent in the extraction solvent supply stage is 50 to 100 ppm, preferably 100 to 500 ppm, based on the extraction solvent. If the amount of water in the extraction solvent is too small, a polymer is likely to be generated, which causes a problem such as clogging of an installation pipe. On the other hand, too much water will promote corrosion of the equipment.
- amide compounds include formamide, NN—dimethylformamide, acetoamide, N—ethylethylacetamide, NN—dimethylethylamide, N — Chloroacetamide, N — Bromoacetamide, Jacetamide, Triacetamide, Propionamide, Petilamide, Isobutylamide, Isobutylamide Mid, Isorel Amid, Hexan Amid, Heptane Amid, Octane Amid, Decan Amid, Acrynorea Amid, Chromoacet Amid, Diclo Low Acet Amid, Trichloro Acet Amid, Glycol Amid, Lact Amid, Pyr Bo Amid, Cyan Acet Amid, 2—Cyan 2—2 To Roacetam, Oxamido, Ma N'a Mi De, click shea N'a Mi de, A Jipoa Mi de, Mar A Mi de, d
- the amount of the extraction solvent is usually 100,000 parts by weight, preferably 200,000 parts by weight, based on 100 parts by weight of the petroleum fraction containing the conjugated gen. Parts by weight.
- the extraction solvent is usually provided at an upper position than the stage for supplying the petroleum fraction (or hydrocarbon mixture) containing the conjugated gen in each extractive distillation column (the petroleum fraction supply stage).
- the extracted solvent is supplied to the extraction distillation column from the extraction solvent supply stage.
- the petroleum fraction containing the conjugated gen is fed to the middle stage of the extractive distillation column, and the distillate coming from the top of the extractive distillation column, preferably from the condenser, is in the gas phase. It is preferable to measure the oxygen concentration and to extract a part of the gas phase so that the oxygen concentration is equal to or less than a specific value.
- the method for measuring the oxygen concentration in the gas phase of the fraction coming out of the extractive distillation tower is not particularly limited.
- the extractive distillation tower or condenser
- a part of the gas phase may be extracted from the line connected to the outlet part of the sample, and the gas phase may be measured, or an oxygen concentration measuring device may be buried in the line to perform the measurement at all times.
- the oxygen concentration in the gas phase of the distillate emerging from the top of the extractive distillation column is preferably 20 ppm or less, more preferably 1 O ppm or less, and even more preferably. Extract a portion of the gas phase so that it is less than 5 ppm.
- the extracted gas phase may be discharged from a freezer or the like, but it is mixed with a petroleum fraction (or hydrocarbon mixture) containing a conjugated gen, which is a feedstock, and supplied to the extraction distillation column again. This is preferable in order to increase the separation and purification yield of the conjugated gen. If the oxygen concentration is too high, a polymer is likely to be generated in a condenser or the like, which may cause soiling of the device or blockage of a pipe or the like.
- heterocyclic aldehyde, aromatic nitro or aromatic aldehyde be present in the extraction solvent.
- Heterocyclic Al used in the present invention
- the aldehyde, the aromatic or aromatic aldehyde is an aldehyde having a heterocycle, a nitro having a benzene ring, or an aldehyde having a benzene ring, respectively.
- Heterocyclic aldehydes include, for example, furfural, 5—methylnorefral, 5— (hydroxymethyl) furfural, thiophencarbaldehyde, Examples include nicotinaldehyde and pyridoxal. Of these, furfural is preferred.
- aromatic aldehyde examples include, for example, benzaldehyde, trialdehyde, cuminaldehyde, phenylacetonaldehyde, gennamaldehyde, phthalanolaldehyde, isoaldehyde.
- aromatic aldehyde examples include phthalaldehyde and telephthalaldehyde. Of these, benzaldehyde is preferred.
- aromatic nitro examples include, for example, nitrobenzene, nitrotoluene, 1-nitronorenene, nitroxylen, nitromesilylene and dinitrobenzene. Nitrobenzen, dinitrothroene, dinitroxylene, trinitrate benzene, trinitroxylen and the like. Of these, nitrobenzene is preferred.
- the amount of the heterocyclic aldehyde, aromatic di- or aromatic aldehyde is usually from 0.01 to 10% by weight, preferably from 0.01 to 10% by weight, based on the extraction solvent in the extraction solvent supply stage. It is 5 to 5% by weight.
- the amount of the heterocyclic aldehyde polycondensate or the aromatic aldehyde polycondensate is usually 0.5 to 10% by weight, preferably 1 to 5% by weight, based on the extraction solvent in the extraction solvent supply stage. %.
- the extraction solvent used in the present invention preferably contains an oxygen scavenger.
- the oxygen scavenger include nitrites such as calcium nitrite and sodium nitrite; amides such as hydroxylamine and hydrazine; sodium dithionite Dithionites such as lime; calcium sulphite, sulphite lime, manganese sulphite, sodium sulphite and the like; and the like. Of these, nitrite is preferred.
- the oxygen scavenger removes oxygen in the extraction solvent and prevents the generation of radicals, further enhancing the polymerization inhibiting effect.
- oxygen in the gaseous phase circulates in the extractive distillation column, and the oxygen scavenger in the extraction solvent And the oxygen concentration in the gas phase of the distillate can be reduced.
- the amount of the oxygen scavenger is usually 0.1 to 1.0 parts by weight of the extraction solvent. ⁇ 1.5 parts by weight, preferably 0.2 ⁇ 0.8 parts by weight.
- the polymerization inhibitor used in the present invention is generally capable of inhibiting or suppressing the polymerization of conjugated gen.
- polymerization inhibitor examples include metal salts such as ferric chloride and ferric bromide.
- polymerization inhibitors those which inhibit or inhibit polymerization by a chain transfer reaction, particularly di-lower alkylhydroxylamine, specifically getylhydroxylamine, are preferred.
- the amount of the polymerization inhibitor is usually 0.1 to 20 ppm, preferably 0.5 to ppm0 ppm, based on the total amount of the petroleum fraction containing the conjugated diene and the extraction solvent. Straightforward.
- the position where the polymerization inhibitor is supplied to the extractive distillation column is, for example, at the side of the extractive distillation column above the extractive solvent supply stage, at the inlet or outlet of the condenser at the top of the extractive distillation column.
- installing at the inlet of the condenser at the top of the tower can effectively suppress the production of polymer in the condenser and also suppress the production of polymer in the next step I like it because I can do it.
- the gasified C4 fraction is fed to the middle stage of the first extractive distillation column A, and N, N-dimethylformamide (1%) containing 1% of full fluor and 300 ppm of water Extraction solvent a.) was supplied from tube 2 and heated at the bottom with a reboiler 8 to perform the first-stage extractive distillation.
- the gas taken out from the top of the extractive distillation column A was condensed by the condenser 4, and a part of the liquid was refluxed and returned to the top.
- the remaining portion was a fraction containing a large amount of butane, petylene, etc., and was taken out of the tube 6.
- Butadiene, high-grade acetylene, and arene-based hydrocarbons are taken out from the top of stripping tower B, liquefied in cooler 11, and a part of the liquefied liquid is transferred to the top of stripping tower B.
- the mixture was refluxed, and the remainder was sent to the washing tower F via the pipe 14.
- Extraction solvent a was taken out from the bottom of the stripping tower B and circulated to the first extractive distillation column A or the second extractive distillation column C via the pipe 2 or 26 via the condenser 24 by the pump 21. .
- the gas exiting the cooler 11 was supplied to the intermediate stage of the second extraction distillation column C via the compressor 16 and the pipe 17.
- Extraction solvent a was supplied from tube 26, and getyl hydroxylamine was supplied from tube 31 provided in front of the inlet of condenser 28.
- the second extractive distillation was performed by heating at the bottom of the second extractive distillation column C with a reboiler 33.
- the liquid removed from the bottom of the second extractive distillation column C is in the middle of the recovery column D. Sent to the stage. The distillate taken out from the top of the recovery tower D was sent to the compressor 16 via the pipe 35.
- the bottoms taken out from the bottom of the recovery tower D is supplied to the top of the second stripping tower E via the pump 39 and the pipe 40, and the extraction solvent is recovered from the bottom of the stripping tower E and the stripping tower.
- the distillate taken out from the top of E was liquefied in a condenser 42, a part of which was refluxed to a stripping tower E, and the remainder was supplied to an intermediate stage of a washing tower F via a pipe 45.
- Water is supplied from the pipe 52 to the top of the washing tower F, and the extraction solvent a is purified so that the amount of water in the extraction solvent a in the pipes 2 and 26 becomes 300 ppm (for example, The amount of water was adjusted (for example, by adding water).
- the extraction solvent a whose water volume has been adjusted, passes through the pipe 55, the pump, 56, and the pipe 57, merges with the extraction solvent a flowing from the pipe 23, passes through the pipe 2 and the pipe 26, and performs the first extraction distillation It was recycled to column A and second extractive distillation column C.
- the gas extracted from the top of the second extractive distillation column C was condensed by the condenser 28, and some of the liquid was refluxed and returned to the top.
- the remainder was taken out of the pipe 30 and fed to the top of the first distillation column G.
- the distillate discharged from the top of the first distillation column G is condensed in a condenser (not shown), part of the distillate is returned, and the remainder is used as fuel for boilers or free fuel. Incinerated.
- the bottoms discharged from the bottom of the first distillation column G was supplied to the middle stage of the second distillation column H.
- the distillate discharged from the top of the second distillation column H is condensed in a condenser (not shown), a part of the distillate is refluxed, and the remainder is high-purity 1,3-butadiene. Extracted and supplied as raw materials such as polybutadiene.
- the popcorn polymer and the rubbery polymer were found in the refining equipment, especially in the condenser 28, the second distillation column C and the reboiler 33. It was generated in large quantities and was very dirty. Also, the reboiler 33 had been closed for a year and a half, so it was necessary to disassemble and clean it.
- Example 1 The extraction solvent a used in Example 1 was replaced with 1,650 ppm of water. 1,3-butadiene was separated and purified from the C4 fraction in the same manner as in Example 1 except that the contained N, N-dimethylformamide was replaced.
- the polymerization reaction can be effectively prevented in the process of separating and purifying conjugated gen from a petroleum fraction containing conjugated gen.
- the production of pucon polymer and rubber-like polymer is small, the inside of the device is not contaminated, the piping is not clogged, and the thermal efficiency in the condenser and reboiler is not reduced. Since the period during which the process does not need to be performed is prolonged, economical separation and purification of conjugated gens can be achieved by long-term continuous operation.
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Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE69834482T DE69834482T2 (de) | 1997-03-11 | 1998-03-11 | Verfahren zur herstellung konjugierter diene |
EP98907169A EP0969074B1 (en) | 1997-03-11 | 1998-03-11 | Process for preparing purified conjugated diene |
US09/380,003 US6395953B1 (en) | 1997-03-11 | 1998-03-11 | Process for preparing purified conjugated diene |
KR1019997008094A KR100542782B1 (ko) | 1997-03-11 | 1998-03-11 | 정제 공액디엔의 제조방법 |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
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JP9/74571 | 1997-03-11 | ||
JP9/74569 | 1997-03-11 | ||
JP7457197A JPH10251661A (ja) | 1997-03-11 | 1997-03-11 | 共役ジエン類の重合防止法 |
JP07456997A JP3941151B2 (ja) | 1997-03-11 | 1997-03-11 | 共役ジエン類の重合防止方法 |
Publications (1)
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WO1998040448A1 true WO1998040448A1 (fr) | 1998-09-17 |
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PCT/JP1998/001011 WO1998040448A1 (fr) | 1997-03-11 | 1998-03-11 | Procede de preparation de diene conjugue purifie |
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US (1) | US6395953B1 (ja) |
EP (1) | EP0969074B1 (ja) |
KR (1) | KR100542782B1 (ja) |
CN (1) | CN1147567C (ja) |
DE (1) | DE69834482T2 (ja) |
ES (1) | ES2262225T3 (ja) |
ID (1) | ID22877A (ja) |
WO (1) | WO1998040448A1 (ja) |
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TWI225492B (en) * | 2000-09-25 | 2004-12-21 | Ciba Sc Holding Ag | Composition and process for enhancing controlled free radical polymerization |
KR100783342B1 (ko) * | 2001-09-28 | 2007-12-07 | 제온 코포레이션 | 공액 디엔의 분리/정제 방법 및 분리/정제 장치 |
EP1443035B1 (en) * | 2001-10-19 | 2012-04-11 | Zeon Corporation | Process and apparatus for separation and purification of conjugated diene |
DE10233621A1 (de) * | 2002-07-24 | 2004-02-19 | Basf Ag | Verfahren zur Aufarbeitung von Roh-1,3-Butadien |
US7348466B2 (en) * | 2005-04-13 | 2008-03-25 | Equistar Chemicals, Lp | Solvent extraction |
US8076526B2 (en) * | 2009-03-30 | 2011-12-13 | Lyondell Chemical Technology | Extractive distillation of conjugated diene |
US8252150B1 (en) * | 2011-04-19 | 2012-08-28 | International Innotech Inc. | Extractive distillation process for recovering butadiene from C4 hydrocarbon mixtures |
RU2608389C2 (ru) | 2012-10-09 | 2017-01-18 | Ламмус Текнолоджи Инк. | Гибкий способ экстракции бутадиена |
MX2015005503A (es) * | 2012-10-30 | 2015-10-22 | Lummus Technology Inc | Proceso de extraccion de butadieno. |
CN105324353B (zh) * | 2013-06-19 | 2017-10-17 | 沙特基础工业公司 | 用于分离和纯化丁二烯和异戊二烯的共提取系统 |
US20150005552A1 (en) * | 2013-06-26 | 2015-01-01 | Uop Llc | Crude Butadiene Pre-Treatment for Removal of High Furan Content |
JP2016533319A (ja) * | 2013-11-22 | 2016-10-27 | エルジー・ケム・リミテッド | 酸化脱水素反応を介したブタジエン製造工程内の吸収溶媒の回収方法 |
FR3053331B1 (fr) * | 2016-06-29 | 2018-08-03 | IFP Energies Nouvelles | Procede de production de butadiene a partir d'ethanol integre avec distillation extractive |
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DE2911395C2 (de) * | 1979-03-23 | 1985-03-14 | Basf Ag, 6700 Ludwigshafen | Verfahren zur Gewinnung eines konjugierten Diolefins aus einem C↓4↓- oder C↓5↓-Kohlenwasserstoffgemisch |
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1998
- 1998-03-11 ES ES98907169T patent/ES2262225T3/es not_active Expired - Lifetime
- 1998-03-11 KR KR1019997008094A patent/KR100542782B1/ko not_active IP Right Cessation
- 1998-03-11 ID IDW991181A patent/ID22877A/id unknown
- 1998-03-11 CN CNB988032201A patent/CN1147567C/zh not_active Expired - Lifetime
- 1998-03-11 WO PCT/JP1998/001011 patent/WO1998040448A1/ja active IP Right Grant
- 1998-03-11 EP EP98907169A patent/EP0969074B1/en not_active Expired - Lifetime
- 1998-03-11 DE DE69834482T patent/DE69834482T2/de not_active Expired - Lifetime
- 1998-03-11 US US09/380,003 patent/US6395953B1/en not_active Expired - Lifetime
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JPS54138508A (en) * | 1978-04-05 | 1979-10-27 | Goodyear Tire & Rubber | Separation of conjugate dioleffin |
JPS5681526A (en) * | 1979-12-06 | 1981-07-03 | Nippon Zeon Co Ltd | Polymerization prevention of conjugated dienes |
JPS5832685A (ja) * | 1981-05-16 | 1983-02-25 | バスフ・アクチエンゲゼルシヤフト | C↓4‐又はc↓5‐酸化水素混合物から共役ジオレフインを収得する方法 |
JPS60166631A (ja) * | 1983-10-21 | 1985-08-29 | バスフ アクチェン ゲゼルシャフト | C↓5−炭化水素混合物からイソプレンを取得する方法 |
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Also Published As
Publication number | Publication date |
---|---|
ES2262225T3 (es) | 2006-11-16 |
US20020052533A1 (en) | 2002-05-02 |
EP0969074B1 (en) | 2006-05-10 |
ID22877A (id) | 1999-12-16 |
DE69834482T2 (de) | 2007-05-03 |
KR20000076008A (ko) | 2000-12-26 |
CN1147567C (zh) | 2004-04-28 |
CN1250466A (zh) | 2000-04-12 |
US6395953B1 (en) | 2002-05-28 |
EP0969074A4 (en) | 2000-05-24 |
EP0969074A1 (en) | 2000-01-05 |
KR100542782B1 (ko) | 2006-01-11 |
DE69834482D1 (de) | 2006-06-14 |
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