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
  • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J19/24—Stationary reactors without moving elements inside
  • B01J19/2455—Stationary reactors without moving elements inside provoking a loop type movement of the reactants
  • B01J19/2465—Stationary reactors without moving elements inside provoking a loop type movement of the reactants externally, i.e. the mixture leaving the vessel and subsequently re-entering it
• • 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
  • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J19/24—Stationary reactors without moving elements inside
  • B01J19/2475—Membrane reactors
• • 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
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
  • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07D—HETEROCYCLIC COMPOUNDS
  • C07D301/00—Preparation of oxiranes
  • C07D301/02—Synthesis of the oxirane ring
  • C07D301/03—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds
  • C07D301/12—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with hydrogen peroxide or inorganic peroxides or peracids
• • 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
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00049—Controlling or regulating processes
  • B01J2219/00051—Controlling the temperature
  • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
  • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
  • B01J2219/00094—Jackets

Definitions

• the present invention relates to a continuous epoxidation process from olefins to epoxides in a reactor which contains at least one catalyst suspended in a liquid phase and optionally also a gas phase, the liquid phase and optionally the gas phase being passed through a device with openings or channels in the reactor and the suspended Catalyst is retained in the reaction system during the separation of the epoxy-containing liquid by means of cross-flow filtration.
• the invention also relates to an apparatus for performing the method.
• the method and device are preferably used in the epoxidation of propene with hydrogen peroxide to propene oxide.
• the epoxidation of olefins with hydroperoxide can be carried out in one or more stages, batch and continuous processes being possible.
• the epoxidation is preferably also catalyzed, either in a heterogeneous or homogeneous phase. Methods are described for example in WO 00/07965.
• the present invention was therefore based on the object of developing a process for the epoxidation of olefins with hydroperoxides, in which the catalyst can be easily replaced during the reaction without the need to shut down the system and at the same time having a high space-time yield.
• the object was achieved by a continuous process for the epoxidation of olefins, characterized in that the epoxidation is carried out in a reactor which contains at least one catalyst suspended in a liquid phase, the liquid phase passing through a device with openings or channels built into the reactor is, and the catalyst is retained in the reaction system by means of cross-flow filtration during the separation of the epoxy-containing liquid.
• a gas phase is present, this can also be passed through the device with openings or channels installed in the reactor.
• the device with openings or channels for the passage of the reaction medium can consist of a bed, a knitted fabric, or a packing element.
• Such devices are already known from distillation and extraction technology.
• said devices basically have a significantly smaller hydraulic diameter than the devices used as internals for distillation and extraction technology.
• said diameter is preferably smaller by a factor of 2 to 10.
• the hydraulic diameter of the device used for installation in the reactor for the process according to the invention is preferably 0.5 to 20 mm.
• the hydraulic diameter is a parameter for describing the equivalent diameter of non-circular openings or channel structures.
• the term “hydraulic diameter” in the context of an opening denotes the quotient of four times the cross section of the opening and its circumference, in the context of a channel structure with a cross section in the form of an isosceles triangle, the size 2bk / (b + 2s), where b stands for the length of the base, k for the height and s for the leg length of the triangle.
• Packing elements that offer the advantage of low pressure loss are e.g. Wire mesh packing.
• packs made of other woven, knitted or felted liquid-permeable materials can also be used.
• Flat sheets preferably without perforation or other larger openings, can be used as further suitable packs or pack elements.
• Examples are commercial types, such as the type B1 from Montz or Mellapak from Sulzer.
• Packings made of expanded metal such as packs of the BSH type from Montz, are also advantageous.
• openings which are formed in the form of perforations, for example, must be kept correspondingly small.
• Decisive for the suitability of a package in the context of the present invention is not its geometry, but rather the opening sizes or channel widths in the package which arise for the sttom guidance.
• catalyst particles with an average particle size of 0.0001 to 2 mm, preferably from 0.0001 to 1 mm, particularly preferably from 0.005 to 0.1 mm, are preferably used in the process according to the invention. With particles of this average particle size, the relative speed and mass transfer can surprisingly be further increased.
• the high relative speed that can be achieved is also extremely advantageous compared to processes in which reactors without said internals are used.
• Increasing the mechanical energy supply beyond the amount required for suspension does not lead to any significant improvement in the mass transfer between the liquid and the suspended solid particles in suspension reactors without internals, since the achievable relative speed only marginally exceeds the sedimentation speed.
• the process can be carried out in various continuously operated reactor designs, such as jet nozzle reactors, bubble columns or tube bundle reactors. It is not necessary for the internals to fill the entire reactor.
• Bubble columns or tube-bundle reactors are particularly preferred embodiments of the reactor.
• a very particularly preferred reactor is a heatable and coolable tube bundle reactor in which the internals are accommodated in the individual tubes.
• Such a reactor has the advantage that the energy required to activate the reaction can be supplied well or the heat of reaction that occurs can be dissipated well.
• the reactor is preferably arranged vertically and flows through from bottom to top.
• the epoxidation is carried out in a reactor with one of the internals described above in the presence of one or more suspension catalysts at a pressure between 1 and 100 bar, preferably 1 and 60 bar, particularly preferably 1 and 50 bar.
• the reaction temperature is between 20 and 100 ° C, preferably between 30 and 80 ° C, particularly preferably between 40 and 70 ° C.
• the procedure is easy to carry out.
• the device described above is installed in the reactor, preferably tissue packs or sheet metal packs.
• the reaction mixture comprising olefin, hydroperoxide and suspension catalyst is now pumped through the reactor at a high speed.
• the cross-sectional area load (empty tube speed) of the liquid phase is preferably 50 to 300 m 3 / m 2 h, in particular in the range from 100 to 250 m 3 / m 2 h.
• the suspended catalyst material is introduced into the reactor using conventional techniques.
• the suspension of the suspension catalyst in the reaction system with simultaneous removal of the epoxy-containing liquid phase is carried out by using a cross stiom filtration.
• Specially treated aluminum oxide or metal sintered membranes with pore diameters of 50 to 500 nm, preferably 50 to 100 nm, such as those e.g. are distributed by Membraflow.
• the membrane modules usually multi-channel modules, are integrated into the reaction circuit in such a way that the flow velocity in the individual channels is between 1 and 6 m / s, preferably between 2 and 4 m / s, and therefore no coating can settle on the membrane surfaces.
• the permeate stream that is to say the epoxy-containing liquid stream which passes through the membrane, is taken off perpendicularly to the main flow direction. The quantity is regulated via the upcoming transmembrane pressure.
• the transmembrane pressure is defined as the difference between the mean pressure on the feed or retentate side and the pressure on the permeate side.
• the liquid containing epoxy is obtained as the permeate and can be processed.
• the activity of the catalyst decreases so much that the process is unsatisfactory, it can be conveniently separated, replaced or regenerated from the system.
• Part of the catalyst suspension is preferably removed from the system during the reaction and replaced by fresh catalyst suspension.
• the deactivated catalyst can then be regenerated externally. An interruption of the epoxidation or the processing stage of the epoxy-containing liquid is therefore not necessary, which is extremely advantageous.
• the starting materials known from the prior art can be used in the process according to the invention for epoxide synthesis.
• Organic compounds which have at least one C-C double bond are preferably reacted.
• alkenes are mentioned as examples of such organic compounds with at least one C-C double bond:
• Alkenes containing 2 to 8 carbon atoms such as ethene, propene and butene, are particularly preferably used.
• Propene is very particularly preferably used.
• Propen can also be used in the "chemical grade" quality level. It is then present together with propane in a volume ratio of propene to propane of approximately 97: 3 to 95: 5.
• the known hydroperoxides which are suitable for the reaction of the organic compound can be used as hydroperoxides. Examples of such hydroperoxides are, for example, tert-butyl hydroperoxide or ethylbenzene hydroperoxide.
• Hydrogen peroxide is preferably used as the hydroperoxide for the epoxide synthesis, preferably as an aqueous hydrogen peroxide solution.
• a porous oxidic material such as. B. a zeolite.
• Catalysts are preferably used which comprise a zeolite containing titanium, germanium, tellurium, vanadium, chromium, niobium or zirconium as the porous oxidic material.
• Titanium-containing zeolites with the structure of ITQ-4, SSZ-24, TTM-1, UTD-1, CIT-1 or CIT-5 are also conceivable for use in the process according to the invention.
• Further titanium-containing zeolites are those with the structure of ZSM-48 or ZSM-12.
• Ti zeolites with an MFI, MEL or MFI / MEL structure are particularly preferred.
• the titanium-containing zeolite catafyzers which are generally referred to as “TS-1”, “TS-2”, “TS-3”, as well as Ti zeolites with a framework structure isomorphic to ⁇ -zeolite are very particularly preferred .
• heterogeneous catalyst comprising the titanium-containing silicalite TS-1 is very favorable.
• porous oxidic material per se as a catalyst.
• a shaped body which comprises the porous oxidic material as the catalyst. All processes according to the prior art can be used to produce the shaped body, starting from the porous oxidic material.
• noble metals in the form of suitable noble metal components can be applied to the catalyst material.
• This method is preferably used to produce oxidation catalysts based on titanium or vanadium silicates with a zeolite structure, it being possible to obtain catalysts which contain from 0.01 to 30% by weight of one or more noble metals from the group of ruthenium, rhodium, Palladium, osmium, iridium, platinum, rhenium, gold and silver.
• Such catalysts are described for example in DE-A 196 23 609.6.
• the moldings can be assembled. All methods of comminution are conceivable, for example by grinding, splitting or breaking the shaped bodies, as are further chemical treatments, as described above, for example.
• a shaped body or more of it can be regenerated in the process according to the invention after deactivation by a process in which the regeneration is carried out by deliberately burning off the deactivation responsible rubbers. It is preferably carried out in an inert gas atmosphere which contains precisely defined amounts of oxygen-adding substances.
• This regeneration process is described in DE-A 197 23 949.8. Furthermore, the regeneration processes specified there with respect to the prior art can be used.
• all solvents can be used as solvents which completely or at least partially dissolve the starting materials used in the epoxide synthesis.
• water can be used; Alcohols, preferably lower alcohols, more preferably alcohols with less than six carbon atoms such as, for example, methanol, ethanol, propanols, butanols, pentanols, diols or polyols, preferably those with less than 6 carbon atoms; Ethers such as diethyl ether, tetrahydrofuran, dioxane, 1,2-diethoxyethane, 2-methoxyethanol; Esters such as methyl acetate or butyrolactone; Amides such as dimethylformamide, dimethylacetamide, N-methylpyrrolidone; Ketones such as acetone; Nitrites such as acetomtril; Sulfoxides such as dimethyl sulfoxide; aliphatic, cycloaliphatic and aromatic hydrocarbons, or mixtures
• Alcohols are preferably used.
• the use of methanol as a solvent is particularly preferred.
• olefin When the olefin is reacted with the hydroperoxide, other compounds which are usually used in epoxidation reactions can also be present. Such compounds are, for example, buffers with which the pH range which is most favorable for the respective epoxidation can be set and the activity of the catalyst can be regulated.
• Another object of the invention is also an apparatus for performing a continuous process for the epoxidation of olefins with hydroperoxide, as described above, comprising a reactor in which the epoxidation is carried out, a crossflow filter for the separation of epoxy-containing solution, the catalyst is retained in the reactor, and a container for the catalyst suspension.
• the device for carrying out a continuous process for the epoxidation of olefins is characterized in that the device comprises a reactor with internals, selected from the group of bed, knitted fabric or packing element, with a hydraulic diameter of 0.5 to 20 mm, one in a liquid suspended catalyst with an average particle size of 0.0001 to 2 mm, a crossflow filter and a container for the catalyst suspension.
• the reactor is a bubble column or a tube bundle reactor.
• the reactor is a tube bundle reactor which enables heat to be removed.
• propene can preferably be converted to propene oxide in methanol as solvent with hydrogen peroxide as epoxidation agent and using a TS-1 suspension catalyst and, if appropriate, buffer additives for controlling the reactivity of the catalyst and the pH.
• Figure 1 shows an example of the experimental setup of a continuously operated reactor 1, for example a bubble column, or particularly preferably a heatable and coolable tube bundle reactor with packings 2, which via lines 3 with a liquid mixture consisting of the olefin, hydrogen peroxide, the solvent and optionally buffer additives is fed.
• a continuously operated reactor for example a bubble column, or particularly preferably a heatable and coolable tube bundle reactor with packings 2, which via lines 3 with a liquid mixture consisting of the olefin, hydrogen peroxide, the solvent and optionally buffer additives is fed.
• the circuit is maintained and the catalyst is thus kept in suspension.
• the reaction solution is fed to crossflow filter 6 via line 5.
• the permeate which is fed via line 7 to the processing stage of the plant, takes place perpendicular to the main flow direction. Since the crossflow filters are impassable for the catalyst, the catalyst remains suspended in the reactor system and is fed to the reactor 1 via the line 8 and, if appropriate, the heat exchanger 9, so that the circuit for the
• the catalyst is introduced or removed, e.g. via a container 10 which can be specifically included in the reaction cycle.
• a container 10 which can be specifically included in the reaction cycle.
• To inject catalyst e.g. a certain amount of catalyst is placed in the container, and this is filled with solvent.
• the valves 11 and 12 are then opened and the valve 13 is closed. In this constellation, the reaction medium flows completely through the container 10 and the catalyst is introduced into the system.
• the procedure for discharging the catalyst is similar.
• the container 10 is e.g. filled with methanol, then the valves 11 and 12 are opened and the valve 13 is closed.
• the reactor is again flowed through.
• the valves 11 u. 12 closed and the valve 13 opened.
• the container 10 is now separated from the reaction medium and contains an aliquot of catalyst. This can then be freed from the solution in a further step and possibly regenerated externally. After regeneration, it can be returned to the system as described above.
• Catalyst material 14 can be supplied to container 10 via valve 15.

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• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Inorganic Chemistry (AREA)
• Engineering & Computer Science (AREA)
• Combustion & Propulsion (AREA)
• Epoxy Compounds (AREA)

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• 2002
  • 2002-10-23 DE DE10249377A patent/DE10249377A1/de not_active Withdrawn
• 2003
  • 2003-10-23 CN CN200380101746.1A patent/CN1705651A/zh active Pending
  • 2003-10-23 EP EP03809313A patent/EP1556367A1/de not_active Withdrawn
  • 2003-10-23 MX MXPA05004017A patent/MXPA05004017A/es unknown
  • 2003-10-23 AU AU2003276152A patent/AU2003276152A1/en not_active Abandoned
  • 2003-10-23 CA CA002502463A patent/CA2502463A1/en not_active Abandoned
  • 2003-10-23 US US10/531,438 patent/US20060014970A1/en not_active Abandoned
  • 2003-10-23 WO PCT/EP2003/011737 patent/WO2004037803A1/de not_active Application Discontinuation
• 2005
  • 2005-04-22 ZA ZA200503267A patent/ZA200503267B/en unknown

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