The method of producing preductal of alkalisation in a gas-liquid dispersion reactor

 

(57) Abstract:

The invention relates to a semi-continuous method and system for producing Preductal of alkalisation by carrying out the reactions of addition of accelerated on the initiator growth macromolecular chain, which has at least one active hydrogen atom. The method involves the use of a reactor 1, consisting of two different diameter portions of the cylinder, which has a large diameter portion is located above the smaller diameter part of the heat exchanger 2 and the bypass line 13, 15, which in the process of obtaining the final product, the reaction mixture is pumped from the bottom of the reactor in its upper part. The method has a high technological flexibility and reduces the time to obtain the final product. The use of the reactor according to the invention allows to start the process of obtaining the final product when the amount of initiator growth circuit, comprising 1/90 of the volume of the final product, provides the possibility of using a single loading of the reactor of the final product with a very high molecular weight or, if necessary, receive smaller quantities of priduct at the same growth of the molecular chain. the treatment of Preductal of alkalisation by carrying out the reactions of addition of alkalinized on the initiator growth macromolecular chain, which has at least one active hydrogen atom. Such products, in particular preaddukta of ethylene oxide and propylene oxide, are mainly used as nonionic surfactants and polyether polyols.

Nonionic surfactants are used as wetting agents, dispersing agents, stabilizers, additives, emulsifiers, animalisation, antispyware and foaming agents, usually as an auxiliary chemical products and functional fluid in the textile, paper, pulp, pharmaceutical, food, cosmetic, paint, plastics, mining and processing minerals and oil industry. In this regard, it is especially important to mention nonionic surfactants based on natural or synthetic fatty alcohols, which are the main components of household and industrial detergent, and polyether polyols as the main intermediates in obtaining polyurethanes (rigid, semi-rigid, flexible foams, elastomers, adhesives, sealants and so on).

In the patent Italy 1226405 described by way of polucheniya and/or propylenoxide, and compounds having active or movable hydrogen atom, using appropriate catalysts. The method described in this patent involves the use of two-reactor upper section of which is a so-called gas-liquid reactor, and the bottom forms a cumulative capacity located essentially horizontally. In the top section of the reactor, in which multiple spray heads mounted on the Central distributor, is the initiator of the chain growth, flows of gas-liquid reaction, obtained as a result of which the product is collected in the bottom section of the book, from which the reaction product is pumped by the pump through an external heat exchanger, and again served in the upper section to continue the polymerization reaction.

In the patent Italy 1226406 describes a method for polymerization products of alkalisation, which involves the use of two-reactor upper section of which is a so-called gas-liquid reactor, and the bottom forms a cumulative capacity, and each of these sections has several spray heads. The first phase of the reaction takes place in the lower section, which is the product of polymerization; after that starts the polymerization reaction in the horizontal top section, in which this reaction continues until the desired product.

The methods described in the aforementioned patents, are however a number of disadvantages. First, they all require the use of two reactors, which complicate the entire installation and increase its cost; two reactors, in addition, have either one large diameter hole, through which their section communicated with each other, or, as in the reactor described in patent Italy 1226406, a few holes, which increases the possibility of leakage of accelerated and education in the reactor dead zones and exposed to internal oxide surfaces. When using two internal distribution ratio of surface to volume in such reactors is increased, which increases the likelihood of secondary reactions. Double-hulled design of the reactor and the internal distributors also lead to the appearance of the inside of the reactor dead zones that impede the drainage of the liquid from the reactor and cleaning, which causes problems when replacing the received praakli, which is collected in the upper horizontal section and then merges into the bottom section, accompanied by re-diffusion and, therefore, too long exposed to the oxidizing atmosphere.

Based on the foregoing, the present invention was used to develop this method of obtaining Preductal of alkalisation, which would not have the disadvantages inherent in the known methods.

To solve this problem the present invention proposes a semi-continuous method of producing Preductal of alkalisation by carrying out the reactions of addition of accelerated on the initiator of the chain growth, which has at least one active hydrogen atom. The proposed method differs in that

- prepare the reactor, made in the form of a cylindrical body essentially vertical longitudinal axis, consisting of two parts of different diameter, the diameter of the upper part of the body exceeds the diameter located underneath the bottom of the hull, and the reactor has an input and output apertures and device for fine spraying of the reaction mixture and a thin spray of accelerated, which are located throughout the inner surface is she initiated the growth of the chain,

- from the reactor through the outlet drains the fluid and its temperature is brought to the desired reaction temperature using a heat exchanger,

the liquid through the spray device thinly sprayed through the spray device in the reactor serves alkalinized with intermediate liquid reaction product which forms a mixture with the liquid initiator growth chain,

- the resulting mixture is continuously pumped through the bypass line and after adjusting its temperature to the desired reaction temperature fed into the reactor by spraying in the upper part of the reactor by means of a spray device, subjecting the interaction with an additional number of accelerated with the final product having the desired chain length.

The amount of initiator, the chain growth is usually equal to the ratio of the final amount of product to the rate of growth of the polymer chain, which is determined by the ratio of the molecular weight of the final product to the molecular weight of the initiator growth chain.

As the initiators of the growth of the macromolecule can be used compounds having, depending on the final product is such as op, Nonylphenol, dodecylphenol, dinonylphenol, tridirectional, natural and synthetic fatty alcohols and their mixtures, such as decroly alcohol, tridecylamine alcohol, alerby alcohol, operacyjny alcohol, cetylstearyl alcohol, lanolin, cholesterol, acetylenyl, fatty amines and hydrogenated amines, such as laurylamine, oleylamine, amino derivatives of coconut oil, soybean and tall oil, soya aminopropylene, abatellis, fatty amides, such as laurylamine, stearylamine, fatty amides derived from coconut oil, fatty acids such as coconut, lauric, tall, stearic, palmitic, oleic, myristic, linoleinovoy, abietic and naphthenic acid, sorbitane esters, such as monolaurate, monopalmitate, monostearate, monooleate, monoobject, dilaurate, tristearate, Triolet, petalura, Exalead, exactearth, monoglycerides and monostearate, for example, coconut oil and glycerol esters of pentaerythritol, such as monolaurate, monooleate and lanolin, etilenglikoli, such as mono-, di-, tri-etilenglikoli and glycols, propylene glycol, such as mono-, di-, tripropyleneglycol and polypropylenglycol, block polymers of ethylene oxide/propylene oxide and unordered polipropilenglikol and so p. , oils, such as castor oil, gidrirovannoe castor oil, mint oil, tall oil, and fats of animal origin, mercaptans, such as dodecylmercaptan.

To activate the reaction alkoxysilane and to increase it when necessary speed in the reactor serves a catalyst to increase the rate of generation of the alcoholate in sutu must be completely atomized in initiating growth of the chain.

In the most preferred embodiment of the invention it is proposed to use a basic catalyst selected from the group comprising hydroxides and alcoholate of alkali metals and hydroxides of alkaline earth metals. In principle, you can use acid catalysts, which, however, are less preferred because they have a certain disadvantage in elevated levels of dioxane in the final product. The catalyst can be added to the reactor in solid form and in aqueous solution, feeding it directly into the bypass line and mixing it before entering the reactor with the initiator of the chain growth.

If necessary, however, the catalyst can be fed into the reactor separately, mixing it with initiatior reaction it is necessary to spray the inside of the reactor into fine droplets. Formation in the reactor such liquid phase is carried out using a large number of nozzles uniformly distributed over the entire inner surface of the upper part of the reactor, in which the bypass line from the bottom of the reactor is fed spray mixture. The spray device spray initiator growth chain into droplets, the diameter Sauter which is less than 500 μm, and is formed in the upper part of the reactor from the drops sprayed initiator growth chain full cone angle which can vary from 15 to 150o.

Each nozzle preferably in the form mounted on the wall of the reactor and the speaker inside the reactor essentially of a hollow truncated cone, whose large diameter is connected with bypass road. Each conical atomizer has a number of evenly spaced across the surface of the nozzles through which the inside of the reactor is fed sprayed liquid phase. It should be noted that this form of spray (truncated cone) allows for orienting nozzles fed into the reactor sprayed liquid on the cone with a very large angle.

To achieve maximum dobavleniya of accelerated, which allows you to accelerate the reaction.

To this end, in one of the preferred variants of the invention it is proposed to use installed in the bypass line heat exchanger, which is used to heat pumped for this line catalyzed initiator growth chain.

In one embodiment of the invention it is also proposed to maintain the temperature in the lower part of the reactor and in the bypass line at a certain specified level, to prevent solidification of the initiators of the growing chain with a high melting point when the flow in the reactor and subsequent heating.

In the preferred embodiment proposed in the invention method, the stage of drying catalyzed initiator of the chain growth is expected to be implemented before the start of the reaction. Drying is carried out inside the reactor through a combination of vacuum and heat. Proposed in the present invention method allows thanks to a very high degree of dispersion catalyzed initiator growth chain in the gas phase in the reactor and a large number of pumping cycles in a closed circuit in a unit of time to reduce the moisture content in the reactor to Velicina or polypropylenglycol, formed during the reaction simultaneously with the final product.

The reaction alkoxysilane usually takes place at temperatures from 70 to 195oC, preferably from 90 to 180oWith depending on the received product and at a relative pressure, which depends in part on the presence of inert gas, mostly nitrogen, and partly from accelerated. Usually the relative pressure of the reaction never exceeded 6102kPa.

Liquid accelerated, which is fed into the reactor, enters the reactor in an atmosphere of inert gas and small droplets catalyzed initiator growth chain. Immediately after contact of the oxide with the initiator of the chain growth oxide evaporates and begins to dissolve in the droplets. As mentioned above, a high degree of dispersion of the liquid phase in the gas promotes very fast mass transfer and exchange of energy between the two phases, the contact between the reagents occurs during the period of time that is equal to the length of the flight drops.

Proposed in the invention is particularly effective in cases when alkalinity selected from the group including ethylene oxide, propylene oxide, butylenes and their setproducts reaction, when this is released during the reaction heat is removed from the reactor through a heat exchanger. In the most preferred embodiment of the invention the heat exchanger is installed in the bypass line and is used in the preceding reaction stage to heat the fluid containing catalyzed initiator growth chain. This version with heat exchanger installed in the bypass line, provides a very efficient heat released during the exothermic reaction.

During the reaction and added to the reactor accelerated carry out automatic adjustment of its mass and pressure and the reaction temperature, while continuously monitoring the temperature inside the reactor, the temperature in the bypass line and the temperature of cooling water supplied under pressure.

The absorption process of accelerated occurs essentially in the upper part of the reactor, i.e., where finely sprayed drops catalyzed initiator growth of the chain are dispersed in consisting of inert gas and vapors of accelerated atmosphere.

When the reaction of alkoxysilane in the liquid phase concentration of alkalinized in the reactor m is CLASS="ptx2">

Decreasing the concentration of alkalinized the temperature in the reactor in the direction from the free surface to the bottom of the reactor due to the exothermic nature of the reaction gradually increases.

The mechanism taking place in the reactor the reaction is not accompanied by retrodiffused, characterized by a gradual decrease in concentrations of dissolved accelerated and simultaneous gradual increase in the temperature of the reaction mass.

At a certain reaction kinetics the concentration of accelerated get in the proposed method, the final product, which is withdrawn from the bottom of the reactor and pumped through the bypass line, is less than other methods, and in particular when using conventional reactors, agitators and reactors with an internal system of Venturi tubes and bubble diffusion accelerated.

Proposed in the invention method also allows to improve the quality of the product that is obtained in the result of secondary reactions of accelerated.

After the reaction alkilinity the remainder is pumped from the reactor, the content of free accelerated the resulting product is less than 1 part./million

In some Laut desorption. In any case, all technological stages of further processing of the obtained product can be performed in the same reactor that was used in the proposed invention the method.

In one embodiment of the invention it is proposed to use an additional at least one reactor and/or the reactor, performed according to the type of reactor used in the present invention method, and coupled with the main reactor either sequentially or in parallel.

Serial connection of reactors creates the possibility of obtaining Preductal with high chain growth in a very short time, and the parallel connection of the reactors can significantly increase the operational flexibility of the whole technological process. This option connection reactors also allows you to start the process with a solid initiators growth of the chain (which should be melted) or in suspension or dissolved in water or solvent and creates opportunities for more Preductal with high viscosity (over 700 SP).

Proposed in the present invention the method also allows the use of initiators growth chain in the form of liquid, solid the way proposed in the present invention method allows you to work with the initiators of the growth of the chain with such varying in a fairly wide range of parameters as viscosity, density, vapor pressure, molecular weight, acidity, saturation and so on

Proposed in the present invention is a method of obtaining Preductal of alkalisation high performance, owing to very high variance and is significantly more efficient gas-liquid transfer material, creating conditions for a better absorption of accelerated at a certain amount of initiator growth of the chain, the type and concentration of catalyst, the partial pressure of accelerated and the reaction temperature, and also due to shorter drying for a given residual moisture content in the final product.

Proposed in the present invention the method also allows to increase the operational flexibility of the whole technological process and reduce downtime; the above scheme allows you to start the process of obtaining Preductal, when the number of the initiator of the chain growth does not exceed 1/90 of the volume of the final reaction product, and creates opportunities for when odnokratno of priduct at the same growth of the molecular chain.

A high degree of transfer material allows you to create a more favorable reaction conditions, and also to provide a more complete deaeration and dehydration initiator growth of the chain and, as a consequence, less formation of undesirable by-products and pollutants final product impurities. The resulting product will have higher quality and greater resistance to various external influences.

The respective shape of the reactor and distributors determine small relative surface of the reactor to its volume and long-lasting contact between gas and liquid in the upper part of the reactor. The proposed reactor is reduced to a minimum ratio of surface (S) of the metal exposed to gaseous accelerated, free volume (V) of vapor, which for reactors with a capacity of 10 tons per load does not exceed 1,55 m-1and for reactors with a capacity of 50 tons per load does not exceed 1.30 m-1and creates a very high differential concentrations of accelerated from the top of the reactor to its bottom and a very high temperature gradient from the bottom to the top. The almost complete absence in the safe operation compared to conventional reactors, based on the bubble dispersion of the oxide in the first place from the point of view of a possible explosion.

Due to the absence in the reactor dead zones the amount of product remaining in the reactor and connected to it by a bypass line after discharge from the reactor of the final product, less than 0.05 kg/m2the inner surface of the reactor. With this small number remaining in the reactor product proposed in the present invention method allows for a single loading of the reactor, a large number of cycles when receiving the same type of end-product, or change the type of the resulting product, without fear of reducing its quality due to the possible presence in the reactor of a significant amount remaining from a previous load of material.

The corresponding distribution of the spray on the inner surface of the upper part of the reactor allows 100% of the inner volume of the reactor in varying degrees, to complete the reaction liquid, thereby ensuring maximum transfer of material to any degree of chain growth with minimal coalescence of liquid drops on the wall of the reactor before they reach the free surface h is Asti reactor eliminates any local overheating of the walls of the reactor under the action of heat, which from the outside is applied to the wall of the reactor, and, as a consequence, significantly reduces the likelihood of explosions in the reactor.

Proposed in the present invention method allows performing only one step of the reaction, to obtain the product, the molecular weight of which is due to the growth of the macromolecule can in ninety times the molecular weight of the initiator of the chain growth; without the need for any subsequent additional operations and/or intermediate ventilation of the reactor and/or, as is the case with conventional methods alkoxysilane, collect the resulting intermediate product in a special collection.

Another advantage of the present invention, especially when ethoxycarbonyl, is the complete absence of the proposed reactor in contact with the pairs of accelerated mechanical seals, which greatly reduces the likelihood that the energy required to initiate the chain reaction in the vapor of ethylene oxide exceeds the minimum allowable threshold value.

Proposed in the present invention the method also allows to decrease in comparison with the known methods the concentration of dioxane in CLASS="ptx2">

In addition, the proposed in the present invention the method is carried out in the reactor, which is due to the small relationship of surface to volume, the absence of dead zones (the absence of valves and other internal parts) and a small amount of residual at the end of the reaction material can (if necessary) rather quickly and relatively easy to clean. The distribution of the nozzles on the inner surface of the upper part of the reactor also contributes to a more effective washing of the whole inner surface of the reactor relatively small amount of water or solvent. Drained from the reactor and the washing liquid contains less harmful substances and therefore easier undergoes regeneration.

Proposed in the present invention method thanks to a special design used for its implementation of the reactor and the other above-mentioned features, for example, a smaller number of remaining at the end of the reaction toxic substances and less energy consumption due to increased efficiency of different reaction cycles, causes significantly less damage to the environment than conventional currently known methods.

Another object of the present ine of accelerated on the initiator of the chain growth, which has at least one active hydrogen atom. This reactor is different in that it has a cylindrical body which is essentially vertical longitudinal axis, consisting of two parts of different diameter, the diameter of the upper part of the body larger than the diameter located underneath the bottom of the hull, and the reactor has an input and output apertures and device for fine spraying of the reaction mixture and accelerated, which are arranged and distributed over the entire inner surface of the upper part of the cylindrical reactor vessel.

Distinctive features and advantages of the invention considered in more detail in the description below, some of the options proposed in the invention method, with reference to the attached drawing, which schematically and only by way of example shows an installation for carrying out the method.

In the shown schematically in the drawing, the installation includes a reactor 1 with a cylindrical consisting of two parts of different diameter housing with a vertical longitudinal axis, the heat exchanger 2 and the centrifugal pump 3, pump formed in the reactor product, which enters the pump from the reactor by Amer which is larger than the diameter of the bottom part 4. In the lower part 4 of the reactor is composed of a cut in half pipes and/or special plates 6 device, which is continuously fed steam or hot water under pressure.

For feed to the reactor 1 initiator growth of chain is used, the pipeline 7. The reactor has four input pipe 8, which in the drawing are visible only three and which are connected to nozzles 9 through which the upper part 5 of the reactor 1 in a spray form is served pumped through the bypass line, the product of the reaction, the four holes 10, of which are visible in the drawing only two and which are communicated with the nozzles 11, through which the upper part 5 of the reactor 1 is atomized accelerated, and the drain hole 12, through which the intermediate reaction product coming from the reactor tubes 13, 15 bypass line.

The nozzles 9 and 11 are made in the form of a truncated cone hollow body with several, for example eight, exposed to the outside and are evenly distributed on it a small nozzles.

The nozzles 9 are distributed over the surface of the upper part 5 of the reactor. One of them is located at the top of the reactor 1, and the other three lie on a circle in ploskoye other nozzle 11 are arranged symmetrically around one of the nozzles 9, mounted in the top of the reactor.

For the circulation pump 3 to the heat exchanger 2 in the pressure line of the pump embedded pipe 16, through which from the unit displays the final product, and the heat exchanger in the bypass line embedded pipe 17 for submission to the installation of the catalyst. The heat exchanger has tubes 18 and 19 to pump through it under pressure in the hot or cold water, instead of which, however, you can use any normal fluid, such as thermal oil.

First, the pipe 7 into the reactor 1 is fed with liquid initiator growth chain flow which stops when his weight quantity in the reactor reaches a certain value. Fed to the reactor liquid initiator growth chain is pumped from the reactor through outlet 12 by a pump 3 and is returned to the reactor through the pipe 15 through the nozzles 9 in the form of finely dispersed liquid droplets. Simultaneously, the pipe 17 into the return pipe 15 flows used for the polymerization reaction catalyst, which is completely dispersed in the liquid phase initiator growth of the chain, forming in the upper part of the reactor finely sprayed dispersion drops, sod the La and vacuum.

After a reactor conditions necessary to start a chain reaction of polymerization (temperature, concentration of catalyst, degree of humidity, pressure and so on), in the reactor begins to flow through the pipeline 14 through the holes 10 and the nozzles 11 accelerated. Fed into the reactor accelerated absorbed drops catalyzed initiator growth chain in the upper part of the reactor 1, and in the lower part of the reactor 1 when this starts a chemical reaction.

Rich alkalization drops coalesce into the reactor 1 at the free surface of the liquid phase, where the reaction takes place alkoxysilane. The liquid phase continuously with a certain time delay is again returned through the pipeline 15 in the upper part of the reactor, where it is sprayed by the nozzles 9.

When pumping on the bypass line liquid phase continuously gives off heat, the majority of which is allocated with the strongly exothermic reaction alkoxysilane, in the heat exchanger 2, which in turn is continuously cooled by pumped through it under pressure in the water. Continuous feed to the reactor as flow therein reactions alkoxysilane fresh accelerated derecognised after desorption and neutralization, if necessary, before the next cycle is drained from the reactor and connected to it by a bypass line through the pipeline 16.

EXAMPLE 1

Getting 10000 kg product consisting of fatty12-C14alcohol and 2.8 mol of ethylene oxide

In the reactor described above installation related S/V, is equal to 1.55 m, uploaded 6125 kg fat C13-C14alcohol (molecular mass (MM) 195) and 2.5 kg of NaOH as catalyst. All loaded in the reactor, the material was dried at 135oWith vacuum < 5 mbar, and then after filling the reactor with nitrogen and heat in it the mixture to the reaction temperature (160o(C) in the reactor was added 3875 kg of ethylene oxide, whose interaction with fatty alcohol occurred in the reactor at the maximum relative reaction pressure equal 4,75102kPa.

Received upon completion of the reaction product was cooled, neutralized and poured from the reactor. After that no desorption or any other processing of the received product is not conducted.

The whole cycle of the final product, since the load of the reactor and to discharge him of the finished product, lasted for 170 minutes

The resulting product is ARNA - max 5

The water content (part./million) - max 100

pH (3% aqueous solution at 25oS) - 6 - 7

Hydroxyl number (mg KOH/g) - 1761,5

The content of polyethylene glycol (wt.%) . - maximum of 0.25

Ash (AA) (part./million) - max 200

The content of dioxane (part./million) - max 1

The content of free ethylene oxide (part./million) - Max. of 0.5.

EXAMPLE 2

Getting 10000 kg of product, consisting of Nonylphenol and 9.0 moles of ethylene oxide

In the reactor described above installation related S/V, is equal to 1.55 m-1, download 3569 of Nonylphenol (220 MM) and 2.5 kg of NaOH as catalyst. All loaded in the reactor, the material was dried at 140oWith vacuum < 5 mbar, and then after filling the reactor with nitrogen and heat in it the mixture to the reaction temperature (165o(C) in the reactor was added 6431 kg of ethylene oxide, whose interaction with fatty alcohol occurred in the reactor at the maximum relative reaction pressure equal 4,75102kPa.

Received upon completion of the reaction product was cooled, neutralized and poured from the reactor. After that no desorption or any other processing of the received product is not conducted.

The whole cycle of receiving a tip the chickpeas.

The resulting product had the following qualitative characteristics:

Appearance at 25oWith - Transparent liquid

Color scale ARNA - max 10

The water content (part./million) - max 100

pH (3% aqueous solution at 25oC) - 6,50,5

Hydroxyl number (mg KOH/g) - 911

The content of polyethylene glycol (wt.%) - max 0,25

Ash (AA) (part./million) - max 200

The content of dioxane (part./million) - max 2

The content of free ethylene oxide (part./million)Max. to 0.5.

1. Semi-continuous method of obtaining Preductal of alkalisation by conducting a reaction between a catalyst of accelerated, representing the initiator of the growth of the chain containing at least one active hydrogen atom, wherein preparing the reactor 1, made in the form of a cylindrical body essentially vertical longitudinal axis, consisting of two parts of different diameter, the diameter of the upper part of the body larger than the diameter located underneath the bottom of the hull, and the reactor 1 has an input 8, 10 and outlet 12 holes in the top of the device 9 for fine spraying of the reaction mixture and the device 11 for fine atomization Alki the EOS 1 load specified by the volume amount of fluid, including the initiator of the growth of the chain, from the reactor through the outlet 12 divert the fluid and its temperature is brought to the desired reaction temperature using a heat exchange device 2, the thin liquid is sprayed through the spray device 9 and through the spray device 11 in the reactor serves alkalinized with intermediate liquid reaction product which forms a mixture with the liquid initiator growth of the chain, the resulting mixture was continuously pumped through the bypass line and after adjusting its temperature to the desired reaction temperature fed into the reactor by spraying in the upper part of the reactor by means of a spray device 9, subjecting the interaction with an additional number of accelerated with the final product having the desired chain length.

2. The method according to p. 1, characterized in that the stage of bringing the temperature of the liquid containing the initiator growth circuit, to a predetermined temperature, the reaction is carried out directly before the stage of mixing the liquid with the catalyst.

3. The method according to p. 2, characterized in that the initiator of the chain growth and the catalyst is subjected to drying, which is carried out before the stage of filing of accelerated in the roar of the liquid, containing initiator growth circuit, to a predetermined temperature using a heat exchanger 2.

5. The method according to p. 4, characterized in that the catalyst serves as received in the reactor mixture after its passage through the heat exchanger 2.

6. The method according to p. 4 or 5, characterized in that the temperature is pumped into the reactor by-pass line of the intermediate product is brought to a predetermined temperature by cooling with heat exchanger 2.

7. The method according to any of the preceding paragraphs, characterized in that the device 9, 11 to spray made in the form mounted on the wall of the reactor and the speaker inside the reactor essentially of a hollow truncated cone, whose large diameter is connected with the corresponding pipeline 14, 15, through one of which the reactor from the bypass line flows obtained mixture, and after another is accelerated, and has a number of evenly spaced across the surface of the nozzles.

8. The method according to any of the preceding paragraphs, characterized in that ethylenoxide selected from the group including ethylene oxide, propylene oxide, butylenes and mixtures thereof.

9. The method according to any of the preceding paragraphs, characterized the alcohols and mixtures thereof, fatty amines and hydrogenated amines, fatty amides, fatty acids, sorbitane esters, monoglycerides and monostearate, esters of pentaerythritol, etilenglikoli, propylene glycols, block-polymers obtained from ethylene oxide/propylene oxide, and polymers derived from their disordered sequences using different initiators growth chain, such as fatty amines, fatty alcohols, glycerin, dipropyleneglycol, castor oil, gidrirovannoe castor oil, tall oil, mint oil, animal fats and mercaptans.

10. The method according to any of the preceding paragraphs, characterized in that the catalyst is chosen from the group comprising hydroxides and alcoholate of alkali metals and hydroxides of alkaline-earth metals.

11. The method according to any of the preceding paragraphs, characterized in that the reaction temperature lies in the range from 70 to 195oC.

12. The method according to any of the preceding paragraphs, characterized in that the relative pressure in the reactor does not exceed 6102kPa.

13. The method according to any of the preceding paragraphs, characterized in that the reactor in series or parallel connected with at least one conventional reactor and/or the reactor according to any lname the cone angle 15-150ointo droplets, the diameter Sauter which are less than 500 microns.

15. The reactor used for carrying out semi-continuous method of producing Preductal of alkalisation on PP. 1-14, having a cylindrical body which is essentially vertical longitudinal axis, consisting of two parts of different diameter, the diameter of the upper part of the body larger than the diameter located underneath the bottom of the hull, and the reactor has an input 8, 10 and outlet 12 holes and a device 9 for fine spraying of the reaction mixture and the device 11 for fine spraying accelerated, and these devices are distributed over the entire inner surface of the upper part of the cylindrical reactor vessel.

16. The reactor under item 15, characterized in that the device 9, 11 to spray made in the form mounted on the wall of the reactor and the speaker inside the reactor essentially of a hollow truncated cone, whose large diameter is connected with the corresponding line 15, 14, through one of which the reactor from the bypass line flows obtained mixture, and after another is accelerated, and has a number of evenly spaced across the surface of the nozzles.

-1.

18. The reactor under item 15 or 16, characterized in that it is made with performance when the disposable loading equal to 10 t, and the ratio of the surface area of metal exposed to gaseous accelerated, and the free volume is equal to or less 1,55 m-1.

 

Same patents:
The invention relates to methods of producing polyether of polyglycols (oligomers of 1,2-oxirane) and can be used in chemical industry for production of surfactants, plasticizers, binders, complexing agents, etc

The invention relates to an improved method for producing polyoxyethyleneglycol, in particular oxyalkylene, higher fatty alcohols, ALKYLPHENOLS, glycols, amines and carboxylic acids, highly effective nonionic surfactants

The invention relates to a method of obtaining polyoxyethyleneglycol with extremely low content of transition metal ions by catalyzed double metallocyanide complex polyoxyalkylene corresponding hydrogen initiator in the presence of 15 or less parts per million (ppm) double metallocyanide complex catalyst

The invention relates to polyetherpolyols, the method of its production, to polyetherpolyols mixture containing the polyol, and the hard polyurethane foam and can be used as insulating material for refrigerators, freezers in industrial plants, construction industry

-oximeter-oxy(oxo) -propyl-anhydride-succinic acid (peak)" target="_blank">

The invention relates to the production of PEAK that can be used as hardeners polymer compositions, varnishes, waxes, thickeners, reagents for the synthesis of surfactants, ion exchange polymers, flocculants water, floating agents, etc

The invention relates to methods for polyoxyethyleneglycol (co)polymerization of cyclic ethers and polyols in the presence of a catalyst based on heteropolyacids (CCP), in particular, the (co)polymerization of tetrahydrofuran, 1,2-alkalisation, epichlohydrin and polyols
The invention relates to the production of water-soluble polymers of acrylic series, which can be used in several branches of engineering and technology, namely as a dressing for finishing textiles, coal mining, and in the processes of purification and clarification of drinking, industrial and waste water as a flocculant, in the drilling technique as a protective means in the chemical industry as the thickening agent
The invention relates to the production of water-soluble polymers of acrylic series, which can be used in several branches of engineering and technology, namely as a dressing for finishing textiles, coal mining, and in the processes of purification and clarification of drinking, industrial and waste water as a flocculant, in the drilling technique as a protective means in the chemical industry as the thickening agent
The invention relates to the production of water-soluble polymers of acrylic series, which can be used in several branches of engineering and technology, namely as a dressing for finishing textiles, coal mining, and in the processes of purification and clarification of drinking, industrial and waste water as a flocculant, in the drilling technique as a protective means in the chemical industry as the thickening agent
The invention relates to the production of water-soluble polymers of acrylic series, which can be used in several branches of engineering and technology, namely as a dressing for finishing textiles, coal mining, and in the processes of purification and clarification of drinking, industrial and waste water as a flocculant, in the drilling technique as a protective means in the chemical industry as the thickening agent

The invention relates to the functionalized copolymers of styrene and isoolefine

The invention relates to the catalytic components of the metallocene type and their application to obtain a (co)polymer C2-C20olefins, in particular copolymers of ethylene with C3-C20preferably3-C10and more preferably3alpha-olefins, possibly in the presence of diene

The invention relates to the catalytic components of the metallocene type and their application to obtain a (co)polymer C2-C20olefins, in particular copolymers of ethylene with C3-C20preferably3-C10and more preferably3alpha-olefins, possibly in the presence of diene

The invention relates to a method for producing a petroleum resin and may find application in chemical, petroleum, paint and coatings industry

The invention relates to agents suppressing the formation of growth on the walls of the reactor during polymerization of vinyl chloride or vinyl acetate

The invention relates to a method of the reaction distillation and apparatus for the alkylation of benzene with a liquid olefin or mixture of olefin-paraffin
Up!