Method of producing synthetic latex. RU patent 2507218.

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing synthetic latex from rubber. The method comprises steps of: (a) emulsifying a binding substance containing rubber, which is dissolved in a suitable organic solvent, together with an aqueous surfactant solution to form an oil-in-water emulsion; (b) step-by-step reduction of content of solvent in the oil-in-water emulsion in two or more steps, resulting in formation of synthetic latex. Also described is a reactor with continuous mixing for removing the organic solvent from the oil-in-water emulsion, which contains rubber dissolved in the organic solvent.

EFFECT: reducing the amount of residual solvent to very low levels with high efficiency of the process.

19 cl, 2 dwg, 1 tbl, 11 ex

The technical field

The present invention relates to a method for producing synthetic latex, including emulsion of rubber in the water. More specifically, the invention involves obtaining latex on the basis of conjugated diene polymer, more specifically, latex on the basis of isoprene rubber.

Preconditions of creation of the invention

Latexes on the basis of both natural and synthetic rubbers are emulsion of rubber in the water. Emulsions stabilized with the help of protein surface-active agents. The average diameter of particles of rubber in the average fluctuates in the range of 0.5 to 2.0 mm thick. It can be up to 0.1 micron for some synthetic latexes and tends to be about 1 micron to natural rubber latex. The term “latex” is applied to synthetic and natural products, and is derived from the Botanical names of the lacteal fluid that is made from rubber and which is the source of natural rubber. “Serum is applied to the aquatic environment.

Method for producing emulsions rubber in water is known for many years. For example, in the US 2595797 disclosed method with the following stages:

1. Getting the solution polymer in insoluble in water flying organic solvent in sufficient concentration to emulsification

2. Introduction of a solution under pressure in water containing surface-active agent (for example, a complex ester sodium salt acid)

3. Adding (for example, oil) and stir the mixture until it is not formed emulsion

4. Removing the solvent through boiling up (still avoiding excessive foaming)

5. Thickening the content of dry substances through the provision of emulsion settle within 24 hours and remove serum (containing less than 2% of dry substance).

In the US 2799662 describes a similar process. The method consists of several stages, which include dissolution of dry polymer material (e.g. rubber) in selected a suitable solvent, dispersion thus obtained polymer solution in a carefully selected and controlled system of water and emulsifier and at the end of the solvent with the receipt of the polymer dispersion. According to this link in obtaining water system emulsifier in highly desirable that there were two emulsifier, one type of which is soluble in hydrocarbons (for example, petroleum sulfonates alkali metals, containing 20 to 21 carbon atoms located in the alkyl-aryl structure), and other water-soluble type (for example, derived alkali metals sulfates higher alcohols). Emulsified mixture of polymer-solvent and water mixture emulsifier committed in the context of preventing the boiling solvent.

The problem of stability of the emulsion when you remove the solvent is addressed in the US 2871137, which provides a way to obtain emulsifiers based on hydrocarbon polymers, which are .

The method of obtaining stable emulsions or containing polymer resin materials is further described in US 2947715. This is accomplished by dissolving rubber or resin in a suitable solvent, adding coagulator to a polymer solution in the course of emulsification and defend the finished latex to remove solvent, solvent removal and then again assertion does not contain solvent latex.

In the US 2955094 as emulsifiers when receiving latex emulsion of hydrocarbon polymers used phosphoric acid and organic sulfate salt. As indicated in this reference, experience has shown that the latexes are relatively unstable and have a tendency to coagulate under the influence of mechanical stress. Mechanical instability can cause a simple motion, mixers, mixing colloid. The increase of expenditures on maintenance of the equipment covered by rubber and, in addition, lost a significant amount of rubber. Another type of instability, occurring in connection with polymer latexes, is that they produce oil and create during the stage of evaporation of the solvent.

US 3250737 offers a concentrated latexes of synthetic elastomers of their organic solutions manner that is both rapid and efficient and economic. This is done by mixing synthetic elastomer solution in organic solvent, water and emulsifier, homogenization of a mixture of at least until finished emulsion is stable, removal of organic solvent at elevated temperatures and pressures below the conditions under which water begins to boil, centrifugation finished diluted aqueous latex, recovery and recycling of water serum from this stage of centrifugation and recovery concentrated latex. This reference focuses on the stages of boiling and centrifugation, not essential, as is made hydrocarbon solution.

To give an idea of the whole process, as described in the prior art, reference is made to the process in Chapter 9 PEP Report № 82 from December 1972 Stanford Research Institute. Thus, the solution of polyisoprene in served in the tank for pre-mixing, where it is mixed with a solution of surface-active substance (usually repeated product serum) from the store serum. Mixture is fed into the cycle of emulsification, in which the ratio of re-product to a fresh portion is approximately 2/1. Emulsifier is a high-speed 3500 rpm) centrifugal pump. Emulsion goes into the tank for aging, which emulsion incubated for 3 hours, give the opportunity to any “cream” (emulsion with non-standard particles rise to the top and recycling. Approximately 1% emulsion thus recycle to ensure full emulsification any small amounts previously not fully emulsified. If any part of emulsified binding substance is in the form of non-standard particles when the solvent boils or removed from this part, ready polymer cannot remain in a colloidal suspension, and will be deposited and contaminate equipment. From the reservoir for aging emulsion passes in a heater where a substantial part of the solvent (but only an insignificant part of water) evaporates gaseous bubbles, causing the formation of foam, reminiscent of whipped cream. Foam is held in a temporary storage tank to allow the solvent to reach its equilibrium concentration relative to the polymer on all pins. Then the foam is cooled down to 110 degrees F (43,33 OC) at approximately 10 psi, causing condensation of the solvent and the destruction of the foam. Condensed solvent forms a liquid phase from phase aqueous emulsion. Mixture goes through coagulator built with steel wool in the separator. Separated solvent moves in the surge tank for solvent. Emulsion is centrifuged and concentrated in a centrifuge, where a number of serum is separated and recycled into a storage tank serum. Because the polymer particles in concentrated emulsion still contain solvent emulsifying passed through the second stage of foam destruction and separation. Dedicated to the second stage of the solvent moves in the surge tank for solvent. Phase emulsion second stage heated to 180 degrees Fahrenheit (82,2 degrees device for instant evaporation of the liquid to evaporate remaining solvent reservoir evaporation. This solvent is condensed and stored in egalitarian reservoir solvent. Also from the reservoir to the evaporation of some water evaporates and condenses, separated and recycled into the tank solution of surface-active substances. Latex for evaporation from the reservoir contains approximately 24% of solid rubber substances. It should be cooled up to 110 degrees F in the cooling device for emulsion concentrate to 64% in the centrifuge and finally collect and store in a vessel for storage of latex product. Serum spin-on the stage of concentration, recycle the vessel for storage of serum.

Removing the solvent from the emulsion, which includes synthetic elastomer, 50-60% of the mass. solvent, water and emulsifying agent (surfactant), would consist of “bleaching”, meaning relatively static periods of storage in the conditions, in accordance with the solvent gradually evaporates. However, in most common uses (for example, surgical gloves and condoms) is unacceptable presence of residual solvent. Thus, removing the solvent, as a rule, includes the operation unaffected by the distillation or operation foaming with the subsequent phase solvent separation from dilute latex. These processes may lead to a reduction of solvent equal to 150 parts per million or less, after the removal (calculated on a diluted aqueous emulsion of rubber; solvent content increases with the concentration of diluted with water emulsion). Removing the solvent in the processes of the prior art, however, is not without problem.

Each of these operations, as a rule, are well understood and widely disclosed in the technique. However, this does not mean that this stage, requiring removal of the solvent from the polyphase system without disrupting the stability of the emulsion is not a difficult stage. In fact, this stage it is impossible to compare with the removal of solvent from a simple two-component system (water/solvent). More precisely, giving the presence of a material with a high molecular weight, surface-active substances, low boiling hydrocarbon solvents etc., this stage is often leads to a significant loss of latex material due to coagulation of particles emulsified rubber and contamination of the equipment. The reason is that the solvent is removed in the multi-stage process with a relatively equal stages of reduction of solvent. Other problems encountered at this stage is reduced bandwidth and/or increased consumption of energy for the reduction of solvent to the required low levels. An additional problem is the residual level of the controlling foaming agents in the final product, which - together with the residual solvent content should be as low as possible.

Therefore, the aim of the present invention is to provide an improved method of obtaining synthetic latex, in which the loss of material and pollution equipment in operation solvent removal undertaken in two or more stages, significantly reduced the way, which is more efficient in terms of capacity and energy consumption.

Disclosure of the invention

Accordingly, the invention provides a method of obtaining synthetic latex, including the stage:

(a) emulsification binder containing rubber, dissolved in a suitable organic solvent, together with an aqueous solution of surface-active substances, thus forming oil in water emulsion;

(b) the gradual decrease of the solvent content of the emulsion oil in water in two or more stages, leading to synthetic latex, characterized in that the stage 1 stage (b) part of the solvent is removed by means of mixture with a part of synthetic latex, heated to a temperature higher than the boiling point of the solvent-emulsion and giving the opportunity for the solvent to evaporate. In addition, the invention provides a reactor with continuous mixing (1) for the removal of the organic the solvent from the emulsion oil in water containing rubber, dissolved in organic solvent, and emulsified with an aqueous solution of surface-active substance with the formation of synthetic latex with a low content of organic solvent, the reactor is equipped with a mixer (2), the charging hole (3), the output vent (for solvent and water) (4) and the outlet to the final product (5)where the inlet (3) and outlet of the final product (5) are part of the circuit re-boiling (6) for part of the product is an aqueous emulsion in which the path of re-boiling (6) in addition, the includes output discharge outlet (7), optional inlet for control agent flushing (7), pump (8), the warming tool (for example, heat exchanger) (10), inlet for emulsion oil in water (11) and optional entry hole for steam (12).

Scheme I figure 1 is a schematic image of comparative procedures to reduce the content of solvent method for producing synthetic latex. Reactor (1)applies, is continuously reactor in the conditions of a vapor state, equipped with a mixer (2), the charging hole (3), the output vent (4) and the outlet to the final product (5). In addition, the reactor has inlet (12) for steam and inlets (8) and (11), is connected directly to the reactor. Ventilation (4) provides for gaseous products consisting of solvent and water vapor. Figure 1 shows a jacketed reactors (which shirt heated water or oil; whereas the contents of the vessel additionally heated by steam).

Scheme II figure 2 is a schematic depiction of the reactor, which can be used in the method of the present invention. In this device, the application of steam is optional. Hydrocarbon solvent evaporates (boils) through the contact portion of the emulsion with a part of the product flow, which is heated to a temperature higher than the boiling point of the solvent in the heating device, for example, heat exchanger (10). Therefore, the heat exchanger is located preferably upstream connection space, uniting the recirculated product (synthetic latex with low solvent content) and emulsion oil in water. In figure 2 you can also use insulating reactor. It should also assess that the reactor can be equipped with more than one circuit re-boiling.

In the conditions of a vapor state is maintained at approximately the same level during the operation. This lower area includes 15 to 25%, preferably approximately 20% of the height of the reactor. Gas cap includes upper part of the reactor and includes 20 to 10%, preferably approximately 20% of the height of the reactor. If it is less than 10%, then there is a risk Hobbies foam in output vent (4). If it is greater, then the vessel obviously does not function at optimal conditions. The intermediate zone, which therefore closes approximately 45 to 75% of the height of the reactor, filled with foam generated during the process of removal of solvent. In equilibrium (steady state) reactor operates at approximately essentially constant temperature and close to atmospheric pressure.

Method (means) of realization of the invention

The method of the present invention of binding substance is formed by dissolving rubber in a suitable petroleum solvent. Rubber, which is used for the education of synthetic latex can be any polymer, usually obtained by polymerization in the solution, a well-known technique. It includes, for example, polyisobutylene and its copolymers, polyvinyl chloride compounds such as esters of acrylic and methacrylic acid and simple polyvinyl chloride esters and derivatives of cellulose, copolymers of styrene and conjugated diene (dienes) and or Acrylonitrile (co)polymers . Auxiliary class of polymers are copolymers obtained from ethylene and one other that contains up to 8 carbon atoms, such as elastomer a copolymer of ethylene and propylene, ethylene and butane-1 and similar. Another class polymers are obtained from ethylene, propylene and diene, such as 1,5-, and the like.

Of special interest are (co)polymers of styrene and conjugated diene (dienes, which may be statistical polymers and block-copolymers (containing blocks homopolymers and/or block copolymers).

Even more interesting are the (co)polymers with and as representatives of dienes. Preferably these (co)polymers are polymerized mortar polymerization to a high of CIS-1,4-content (at least of the order of approximately 90%). These (co)polymers additionally characterized by (very) high molecular weight, typically in the range of at least 1000000 g/mol. More preferably, they receive anionic polymerization in the presence of lithium catalyst, thus ensuring a very low ash content. However, they may also be obtained through the catalyst type Ziegler or based on neodymium catalyst. More preferably polymer is isoprene rubber, for example, any one of the varieties that are commercially available from KRATON Polymers.

Note that the method of the present invention can also be used in case, when synthetic latex obtained using instrumentation natural rubber.

Rubber, preferably isoprene rubber, can be dissolved in a suitable solvent. As regards the choice of solvent, his choice will depend to some extent on the exact nature of the rubber and the boiling point of the solvent. It is necessary to apply the solvent (quick and easy) dissolve rubber. For the less polar polymers used as a rubber suitable are aliphatic hydrocarbon solvents, containing up to approximately ten carbon atoms. They include isopentane, cyclopentane, n-pentane, , , octane and such. Preferably applied solvent with a boiling point below 82 o C, preferably not more than 55 degrees, preferably chosen from the n-pentane addition a cyclopentane, n-hexane, cyclohexane, their isomers and their mixtures. For isoprene rubber preferred solvent is n-pentane.

The number of rubber, dissolved in a solvent, will depend on the solubility of polymer in solution and limited to that. In the case of isoprene rubber preferable number, is described as the content of dry substances is less than approximately 20% of the mass., preferably from approximately 8 to approximately 17% of the mass., more preferably from about 10 to about 15% of the mass. Another way to define the maximum number consists in determination by low dynamic shear viscosity of a binding material, which should preferably be 20000 CP or lower viscosity Б at room temperature).

Rubber can be dissolved in a solvent in any normal way. For example, it can be dissolved in a solvent in an agitated vessel. No specific conditions with regard to this preparatory stage. Obviously, you must follow the terms of security set by the manufacturer and should be avoided decomposition of rubber.

After the formation of a binding material by dissolving rubber in a suitable solvent, it together with an aqueous solution of surface-active substances with emulsion oil in water. With regard to use aqueous solution of surface-active substances, in principle, you can apply any surfactant. However, because the underlying problem of the invention is to avoid extraneous materials, which limits the application of the received latex, surfactant is a preferable approved for contact with food and skin. In obtaining isoprene rubber latex preferably used surfactant type of resin acid approved for contact with food and skin. Surface-active substances, such as resin acids are preferred due to their relatively low tendency to foam formation.

Surface-active substance can be used in concentrations between 0.5 and 5.0% of the mass. in water. More preferably used at a concentration of between 0.75 and 3.0% of the mass., even more preferably between 0.9 and 1.5% of the mass. While you can apply more concentrated solutions, they usually do not provide benefits. In this regard, we note that may be important rigidity of water used to obtain the solution of surface-active substances. Preferably to obtain a solution of surface-active substances use very soft water (0-4 DH) or soft water (4-8 DH). You can use the usual means to obtain aqueous solution of surface-active substances.

Volumetric ratio of aqueous solution of surface-active substances to connecting substance is also somewhat predetermined. Apply a small amount of water surface-active substance can cause phase inversion, while the use of excess surface-active substances will be difficult in the next stage of the removal of hydrocarbon solvent and in the subsequent stage of concentration aqueous emulsion. A typical ratio of binding substance/surfactant will be in the range from approximately 1:1.5 to 1:3,0, preferably from 1:2,0 1:2,5 volume. Therefore, the original content of the solvent is preferably approximately 50-60% of the mass.

Emulsification binding agent with a water solution of surface-active substances can be made with homogenizer or a similar tool. Preferably use a homogenizer, or series of homogenizers, which generate stable emulsion oil in water with particles size during solvent removal, equal to approximately 0.5 to 2 microns (average diameter). Neither coarse nor finer particle size will not bring any advantage.

It is worth noting again that found that removing the solvent of a multicomponent system is not as direct as would be expected. The initial product is oil in water emulsion, which in itself is quite complicated. The solvent must be removed from emulsified oil without destabilizing and coagulation of these emulsified particles. In addition, for further use of synthetic latex for example, in obtaining gloves and condoms, it is necessary that the number of residual solvents was reduced to very low levels. You also need to levels agent control of foaming were low. Besides, it is necessary to economically possible processes were able to create high performance that are difficult to achieve, the more solvent should be removed. The same is true for the consumption of energy (heat required to evaporate the solvent).

To meet these contradicting to the requirements, the stage of evaporation of the solvent according to the present invention requires at least two steps solvent removal, in accordance with the first stage reached a significant reduction in solvent followed by the second stage of removal, which achieved the final low levels of solvent.

The second stage preferably carry out the distillation of the solvent in the conditions of high temperature and low pressure over the boiling point of the solvent, but below the boiling point of water, preferably at a temperature in the range of 70-85 OC and a pressure of 0.2 to 1.0 bar. The second stage can be performed in a single vessel or sequentially in numerous vessels.

As it is known, for example, of the US 3250737, during the distillation of the solvent will be some foaming. Although the US 3250737 specified that application agent is not usually recommended, in the way of this invention application of such an agent in small quantities to some degree is preferable. Agent control of foaming (FCA)applied in method, may be the agent on the basis of polysiloxane or silica or a combination of them. The number of FCA is preferably a small, typically in the range of millions of parts. The number is a function of many factors, such as the nature of rubber and solvent content of dry substances of rubber in the solvent, the number of surface-active substances, etc. in Other words, there is no specific upper limit and lower limit. Instead, it is recommended to spend some searching tests in the laboratory scale, the results of which can then be used when developing technical means for production in a large scale. Significant in this way is the use of contour re-boiling, in accordance with part of synthetic latex obtained in step 1, heated, for example, heat exchanger and is mixed with emulsion oil in water. This is done preferably in a quantity sufficient to reduce the content of the solvent (through dilution) to no more than 10% of the mass., more preferably not more than 5% by mass. The mass ratio of the flow of product to the emulsion is preferably at least 20:1, more preferably at least 30:1.

As mentioned, the recirculated product flow preferably takes place on the heat exchanger before it is mixed with emulsion oil in water. Here it can be heated to temperatures above the boiling point of the solvent, but clearly below the boiling point of water. For example, the heat exchanger can increase the temperature of the return of synthetic latex with low solvent content for 2 to 10 C, preferably on a 3 to 4 OC C.

Recycling of part of the flow of product is a preferred way of heating the reactor's content, although you can apply additional heating (for example, using a heater with a jacket or heated steam). The advantage of this implementation of the preferred option is that some amount of solvent already evaporated from the emulsion oil in water before she entered the reactor.

In step 1 operation to reduce the quantity of solvent can be performed at a temperature sufficient for the reduction of the solvent content of the product the aqueous emulsion in the range from 0,5 to 1% of the mass. In this variant of the implementation of the operation preferably carried out at a temperature of 75 to 85 degrees C. This option implementation has a low level of residual solvents as an advantage, but regarding the implementation of the preferred option, described later in this document, leads to high levels of pollution and problematic foam control, requiring high levels of FCA and limits and performance.

The more preferred embodiment phase 1 operations reduction of solvent is carried out at a temperature sufficient for the reduction of the solvent content of the product the aqueous emulsion in the first vessel in the range from 1 to 3% of the mass., preferably 1 to 2% of the mass. In a preferred embodiment operation in the vessel preferably carried out at a temperature from 70 up to 90 degrees With, preferably from 55 to 65 degrees C. implementation of This option has the advantage of high performance in combination with reduced pollution and ease of control of foaming with relatively low levels of FCA. The only drawback is somewhat higher levels of residual solvent that should be removed at the second stage.

As noted, the objective of the first stage is the reduction of the solvent content of the initial content, typically in the range of 50 to 60% of the mass. for a much more low content, typically in the range from 0,05 to 3% of the mass. Conditions of operation and process to achieve the desired level of reduction mentioned above. However, they should be optimized based on the type of solvent, the type of the polymer and the type of equipment used. On the other hand, these conditions can be easily defined as soon as the specialist in the art to understand that at this first stage requires more extensive solvent, than it was supposed in the ordinary processes of prior art. Example of a suitable structure for this first stage can be found in the examples.

Next, the remaining solvent must be reduced to the desired low levels. Of course, in many applications of synthetic latex presence of residual solvent brings harm or even prohibited. It is judged that the lower the required levels of solvent in the final synthetic latex, the more difficult or time costs or energy consumption. Reduction to the data declared levels is difficult, but attainable until the solvent levels were significantly reduced during phase 1. Through two stages stage of the process of the invention of the authors reached the goal in obtaining synthetic latex with excellent quality effective for time and energy. The fact that this stage with two steps of the process can be successful, is not expected. Of course, in a simple system of water and solvent is not intended for the process of two phases and could not be expected that this will improve the full reduction of solvent. Used in this second step equipment is not limited. You can use the same vessel, which was used in step 1. On the other hand, due to the significant removal of solvent from the complex emulsion oil in water in step 1 into the next stage you can apply a wide range of equipment. For example, in the subsequent stage, you can use the device for instant heating, acting under vacuum from 200 to 600 millibar. Thus, the solvent content can be reduced to the desired levels, with little pollution or without due, for example, foaming and similar.

Also in the second stage you can apply anti-foam additives. Application additives is a normal and already described in US 2595797 (for example, oil).

The initial stages of production of emulsion oil in water can be done using any of the processes that are already known in the art. This includes each of the links to the previous level of technology relating to paragraphs [0003] to [0008]included in this document as a reference and NL 287078; GB 1004441; US 3249566; US 3261792; US 3268501; US 3268501; US 3277037; US 3281386; US 3287301; US 3285869; US 3305508; US 3310151; US 3310516; US 3313759; US 3320220; US 3294719; GB 1162569; GB 1199325; US 3424705; US 3445414; SU 265434; US 3503917; US 3583967; GB 1327127; US 3644263; US 3652482; US 3808166; US 3719572; DE 2245370; JP 48038337; FR 2153913; GB 1296107; FR 2172455; US 3815655; US 3839258; US 3842052; GB 1384591; US 3879326; US 3892698; US 3862078; US 3879327; US 3886109; US 3920601; JP 51080344; JP 50127950; JP 54124042; JP 54124040; US 4243566; JP 56161424; US 4344859; SU 1014834; JP 58091702; SU 1375629; JP 1123834; SU 520769 and RO 102665; and US 3007852; US 3622127; US 4160726; GB 2051086; JP 58147406; SU 1058974; EP 512736; JP 8120124 and US 6075073, also included in this document by reference. Also in the prior art is largely described optional step concentration latex, typically through the use of a centrifuge or the possibility of settling for emulsion within a reasonable amount of time (such as 24 hours) and remove serum (containing less than 2% of the mass. dry substances).

The following examples will be more advanced illustrate how you can implement this invention. However, it is not intended to limit the invention in any way.

Binder on the basis of rubber obtained by dissolving polyisoprene with high content of TRANS-links (MM approximately 3 million, received anionic polymerization) in n-. This was the content of dry substances approximately 10% of the mass. Aqueous solution of surface-active substances obtained using surfactant resin type in a concentration of approximately 1% of the mass.

Consistently received a stable emulsion oil in water at volumetric ratio binder to the water surface-active substance 2,3. Emulsion oil in water received in a continuous process with the use of homogenizer. Stable oil in water emulsion contained approximately 55% of the mass. n-pentane.

The emulsion on the basis of n-pentane subjected to continuous removal of solvent phase 1. Have a comparative reactor, as shown in figure I, or reactor, as shown in figure II. Thus, the first cycles are comparative.

The table below shows the conditions and results of these cycles. Product samples taken and analysed after cycles lasted at least 5 times of stay in the vessel.

The operation to reduce solvent at 60 degrees C leads to less pollution, while applying fewer agent control of foaming. Therefore, examples of 9 to 11 illustrate the preferred option of the implementation of the present invention.

1. Method of production of synthetic latex, including the stages: (a) emulsification binder containing rubber, dissolved in a suitable organic solvent, together with an aqueous solution of surface-active substances, thus forming an emulsion oil in water; (b) a phased reduction of the content solvent-emulsion oil in water in two or more stages, resulting in a synthetic latex, in a reactor with continuous mixing (1)equipped with a means of mixing (2), the charging hole (3), the output vent (4) and the outlet to the product (5)where the inlet (3) and the outlet for the product (5) are part of the circuit re-boiling (6) for part of synthetic latex, in which the path of re-boiling (6) includes in addition to the output discharge outlet (7), optional inlet for control agent flushing (8), pump (9), heating unit (10), inlet for emulsion oil in water (11) and optional entry hole for steam (12), in which synthetic latex obtained at the stage 1 stage (b) has reduced solvent content in relation to the original content preferably in the range from 0,05 to 3 wt.% in relation to the whole of the emulsion, characterized in that the stage 1 stage (b) part of the solvent is removed by means of mixing parts of synthetic latex heated to a temperature of over the boiling point of the solvent-emulsion and by providing opportunities for the solvent to evaporate.

2. The method according to claim 1, which uses a circuit re-boiling, in accordance with part of synthetic latex obtained in step 1 heated and mixed with emulsion oil in water.

3. The method according to claim 1, wherein a synthetic latex and emulsion mixed in volumetric ratio so that the solvent content was not more than 5 wt.%.

4. The method according to claim 1, which shall be control agent foaming at one or more stages of the stage of (b) to reduce foaming.

5. The method according to claim 1, wherein the emulsion has the original solvent content between 50 and 60 wt.% in relation to the whole of the emulsion.

6. The method according to claim 1, wherein a synthetic latex in the late stages (b) has the solvent content of less than 150 ppm.

7. The method according to claim 1, wherein the first stage of the stage of (b) conduct by the distillation of the solvent in the conditions of high temperature and approximately atmospheric pressure above the boiling point of the solvent, but below the boiling point of water, preferably at a temperature in the range of 50-85 degrees, if The manometer scale from 0 to 100 millibars.

8. The method according to claim 1, wherein the recirculated synthetic latex and emulsion mix in the mass ratio equal to at least 20 to 1.

9. The method according to claim 1, wherein a contour re-boiling equipped with a heat exchanger as a heating device, located upstream of designated uniting the recirculated synthetic latex and emulsion oil in water.

10. The method of claim 9, which increases the temperature of the heat exchanger return synthetic latex for 2 to 10 C, preferably 3 to 4 OC C.

11. The method according to claim 1, held at a temperature sufficient to reduce the content of solvent-emulsion on stage 1 stage (b) to the interval from 0.5 to 1.0 wt%.

12. The method according to claim 11, held at the temperature 75-85°N

13. The method according to claim 1, held at a temperature sufficient to reduce the content of solvent-emulsion on stage 1 stage (b) to the interval from 1.0 to 3.0%by weight.

14. The method according to item 13, held at a temperature of 50-70°With, preferably 55-65°N

15. The method according to claim 1, wherein the second stage of the stage of (b) conduct by the distillation of the solvent in the conditions of high temperature and low atmospheric pressure above the boiling point of the solvent, but below the boiling point of water, preferably at a temperature of 70 to 85 C, and reduced pressure from 200 to 600 millibar.

16. The method according to claim 1, wherein a rubber is an isoprene rubber.

17. The method according to claim 1, wherein a number of rubber, dissolved in a solvent is less than approximately 20 wt.%, preferably from approximately 8 to 17 wt.%.

18. The method according to claim 1 in which the solvent is an organic solvent, has a boiling point of not more than 82 o C, preferably not more than 55 degrees, more preferably selected from the pentane addition a cyclopentane, hexane, cyclohexane, their isomers and their mixtures.

19. Reactor with continuous mixing (1) for the removal of organic solvent from the emulsion oil in water, including rubber, dissolved in organic solvent, and emulsified with an aqueous solution of surface-active substance with the formation of synthetic latex with a low content of organic solvent, where the reactor is equipped with means of mixing (2), the charging hole (3), the output vent (4) and the outlet to the product (5)where the inlet (3) and the outlet for the product (5) are part of the circuit re-boiling (6) for part of synthetic latex, in which the path of re-boiling (6) includes in addition to the output discharge outlet (7), optional inlet for control agent flushing (8), pump (9), heating unit (10), inlet for emulsion oil in water (11) and optional entry hole for steam (12).