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
• • 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
  • B01J19/2405—Stationary reactors without moving elements inside provoking a turbulent flow of the reactants, such as in cyclones, or having a high Reynolds-number
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
  • B01F25/20—Jet mixers, i.e. mixers using high-speed fluid streams
  • B01F25/23—Mixing by intersecting jets
• • 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
  • B01J19/2415—Tubular 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
  • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J19/24—Stationary reactors without moving elements inside
  • B01J19/2415—Tubular reactors
  • B01J19/244—Concentric tubes
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
  • B01F2025/91—Direction of flow or arrangement of feed and discharge openings
  • B01F2025/915—Reverse flow, i.e. flow changing substantially 180° in direction
• • 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
  • B01J2219/00159—Controlling the temperature controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
• • 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
  • B01J2219/00162—Controlling or regulating processes controlling the pressure
• • 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
  • B01J2219/00164—Controlling or regulating processes controlling the flow

Definitions

• the invention relates to a method and a device for the continuous production of organic mono- or polyisocyanates by reacting the mono- or polyamines corresponding to the mono- or polyisocyanates with phosgene at elevated temperature, it being possible for the amines or the phosgene to be dissolved in organic solvent ,
• DE 2 153 268 relates to a continuous pre-phosgenation process for the production of organic isocyanates.
• a turbulent phosgene solution and diamine solution are continuously mixed in a driven centrifugal pump.
• the phosgene solution is introduced into the centrifugal pump through the suction port of the multistage centrifugal pump and the amine solution into the additional side access in the middle between the first and second centrifugal pumps, before the pre-phosgenation mixture is conveyed through the multistage centrifugal pump into a downstream hot phosgenation stage.
• EP 0 291 891 B1 relates to a process for the preparation of isocyanates. Solutions and suspensions of primary amines and their salts are mixed and reacted with phosgene solutions, the two substances being introduced into a mixing zone which has at least one rotor disk. The resulting preliminary product is carried out again, the further conversion of the primary products formed is carried out with heating. When mixing is carried out, the phosgene solution is fed axially to the rotor disk and the dissolved amine is sprayed parallel to the stream, but at a distance from the stream of the phosgene solution against the rotor disk.
• a process for the continuous production of mono- or polyisocyanates is known from EP 0 322 647 B1, in which, in order to produce the starting mixtures, the amine component, which is optionally dissolved in an inert solvent, and the phosgene solution are brought together in a nozzle by the one of the two components in the latter Nozzle is constricted and the other component in this constriction is fed from the side to the flow of the first component in a plurality of partial flows through a corresponding number of bores distributed over the circumference of the constriction.
• the total length of the constriction is chosen to include a partial length in which the reaction of the free amine is essentially complete.
• the disadvantage of this arrangement is that the slightest solid buildup in individual holes can lead to a lower flow through them.
• the first component is introduced under pressure in the form of a fan-shaped spray jet into an essentially cylindrical mixing chamber flowing in the longitudinal axis thereof.
• the second component is simultaneously introduced under pressure in the form of at least two fan-shaped spray jets into the spray jet of the first component, in its flow area.
• the resulting mixture of the two liquid components is then passed from the mixing chamber into a downstream reaction zone.
• the process appears unsatisfactory.
• SU 519 129 shows a production process for the production of isocyanates.
• a production process for isocyanates is presented, in which phosgene is supplied in gaseous form to the bottom of a reactor at temperatures between 100 ° C. and 180 ° C., which meets an amine salt which is supplied in the upper region of the reactor. The amine salt is fed to the upper region of the reactor at temperatures between 40 ° C. and 100 ° C.
• a venturi mixing device is known from US Pat. No. 3,507,626. This mixing device is specially designed for mixing phosgene with amine so that isocyanates can be prepared and comprises a first and a second inlet and an outlet.
• a first line section comprises a venturi section with a converging section, a constriction and a diverging section.
• a second section is coaxially received in the first line section and acts as the first inlet.
• the second line section comprises a bevel which leads to the converging section corresponds.
• the second line section opens into a mixing chamber which extends around the venturi section of the first line section. The mixing device ensures mixing and prevents clogging by the formation of by-products.
• DE-AS 17 92 660 B2 relates to a method and a device for mixing and reacting an amine with phosgene to form an isocyanate.
• amine and phosgene are coarxially guided to one another and mixed with one another, the two streams of amine and phosgene being ring-shaped or conical, intersecting at an acute angle to a crossing mixing point and immediately before, at and after this crossing point the entry be accelerated into a further reaction space, so that backflow of isocyanate into the amine stream is avoided.
• This section redirects the amine stream entering the cylindrical member at an angle away from the outer surface of the profile section and adjacent to the reaction area at an angle across the passageway.
• the amine stream flowing through the passage which is narrowed through the end portion of the cylindrical member, cuts the phosgene flowing in from the reaction area at an angle.
• EP 0 830 894 AI relates to a mixer reactor and a process for carrying out reactions, in particular the phosgenation of primary amines.
• this mixer reactor it is provided to prevent the blockage of nozzles arranged rotationally symmetrically to the mixing chamber by assigning a pin which can be displaced in the direction of the nozzle axis. Moving parts of reactors converting phosgene represent potential leakage points and should therefore be avoided if possible.
• the object of the invention is to provide a process for the phosgenation of amines which requires less solvent and less phosgene excess and in which fewer by-products are formed.
• This object is achieved in that in a process for mixing educt streams in a mixer for the phosgenation of amines, in which the reaction product is discharged in a closed manner and the educt streams can contain organic solvents, main streams and / or partial streams of the educts meet according to the countercurrent principle.
• the countercurrent principle is preserved when the educt streams are mixed at feed angles which are greater than 90 °, so that the educt jets each have an axially directed velocity component.
• the main educt streams can be supplied encased by educt substreams of the other component to be mixed, so that, for example, a slight excess of phosgene can be set which helps to avoid deposits in the area of the derivatives of the reaction product from the mixing zone of the feed channels.
• both the main stream of the first starting material is encased by a partial stream of the second starting material and the main stream of the second starting material can be encased by a partial stream of the first starting material.
• the reaction product can be discharged from the mixing zone within the feed channels on the one hand by a radial discharge or else by a discharge inclined at a certain angle.
• the main streams of two educts can be directed towards one another in a targeted manner, so that the respective impulse can be completely converted into mixing energy.
• the feed channels receiving the main streams of the starting materials can each be surrounded by an annular gap.
• the openings of the annular gaps can open positioned opposite one another in the area of the derivation of the reaction product.
• Fig. 7 shows the countercurrent mixture with a generally inclined discharge for the reaction product.
• FIG. 1 shows the schematic arrangement of a Y mixer 13.
• a first feed stream 1 and a second feed stream 2 are fed in at a feed angle 4 which is greater than 90 °.
• the resulting reaction product 3 is discharged closed in a spatial direction extending into the lower region of the mixer configuration 13 shown.
• FIG. 2 shows the countercurrent mixture of two reactant streams with the reaction product being discharged essentially in the axial direction.
• a main stream 2.1 of the second educt flows in within a feed channel 6, while the main stream 1.1 of the first educt 1 flows in opposite directions in the flow direction of the main stream 2.1 in a feed channel.
• the two feed channels 6 and 7 are, for example, symmetrical about an axis of symmetry 10.
• a discharge 5 branches off, which is delimited by a boundary wall 6.1 on the one hand and by a partition 7.1 is separated from the feed channel 7 of the first educt main stream 1.1.
• the discharge line 5 extends essentially in the axial direction parallel to the feed channels 6 and 7 shown for the respective educt main streams 1.1 and 2.1 and derives the reaction product 3 formed from the mixing of the two educt main streams 1.1 and 2.1.
• the feed angle 4 of the two educt main streams 2.1 and 1.1 of the first and second educt is approximately 180 °, so that the flow control used here causes the impulses to achieve a maximum mixing intensity and the impingement of the two jets Generation of maximum mixing energy can be used.
• On the partition 7.1, which the feed channel 7 of the first educt main stream 1.1 from the derivative 5 of the Reaction product 3 separates, are marked with the letters A and B, the critical points for the deposition of reaction components.
• 3 shows the countercurrent mixture when one of the reactant streams is divided into a main stream and a partial stream.
• the main stream 1.1 of the first reactants flows into a feed channel 1, which, however, to the discharge line 5, through which the reaction product 3 leaves the mixing zone, not through a partition 7.1 according to FIG. 2, but through one Annular gap 8 is separated.
• a partial stream 2.2 of the second educt flows through the annular gap 8, so that a phosgene, in the present case a surplus of phosgene, can be set in the region of the annular gap opening 9 of the annular gap 8.
• the feed channels 6 and 7 for the main stream 1.1 of the first educt and the main stream 2.1 of the second educt are symmetrical to an axis of symmetry 10.
• other cross sections can of course also be realized in these.
• FIG. 4 shows the countercurrent mixture with an annular gap encasing a feed channel with a shortened inner cylinder.
• annular gap 8 between the discharge line 5 for the reaction product 3 and the feed channel 7 for the main stream 1.1 of the first educt, approximately comparable to the embodiment variant according to FIG. 3 a partial stream 2.2 of the second educt of the mixing zone of the two main streams 1.1 and 2.1 of the educts 1 and 2 is fed to the annular gap 8, so that a phosgene, in the present case an excess of phosgene, is present in the mixing zone.
• elements which generate swirl can be installed in the feed channels 6 for the main stream 2.1 of the second educt and in the feed channel 7 for the main stream 1.1 of the first educt.
• the mixing energy released when the swirl is reduced in the mixing zone can be used to accelerate the mixing process.
• a swirl-generating element for example, a twisted band or spiral would be let into the respective feed channels 6 and 7 for the main streams 2.1 and 1.1 of the two starting materials.
• the feed channels 6 and 7 for the main streams 2.1 and 1.1 of the two starting materials 1 and 2 are each rotationally symmetrical to an axis of symmetry 10.
• the feed channel 6 for the main stream 2.1 of the second product has a larger diameter 16, compared to the feed channel 7 for the main stream 1.1 of the first educt.
• the two feed channels 6 and 7 open into a two common radial derivative, which is arranged exactly vertically compared to the axis of symmetry 10 of the feed channels 6 and 7 and allows the reaction product to be discharged vertically.
• the derivation 5 through which the reaction product 3 leaves the mixing zone is separated by an annular gap 8 in the embodiment variant according to FIG. 6.
• the annular gap 8 is delimited in each case by an outer tube 11 and an inner tube 12 which, in the embodiment variant shown, open into the annular gap opening, both the outer tube and the inner tube being of the same length and leading a partial flow 2.2 of the second starting material of the mixing zone.
• the outer wall of the feed channel 6 is also designed as a further annular gap 17.
• the annular gap consists of an outer tube 18 and an inner tube 19 and opens into the annular gap opening 9 of the first annular gap 8 opposite with in the annular gap opening 20 in the mixing zone of the two main streams 2.1 of the second reactant and 1.1 of the first reactant fed to one another.
• the outer tube 18 of the further annular gap 17 merges into the boundary wall 6.1 of the derivative 5 for the reaction product 3, it being possible for the transitions to be made with rounded edges which favor the flow.
• a main stream 2.1 of a second educt is fed to a mixing zone through a feed channel 6, which is also fed through the outer wall 15 through the outer wall 15, a main stream 1.1 of the first educt being fed through the feed channel 6.
• further transitional forms between an axial derivative according to the reaction products 3 as shown in FIGS. 2 and 3 and the radially oriented derivative 14 according to FIG. 5 are conceivable.
• mixing can take place with particularly effective use of the kinetic energy of the fluid streams.
• the type of mixing results in particularly intensive contact between the educts, since the energy inherent in the educt jets can be completely converted into mixing energy.
• the resulting high mixture intentions push the by-product formation largely back and allow by means of the method according to the invention and the device proposed according to the invention for mixing two streams the advantages of high operational safety, the avoidance of moving parts and the achievement of high yields. Large excesses of phosgene and high proportions of solvents in which the phosgene or the amines to be reacted have to be dissolved can be avoided, which is advantageous for later processing of the starting materials of the reaction product.
• TDA 2,4-toluenediamine
• ODB o-dichlorobenzene
• 8100 kg / h of a 65% phosgene solution in a T-mixer were injected.
• the inlet diameters of the T mixer were chosen so that the mean entry velocity of the phosgene and amine solution jets was about 10 m / s. After clear phosgenation and preparation by distillation, the yield was 96.4%.

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• Chemical & Material Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Organic Chemistry (AREA)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Accessories For Mixers (AREA)
• Physical Or Chemical Processes And Apparatus (AREA)

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Citations (7)

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• 2000
  • 2000-05-26 DE DE10026142A patent/DE10026142A1/de not_active Withdrawn
• 2001
  • 2001-05-21 HU HU0301844A patent/HU229267B1/hu not_active IP Right Cessation
  • 2001-05-21 PT PT01945178T patent/PT1289649E/pt unknown
  • 2001-05-21 ES ES01945178T patent/ES2282264T3/es not_active Expired - Lifetime
  • 2001-05-21 AU AU2001267470A patent/AU2001267470A1/en not_active Abandoned
  • 2001-05-21 KR KR1020027015867A patent/KR100809167B1/ko not_active Expired - Fee Related
  • 2001-05-21 CN CN018099327A patent/CN1216681C/zh not_active Expired - Fee Related
  • 2001-05-21 JP JP2001587903A patent/JP4959092B2/ja not_active Expired - Fee Related
  • 2001-05-21 DE DE50112295T patent/DE50112295D1/de not_active Expired - Lifetime
  • 2001-05-21 US US10/296,595 patent/US6867324B2/en not_active Expired - Fee Related
  • 2001-05-21 AT AT01945178T patent/ATE358532T1/de not_active IP Right Cessation
  • 2001-05-21 WO PCT/EP2001/005818 patent/WO2001091898A1/de not_active Ceased
  • 2001-05-21 EP EP01945178A patent/EP1289649B1/de not_active Expired - Lifetime

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