EP3194363A1 - Procédé de préparation d'isocyanates en phase gazeuse - Google Patents

Procédé de préparation d'isocyanates en phase gazeuse

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Publication number
EP3194363A1
EP3194363A1 EP15763939.4A EP15763939A EP3194363A1 EP 3194363 A1 EP3194363 A1 EP 3194363A1 EP 15763939 A EP15763939 A EP 15763939A EP 3194363 A1 EP3194363 A1 EP 3194363A1
Authority
EP
European Patent Office
Prior art keywords
phosgene
amine
mixing
stream
flow
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP15763939.4A
Other languages
German (de)
English (en)
Inventor
Josef Sanders
Armin SCHYMURA
Martin Ehrig
Manfred Keller-Killewald
Dietmar Wastian
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Covestro Intellectual Property GmbH and Co KG
Original Assignee
Covestro Deutschland AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Covestro Deutschland AG filed Critical Covestro Deutschland AG
Publication of EP3194363A1 publication Critical patent/EP3194363A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C263/00—Preparation of derivatives of isocyanic acid
    • C07C263/10—Preparation of derivatives of isocyanic acid by reaction of amines with carbonyl halides, e.g. with phosgene
    • 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
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/1812—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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B01J8/065—Feeding reactive fluids
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C265/00—Derivatives of isocyanic acid
    • C07C265/14—Derivatives of isocyanic acid containing at least two isocyanate groups bound to the same carbon skeleton
    • 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
    • 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
    • B01J2219/00166—Controlling or regulating processes controlling the flow controlling the residence time inside the reactor vessel

Definitions

  • the invention relates to a process for the preparation of isocyanates by reacting the corresponding primary amines with phosgene in the gas phase.
  • Isocyanates are produced in large quantities and serve mainly as starting materials for the production of polyurethanes. They are usually prepared by reacting the corresponding amines with phosgene. One possibility for the preparation of isocyanates is the reaction of the amines with the phosgene in the gas phase.
  • EP 1 449 826 B1 discloses a process in which, for mixing the vaporous educts, multiple nozzles parallel to the
  • Flow direction can be used.
  • EP 1 526 1 29 AI discloses a method in which the flow turbulence in the mixing zone by internals, for. B. by spin turning, is increased.
  • EP 1 555 258 A1 discloses a process using a ring-die nozzle in which the gaseous amine, optionally diluted with an inert gas, is fed to the reactor via the annular gap and the phosgene is supplied via the inner nozzle as a central jet and over the remaining Reaktorquers chnitt.
  • EP 188 247 A1 (WO 2009/027232 A1) and EP 2 188 248 A1 (WO 2009/027234 A1) describe processes in which between the two fluid streams of amine and phosgene in a mixing means, e.g. in a ternary mixing nozzle, an inert medium, e.g. Nitrogen, is dosed.
  • an inert medium e.g. Nitrogen
  • the turbulent flow boundary layer of at least one fluid stream before being brought into contact with the other stream is reduced by at least one mechanical baffle.
  • EP 0 928 785 A1 discloses a process in which microstructure mixers are used for rapid mixing of the fluid reactant streams.
  • the disadvantage here is that it is very easy due to the small dimensions of the mixer at the high temperatures to blockages by deposition of solid by-products or decomposition products, which is why this method has not prevailed on an industrial scale.
  • EP 2 088 139 A1 describes a process in which gaseous amine is injected at 200 ° -600 ° C. at right angles into excess phosgene from an outer annular channel via radial bores and flows in a flow tube. After mixing, the reactant stream is first accelerated by a cross-sectional reduction and then slowed down again by cross-sectional enlargement, before it is then passed into a reactor.
  • WO 2011/1 15848 A1 discloses a static mixer and its use for the preparation of isocyanates by phosgenation of primary amines, wherein an up to 90% solvent-containing amine stream injected at right angles through an outer annular channel through a plurality of radial holes in the phosgene stream inside a flow tube is where a (very short) Stömungselement in the flow tube at the height of the bores the phosgene stream without changing the flow velocity imposes an annular flow, whereby the mixing with the amine stream is favored.
  • no examples of isocyanate production are cited, as well as quantity, pressure and temperature specifications are missing, so that no conclusions about the state of matter of the educts are possible.
  • the object of the present invention was therefore to provide a process for the preparation of isocyanates by reacting the corresponding primary amines with phosgene in the gas phase, which avoids the described disadvantages of the known processes and can be achieved with the high yields and, at the same time, long plant service lives .
  • primary amines with phosgene in a tubular reactor above the boiling point of the amine in the gas phase can be advantageously reacted with long plant service lives, if the phosgene via an outer R ingkanal by several radial channels at an angle of ⁇ 90 ° to the flow direction of gaseous amine troms is injected into the gaseous amine stream in the interior of a flow tube, wherein inside the flow tube is coaxial with a static mixer Kenics type.
  • Such mixers are also referred to in the literature as gas mixer, reversing label or V-E 1 t-M i sc.
  • the invention relates to a process for preparing diisocyanates or triisocyanates of the general formein (I) or (II)
  • R is a (cyclo) aliphatic, araliphatic or aromatic hydrocarbon radical having up to 15 carbon atoms, with the proviso that at least 2 carbon atoms are arranged between the NCO groups, by phosgenation of the corresponding di- and / or triamines of the general formula ( III) or (IV)
  • di- and triamines understood that are present in gaseous form and may optionally contain portions of non-vaporized amine droplets (aerosol). However, the vaporous amines preferably contain no droplets of unvaporized amines.
  • the angle is> 60 ° and ⁇ 90 °, preferably> 75 ° and ⁇ 90 ° and particularly preferably 90 °.
  • An angle of 90 ° according to the invention is also referred to as rectangular or vertical.
  • channels are understood as meaning openings which are permeable to the educt streams.
  • the openings may have any shape and can be, for example, with
  • the channels are holes and the angle is 90 °, so that the phosgene is injected via an outer annular channel through a plurality of radial bores at right angles to the gaseous amine stream in the interior of a flow tube.
  • Suitable aliphatic amines are e.g. mentioned in EP 0 289 840 AI.
  • diamines such as the pure isomers or the isomer mixtures of isophorone diamine (IPDA, mixture of isomers), 1,6-hexamethylenediamine (H DA).
  • IPDA isophorone diamine
  • H DA 1,6-hexamethylenediamine
  • the preferred triamine is l, 8-diamino-4- (aminomethyl) octane (triaminononane).
  • Suitable aromatic amines are the pure isomers or isomer mixtures of diaminobenzene, diaminotoluene, diaminodimethylbenzene, diaminonaphthaiine and diaminodiphenylmethane. Preference is given to using 2,4- / 2,6-toluylenediamine mixtures of the isomer ratios 80/20 and 65/35 or the pure 2,4-tolylenediamine isomer.
  • the starting amines of the formula (III) and (IV) are evaporated before carrying out the process according to the invention, optionally with an inert gas such as N 2, He, Ar or with the vapors of an inert solvent, for. B. aromatic hydrocarbons with or without halogen substitution, heated to 200 ° C to 600 ° C, preferably 250 ° C to 450 ° C, and fed to the mixer or reactor.
  • an inert gas such as N 2, He, Ar or with the vapors of an inert solvent, for.
  • aromatic hydrocarbons with or without halogen substitution heated to 200 ° C to 600 ° C, preferably 250 ° C to 450 ° C, and fed to the mixer or reactor.
  • the amount of inert gas optionally used as a diluent or gaseous solvent is not critical.
  • the volume ratio of amine vapor to inert gas or solvent vapor can be between 1: 0.5 and 1: 2.
  • the phosgene used in the phosgenation is used, based on the amine, in excess. In general, the molar phosgene excess based on an amino group is 30 to 300%, preferably 60 to 200%. Before being fed into the mixer or reactor, the phosgene is heated to a temperature of from 200 ° C to 600 ° C, preferably from 250 ° C to 450 ° C.
  • the phosgene can be treated with an inert gas such as N 2, He, Ar, or with the vapors of an inert solvent, e.g. As aromatic hydrocarbons are diluted with or without halogen substitution. Preference is given to the undiluted variant.
  • an inert gas such as N 2, He, Ar
  • an inert solvent e.g.
  • aromatic hydrocarbons are diluted with or without halogen substitution. Preference is given to the undiluted variant.
  • the mixing of the two educt streams takes place in a flow tube in which a co-axial static mixer of Ken i es type is, wherein the optionally diluted with an inert gas gaseous amine (gas stream A) is passed coaxially through the flow tube and the mixer and the Phosgene via an outer annular channel through a plurality of radial channels, preferably bores, which are located on a plane on the circumference of the flow tube (introduction level), with an angle of ⁇ 90 °, preferably> 60 ° and ⁇ 90 °, more preferably> 75 ° and ⁇ 90 ° and most preferably 90 ° to the flow direction of the amine stream is introduced.
  • the static mixer begins in the flow direction already above the introduction level of the phosgene and ends downstream significantly below the incipient level of the phosgene, its length depends on the reactivity of the amine used.
  • the number of mixing elements of the static mixer above the introduction level is such that the inert gas possibly added to the amine is mixed homogeneously with it, i.e., in a homogeneous manner.
  • the degree of mixing of amine and inert gas immediately before the introduction level is 50 to 100, preferably 70 to 95%.
  • the ratio of the length of the static mixer before the introduction level to the length behind the introduction level is 0.1 to 1.0, more preferably 0.2 to 0.8.
  • the phosgene stream is introduced into the gas stream A at a rate of 15-90 m / s, more preferably 20-80 m / s.
  • the number of channels and their cross-sectional area result from the phosgene volume flow to be introduced. Preferred is an odd number of channels.
  • the diameter of the mixing tube is dimensioned so that the flow velocity of the gas mixture of all components immediately below (downstream) the introduction level 4-25 m / s, preferably 6-! 5 m / s, more preferably 8-12 m / s.
  • the length of the Kenics type static mixer and the number of its mixing elements are sized so that a sufficient degree of mixing is achieved at the end of the mixer and can be calculated.
  • the tube reactors are generally made of steel. Glass, alloyed or enamelled steel and are dimensioned to be among the
  • Process conditions complete conversion of the amine is made possible with the phosgene.
  • the gas streams are introduced via a mixing device described in more detail above at one end of the tubular reactor in this.
  • the temperature in the reactor is 200 ° C to 600 ° C, preferably 250 ° C to 450 ° C, which temperature can optionally be maintained by heating the tubular reactor upright.
  • the refining time is calculated from the time throughput of the educt streams, the reactor dimensioning and the reaction parameters pressure and temperature.
  • the retention time of the reaction mixture in the reactor is 0.05 s to 10 s, preferably 0.08 s to 4 s.
  • the gaseous mixture leaving the reaction space continuously is freed of the isocyanate formed.
  • This can be done for example by means of an inert solvent whose temperature is chosen so that it is above the decomposition temperature of the isocyanate carbamic acid and on the other hand below the condensation temperature of the isocyanate and preferably also of the optionally used in the vapor form as a diluent solvent, so that Isocyanate and auxiliary solvents condense or the isocyanate dissolves in the auxiliary solvent, while excess phosgene, hydrogen chloride and optionally used as diluent mitver Listetes inert gas through the condensation stage or the solvent in gaseous form.
  • auxiliary solvent for selective recovery of the auxiliary solvent from the gas leaving the reaction space mixture are particularly suitable at a temperature of 60 to 200 ° C, preferably 90 to 170 ° C, held solvent of the type exemplified above, in particular technical mono- (MCB) and dichlorobenzene (ODB).
  • MCB technical mono-
  • ODB dichlorobenzene
  • Solvent solvent mist
  • the gas mixture passing through the condensation stage to obtain the isocyanate is then freed of excess phosgene in a manner known per se. This can be done by means of a cold trap, absorption in an inert solvent (e.g., MCB or ODB) maintained at a temperature of -10 ° C to 8 ° C, or by adsorption and hydrolysis on activated carbon.
  • the chioreactor gas passing through the phosgene recovery stage can be recycled in a manner known per se for recovery of the chlorine required for phosgene synthesis.
  • the purification of the isocyanate can be carried out by fractional distillation or by recrystallization or adsorptive removal of impurities, e.g. by treatment with activated charcoal. Diatomaceous earth, silica gel or bleaching earth. If the isocyanate is sufficiently stable in thennish, purification is preferably carried out by the mildest possible distillative workup of the crude isocyanate solution in the solvent used for the isocyanate condensation, the isocyanate fraction optionally being distilled in vacuo.
  • very reactive amines such as e.g. 1, 5-pentanediamine (PDA) can be phosgenated with excellent yields and system lifetime to 1, 5-pentane diisocyanate (PDI).
  • PDA 5-pentanediamine
  • PDI 1, 5-pentane diisocyanate
  • the required flow rates are comparatively low, so that shorter reactors can be used than when using jet mixers.
  • the amine in contrast to the method described in EP 2 088 139 AI and WO 2011/115848 not injected through narrow holes, but is fed through a flow tube with a significantly larger cross-section of the reactor, the pressure drop is very low and thus the United evaporation temp low.
  • especially sensitive amines such as. Bis (p-aminocyclohexyl) methane or 1, 3 -xylylenediamine be phosgenated with better yields.
  • the invention relates to a process for the preparation of di- or triisocyanates of the general formulas (I) or (II) OCN-R-NCO OCN-R-NCO
  • R is a (cyclo) aliphatic, araliphatic or aromatic hydrocarbon radical having up to 15 carbon atoms, with the proviso that at least 2 carbon atoms are arranged between the NCO groups, by phosgenation of the corresponding di- and / or triamines of the general formula ( III) or
  • R has the abovementioned meaning, in which the vaporous di- and triamines, optionally diluted with an inert gas or with the vapors of an inert solvent, and phosgene separately heated to temperatures of 200 ° C to 600 ° C, mixed in a tubular reactor and Be brought reaction, characterized in that the phosgene is injected via an outer annular channel through a plurality of radial channels at an angle of ⁇ 90 ° to the flow direction of the gaseous amine stream in the gaseous amine trom inside a flow tube, wherein in the interior of the flow tube coaxial a static one
  • Kenics-type mixer is located.
  • the channels are bores.
  • the angle is> 60 ° and ⁇ 90 °.
  • the angle is> 75 ° and ⁇ 90 °. In a fifth embodiment of the method according to one of the embodiments 1 or 2, the angle is 90 °. In a sixth embodiment of the method, the method is performed so that the phosgene is injected via an outer annular channel through a plurality of radial bores at right angles in the gaseous amine trom in the interior of a flow tube.
  • the method according to any one of embodiments 1 to 6 is performed so that the amine trom heated to 250 ° C to 450 ° C before being fed into the mixer.
  • the process according to any one of the embodiments 1 to 7 is carried out so that the phosgene stream is heated to 250 ° C to 450 ° C before being fed into the mixer.
  • the process according to one of the embodiments 1 to 8 is carried out so that the phosgene is used in excess relative to the amine and the molar phosgene excess based on an amino group is 30 to 300%.
  • the process according to one of the embodiments 1 to 8 is carried out so that the phosgene is used in excess relative to the amine and the molar phosgene excess based on an amino group is 60 to 200%.
  • the process according to one of the embodiments 1 to 10 is carried out so that the phosgene stream is introduced at a rate of 15-90 m / s into the gaseous amine gas possibly diluted with an inert gas.
  • the method according to one of Aus collirungsformen 1 to 10 is performed so that the phosgene stream is introduced at a rate of 20-80 m / s in the optionally diluted with an inert gas gaseous amine trom.
  • the method according to one of embodiments 1 to 12 is performed such that the ratio of the length of the static mixer upstream of the entry level (upstream) to the length downstream of the entry level (downstream) ( Figure 1) is 0.1 to 1.0 is.
  • the method according to one of embodiments 1 to 12 is performed such that the ratio of the length of the static mixer upstream of the entry level (upstream) to the length downstream of the entry level (downstream) (Figure 1) is 0.2 to 0.8 is.
  • the method according to one of embodiments 1 to 14 is performed so that the diameter of the mixing tube is dimensioned so that the flow velocity of the gas mixture of all components immediately below (downstream) the introduction level (Figure 1) 4-25 m / s is.
  • the method according to one of the embodiments 1 to 14 is performed so that the diameter of the mixing tube is dimensioned such that the Flow rate of the gas mixture of all components immediately below (downstream) of the inlet level ( Figure 1) is preferably 6-15 m / s.
  • the method according to one of the embodiments 1 to 14 is performed so that the diameter of the mixing tube is dimensioned so that the flow velocity of the gas mixture of all components immediately below (downstream) the introduction level (Figure 1) 8-12 m / s is.
  • the method according to any one of embodiments 1 to 17 is performed so that the length of the Kenics type static mixer and the number of its mixing elements are such that at the end of the mixer a mixing degree of 80-99% is achieved becomes.
  • the method according to one of the embodiments 1 to 17 is performed such that the length of the Kenics type static mixer and the number of its mixing elements are so dimensioned that at the end of the mixer a mixing degree of 95-98% is achieved. is reached.
  • the process according to any of embodiments 1 to 20 is conducted by adding an inert gas to the amine and by measuring the number of mixing elements of the static mixer above the introduction level (Figure 1) such that the degree of mixing of amine and inert gas immediately before the introduction level (upstream) is 50 to 100%.
  • the process according to one of the embodiments 1 to 20 is conducted in such a way that an inert gas is added to the amine and the number of mixing elements of the static mixer above the introduction level (Figure 1) is dimensioned so that the degree of mixing of amine and inert gas immediately before the introduction level (upstream) at 70 to 95%.
  • the method according to any one of embodiments 1 to 22 is performed so that the temperature in the reaction space at 200 ° C to 600 ° C.
  • the process according to any one of embodiments 1 to 22 is conducted such that the temperature in the reaction space is 250 ° C to 450 ° C.
  • the method according to one of the embodiments 1 to 24 is carried out so that the pressure in the supply lines to the reaction space is 200 to 3,000 mbar abs. and at the exit from the reaction space at 150-2000 mbar abs. lies.
  • the method according to one of the imple mentation forms 1 to 24 out so that the pressure in the supply lines to the reaction chamber at 800 1500 mbar abs. and at the exit from the reaction space at 750 - 1.440 mbar abs. lies.
  • Execution forms 1 to 26 performed so that a flow rate within the reaction space of 3 to 120 m / s is maintained.
  • Embodiments 1 to 26 performed so that a flow rate within the reaction space of 5 to 75 m / s is maintained.
  • the process according to any one of embodiments 1 to 28 is conducted so that the residence time of the reaction mixture in the reactor is 0.05 s to 10 s.
  • the process according to one of embodiments 1 to 28 is conducted such that the residence time of the reaction mixture in the reactor is from 0.08 s to 4 s.
  • Fig. 1 Schematic structure of a mixing device according to the invention, in which the numbers 1 -3 have the following meaning: 1: amine + inert gas; 2: phosgene; 3: introduction level.
  • Carrier gas hydrogen
  • a tubular reactor (length 720 mm, inner diameter 8 mm) with a arranged on the reactor axis coaxial nozzle (inner diameter 2 mm) and a downstream isocyanate condensation stage were measured at a pressure of 700 mbar abs at the end of the isocyanate condensation step, continuously 250 gh PDA vaporized under introduction of a nitrogen stream of 37 g / h, superheated to 270 ° C and fed via the coaxial nozzle (simple smooth-jet nozzle) to the reactor.
  • 1090 g / h of phosgene were heated to 300 ° C.
  • the MCB and formed PDI-containing vapors were passed to an isocyanate absorption column along with the offgas of the reaction.
  • Isocyanate and MCB were condensed in a downstream condenser and returned to the quench, while the off-gas, consisting essentially of nitrogen, excess phosgene and HCl, was phosgene-killed.
  • the resulting solution of isocyanate in MCB was collected and worked up in portions by distillation.
  • Chloropentyl isocyanate N-carbamoylpiperidine, N-carbamoyltetrahydropyridine,
  • Example 1 Phosgenation of 1, 5-pentanediamine (PDA) with static mixer (according to the invention)
  • a tubular reactor (length: 400 mm, internal diameter 8.8 mm) with a mixing tube arranged on the reactor axis (length: 210 mm, internal diameter 8 mm) in which a static mixer of the Kenics type is installed coaxially (length 200 mm, diameter 7.9 mm, 15 mixing elements) and a subsequent isocyanate condensation stage were abs.
  • Example 2 Phosgenation of an isomer mixture of 2,4- and 2,6-toluenediamine with static
  • a tubular reactor (length: 31 00 mm, inner diameter 16.0 mm) with a arranged on the reactor axis mixing tube (length: 210 mm, mecanic prepare for continuous vapor phase phosgenation with a Aminverdampfungscut, a tubular reactor (length: 31 00 mm, inner diameter 16.0 mm) with a arranged on the reactor axis mixing tube (length: 210 mm, mecanic prepare for a tubular reactor (length: 31 00 mm, inner diameter 16.0 mm) with a arranged on the reactor axis mixing tube (length: 210 mm, rios prepare for the coaxial one built-in static mixer of Kenics type (length 200 mm, diameter 7.9 mm, 1 5 mixing elements) and a subsequent isocyanate condensation stage are continuously at a pressure of 1000 mbar abs.
  • 1020 g / h of phosgene are metered into the interior of the mixing tube via an outer annular channel through 7 radial bores (diameter 1 mm) perpendicular to the flow direction of the amine.
  • the mean residence time in the mixer is 0.03 s.
  • the reaction mixture leaving the mixer is fed to the reactor.
  • the average velocity of the gas stream in the reactor is about 1.3 m / s and the rate of flow of amine / nitrogen to phosgene stream is 0.04.
  • the gas stream containing the reaction product toluene diisocyanate (TDI) is quenched and worked up analogously to the comparative example with 5 kg / h of liquid o-dichlorobenzene (ODB).
  • the Miniplant 80 h could be operated without problems.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

Procédé de préparation d'isocyanates par mise en réaction des amines primaires correspondantes avec du phosgène en phase gazeuse, le phosgène étant introduit par une buse dans l'intérieur d'un tuyau d'écoulement dans le flux d'amine gazeux, par l'intermédiaire d'un canal annulaire externe par plusieurs canaux radiaux à un angle ≤ 90° par rapport à la direction d'écoulement du flux d'amine gazeux, un mélangeur statique du type Kenics se trouvant placé coaxialement à l'intérieur du tuyau d'écoulement.
EP15763939.4A 2014-09-19 2015-09-18 Procédé de préparation d'isocyanates en phase gazeuse Withdrawn EP3194363A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP14185562 2014-09-19
EP15171773 2015-06-12
PCT/EP2015/071436 WO2016042124A1 (fr) 2014-09-19 2015-09-18 Procédé de préparation d'isocyanates en phase gazeuse

Publications (1)

Publication Number Publication Date
EP3194363A1 true EP3194363A1 (fr) 2017-07-26

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EP15763939.4A Withdrawn EP3194363A1 (fr) 2014-09-19 2015-09-18 Procédé de préparation d'isocyanates en phase gazeuse

Country Status (6)

Country Link
US (1) US20170305842A1 (fr)
EP (1) EP3194363A1 (fr)
JP (1) JP2017527596A (fr)
KR (1) KR20170058927A (fr)
CN (1) CN106715385B (fr)
WO (1) WO2016042124A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
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US10689481B2 (en) 2015-06-12 2020-06-23 Mitsui Chemicals, Inc. Polyisocyanate composition, polyurethane resin, two-component curable polyurethane composition, and coating material
US10689477B2 (en) 2015-06-12 2020-06-23 Mitsui Chemicals, Inc. Polyisocyanate composition, polyurethane resin, two-component curable polyurethane composition, and coating material
US10793666B2 (en) 2015-06-12 2020-10-06 Mitsui Chemicals, Inc. Polyisocyanate composition, polyurethane resin and two-component curable polyurethane composition
US10865269B2 (en) 2015-06-12 2020-12-15 Mitsui Chemicals, Inc. Polyisocyanate composition, polyurethane resin, two-component curable polyurethane composition, coating material, and adhesive material

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3506993B1 (fr) * 2016-09-01 2021-01-06 Covestro Intellectual Property GmbH & Co. KG Procédé de fabrication d'isocyanates
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CN106715385A (zh) 2017-05-24
KR20170058927A (ko) 2017-05-29
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JP2017527596A (ja) 2017-09-21
US20170305842A1 (en) 2017-10-26

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