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EP0927197A1 - Procede de preparation de polymeres de methylmethacrylate dans un reacteur a recirculation - Google Patents

Procede de preparation de polymeres de methylmethacrylate dans un reacteur a recirculation

Info

Publication number
EP0927197A1
EP0927197A1 EP97943868A EP97943868A EP0927197A1 EP 0927197 A1 EP0927197 A1 EP 0927197A1 EP 97943868 A EP97943868 A EP 97943868A EP 97943868 A EP97943868 A EP 97943868A EP 0927197 A1 EP0927197 A1 EP 0927197A1
Authority
EP
European Patent Office
Prior art keywords
reactor
circulation
polymerization
circuit
polymers
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.)
Ceased
Application number
EP97943868A
Other languages
German (de)
English (en)
Inventor
Klaus-Dieter Hungenberg
Michael BAUMGÄRTEL
Jürgen Koch
Wolfgang Fischer
Reiner Thiele
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.)
BASF SE
Original Assignee
BASF SE
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 BASF SE filed Critical BASF SE
Publication of EP0927197A1 publication Critical patent/EP0927197A1/fr
Ceased legal-status Critical Current

Links

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
    • B01J19/245—Stationary reactors without moving elements inside placed in series
    • 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
    • B01J19/2435—Loop-type reactors
    • 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
    • C08F2/00—Processes of polymerisation
    • C08F2/02—Polymerisation in bulk
    • 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
    • C08F20/00—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and only one being terminated by only one carboxyl radical or a salt, anhydride, ester, amide, imide or nitrile thereof
    • C08F20/02—Monocarboxylic acids having less than ten carbon atoms, Derivatives thereof
    • C08F20/10—Esters
    • C08F20/12—Esters of monohydric alcohols or phenols
    • C08F20/14—Methyl esters, e.g. methyl (meth)acrylate
    • 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
    • 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 continuous process for the production of methyl methacrylate polymers with a narrow molecular weight distribution by polymerization in bulk in a circulation reactor.
  • polymethyl methacrylate which is used as acrylic glass in amounts of more than 500,000 t per year, by polymerizing methyl methacrylate in emulsion, suspension or by bulk or bulk polymerization (previously also called block polymerization).
  • block polymerization For a long time, high-molecular semi-finished products made of polymethyl methacrylate as high-quality acrylic glass have been produced by casting processes (flat chamber process, double-belt process), 20-25% solutions of polymethyl methacrylate in mono methyl methacrylate obtained by prepolymerization often being used to shorten the production time.
  • prepolymerization in a stirred tank was combined with a subsequent reaction in screw extruders. It is e.g.
  • methyl methacrylate In contrast to bulk polymerization, for example styrene, methyl methacrylate, when polymerized alone or largely alone in bulk, has many special features that must be taken into account in bulk polymerization. For example, methyl methacrylate shows an enormous polymerization shrinkage of 20 to 21% during the polymerization. In addition, methyl methacrylate in bulk polymerization already shows a polymerization acceleration of only about 20% due to the Trommsdorff or gel effect, which leads to an acceleration of the reaction rate of 1-2 orders of magnitude with isothermal reaction control. With the high heat of polymerization of methyl methacrylate combined with low thermal conductivity of the system, a sharp rise in temperature can very quickly occur, which can result in a hardly manageable reaction.
  • the methyl methacrylate polymerization shows a glass effect and ceiling effect influencing the polymerization process (limit conversion due to freezing of the reaction, above the glass transition temperature T g of 105 ° C. decrease in conversion due to depolymerization / polymerization equilibrium, the depolymerization due to comonomers and Controller can be influenced).
  • a poly methacrylate with an average molecular weight M w of more than 300,000 can only be deformed thermo-elastically.
  • the object of the present invention was to polymerize methyl methacrylate in bulk continuously in circuit reactors to give polymers with very little non-uniformity, without the formation of large amounts of disruptive deposits on the circuit reactor walls during long-term operation.
  • the task also included delimiting the areas of the operating variables (half-life of the initiator, conversion, flow rate, circulation ratio, polymerization temperature, average residence time) in which the polymerization proceeds without problems and leads to a high-quality product.
  • REPLACEMENT SHEET (REGEL26 ⁇ polymerized in bulk in a circulation reactor with feed mixture feed, reactor outlet, mixing device, circulation pump and cooling surface such that a) the circulation ratio K R is greater than 20 / n E , where n E represents the number of feeds per circulation loop, and preferably K R is about 10 to 60, b) the mean effective axial flow velocity W eff # ax is greater than 5 cm / second and is preferably 7 to 40 cm / second, c) the polymerization temperature is 135 to 150 ° C, d) a polymerization initiator is used whose batch half-life t ⁇ / 2 ( batch ) is between 3 and 10 and preferably between 4 and 6 minutes at the polymerization temperature, e) the initiator feed concentration being adjusted so that the reaction mass has an average residence time t of 1 , 3 to 2.5 hours at the reactor outlet, a polymer mass fraction y p of 0.50 to 0.70 and in particular of about 0.55 to 0.65 is achieved.
  • the method according to the invention is carried out in a circuit reactor which has at least one inlet, outlet or reactor outlet, at least one mixing device such as a static mixing element, a circuit pump and cooling surface.
  • Circuit reactors are described in the technical literature and can be assembled by the process engineer in an appropriate manner if the critical process characteristics are known.
  • the circulation reactor is preferably filled hydraulically, so that the mass flows of the inlet and the outlet are the same during stationary operation.
  • the low-viscosity inlet mixture which generally has a temperature of about 20 ° C.
  • the metered inlet mixture when added, consists primarily of the freshly fed monomers and the volatile and then condensed fractions, in particular monomers, which are returned after leaving the circulation reactor, furthermore from the metered-in polymerization initiator and usual additives, such as added controllers.
  • the metered inlet mixture is advantageously already pre-mixed before mixing devices, such as, in particular, static mixers, rapidly mix the low-viscosity inlet mixture into the higher-viscosity circuit stream after each inlet position. Since narrow molar mass distributions can only be achieved with small temperature and concentration differences in the polymerization reactor, rapid mixing in of the premixed feed at high circulation ratio is of great importance. This keeps the axial temperature and concentration gradients small.
  • REPLACEMENT BLA ⁇ (RULE 26) Preferred mixing devices for the feed are static mixers such as commercially available SMX mixers
  • Suitable monomers for the process according to the invention are methyl methacrylate, which, however, can contain up to 10 and preferably up to 5% by weight of the total amount of monomers another copolymerizable olefinically unsaturated compound as comonomer, and mixtures thereof.
  • Other esters are particularly suitable as such comonomers the methacrylic acid and the acrylic acid with an alcohol having 1 to 8 carbon atoms, maleic anhydride d and preferably styrene.
  • the feed or the metered run-in mixture further contains a polymerization initiator which, according to the process according to the invention, has a batch half-life t ⁇ / 2 b at ch of between 3 and 10 and preferably between 4 and 6 minutes at the polymerization temperature, the polymerization temperature being 135 to 150, preferably 140 is up to 145 ° C.
  • the feed concentration of the polymerization initiator is to be set so that with an average residence time t of the reaction aces in the reactor of 1.3 to 2.5 and preferably 1.5 to 2.0 hours at the reactor outlet or outlet a polymer fraction y p of 0.5 to 0.7, in particular 0.55 to 0.65 and particularly preferably 0.57 to 0.63, is achieved
  • TBPA Butyl peracetate
  • TBPN Butylper-3, 5, 5-tr ⁇ methylhexanoat
  • n E of the feed or feed points per loop can be 1 to 4. Higher numbers generally do not occur in an industrial circulation reactor because of the high pressure loss in the mixing devices or static mixers. Preferably, n ⁇ 1 or 2. If there is more than one feed per circuit loop, it is advantageous to use approximately the same premixed feed volumes Vo0 ⁇ 02 etc. and the Arrange inlet positions so that approximately equal reaction volumes are between them.
  • a sufficient cooling surface A ⁇ must also be present in the circuit reactors for the entire reaction volume V R.
  • the temperature of the coolant should, if possible, not be more than 5 ° C. below the average temperature of the reaction mass (polymerization temperature).
  • the mean effective axial flow velocity W ef . ax be greater than 5 cm / second.
  • An upper limit is given by the pressure loss.
  • advantageous average effective axial flow velocities W eff, a ⁇ are between 7 and 40 cm / second.
  • the circulation flow ⁇ ⁇ which represents the volume flow in m 3 / hour after the last feed of the circulation loop 25 and shortly before the position of the outlet or reactor outlet is set accordingly high.
  • the circulation ratio K R is the quotient of the circulation flow V «measured before the reactor outlet - and the sum of the inflows
  • the circulation ratio K R should be greater than 20, divided by n E , the number of feeds in via the circulation loop. K R is preferably about 10 to 60.
  • the average circulation time t z in the circulation reactor is in particular
  • Particularly suitable circulation reactors are those whose predominant reaction volume consists of at least one, preferably 2 to 6 tube or tube bundle reactors. Allow tubular reactors
  • Suitable circulation reactors are shown schematically in FIGS. 1 to 4 and described in the examples.
  • Mixing devices preferably static mixers (2, 7, 14, or 20 and 21) are arranged directly behind the feed line or feeds into the reaction mixture (1, 6, 13 or 18 and 19) in order to allow the mederviscose to be mixed in quickly To use mixtures in the highly viscous reaction mass in the reactor.
  • the reaction mass then runs through the actual reactors (3, 8, 15, 22), in particular tubes, tube bundles, tubes with cooled static mixers such as SMXL elements from Sulzer (8) (with coolant inflow (11) and coolant outflow ( 12)) or cylindrical tubes with Kenics mixers and double jacket for cooling (15).
  • the circuit reactor of FIG. 4 has 2 feeds with associated mixing devices m of the circuit loop.
  • the circulation flow V ⁇ r (m 3 / hour) is measured directly before the reactor exits or exits (4, 9, 16, 23). It is important that a flow without jerk mixing is effected in the circulation reactor (except in the circulation pump (5, 10, 17, 24)).
  • the reaction mass which leaves the circulation reactor at the reactor outlet or outlet (4, 9, 16, 23), has a polymer mass fraction y p of 0.5 to 0.7 there, as stated, and thus still contains a lot of unreacted monomers.
  • the reaction mass which has escaped can be worked up in a known manner, the volatile fractions, such as the monomers, contained in the mass expediently being recycled in whole or in part after their condensation.
  • One way of working up in snake evaporators and screw evaporators is described in process stages 2 and 3 of DE-A 2724360.
  • the polymers obtained are outstandingly thermoplastic
  • SPARE BLADE (RULE 26) Processable and, due to their uniformity, transparency, brilliance and very good mechanical strength, they are ideal for the production of molded parts with high-quality optical properties such as domelights, lighting fixtures, 5 glazing, lenses, prisms, reflectors or light guides.
  • a tube-and-tube circuit reactor as shown schematically in FIG. 1, was used as the circulation reactor. It has two tube bundles (3), each with 19 tubes, with an inner tube diameter 5 ⁇ of 0.03 m and a height H R of 3 m
  • the circulation reactor has a specific cooling area of 107 m 2 / m 3.
  • the feed or feed mixture contained, in addition to 100 ppm of dodecyl merecaptan as regulator, 97.5% by weight of methyl methacrylate and 2.5% by weight of styrene, the percentages being based on one another refer to the total amount of monomers in the feed.
  • the polymerization initiator was tert.
  • Butyl peracetate (TBPA) is used, which has a batch half-life t ⁇ / 2 ( batch ) of 5.6 minutes at the average polymerization temperature of 145 ° C.
  • the initiator feed concentration I 0 of 9 x 10 ⁇ 4 kmol / m 3 has been set so that, for a mean residence time of the reaction mass 5 of 1.5 hours, the polymer weight fraction y t p at the reactor outlet at about 0.60
  • a circulation flow V K ⁇ of 3 m 3 / hour was set, which corresponds to an average effective axial flow velocity ⁇ w eff ax ⁇ n in the individual tubes of the tubular bundle from the circulation reactor of 6.2 cm / second.
  • the circulation ratio K was 45 and the average circulation time t z 1.5 minutes
  • the circuit reactor was able to operate in long-term operation without any significant 5 deposits. Reactor walls are operated stably.
  • the resulting degassed polymer had a mass-average degree of polymerization P w of 1230.
  • the molecular nonuniformity of the product U n P w / P n - 1, determined by gel permeation chromatography, was 1.1 0
  • Example 2 It was polymerized in the same tube bundle cycle reactor as in Example 1 and in the same way, but tert-butylper-3, 5,5-tr methylhexanoate (TBPN) was used as the polymerization initiator, which was one at the average polymerization temperature in the cycle reactor of 145 ° C. Batch half-life t ⁇ / 2 ( ba tc h ) of 4.8 minutes Has.
  • the initiator feed concentration I 0 was 8 ⁇ 10 -4 kmol / m 3 and was determined so that with a mean residence time of the reaction mass of 1.5 hours the polymer mass fraction is about 0.60.
  • the flow parameters corresponded to those of Example 1:
  • the reactor could be operated in long-term operation without any significant build-up on the reactor walls.
  • the resulting polymer had a mass average degree of polymerization P w of 1250 and a non-uniformity of 1.1.
  • a circulation reactor as shown schematically in FIG. 2 was used as the circulation reactor. It contained tubes with cooled static mixers (8) Sulzer-SMXL elements with an inner diameter of 0.15 m.
  • the feed or feed mixture corresponded to that of Example 1, but tert-butylper-3,5,5-trimethylhexanoate (TBPN) was used as the polymerization initiator, the batch half-life and initiator feed concentration of which are given in Example 2.
  • a circulation flow ⁇ r of 4 m 3 / hour was set. This corresponds to an average effective axial flow velocity W eff # ax of 7.1 cm / second.
  • the circulation ratio K R was 60 and the average circulation time t z 1 minute.
  • the cycle reactor could be operated stably in long-term operation. Wall coverings were not found.
  • the resulting degassed polymer had a mass average degree of polymerization P w of 1220 and a molecular non-uniformity of 1.1.
  • a Kenics cycle reactor as shown schematically in FIG. 3 was used as the cycle reactor. It contained cylindrical jacketed pipes (15) with non-cooled static mixers (Kenics mixers) of a length L R of 12 m and an inner diameter dj. of 0.1 m. The feed or feed mixture corresponded to that of Example 1, and the polymerization initiator given in Example 1 with the initiator feed concentration I 0 given there was also used.
  • a circulation flow V R ⁇ of 2 m 3 / hour was set. This corresponds to an average effective axial flow velocity W eff , a ⁇ of 7.1 cm / second.
  • the circulation ratio K R was 30, the average circulation time t z 3 minutes.
  • the cycle reactor worked trouble-free in long-term operation.
  • the resulting product had one mass average degree of polymerization P w of 1210 and a non-uniformity value of 1.1.
  • Example 2 The procedure was as in Example 1, but tert-butyl peroxide (TBPO) was used as the polymerization initiator, which has a batch half-life t ⁇ 2 ( batch ) of 1.24 hours at the average polymerization temperature of 145 ° C.
  • the initiator feed concentration I D of 1.7 ⁇ 10 -3 kmol / m 3 was determined in such a way that with a mean residence time t of the reaction mass of 1.5 hours at the reactor outlet, a polymer mass fraction of about 0.60 is achieved.
  • a circulation flow V K ⁇ of 3 3 / hour was set.
  • the average effective flow velocity W ef, ax in the tubes of the tube bundles was 6.2 cm / second, the circulation ratio K R was 45 and the average circulation time t z 1.5 minutes.
  • the operation of the tube bundle cycle reactor was characterized by an unstable behavior. The desired stationary operating point could not be set. After the reactor was shut down, the formation of a substantial wall covering was observed.
  • Example 2 The procedure was as in Example 2, polymerization was carried out in a tube bundle cycle reactor as shown in FIG. 1 and, as in Example 2, as the polymerization initiator. Butylper-3, 5, 5-trimethylhexanoate (TBPN) used with the feed concentration I 0 given in Example 2.
  • a circulation flow V K ⁇ of 1.5 m 3 / hour was set. This corresponds to an average effective flow velocity W eff; a ⁇ in the tubes of the tube bundle of 3.1 cm / second.
  • the circulation ratio K R was 30 and the average circulation time t z 3 minutes. After a long period of operation, the cycle reactor tended to vibrate. After the reactor was switched off, wall coverings were found in the reactor.
  • Example 3 The procedure was as in Example 3, a circulation reactor according to FIG. 2 was used, but tert-butyl peroxide (TBPO) with the initiator feed concentration I 0 given in Comparative Experiment 1 was used as the polymerization initiator as in Comparative Experiment 1.
  • a circulation flow V K ⁇ of 4 m 3 / hour was set. This corresponds to an average effective axial flow velocity W eff , ax of 7.1 cm / second.
  • the circulation ratio K was 60 and the average circulation time t z 1 minute.
  • the circulation reactor could only be operated for a short time. A steady state in the reactor could not be achieved. After the reactor was turned off, heavy wall coverings were found in it.
  • Example 3 The procedure was as in Example 3, including a Sulzer cycle reactor according to FIG. 2 and, as in Example 3, as a polymerization mediator. Butylper-3, 5, 5-tr ⁇ methylhexanoat (TBPN) with the same initiator feed concentration I 0 used. A circulation flow of 2 3 / hour was set. This corresponds to an average effective axial flow rate W eff, ax of 3.4 cm / second. The circulation ratio K R was 45 and the average circulation time t z 2 minutes. After a relatively short operating time of the cycle reactor, temperature fluctuations occurred. After the reactor was switched off, wall coverings were present on the cooled mixing elements.
  • Butylper-3, 5, 5-tr ⁇ methylhexanoat (TBPN) with the same initiator feed concentration I 0 used.
  • a circulation flow of 2 3 / hour was set. This corresponds to an average effective axial flow rate W eff, ax of 3.4 cm / second.
  • the circulation ratio K R was 45 and the average circulation time t z 2 minutes
  • Feed mixture approx. 97.5% by weight methyl methacrylate, based on total monomers approx. 2.5% by weight styrene, based on total monomers approx. 20 pp dodecyl mercaptan, based on monomers
  • Feed mixture approx. 97.5% by weight methyl methacrylate, based on total monomers approx. 2.5% by weight styrene, based on total monomers approx. 20 pp dodecyl mercaptan, based on monomers 8 ⁇ 10 "4 kmol / m 3 tert. Butyl 3, 5, 5, trimethylhexanoate
  • Circulation time t 6.2 minutes

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Polymerisation Methods In General (AREA)
  • Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)

Abstract

L'invention concerne des polymères de méthylméthacrylate présentant une hétérogénéité de 1,0 à 1,2, obtenus en continu par polymérisation en substance à partir de monomères constitués à au moins 90 % en poids de méthylméthacrylate, dans un réacteur à recirculation comportant de préférence au moins un réacteur tubulaire ou à faisceaux tubulaires, et sans formation gênante de dépôts sur les parois. La préparation desdits polymères est effectuée de sorte que la température de polymérisation s'élève à 135-150 °C, le rapport de recirculation est supérieur à 20, divisé par le nombre d'alimentations par boucle de recirculation, la vitesse moyenne d'écoulement axial effective est supérieure à 5 cm/s, on utilise un initiateur de polymérisation présentant une demi-vie dans le lot comprise entre 3 et 10 min, et la concentration d'afflux de l'initiateur est ajustée de façon à obtenir, pour un temps de séjour moyen de 1,3 à 2,5 heures à la sortie du réacteur une rupture du polymère de 0,50 à 0,70. A partir des polymères homogènes, on peut obtenir des corps moulés présentant de très bonnes propriétés optiques.
EP97943868A 1996-09-18 1997-09-18 Procede de preparation de polymeres de methylmethacrylate dans un reacteur a recirculation Ceased EP0927197A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19638094A DE19638094A1 (de) 1996-09-18 1996-09-18 Verfahren zur Herstellung von Methylmethacrylat-Polymeren in einem Kreislaufreaktor
DE19638094 1996-09-18
PCT/EP1997/005125 WO1998012229A1 (fr) 1996-09-18 1997-09-18 Procede de preparation de polymeres de methylmethacrylate dans un reacteur a recirculation

Publications (1)

Publication Number Publication Date
EP0927197A1 true EP0927197A1 (fr) 1999-07-07

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EP97943868A Ceased EP0927197A1 (fr) 1996-09-18 1997-09-18 Procede de preparation de polymeres de methylmethacrylate dans un reacteur a recirculation

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EP (1) EP0927197A1 (fr)
DE (1) DE19638094A1 (fr)
WO (1) WO1998012229A1 (fr)

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DE19638094A1 (de) 1998-03-19
WO1998012229A1 (fr) 1998-03-26

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