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
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/40—Regeneration or reactivation
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
  • C07F15/00—Compounds containing elements of Groups 8, 9, 10 or 18 of the Periodic Table
  • C07F15/0006—Compounds containing elements of Groups 8, 9, 10 or 18 of the Periodic Table compounds of the platinum group
  • C07F15/0073—Rhodium compounds
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
  • C07F15/00—Compounds containing elements of Groups 8, 9, 10 or 18 of the Periodic Table
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
  • C07F15/00—Compounds containing elements of Groups 8, 9, 10 or 18 of the Periodic Table
  • C07F15/0006—Compounds containing elements of Groups 8, 9, 10 or 18 of the Periodic Table compounds of the platinum group
  • C07F15/0073—Rhodium compounds
  • C07F15/008—Rhodium compounds without a metal-carbon linkage
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
  • C07F17/00—Metallocenes
  • C07F17/02—Metallocenes of metals of Groups 8, 9 or 10 of the Periodic System
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
  • C08F4/00—Polymerisation catalysts
  • C08F4/06—Metallic compounds other than hydrides and other than metallo-organic compounds; Boron halide or aluminium halide complexes with organic compounds containing oxygen
  • C08F4/26—Metallic compounds other than hydrides and other than metallo-organic compounds; Boron halide or aluminium halide complexes with organic compounds containing oxygen of manganese, iron group metals or platinum group metals

Definitions

• the present invention relates to a process for separating a mixture comprising
• a monoolefinically unsaturated compound which can be obtained by adding two terminal olefins which carry the functional groups required for the preparation of the monoolefinically unsaturated compound containing at least two functional groups, or a saturated compound obtained by hydrogenating such a compound,
• a compound containing a transition metal which is homogeneous with respect to the mixture and is suitable as a catalyst for the preparation of a monoolefinically unsaturated compound by addition of two terminal olefins which carry the functional groups required for the preparation of the monoolefinically unsaturated compound containing at least two functional groups
• adipic acid or its derivatives are important starting compounds for the production of technically important polymers such as polyamide 6 or polyamide 66.
• Such compounds can be obtained, for example, by adding two terminal olefins which carry the functional groups required for the preparation of the monoolefinically unsaturated compound containing at least two functional groups.
• hexadioic diester can be prepared by adding acrylic acid ester in the presence of appropriate catalyst systems, in particular homogeneous catalyst systems containing rhodium, as described, for example, in J. Organomet. Chem. 1987, 320, C56, US 4,451, 665, FR 2,524,341, US 4,889,949, Organometallics, 1986, 5, 1752, J. Mol. Catal. 1993, 85, 149, US 4,594,447, Angew. Chem. Int. Ed. Engl., 1988, 27. 185, US 3,013,066, US, 4,638,084, EP-A-475 386, JACS 1991, 113, 2777-2779, JACS 1994, 116, 8038-8060.
• monoolefinically unsaturated compounds which have at least two functional groups independently selected from the group consisting of nitrile group, carboxylic acid revous, carboxylic acid ester group, carboxamide group.
• the corresponding saturated compounds can be obtained from such monoolefinically unsaturated compounds by hydrogenation.
• the catalyst For a technically feasible and economical process, it is desirable to be able to recover the catalyst from the product stream, preferably in a manner that enables recycling into the addition reaction. From the recovered catalyst, the noble metal can optionally also be recovered, for example in the case of the preferred noble metal-containing catalysts.
• the object of the present invention was to provide a process which enables the separation of a compound which can be obtained by adding more than two two terminal olefins which carry the functional groups required for the preparation of the monoolefinically unsaturated compound containing at least two functional groups, and at the same time a slight depletion of a compound containing a transition metal which is suitable as a catalyst for the production of a monoolefinically unsaturated compound by addition of two terminal olefins which carry the functional groups necessary for the production of the monoolefinically unsaturated compound containing at least two functional groups, from im Has product stream of such an addition reaction.
• This separation task should be solved in a technically simple and economical manner. Accordingly, the process defined at the outset was found.
• catalysts in the context of the present invention relate to the compounds which are used as catalysts; the structures of the species which are catalytically active under the respective reaction conditions can differ from this, but are also included in the term “catalyst” mentioned.
• the product stream supplied to the semipermeable membrane for separation contains
• a compound a) is understood to mean a single compound or a mixture of such compounds.
• a compound b) is understood to mean a single such compound or a mixture of such compounds.
• a compound c) is understood to mean a single such compound or a mixture of such compounds.
• esters of aliphatic, aromatic or heteroaromatic alcohols in particular aliphatic alcohol len into consideration.
• aliphatic alcohols can preferably be -C 10 alkanols, especially dC alkanols, such as methanol, ethanol, i-propanol, n-propanol, n-butanol, i-butanol, s-butanol, t-butanol, particularly preferably methanol become.
• the carboxamide groups can be N- or N, N-substituted, where the N, N substitution can be the same or different, preferably the same.
• Suitable substituents are preferably aliphatic, aromatic or heteroaromatic substituents, in particular aliphatic substituents, particularly preferably CC 4 alkyl radicals, such as methyl, ethyl, i-propyl, n-propyl, n-butyl, i-butyl, s-butyl , t-Butyl, particularly preferably methyl.
• acrylic acid or its ester can be used as the terminal olefin with a functional group.
• the production of acrylic acid for example by gas phase oxidation of propene or propane in the presence of heterogeneous catalysts, and the production of acrylic acid esters, for example by esterification of acrylic acid with the corresponding alcohols in the presence of homogeneous catalysts, such as p-toluenesulfonic acid, are known per se.
• Acrylic acid is usually added during storage or processing, one or more stabilizers which, for example, prevent or reduce the polymerization or decomposition of acrylic acid, such as p-methoxyphenol or 4-hydroxy-2,2,4,4-tetramethylpiperidine -N-oxide ("4-hydroxy-TEMPO").
• stabilizers such as p-methoxyphenol or 4-hydroxy-2,2,4,4-tetramethylpiperidine -N-oxide ("4-hydroxy-TEMPO"
• Such stabilizers can be partially or completely removed in the addition step before the use of acrylic acid or its esters.
• the stabilizer can be removed by methods known per se, such as distillation, extraction or crystallization.
• Such stabilizers can remain in the amount used previously in acrylic acid or its esters.
• Such stabilizers can be added to the acrylic acid or its ester before the addition reaction.
• the monoolefinically unsaturated compound which carries at least two functional groups, independently of one another selected from the group consisting of nitrile group, carboxylic acid group, carboxylic acid ester group, carboxamide group, is hexadedioate diester, in particular dimethylhexadateate, with particular preference being given to adipate diester Dimethyl adipate, by hydrogenation.
• Adipic acid can be obtained from cleavage of the ester group from diester of adipic acid, in particular dimethyl adipate.
• known processes for the cleavage of esters come into consideration.
• the monoolefinically unsaturated compound which carries at least two functional groups, independently of one another selected from the group consisting of nitrile group, carboxylic acid group, carboxylic acid ester group, carboxamide group, butenonitrile to give adiponitrile by hydrogenation.
• 5-cyanopentenoate in particular methyl 5-cyanopentate
• 5-cyanopentenoate is suitable as a monoolefinically unsaturated compound which carries at least two functional groups, independently selected from the group consisting of nitrile group, carboxylic acid group, carboxylic ester group, carboxamide group, to give 5- Cyanovaleric acid esters, especially methyl 5-cyanovaleric acid, by hydrogenation.
• the addition reaction can take place partially or completely. Accordingly, with partial conversion, the reaction mixture may contain unreacted olefin.
• the addition reaction can advantageously be carried out in the presence of hydrogen.
• a hydrogen pressure in the range from 0.1 to 1 MPa has proven to be advantageous.
• the addition can advantageously be carried out in the presence of a compound which is homogeneous with respect to the reaction mixture and contains rhodium, ruthenium, palladium or nickel, preferably rhodium, as the catalyst.
• the mixture obtained in this addition reaction can be hydrogenated to give a saturated compound.
• the hydrogenation can advantageously be carried out in the presence of a substance which is heterogeneous with respect to the reaction mixture as a catalyst.
• Suitable heterogeneous catalysts are preferably those which contain a noble metal from Group 8 of the Periodic Table of the Elements, such as palladium, ruthenium, rhodium, iridium, platinum, nickel, cobalt, copper, preferably palladium, as the catalytically active component.
• a noble metal from Group 8 of the Periodic Table of the Elements, such as palladium, ruthenium, rhodium, iridium, platinum, nickel, cobalt, copper, preferably palladium, as the catalytically active component.
• metals can be used in unsupported form, for example as suspension catalysts, preferably in the case of nickel or cobalt.
• metals can be used in supported form, for example on activated carbon, metal oxides, transition metal oxides, in particular aluminum oxide, silicon dioxide, preferably as fixed bed catalysts.
• the hydrogenation can advantageously be carried out in the presence of a compound which is homogeneous with respect to the reaction mixture and contains rhodium, ruthenium, palladium or nickel, preferably rhodium, as a catalyst.
• the addition can be carried out in the presence of the same, as the catalyst, homogeneous rhodium-containing compound with respect to the reaction mixture as the hydrogenation mentioned.
• this hydrogenation can be carried out without separation or depletion of the homogeneous rhodium-containing compound used in the addition.
• the mixture obtained in the addition can be converted into this hydrogenation without a work-up step.
• This can be done, for example, by transferring the mixture obtained in the addition from the reaction apparatus into a further apparatus intended for the hydrogenation, that is to say by spatially separating the affection and hydrogenation.
• the addition can be carried out in a reactor, such as a stirred tank, a stirred tank cascade, or a flow tube or in a combination of one of these types of reactor with another reactor suitable for the hydrogenation.
• the addition or hydrogenation or both can preferably be carried out in the presence of a rhodium-containing compound of the formula [L 1 RhL 2 L 3 R] + X " as a catalyst which is homogeneous with respect to the reaction mixture, in which
• L 2 represents a neutral 2-electron donor
• L 3 represents a neutral 2-electron donor
• R is selected from the group consisting of H, CrC 10 alkyl, C 6 -C 10 aryl and C 7 -C 10 aralkyl ligands X " for a non-coordinating anion preferably stands for one from the
• R F is the same or different partially fluorinated or perfluorinated aliphatic or aromatic Radicals, in particular for perfluoroisopropyl or perfluoro-tert-butyl, is;
• L 2 and L 3 can be connected to one another.
• L 2 and L 3 together can represent, in particular, acrylonitrile or 5-cyanopentenoate.
• L 2 and R can be connected to one another. In this case, L 2 and R together can represent in particular -CH 2 -CH 2 C0 2 Me.
• L 2 , L 3 and R can be connected to one another.
• L 2 , L 3 and R together can in particular represent Me0 2 C (CH 2 ) 2 - (CH) - (CH 2 ) C0 2 Me.
• the addition or the hydrogenation or both can be carried out in the presence of a rhodium-containing compound which is homogeneous with respect to the reaction mixture as a catalyst selected from the group consisting of
• R F stands for the same or different partially fluorinated or perfluorinated aliphatic or aromatic radicals, in particular for perfluoro-iso-propyl or perfluoro-tert-butyl.
• Such catalysts and their preparation can be carried out by processes known per se, as described, for example, in EP-A-475 386, JACS 1991, 113, 2777-2779, JACS 1994, 116, 8038-8060.
• the hydrogenation can be carried out in such a way that the monoolefinically unsaturated compound, which has at least two functional groups, is independent of one another. selected from the group consisting of nitrile group, carboxylic acid group, carboxylic acid ester group, carboxamide group, is converted to a saturated compound to obtain the functional groups mentioned.
• This hydrogenation can advantageously be carried out at a hydrogen partial pressure in the range from 0.01 to 20 MPa.
• an average mean residence time of the monoolefinically unsaturated compound which bears at least two functional groups, independently selected from the group consisting of nitrile group, carboxylic acid group, carboxylic acid ester group, carboxamide group has proven to be advantageous in the range from 0.1 to 100 hours . Furthermore, a temperature in the range from 30 ° C. to 160 ° C. is preferably suitable for the hydrogenation.
• the hydrogenation can be carried out in such a way that the monoolefinically unsaturated compound which carries at least two functional groups, independently of one another selected from the group consisting of nitrile group, carboxylic acid group, carboxylic acid ester group, carboxamide group, leads to a saturated compound with hydrogenation of at least one, preferably all the functional groups mentioned, particularly preferably one or more groups selected from carboxylic acid groups and carboxylic acid ester groups, in particular carboxylic acid ester groups, is reacted, in particular by converting said group or groups into one or more groups of the structure —CH 2 OH.
• This hydrogenation can advantageously be carried out at a hydrogen partial pressure in the range from 10 to 30 MPa.
• an average mean residence time of the monoolefinically unsaturated compound which has at least two functional groups, independently of one another selected from the group consisting of nitrile group, carboxylic acid group, carboxylic acid ester group, carboxamide group, is in the range from 0.1 to 100 hours proven advantageous. Furthermore, a temperature in the range from 200 ° C. to 350 ° C. is preferably suitable for the hydrogenation.
• the advantages of the hydrogenation are particularly evident if at least 0.5%, preferably at least 1%, in particular at least 5%, of the monoolefinically unsaturated compound used, the at least two functional groups, selected independently of one another from the group consisting of nitrile group, carboxylic acid group, Carboxylic acid ester group, carboxamide group, hydrogenated to a saturated compound which carries the same at least two functional groups.
• component a) can be depleted from the mixture obtained in the addition or in the hydrogenation. This can be done by methods known per se, such as distillation, extraction or membrane processes, preferably by distillation.
• the distillation can advantageously be carried out at a bottom temperature in the range from 50 to 200 ° C., preferably 60 to 160 ° C., in particular 70 to 150 ° C.
• Pressures measured in the bottom of the distillation device, in the range from 0.05 kPa to 50 kPa, preferably 0.1 to 10 kPa, in particular 0.2 to 6 kPa, are suitable here.
• the distillation can be carried out in several, such as 2 or 3, advantageously one apparatus.
• the component obtained as the top product in such a distillation can be worked up or processed further by methods known per se.
• an unsaturated compound was obtained as the top product, this can be hydrogenated to a saturated compound by methods known per se.
• an unsaturated dicarboxylic acid or its ester such as diester, for example butenedicarboxylic acid or its mono- or diester
• diester for example butenedicarboxylic acid or its mono- or diester
• the corresponding saturated dicarboxylic acid or its ester such as diester, for example adipic acid or its mono- or diester
• the corresponding, in particular saturated alcohol for example hexane-1,6-diol.
• a diester such as adipic acid diester or butenedicarboxylic acid diester
• this can advantageously be reacted, for example, with a terminally unsaturated carboxylic acid, such as acrylic acid, to give a dicarboxylic acid, such as butenedicarboxylic acid or adipic acid, and the corresponding esters of the terminally unsaturated carboxylic acid.
• a terminally unsaturated carboxylic acid such as acrylic acid
• a mixture comprising components a), b) and c) is separated by means of a semipermeable membrane to give a permeate and a retentate, such that the weight ratio of component b) to component c) in that semipermeable membrane fed mixture is smaller than in the retentate.
• Suitable semipermeable membranes are preferably those which have a higher permeability for component c) than for component b).
• semipermeable membranes are preferably those which have a higher permeability for component a) than for component b).
• a separating layer of the semipermeable membranes can contain one or more materials selected from the group consisting of organic polymer, ceramic materials, metals and carbon or their combinations. They should be stable at the filtration temperature in the feed medium.
• Alpha-aluminum oxide, zirconium oxide, titanium dioxide, silicon carbide or mixed ceramic materials are preferably considered as ceramics.
• Polypropylene, polytetrafluoroethylene, polyvinylidene difluoride, polysulfone, polyether sulfone, polyether ketone, polyamide, polyimide, polyacrylonitrile, regenerated cellulose or silicone can advantageously be used as the organic polymer.
• the separating layers are generally applied to a single-layer or multilayer porous substructure made of the same or a different material as the separating layer.
• the lower layer is generally coarser than the separating layer. Examples of advantageous material combinations are listed in the following table:
• the average average pore size of the membrane should advantageously be in the range from 0.9 to 50 nm, in particular 3 to 20 nm in the case of inorganic membranes.
• the separation limits should preferably be in the range from 500 to 100,000 daltons, in particular in the range from 2,000 to 40,000 daltons in the case of organic membranes.
• the membranes can be used in various geometries, such as flat, tube, multichannel element, capillary or winding geometry, for which the corresponding pressure housing, which allows a separation between retentate and permeate, is available.
• the optimal transmembrane pressures are essentially dependent on the diameter of the membrane pores, the hydrodynamic conditions that influence the structure of the cover layer, and the mechanical stability of the membrane at the filtration temperature.
• the transmembrane pressure can be in the range from 0.02 to 10 MPa, in particular 0.1 to 6 MPa.
• the ratio of the pressure on the retentate side to the pressure on the permeate side of the membrane can preferably be in the range from 2 to 100.
• a pressure in the range from 0.1 to 10 MPa can advantageously be used on the retentate side.
• a pressure in the range from 1 to 1000 kPa can advantageously be used on the permeate side.
• the membrane separation can in particular be carried out at a temperature in the range from 0 to 150 ° C.
• the permeate flows should advantageously be in the range from 1 to 50 kg / m 2 / h.
• the membrane separation can take place continuously, for example by a single pass through one or more successive membrane separation stages.
• the membrane separation can be carried out discontinuously, for example by repeated passage through the membrane modules.
• component a such as was previously separated from the product stream, has preferably proven to be advantageous, in particular to the extent that component a) is taken off as permeate.
• Component a) can then be separated from the retentate by methods known per se, for example by distillation, extraction, membrane separation, preferably by distillation.
• the permeate obtained in the process according to the invention can be partially or completely returned to the addition or hydrogenation mentioned, preferably the addition, as a compound which is homogeneous with respect to the reaction mixture and is suitable as a catalyst.
• TMP ((module input + module output) '2) - permeate
• a stirred glass autoclave with an internal volume of 750 mL and a stirred glass autoclave with an internal volume of 400 mL are reactors R1 and R2 in Series switched.
• the first autoclave MA is fed as a starting material. It is fed into the liquid chamber of the R1 via an immersion tube. Hydrogen is also introduced in gaseous form via this line via a mass flow controller F1.
• the level of the R1 is set via a second dip tube, which serves as an overflow to R2. Gaseous hydrogen is also metered into the overflow line to the R2 via a mass flow controller F2.
• the inflow to R2 is likewise entered into R2 via an immersion tube and the discharge from R2 via an additional immersion tube via a pressure regulating valve from Reco into a thin-film evaporator with an evaporator area of 0.046 m 2 .
• the evaporator is set to a predetermined pressure via a vacuum station.
• the evaporator is heated with an oil bath W1.
• the level in the drain vessel of the thin-film evaporator is regulated via the temperature in W1.
• a pump P2 conveys a circuit stream via the evaporator and another pump P3 from this circuit a recycle stream into the reactor R1, which is also introduced via the immersion tube, via which the MA feed is also metered.
• the pumps P1 and P3 each deliver the same volumes per time.
• the vapor stream of the evaporator is passed through an intensive cooler and condensed there.
• the condensate is then collected (discharge).
• the constituents not condensed under these conditions are subjected to
• the reactors are filled with a solution which contains Cp * Rh (C 2 H 4 ) 2 and a stoichiometric amount of HBAr F 4 and 250 ppm of PTZ in HDME.
• the reaction mixture is first circulated at room temperature for about 20 hours.
• the thin film evaporator is then preheated to a start temperature of 100 ° C.
• the hydrogen stream and the MA feed 120 ml / h, contains 100 ppm by weight of PTZ
• the reactors are heated to 70 ° C. and the evaporator is operated in vacuo.
• composition of this solution is characterized as follows:
• Rh 16 ppm high boiler: 65 g / kg (residue determination: evaporation in vac. At 250 ° C)
• the solution is subjected to continuous membrane filtration, which is described in more detail in Example 4.
• Example 4 containing MA and rhodium catalyst could be used directly as a feed in the continuous dimerization plant and thus a return of the catalyst with simultaneous removal of the polymer could be achieved.
• Example 1 A laboratory apparatus as described in Example 1 is used. The feed is only not dosed in R1, but in R2.
• the reactors are filled with a solution which contains Cp * Rh (C 2 H 4 ) 2 and a stoichiometric amount of HBAr F 4 and 250 ppm of PTZ in HDME.
• the reaction mixture is first circulated at room temperature for about 20 hours.
• the thin film evaporator is then preheated to a start temperature of 100 ° C.
• the hydrogen flow and the MA feed 120 ml / h, contains 100 ppm by weight PTZ
• the reactors are heated to 70 ° C. and the evaporator is operated in vacuo.
• the hydrogen in this example contains 50 ppm 0 2 .
• Rh Conc. R1 175 ppm
• Rh Conc. R2 110 ppm
• thermostattable circuit apparatus with a minimum hold up of 3 l was used for the tests.
• a reservoir, a pump for generating pressure and overflow of the membrane, a heat exchanger for maintaining the temperature, a membrane module with a built-in ceramic tube membrane and a pressure control valve were integrated in the circuit.
• the permeate outlet was depressurized.
• the hold-up of the system could be kept constant by maintaining a stand (diafiltration mode).
• All templates of the apparatus were made inert with nitrogen.
• the ceramic tube membrane used (manufacturer: Inocermic GmbH) had an outer diameter of 10 mm, an inner diameter of 7 mm and a length of 1000 mm.
• the support body consisted of Al 2 0 3 and the inner separating layer contained 5 nm pores of Ti0 2 . The membrane was flown from the inside and the permeate was removed on the outside.
• Example 4 describes the membrane filtration of a partial stream from Example 1. Table 1

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