Description

The invention relates to a process for the polymerisation of vinyl-containing monomers such as, for example, vinyl halides, in a reaction mixture, in which process less waste is generated.

The polymerisation of vinyl-containing monomers, such as , for example, vinyl chloride to polyvinyl chloride (PVC) , is usually carried out discontinuously, using the suspension process, in fully demineralised water, as described, for example, in the review on Technical progress for PVC production, Progress in Polymer Science 27 (2002 ) , ELSEVIER, page 2070/2071 and Harold Sarvetnick, Polyvinyl Chloride, page 42/43 , van Nostrand Reinold Company, New York 1969 and Encyclopedia of PVC, VoI 1 page 74 , Nass/Heiberger, Marcel Dekker, New York 1986 and http : / /www. solvin . com/production/ producti .htm. The suspension thereby produced typically has a solids content of from 25 to 40 % . Usually the PVC suspension is, after degassing, dewatered in a decanter, whereupon the residual moisture content of the PVC product drops to from 10 to

30 % . The decanted reaction mixture typically has a solids content of from 50 to 250 mg/1 and is usually, after preliminary separation, sent to a biological purification plant in the form of waste water . The amount of waste water is , depending on the type of PVC produced, between 2.3 and 3.0 m ³ per tonne of PVC .

It is well known in the technical field that, in the polymerisation of vinyl-containing monomers such as , for example , vinyl chloride, using the suspension process , the product quality of the PVC produced is adversely affected by impurities . For that reason, only high-purity solvents are used for the reaction mixture in the discontinuous polymerisation processes customary today; for example, fresh fully demineralised water is used as solvent in the polymerisation of vinyl chloride to PVC . In addition to the costs associated with the provision of fresh high-purity solvents such as , for example, fresh fully demineralised water, the costs then associated with the environmentally acceptable disposal of the used solvent or waste water also have a disadvantageous effect on the economy of the process .

It is accordingly a problem of the present invention to make available a process for the polymerisation of vinyl- containing monomers by means of which process the disadvantages of the prior art are avoided. It is also a problem of the invention to provide an apparatus for carrying out a polymerisation process of such a kind.

The problem is solved by the subject-matter of the independent and dependent claims and of the description in conjunction with the Figures . The invention makes it possible to overcome the above-mentioned disadvantages of the prior art .

The invention accordingly relates to a polymerisation process in which vinyl-containing monomers , especially monomeric vinyl halides, are polymerised in a reaction mixture, at least one polymerisation product is separated

off from the reaction mixture, and the reaction mixture is then purified and used again . As a result of the process according to the invention, compared to the prior art, less fresh high-purity solvent, especially fresh fully demineralised water, is required per tonne of polymer product produced, and consequently less waste and/or waste water is generated and as a result operation is especially economical and environmentally friendly .

Any known process for the polymerisation of vinyl- containing monomers in a reaction mixture can be used therein. In accordance with the invention, the expression "polymerisation" includes both homopolymerisation of monomers and also copolymerisation of two or more different monomers .

In accordance with the invention preference is given to separating off exactly one polymerisation product, which may also be a polymer mixture having a statistical distribution, such as , for example, PVC .

Preferably, the reaction mixture comprises , in addition to the monomers used and at least one solvent and also the products formed in the course of polymerisation, further constituents and additives, preferably initiators, antifoams , neutralising agents , suspension agents , antioxidants etc .. In addition, the invention relates to an apparatus which allows the process according to the invention to be carried out .

The polymerisation of vinyl-containing monomers , vinyl halides and especially vinyl chloride is known per se. It will furthermore be known to the skilled person that the

recovered water produced in customary polymerisation processes cannot, because of the micropolymers present therein, be used again in a subsequent reaction, because those micropolymers act as polymerisation seeds and irreparably impair the quality of the polymerisation product .

However, it has now been found, surprisingly, that by means of the process according to the invention products are produced which have characteristics that are as good as those of products produced using customary processes whilst the amount of used solvent waste that is generated is substantially reduced in comparison with the customary production process . As a result it is possible both to reduce advantageously the costs for the provision of fresh high-purity solvent and also the costs for the environmentally acceptable disposal of the used solvent waste generated and also to produce the polymer product in especially economical manner . Preferably, all the purified reaction mixture is used again, although use of part thereof in combination with fresh solvent is also possible .

It has also been found, surprisingly, that, using the process of the invention, repeated production of polymerisation product of a consistent quality is possible, in which case as a result of the recovery and re-use of the solvent-comprising reaction mixture the costs can be reduced for especially economical production of polymer products .

Furthermore, the consistent quality of the polymerisation products can be especially well controlled by the present invention . Preferably, vinyl chloride is used as monomeric

vinyl halide, in which case the polymer produced can consist of comprise, for example, 50 % to 100 % polyvinyl chloride . Also preferably, identical or different monomer units can be polymerised in accordance with the invention to form a homo- , co- and/or ter-polymer etc .. Polymer products produced by the process according to the invention advantageously contain no impurities . As a result of selection of the filter medium having a separation limit of 10 - 1000 kDalton, very fine polymer particles are filtered out of the polymerisation mixture before it is returned to the process . It is also possible in the method according to the invention for residual monomers to be returned, at least partially, to the polymerisation process so that the yield is increased, and degassing needs less outlay in its performance or can be dispensed with entirely . As a result , the disposal of especially halogen-containing vinyl monomers is dispensed with partially or entirely .

In accordance with the invention, the polymerisation can be carried out in the reaction mixture in solution or in dispersion, that is to say starting materials and/or products of the reaction can be present, independently of one another, dissolved in the solvent and/or in the form of solids or liquids dispersed therein. Preference is given to carrying out the polymerisation reaction in the process according to the invention in an aqueous reaction mixture, and special preference is given to carrying out the polymerisation in the process according to the invention in an aqueous suspension . Special preference is given to using the process according to the invention for the polymerisation of vinyl chloride to form PVC in aqueous suspension. In that case, the aqueous reaction mixture can, especially advantageously, be purified and used again

instead of fully demineralised water, without having to dispose of large amounts of waste water . Instead of fully demineralised water, the purified reaction mixture can be used again, entirely or partially, for the polymerisation of vinyl chloride .

The process of the invention can be carried out, for example, under a pressure that is higher than normal pressure, preferably under a pressure of from 0.3 to 2 MPa . Preferably, the polymerisation is carried out discontinuously .

Preferably, the reaction mixture is degassed after polymerisation and before separating off the at least one polymerisation product . The degassing can be carried out in any known manner; preferably, the reaction mixture is degassed using a distillation column. As a result of the degassing of the reaction mixture, unreacted starting materials (monomers) can be recovered, which can be returned to the process (to the reactor) .

Preferably, the at least one polymerisation product is separated off by centrifuging the reaction mixture . In that case, any known centrifugation method can be used. Preferably, a solid bowl centrifuge or a screen centrifuge is used.

Preferably, the reaction mixture is purified by filtration, preferably by microfiltration, after separating off the at least one reaction product . Filtration or microfiltration as understood by the invention refers to filter media having a separation limit of 10 - 1000 kDalton and filtrate yields of > 99 % .

In accordance with the invention, a microfiltration module can be a module conventional in the technical field, comprising, for example, filter elements in the form of tubes , plates or other constructional forms . As filter material there can be used, for example, ceramic , sintered metal or metal mesh, preferably polymer-coated filter elements . In addition, in order to increase the filtration performance, any conventional filtration aids can be used such as , for example, cellulose or diatomaceous earth.

Plastic materials such as , for example, PVC, are likewise suitable as filtration aids .

It has been found, surprisingly, that a reaction mixture, for example the aqueous reaction mixture obtained on centrifuging an aqueous PVC suspension, which has been purified by microfiltration by way of a microfiltration module can be used again for the polymerisation of vinyl chloride without the characteristics of the product being impaired.

Preferably, in the process according to the invention the solids separated off by filtration or microfiltration can be returned to the reaction mixture before separating off the at least one polymerisation product . Surprisingly, it has been found, in particular, that PVC solid particles separated off in the process according to the invention can be introduced back into the process, as a result of which the amount of solid waste is reduced.

The apparatus provided for carrying out the process according to the invention is a reaction vessel (reactor) (1) which is connected by way of a fluid

connection to an apparatus (5 ) for separating off a polymerisation product from the reaction mixture, the apparatus ( 5 ) for separating off a polymerisation product from the reaction mixture being connected by way of a further fluid connection to an apparatus (7 ) for purifying the reaction mixture, and the apparatus (7 ) for purifying the reaction mixture being connected by way of a further fluid connection to the reaction vessel ( 1) . The apparatus ( 5 ) for separating off a polymerisation product is preferably a centrifuge . The apparatus (7 ) for purifying the reaction mixture is preferably a filtration apparatus , especially a microfiltration apparatus . Special preference is given to the microfiltration apparatus comprising filter elements in the form of plates or tubes .

The present invention overcomes the disadvantages of the prior art , especially in that, in comparison to the prior art, less fresh high-purity solvent, especially fresh fully demineralised water, is required per tonne of polymer product produced, less waste and/or waste water is consequently generated, and the solution according to the invention is, as a result, especially economical and environmentally friendly without the characteristics of the product being impaired. Also, the consistent quality of the polymerisation products can be especially well controlled by means of the present invention.

Description of the Figures

The invention is explained hereinbelow with reference to Figures showing preferred embodiments of the apparatus according to the invention . Components having the same

functions are referred to in the Figures by the same reference numerals .

Figure 1 shows a flow diagram of an embodiment of the apparatus according to the invention . After polymerisation, a reaction mixture 2 produced in the polymerisation reactor 1 is passed on to degassing 3. The degassed reaction mixture 4 is mechanically separated from a polymerisation product in a centrifuge 5. The reaction mixture 6 separated off is freed of solids 8 in a plate filter 7. The purified reaction mixture 9 is returned to the polymerisation reactor 1.

Figure 2 shows a flow diagram of a further embodiment of the apparatus according to the invention . After polymerisation, a reaction mixture 2 produced in the polymerisation reactor 1 is passed on to degassing 3. The degassed reaction mixture 4 is mechanically separated from a polymerisation product in a centrifuge 5. The reaction mixture 6 separated off is freed of solids 8 in a tube module filter 7. The purified reaction mixture 9 is returned to the polymerisation reactor 1.

Figure 3 shows a flow diagram of a further embodiment of the apparatus according to the invention. After polymerisation, a reaction mixture 2 produced in the polymerisation reactor 1 is passed on to degassing 3. The degassed reaction mixture 4 is mechanically separated from a polymerisation product in a centrifuge 5. The reaction mixture 6 separated off is freed of solids 8 in a plate filter 7. The purified reaction mixture 9 is returned to the polymerisation reactor 1. The solids 8 separated off

are passed on to the centrifuge 5 together with the degassed suspension 4.

Figure 4 shows a flow diagram of a conventional apparatus in which a reaction mixture 2 produced in a polymerisation reactor 1 using fresh fully demineralised water 12 is , after polymerisation, passed on to degassing 3. The degassed reaction mixture 4 is mechanically dewatered in a centrifuge 5 and a polymerisation product is separated off . The waste water 6 separated off is passed on to waste water treatment 11.

Examples

Comparison Example 1

S-PVC, K-value 70

Polymerisation of vinyl chloride was carried out at a temperature of 53 ⁰ C using the conventional apparatus outlined in Figure 4. After degassing, the suspension produced was mechanically dewatered in a centrifuge and the polymerisation product was separated off . The powder characteristics of the polymerisation product are collated in Table 1.

Table 1 ; Powder characteristics of S-PVC, K-value 70

S-PVC, K-value 70 Unit Comparison, using fully demineralised water

K-value [-] 69.9

Bulk density [g/i] 472

Porosity C%3 30.6

Average particle diameter [μm] 127

Sieve residue >63 [%] 99.7

Sieve residue >125 [%] 65.9

Sieve residue >250 [% ^] 0.4

Measure of the width of [-] 2.33 particle distribution

Comparison Example 2 S-PVC , K-value 68

Polymerisation of vinyl chloride was carried out at a temperature of 53 ⁰ C using the conventional apparatus outlined in Figure 4. After degassing, the suspension produced was mechanically dewatered in a centrifuge and the polymerisation product was separated off . The powder characteristics of the polymerisation product are collated in Table 2.

Table 2 : Powder characteristics of S-PVC, K-value 68

S-PVC, K-value 68 Unit Comparison, using fully demineralised water

K-value [ - ] 66.1

Bulk density [g/i] 552

Porosity [% ] 21.6

Average particle diameter [μm] 179.8

Sieve residue >63 [%] 100

Sieve residue >250 [% ] 13.5

Sieve residue >355 [%] 0.5

Measure of the breadth of [- ] 2.22 particle distribution

Example 1 S-PVC, K-value 70

Polymerisation of vinyl chloride was carried out at a temperature of 53 ⁰ C in an aqueous reaction mixture in a reactor, using the process of the invention outlined in Figure 1. After degassing, the reaction mixture produced was mechanically dewatered in a centrifuge and a polymerisation product was separated off . The reaction mixture emerging from the centrifuge was filtered over a conventional plate module . The solid filtered off was disposed of , and the filtered reaction mixture was returned to the reactor and used again for further polymerisation . The procedure was repeated several times for this PVC type . The quality of the filtered reaction mixture (Table 3 ) and the product quality (Table 4 ) changed only very slightly as a result of using the reaction mixture several times ; in

particular, the powder characteristics of the product were not subj ect to any significant change .

Table 3 : Test data of filtered reaction mixture

Table 4 : Powder characteristics of S-PVC, K-value 70

Example 2

S-PVC, K-value 68

Polymerisation of vinyl chloride was carried out at a temperature of 53 ⁰ C in an aqueous reaction mixture in a reactor, using the process of the invention outlined in Figure 1. After degassing, the reaction mixture produced was mechanically dewatered in a centrifuge and a polymerisation product was separated off . The reaction mixture emerging from the centrifuge was filtered over a conventional plate module . The solid filtered off was disposed of , and the filtered reaction mixture was returned to the reactor and used again for further polymerisation. The procedure was repeated several times for this PVC type . The quality of the filtered reaction mixture (Table 5 ) and the product quality (Table 6 ) changed only very slightly as a result of using the reaction mixture several times; in particular, the powder characteristics of the product were not subj ect to any significant change .

Table 5 : Test data of filtered reaction mixture

Table 6 : Powder characteristics of S-PVC, K-value 68

S-PVC , K-value 68 Unit Batch 1 Batch 2 Batch 3

K-value [ -] 66.3 66.1 66.7

Bulk density [g/i] 552 549 548

Porosity [%] 21.7 21.6 21.3

Average particle diameter [μm] 179.8 178.3 179.6

Sieve residue >63 [%] 100 100 100

Sieve residue >250 [%] 13.5 15.4 17.3

Sieve residue >355 [%] 0.5 0.3 0.2

Measure of the breadth of [ -] 2.22 2.18 2.26 particle distribution

Example 3

S-PVC, K-value 70

Polymerisation of vinyl chloride was carried out at a temperature of 53 ⁰ C in an aqueous reaction mixture in a reactor, using the process of the invention outlined in Figure 2. After degassing, the reaction mixture produced was mechanically dewatered in a centrifuge and a polymerisation product was separated off . The reaction mixture emerging from the centrifuge was filtered over a conventional tube module . The solid filtered off was disposed of , and the filtered reaction mixture was returned to the reactor and used again for further polymerisation . The procedure was repeated several times for this PVC type . The quality of the filtered reaction mixture (Table 7 ) and the product quality (Table 8) changed only very slightly as a result of using the reaction mixture several times ; in

particular, the powder characteristics of the product were not subj ect to any significant change .

Table 7 : Test data of filtered waste water

Table 8 ; Powder characteristics of S-PVC _/ K-value 70

Example 4

S-PVC, K-value 70

Polymerisation of vinyl chloride was carried out at a temperature of 53 ⁰ C in an aqueous reaction mixture in a reactor, using the process of the invention outlined in Figure 3. After degassing, the reaction mixture produced was mechanically dewatered in a centrifuge and a polymerisation product was separated off . The reaction mixture emerging from the centrifuge was filtered over a conventional plate module . The solid filtered off was disposed of, and the filtered reaction mixture was returned to the reactor and used again for further polymerisation . The procedure was repeated several times for this PVC type . The quality of the filtered reaction mixture (Table 9 ) and the product quality (Table 10) changed only very slightly as a result of using the reaction mixture several times ; in particular, the powder characteristics of the product were not subj ect to any significant change .

Table 9 s Test data of filtered waste water

Table 10 ; Powder characteristics of S-PVC ₁ K-value 70

S-PVC, K-value 70 Unit Batch 1 Batch 2 Batch 3

K-value [-] 69.7 69.8 69.5

Bulk density [g/i] 475 472 471

Porosity [%] 32.8 33.4 33.1

Average particle diameter [μm] 122 124 125.2

Sieve residue >63 [%] 99.1 99.3 99.2

Sieve residue >125 [%] 64.9 64.6 65.2

Sieve residue >250 [%] 0.2 0 , 3 0.2

Measure of the breadth of [-] 2.31 2.35 2.29 particle distribution

From the Examples and Comparison Examples it can be seen that, using the process according to the invention, products of consistent quality can be produced without fresh fully demineralised water being required for each batch, as a result of which the production of PVC can be carried out with less waste water and, as a result, in especially economical and environmentally friendly manner without the characteristics of the product being impaired.