WO2022124863A1 - 선택적 균일계 수소화 촉매의 회수 방법 및 재사용 방법 - Google Patents
선택적 균일계 수소화 촉매의 회수 방법 및 재사용 방법 Download PDFInfo
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- WO2022124863A1 WO2022124863A1 PCT/KR2021/018789 KR2021018789W WO2022124863A1 WO 2022124863 A1 WO2022124863 A1 WO 2022124863A1 KR 2021018789 W KR2021018789 W KR 2021018789W WO 2022124863 A1 WO2022124863 A1 WO 2022124863A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- selective
- hydrogenation catalyst
- homogeneous hydrogenation
- recovering
- cyclododecene
- Prior art date
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- 239000003054 catalyst Substances 0.000 title claims abstract description 127
- 238000009905 homogeneous catalytic hydrogenation reaction Methods 0.000 title claims abstract description 78
- 238000000034 method Methods 0.000 title claims abstract description 72
- SXVPOSFURRDKBO-UHFFFAOYSA-N Cyclododecanone Chemical compound O=C1CCCCCCCCCCC1 SXVPOSFURRDKBO-UHFFFAOYSA-N 0.000 claims abstract description 76
- 238000006243 chemical reaction Methods 0.000 claims abstract description 75
- RIOQSEWOXXDEQQ-UHFFFAOYSA-N triphenylphosphine Chemical compound C1=CC=CC=C1P(C=1C=CC=CC=1)C1=CC=CC=C1 RIOQSEWOXXDEQQ-UHFFFAOYSA-N 0.000 claims abstract description 66
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 claims abstract description 64
- HYPABJGVBDSCIT-UPHRSURJSA-N cyclododecene Chemical compound C1CCCCC\C=C/CCCC1 HYPABJGVBDSCIT-UPHRSURJSA-N 0.000 claims abstract description 60
- ZOLLIQAKMYWTBR-RYMQXAEESA-N cyclododecatriene Chemical compound C/1C\C=C\CC\C=C/CC\C=C\1 ZOLLIQAKMYWTBR-RYMQXAEESA-N 0.000 claims abstract description 56
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 43
- 239000002904 solvent Substances 0.000 claims abstract description 33
- 238000004821 distillation Methods 0.000 claims abstract description 31
- YBCAZPLXEGKKFM-UHFFFAOYSA-K ruthenium(iii) chloride Chemical compound [Cl-].[Cl-].[Cl-].[Ru+3] YBCAZPLXEGKKFM-UHFFFAOYSA-K 0.000 claims abstract description 24
- 238000000926 separation method Methods 0.000 claims abstract description 21
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 11
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 10
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 15
- 238000011084 recovery Methods 0.000 claims description 15
- 239000007789 gas Substances 0.000 claims description 13
- 230000002194 synthesizing effect Effects 0.000 claims description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 8
- 239000012190 activator Substances 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 3
- 239000000047 product Substances 0.000 description 20
- 230000008569 process Effects 0.000 description 11
- RZUNIXAGSKNOIB-HSFFGMMNSA-N (1z,3e)-cyclododeca-1,3-diene Chemical compound C1CCCC\C=C/C=C/CCC1 RZUNIXAGSKNOIB-HSFFGMMNSA-N 0.000 description 8
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000010970 precious metal Substances 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- JHWNWJKBPDFINM-UHFFFAOYSA-N Laurolactam Chemical compound O=C1CCCCCCCCCCCN1 JHWNWJKBPDFINM-UHFFFAOYSA-N 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 239000013067 intermediate product Substances 0.000 description 3
- 239000003446 ligand Substances 0.000 description 3
- 239000000376 reactant Substances 0.000 description 3
- 230000035484 reaction time Effects 0.000 description 3
- 238000010517 secondary reaction Methods 0.000 description 3
- 230000003213 activating effect Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 229910052736 halogen Inorganic materials 0.000 description 2
- 150000002367 halogens Chemical class 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 230000006698 induction Effects 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000012299 nitrogen atmosphere Substances 0.000 description 2
- 238000005191 phase separation Methods 0.000 description 2
- 230000009257 reactivity Effects 0.000 description 2
- -1 that is Chemical compound 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- TXZNVWGSLKSTDH-XCADPSHZSA-N (1Z,3Z,5Z)-cyclodeca-1,3,5-triene Chemical compound C1CC\C=C/C=C\C=C/C1 TXZNVWGSLKSTDH-XCADPSHZSA-N 0.000 description 1
- CRSBERNSMYQZNG-UHFFFAOYSA-N 1 -dodecene Natural products CCCCCCCCCCC=C CRSBERNSMYQZNG-UHFFFAOYSA-N 0.000 description 1
- SNRUBQQJIBEYMU-UHFFFAOYSA-N Dodecane Natural products CCCCCCCCCCCC SNRUBQQJIBEYMU-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- UMYVESYOFCWRIW-UHFFFAOYSA-N cobalt;methanone Chemical compound O=C=[Co] UMYVESYOFCWRIW-UHFFFAOYSA-N 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- UCIYGNATMHQYCT-OWOJBTEDSA-N cyclodecene Chemical compound C1CCCC\C=C\CCC1 UCIYGNATMHQYCT-OWOJBTEDSA-N 0.000 description 1
- DDTBPAQBQHZRDW-UHFFFAOYSA-N cyclododecane Chemical compound C1CCCCCCCCCCC1 DDTBPAQBQHZRDW-UHFFFAOYSA-N 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 229940069096 dodecene Drugs 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- QBERHIJABFXGRZ-UHFFFAOYSA-M rhodium;triphenylphosphane;chloride Chemical compound [Cl-].[Rh].C1=CC=CC=C1P(C=1C=CC=CC=1)C1=CC=CC=C1.C1=CC=CC=C1P(C=1C=CC=CC=1)C1=CC=CC=C1.C1=CC=CC=C1P(C=1C=CC=CC=1)C1=CC=CC=C1 QBERHIJABFXGRZ-UHFFFAOYSA-M 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- CMTKJYPJPSONIT-UHFFFAOYSA-K trichlororuthenium;triphenylphosphane Chemical compound Cl[Ru](Cl)Cl.C1=CC=CC=C1P(C=1C=CC=CC=1)C1=CC=CC=C1 CMTKJYPJPSONIT-UHFFFAOYSA-K 0.000 description 1
- 239000011995 wilkinson's catalyst Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J38/00—Regeneration or reactivation of catalysts, in general
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/03—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
- C07C5/05—Partial hydrogenation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- B01J31/40—Regeneration or reactivation
-
- 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
- C07C13/02—Monocyclic hydrocarbons or acyclic hydrocarbon derivatives thereof
- C07C13/273—Monocyclic hydrocarbons or acyclic hydrocarbon derivatives thereof with a twelve-membered ring
- C07C13/275—Monocyclic hydrocarbons or acyclic hydrocarbon derivatives thereof with a twelve-membered ring the twelve-membered ring being unsaturated
-
- 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
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/10—Purification; Separation; Use of additives by extraction, i.e. purification or separation of liquid hydrocarbons with the aid of liquids
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/20—Use of additives, e.g. for stabilisation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2531/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- C07C2531/16—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes
- C07C2531/24—Phosphines
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2601/00—Systems containing only non-condensed rings
- C07C2601/18—Systems containing only non-condensed rings with a ring being at least seven-membered
- C07C2601/20—Systems containing only non-condensed rings with a ring being at least seven-membered the ring being twelve-membered
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Definitions
- the present invention relates to a method for recovering and reusing a selective homogeneous hydrogenation catalyst.
- CDEN cyclododecene
- CDT cyclododecatriene
- a metal ligand catalyst known as a Wilkinson catalyst that is, triphenylphosphine, TPP
- TPP triphenylphosphine
- Catalysts are essential substances in the chemical industry as a substance that activates the entire reaction to occur quickly without reacting itself in a certain reaction system in general. Catalysts are usually present in a small amount in the reaction system to perform their role, but as the chemical industry develops, the amount used increases, and the amount of waste catalyst waste is also rapidly increasing. In Korea, which has no natural resources and is dependent on imports of precious metal-related industrial raw materials, it is urgent to recover precious metals from spent catalysts and reuse them as industrial raw materials.
- a method of recovering the catalyst after the selective hydrogenation reaction is known depending on the state and conditions of the catalyst.
- the interaction process takes a lot of time and requires cooling to near 0°C.
- the present inventors have intensified the study of efficient methods for the recovery method and reuse method of the selective hydrogenation catalyst.
- the selective hydrogenation catalyst can be separated and recovered through a simple method, the design and operation of the distillation separation device is easy to maintain, and the conversion rate of cyclododecatriene and cyclododecene even when solvent is added.
- the present invention was completed by confirming that it was possible to maintain all of the selectivity at a high level.
- the present invention can separate and recover a selective homogeneous hydrogenation catalyst through a relatively simple method within a short process time, while designing and operating a distillation separation device is easy, and cyclododecatriene is
- An object of the present invention is to provide a method for recovering and reusing a selective homogeneous hydrogenation catalyst capable of maintaining both a conversion rate and a selectivity of cyclododecene at a high level.
- cyclododecene is synthesized by selectively hydrogenating the first reaction solution containing cyclododecatriene, triphenylphosphine, formaldehyde and ruthenium chloride, and then, the cyclo
- the selective homogeneous hydrogenation from the triphenylphosphine, formaldehyde and ruthenium chloride during the selective hydrogenation of the first reaction solution preparing a catalyst and synthesizing cyclododecene; mixing a solvent containing cyclododecanone with the first reaction solution; and recovering the selective homogeneous hydrogenation catalyst by distilling the second reaction solution in which the synthesis of cyclododecene is completed.
- the solvent may be cyclododecanone dissolved in cyclododecatriene.
- the distillation separation is performed through a distillation column, wherein the distillation column includes an upper column from which a product containing cyclododecene is discharged, and the selective uniformity It is provided as a lower column in which the hydrogenation catalyst and the solvent are separated, and during the distillation separation, the pressure of the upper column is 0.1 bar or less and the temperature is 100° C. to 200° C., and the pressure of the lower column is 0.1 bar or less and the temperature is It may be 150 °C to 250 °C.
- the molar ratio of ruthenium chloride: triphenylphosphine: formaldehyde may be 1: 100 to 300: 150 to 500.
- the selective hydrogenation reaction may be performed in a stirred tank reactor equipped with a gas-induced hollow stirrer.
- hydrogen gas present in the gas phase at the top of the stirred tank reactor may be supplied to the reaction solution through the hollow of the gas-induced hollow stirrer.
- the first reaction solution may further include a catalyst activator including acetic acid.
- the catalyst activator may be added in an amount of 0.01 to 2 parts by weight based on 100 parts by weight of cyclododecatriene.
- the selective hydrogenation reaction may be performed at a temperature of 100 to 200° C. and a pressure of 10 to 80 bar.
- the selective homogeneous hydrogenation catalyst recovered by the above-described method is re-injected into the third reaction solution containing cyclododecatriene and subjected to a secondary selective hydrogenation reaction to cyclodode synthesizing Sen.
- the method for recovering and reusing the selective homogeneous hydrogenation catalyst according to the present invention is only a method of adding a solvent containing cyclododecanone (CDON) to a reactant and then separating the unreacted cyclododecatriene and cyclodo Decadiene and product cyclododecene, selective homogeneous hydrogenation catalyst, and excess triphenylphosphine can be separated, and the selective homogeneous hydrogenation catalyst and excess triphenylphosphine that are separated and recovered without separate post-treatment are subjected to the following selective hydrogenation reaction can be used as is.
- CDON cyclododecanone
- both the conversion rate of cyclododecatriene and the selectivity of cyclododecene can be maintained at high levels.
- the unit of % used without special mention means % by weight unless otherwise specified.
- the present inventors can easily separate and recover the selective homogeneous hydrogenation catalyst by additionally using an appropriate solvent for the catalyst, while designing and maintaining the distillation separation device is easy.
- the recovered selective homogeneous hydrogenation catalyst is reused, it is intended to provide a recovery method and a reuse method of a selective homogeneous hydrogenation catalyst capable of maintaining both the conversion rate of cyclododecatriene and the selectivity of cyclododecene at high levels.
- the method for recovering the selective homogeneous hydrogenation catalyst according to the present invention is a first reaction comprising cyclododecatriene (CDT), triphenylphosphine (TPP), formaldehyde and ruthenium chloride (RhCl3)
- CDT cyclododecatriene
- TPP triphenylphosphine
- RhCl3 ruthenium chloride
- the selective reaction of the first reaction solution During the hydrogenation reaction, a selective homogeneous hydrogenation catalyst is prepared from triphenylphosphine, formaldehyde and ruthenium chloride to synthesize cyclododecene, and a solvent containing cyclododecanone (CDON) is mixed with the first reaction solution. and recovering the selective homogeneous hydrogenation catalyst by separating the second reaction solution from which the synthesis of cyclododecene
- CDON solvent containing cyclododecanone
- a selective homogeneous hydrogenation catalyst and excess triphenylphosphine can be separated only by the evaporation separation method, and without a separate post-treatment The separated and recovered selective homogeneous hydrogenation catalyst and excess triphenylphosphine can be used as it is in the next selective hydrogenation reaction.
- the catalyst uses a solvent containing cyclododecanone (CDON), which is an intermediate product of the laurolactam manufacturing process, even if cyclododecanone is included in the product, the quality of the product is not affected. There is no need to perform an elaborate and complicated process to completely separate the cyclododecanone, and since the catalyst containing the solvent cyclododecanone can be directly introduced into the process, the catalyst can be efficiently recovered and reused.
- CDON solvent containing cyclododecanone
- both the conversion rate of cyclododecatriene and the selectivity of cyclododecene can be maintained at a high level.
- hydrogen gas (H 2 ) is added through a conventional method for the selective hydrogenation reaction.
- This step is a step for synthesizing cyclododecene, and cyclododecene may be synthesized through a method described below or a known method.
- the selective hydrogenation reaction may be performed in a stirred tank reactor equipped with a gas-induced hollow stirrer.
- a gas-induced hollow stirrer As such, when the reaction is carried out by adopting a means using a gas-induced hollow stirrer, reactivity can be secured without an organic solvent usually used to increase reactivity, and at the same time, the reaction time can be significantly reduced.
- a gas-induced hollow stirrer is rotated and stirred to perform a reaction, and hydrogen gas present in the gas phase at the top of the stirred tank reactor through the hollow of the gas-induced hollow stirrer can be supplied to the reaction solution to supply hydrogen to cyclododecariene.
- the gas-induced hollow stirrer has a hollow passage formed therein, and hydrogen gas is introduced through the hollow passage and comes into contact with cyclododecatriene so that a selective hydrogenation reaction can proceed.
- cyclododecene may be synthesized by a known method.
- a selective homogeneous hydrogenation catalyst is prepared from triphenylphosphine, formaldehyde and ruthenium chloride to synthesize cyclododecene, and the homogeneous complex catalyst, which is the selective homogeneous hydrogenation catalyst, is RuH ( PPh 3 ) 3 (CO)Cl or Ru(PPh 3 ) 2 (CO) 2 Cl 2 , or both.
- triphenylphosphine and formaldehyde form a complex with the ruthenium chloride and serve as a catalyst for the selective hydrogenation reaction.
- the molar ratio of ruthenium chloride: triphenylphosphine: formaldehyde may be 1: 100 to 300: 150 to 500, and more preferably, the molar ratio of ruthenium chloride: triphenylphosphine: formaldehyde is 1 : 130 to 250: may be 200 to 400, and more preferably, the molar ratio of ruthenium chloride: triphenylphosphine: formaldehyde may be 1: 170 to 230: 250 to 350.
- the conversion rate and selectivity can be significantly improved. However, this is only a preferred example, and of course, the present invention is not limited thereto.
- the first reaction solution may further include a catalyst activator including acetic acid.
- acetic acid When acetic acid is added, the conversion rate and selectivity can be further improved by activating the reaction of the ruthenium chloride-triphenylphosphine complex catalyst.
- acetic acid may be added in an amount of 0.01 to 2 parts by weight based on 100 parts by weight of cyclododecatriene, more preferably 0.05 to 1.5 parts by weight based on 100 parts by weight of cyclododecatriene, and even more preferably cyclododecatriene. It may be added in an amount of 0.1 to 1 part by weight based on 100 parts by weight.
- this is only a preferred example, and of course, the present invention is not limited thereto.
- the amount of the catalyst containing triphenylphosphine, formaldehyde and ruthenium chloride is sufficient as long as the reaction of the reactants can proceed sufficiently, preferably in 100 parts by weight of cyclododecatriene.
- a catalyst containing triphenylphosphine, formaldehyde, and ruthenium chloride may be added to 1 to 20 parts by weight, preferably 1 to 10, more preferably 1 to 7 parts by weight of triphenylphosphine, formaldehyde And a catalyst containing ruthenium chloride may be added.
- this is only a preferred example for improving the conversion rate and selectivity, and the present invention is not limited thereto.
- the selective hydrogenation reaction may be performed under a temperature of 100 to 200 °C and a pressure of 10 to 80 bar, and more preferably, a temperature of 140 to 180 °C and 20 to 60 bar. Under pressure conditions, more preferably, it may be carried out at a temperature of 150 to 175° C. and a pressure condition of 20 to 40 bar, but this is only a preferred example for improving the conversion rate and selectivity, and the present invention is not limited thereto. Of course.
- a step of mixing a solvent containing cyclododecanone (CDON) with the first reaction solution may be performed.
- the solvent may be added after the selective homogeneous hydrogenation catalyst is formed by the triphenylphosphine, formaldehyde and ruthenium chloride of the first reaction solution, but, in contrast, may be added before the catalyst is formed.
- the solvent may be cyclododecanone itself, or may further contain cyclododecatriene.
- cyclododecanone dissolved in cyclododecatriene may be used.
- the amount of cyclododecanone in the solvent is not limited as long as it can be dissolved in cyclododecatriene.
- a solvent uses a solvent in which cyclododecanone (CDON), an intermediate product of the laurolactam manufacturing process, is dissolved, even if cyclododecanone is included in the product, it does not affect the quality of the product, and the product and the solvent are completely separated
- CDON cyclododecanone
- the catalyst containing the solvent cyclododecanone can be directly introduced into the process, the catalyst can be efficiently recovered and reused.
- cyclododecanone is dissolved
- the recovered cyclodecatriene is a substance that participates in this reaction and does not affect the catalyst activity, so there is no problem in reuse even if it remains in the recovered catalyst.
- the first reaction solution is subjected to a selective hydrogenation reaction, and the second reaction solution in which the synthesis of cyclododecene is completed is distilled and separated, and unreacted cyclododecatriene, cyclododecadiene, and the product cyclododecene are distilled and separated. Recovering the selective homogeneous hydrogenation catalyst and solvent may be performed.
- the solvent containing cyclododecanone of the present invention has good flowability at the melting point of cyclododecanone, which is a relatively low temperature, it is possible to keep the temperature of the process line lower than when distillation separation without adding a solvent is possible Thus, energy can be saved and the catalyst can be recovered more efficiently.
- the distillation separation may be made through a distillation column, in which case the distillation column is an upper column from which a product containing cyclodecene is discharged, and a selective homogeneous hydrogenation catalyst and solvent It can be divided into a separate sub-column.
- the pressure of the upper column may be 0.3 bar or less and the temperature may be carried out under the conditions of 100 to 200°C, and more preferably, it may be performed under the temperature of 130 to 170°C and the pressure of 0.1 bar or less.
- the pressure of the lower column may be 0.3 bar or less and the temperature may be carried out under the conditions of 150 to 250 °C, more preferably, it may be carried out under the pressure of 0.1 bar or less and 180 to 230 °C temperature conditions.
- the reflux ratio in the distillation column may be 0.5 to 5, specifically 1 to 2, and the boiling ratio may be 1 to 8, specifically 4 to 5, but is not limited thereto.
- unreacted cyclododecatriene and cyclododecadiene and product cyclododecene can be effectively separated by distillation within the above range.
- the recovery of the selective homogeneous hydrogenation catalyst may be performed at a temperature of 10 to 30° C., and a pressure of 0.1 bar or less or a nitrogen atmosphere. That is, the selective homogeneous hydrogenation catalyst can be recovered by cooling the temperature raised by the distillation separation process to a room temperature level.
- the present invention re-injects the recovered selective homogeneous hydrogenation catalyst into a third reaction solution containing cyclododecatriene and performs a secondary selective hydrogenation reaction to synthesize cyclododecene; It relates to a method of reusing a selective homogeneous hydrogenation catalyst.
- the recovered selective homogeneous hydrogenation catalyst is re-injected into the third reaction solution containing cyclododecatriene and subjected to a secondary selective hydrogenation reaction to cyclododecene can be synthesized.
- the secondary selective hydrogenation reaction for synthesizing the cyclododecene may be performed through a known method.
- the third reaction solution may further add a solvent including ethanol as well as cyclododecatriene. Since the ethanol has a high dielectric constant, the conversion rate and selectivity may be improved by further activating the reaction of the reactants in the selective hydrogenation reaction.
- the amount of ethanol used may be sufficient as long as it allows selective hydrogenation of hydrogen to cyclododecatriene, preferably 1 to 20 parts by weight, more preferably 2 to 15 parts by weight, based on 100 parts by weight of cyclododecatriene. , more preferably 3 to 10 parts by weight may be added.
- this is only a preferred example, and of course, the present invention is not limited thereto.
- the secondary selective hydrogenation reaction may be carried out at a temperature of 120 to 200 °C and a pressure of 10 to 80 bar, and more preferably at a temperature of 140 to 180 °C and 20 to 60 Under a pressure condition of bar, it may be more preferably carried out under a temperature of 150 to 175 °C and a pressure condition of 20 to 40 bar, but this is only a preferred example for improving the conversion rate and selectivity, and the present invention is not limited thereto. Of course not.
- Cyclododecatriene (CDT): Ruthenium chloride (RuCl 3 ): Triphenylphosphine (TPP): Formaldehyde was added in a molar ratio of 7500:1:110:220, and cyclododecatriene (CDT) 100 parts by weight About 80 parts by weight of cyclododecanone (CDON) was added. At this time, the mixture was heated to 70 °C under nitrogen condition to dissolve cyclododecanone (CDON). Thereafter, the reaction solution was stirred at 1600 rpm under hydrogen 6 bar conditions and heated to 140°C. Then, a selective hydrogenation reaction was performed at a temperature of 180° C. under a condition in which a hydrogen pressure of 20 bar was maintained, and in this case, the reaction was performed in a stirred tank reactor equipped with a gas induction hollow stirrer.
- the second reaction solution was recovered after cooling to 30° C. or less under nitrogen condition.
- the second reaction solution was put into a distillation column and distilled.
- the internal pressure of the upper column was -0.9 bar
- the temperature was 155.9 °C
- the internal pressure of the lower column was -0.85 bar
- the temperature was 203.5 °C.
- the selective homogeneous hydrogenation catalyst was recovered by cooling to 30° C. or less in a nitrogen atmosphere.
- Example 1 In the selective homogeneous hydrogenation catalyst recovery method of Example 1, the selective hydrogenation reaction was performed in the same manner as in Example 1, except that the selective hydrogenation reaction was carried out at a temperature of 170° C. instead of at a temperature of 180° C. The homogeneous hydrogenation catalyst was recovered and reused.
- CDT 0 is the number of moles of cyclododecatriene added
- CDT 1 is the number of moles of cyclododecatriene after the reaction
- CDDN 1 is the number of moles of cyclododecatriene.
- Equation 2 CDEN 1 is the number of moles of the produced cyclododecene, and CDAN 1 is the number of moles of the produced by-product, cyclododecane.
- Example 1 Example 2 comparative example division primary reaction secondary reaction primary reaction secondary reaction primary reaction secondary reaction Reaction time (h) 2.0 1.5 3.0 2.5 2.0 1.5 Conversion rate (%) 98.8 98.3 98.7 98.1 98.1 97.8 Selectivity (%) 97.6 97.4 98.1 98.3 97.6 97.8 transference number(%) 96.4 95.7 96.8 96.4 95.7 95.6
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Abstract
Description
실시예1 | 실시예2 | 비교예 | ||||
구분 | 1차반응 | 2차반응 | 1차반응 | 2차반응 | 1차반응 | 2차반응 |
반응시간(h) | 2.0 | 1.5 | 3.0 | 2.5 | 2.0 | 1.5 |
전환율(%) | 98.8 | 98.3 | 98.7 | 98.1 | 98.1 | 97.8 |
선택도(%) | 97.6 | 97.4 | 98.1 | 98.3 | 97.6 | 97.8 |
수율(%) | 96.4 | 95.7 | 96.8 | 96.4 | 95.7 | 95.6 |
Claims (10)
- 사이클로도데카트리엔, 트리페닐포스핀, 포름알데히드 및 염화루테늄을 포함하는 제1반응용액을 선택적 수소 첨가 반응시켜 사이클로도데센을 합성한 후, 상기 사이클로도데센의 합성이 완료된 제2반응용액으로부터 선택적 균일계 수소화 촉매를 회수하는 방법에 있어서,상기 제1반응용액의 선택적 수소 첨가 반응 중 상기 트리페닐포스핀, 포름알데히드 및 염화루테늄으로부터 선택적 균일계 수소화 촉매가 제조되며 사이클로도데센이 합성되는 단계;상기 제1반응용액에 사이클로도데카논을 함유하는 용매를 혼합하는 단계; 및상기 사이클로도데센의 합성이 완료된 제2반응용액을 증류 분리하여 선택적 균일계 수소화 촉매를 회수하는 단계;를 포함하는, 선택적 균일계 수소화 촉매의 회수 방법.
- 제1항에 있어서,상기 용매는 사이클로도데카트리엔에 용해된 사이클로도데카논인 선택적 균일계 수소화 촉매의 회수 방법.
- 제1항에 있어서,상기 증류 분리는 증류컬럼을 통해 이루어지며,상기 증류컬럼은 사이클로도데센을 포함하는 생성물이 배출되는 상부컬럼과, 상기 선택적 균일계 수소화 촉매 및 용매가 분리되는 하부컬럼으로 구비되고,상기 증류분리 시, 상기 상부컬럼의 압력은 0.1bar 이하 및 온도는 100℃내지 200℃이며, 상기 하부컬럼의 압력은 0.1bar 이하 및 온도는 150℃내지 250℃인 선택적 균일계 수소화 촉매의 회수방법.
- 제1항에 있어서,상기 염화루테늄 : 트리페닐포스핀 : 포름알데히드의 몰비는 1 : 100 내지 300 : 150 내지 500인, 선택적 균일계 수소화 촉매의 회수 방법.
- 제1항에 있어서,상기 선택적 수소 첨가 반응은 가스 유도 중공형 교반기가 구비된 교반탱크반응기에서 수행되는 것인, 선택적 균일계 수소화 촉매의 회수 방법.
- 제5항에 있어서,상기 가스 유도 중공형 교반기의 중공을 통해 교반탱크반응기 상단에 기상으로 존재하는 수소 기체가 반응용액에 공급되는 것인, 선택적 균일계 수소화 촉매의 회수 방법.
- 제1항에 있어서,상기 제1반응용액은 아세트산을 포함하는 촉매 활성제가 더 포함되는 것인, 선택적 균일계 수소화 촉매의 회수 방법.
- 제7항에 있어서,상기 촉매 활성제는 사이클로도데카트리엔 100 중량부에 대하여 0.01 내지 2 중량부로 첨가되는 것인, 선택적 균일계 수소화 촉매의 회수 방법.
- 제1항에 있어서,상기 선택적 수소 첨가 반응은 100 내지 200℃의 온도 및 10 내지 80 bar의 압력 조건 하에서 수행되는 것인, 선택적 균일계 수소화 촉매의 회수 방법.
- 제1항 내지 제9항 중 어느 한 항의 방법으로 회수된 선택적 균일계 수소화 촉매를 사이클로도데카트리엔이 포함된 제3반응용액에 재투입하고 2차 선택적 수소 첨가 반응시켜 사이클로도데센을 합성하는 단계;를 포함하는, 회수된 선택적 균일계 수소화 촉매의 재사용 방법.
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JP2023535503A JP2023553148A (ja) | 2020-12-11 | 2021-12-10 | 選択的均一系水素化触媒の回収方法および再使用方法 |
US18/256,648 US20240033721A1 (en) | 2020-12-11 | 2021-12-10 | Method for recovering and reusing selective homogeneous hydrogenation catalyst |
CN202180083388.4A CN116547257A (zh) | 2020-12-11 | 2021-12-10 | 选择性均相氢化催化剂的回收方法及再使用方法 |
EP21903908.8A EP4265588A1 (en) | 2020-12-11 | 2021-12-10 | Method for recovering and reusing selective homogeneous hydrogenation catalyst |
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Citations (7)
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US3715405A (en) | 1967-11-06 | 1973-02-06 | Nippon Oil Co Ltd | Process for selective hydrogenation of highly unsaturated compounds |
US4413118A (en) | 1981-03-02 | 1983-11-01 | Merck & Co., Inc. | Process for removal of homogeneous catalyst group VIII metals from process streams |
JP2007506695A (ja) * | 2003-09-25 | 2007-03-22 | ビーエーエスエフ アクチェンゲゼルシャフト | ケトンの製造方法 |
JP2007506694A (ja) * | 2003-09-25 | 2007-03-22 | ビーエーエスエフ アクチェンゲゼルシャフト | シクロドデカノンの製造方法 |
KR20190058075A (ko) * | 2017-11-21 | 2019-05-29 | 한화케미칼 주식회사 | 사이클로도데카트라이엔의 선택적 수소화 촉매 및 이의 제조방법 |
JP2019523121A (ja) * | 2016-06-30 | 2019-08-22 | エボニック デグサ ゲーエムベーハーEvonik Degussa GmbH | 均一系酸化触媒を再活性化する方法 |
KR20200076301A (ko) | 2018-12-19 | 2020-06-29 | 한화솔루션 주식회사 | 선택적 균일계 수소화 촉매의 회수 방법 및 재사용 방법 |
-
2020
- 2020-12-11 KR KR1020200173362A patent/KR20220083279A/ko unknown
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2021
- 2021-12-10 EP EP21903908.8A patent/EP4265588A1/en active Pending
- 2021-12-10 CN CN202180083388.4A patent/CN116547257A/zh active Pending
- 2021-12-10 US US18/256,648 patent/US20240033721A1/en active Pending
- 2021-12-10 JP JP2023535503A patent/JP2023553148A/ja active Pending
- 2021-12-10 WO PCT/KR2021/018789 patent/WO2022124863A1/ko active Application Filing
Patent Citations (7)
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US3715405A (en) | 1967-11-06 | 1973-02-06 | Nippon Oil Co Ltd | Process for selective hydrogenation of highly unsaturated compounds |
US4413118A (en) | 1981-03-02 | 1983-11-01 | Merck & Co., Inc. | Process for removal of homogeneous catalyst group VIII metals from process streams |
JP2007506695A (ja) * | 2003-09-25 | 2007-03-22 | ビーエーエスエフ アクチェンゲゼルシャフト | ケトンの製造方法 |
JP2007506694A (ja) * | 2003-09-25 | 2007-03-22 | ビーエーエスエフ アクチェンゲゼルシャフト | シクロドデカノンの製造方法 |
JP2019523121A (ja) * | 2016-06-30 | 2019-08-22 | エボニック デグサ ゲーエムベーハーEvonik Degussa GmbH | 均一系酸化触媒を再活性化する方法 |
KR20190058075A (ko) * | 2017-11-21 | 2019-05-29 | 한화케미칼 주식회사 | 사이클로도데카트라이엔의 선택적 수소화 촉매 및 이의 제조방법 |
KR20200076301A (ko) | 2018-12-19 | 2020-06-29 | 한화솔루션 주식회사 | 선택적 균일계 수소화 촉매의 회수 방법 및 재사용 방법 |
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US20240033721A1 (en) | 2024-02-01 |
CN116547257A (zh) | 2023-08-04 |
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