Method for production of phenol, acetone andmethylstyrene

 

(57) Abstract:

The invention relates to the field of petrochemical synthesis, in particular to a method for production of phenol, acetone and alpha-methylstyrene Kukolnik method. The decomposition process is performed with the supply of acetone in a reactor for the decomposition of cumene hydroperoxide by the following algorithm: GandC= GGPTO0,125 [CCP] + (35/GGPTO[CCP] ), where GGPTO, GandC- quantity supplied to the decomposition of technical CCP and acetone, t/h; [CCP] is the concentration of CPC in the technical code of civil procedure, wt. share. The decomposition of cumene hydroperoxide and dicumylperoxide cumene are at the same pressure (4 to 5 ATM.) in reactors offset, where decomposes the CCP, and in the reactor displacement, where decomposes disoproxil. The decomposition of cumene hydroperoxide is carried out in conditions that are close to isothermal, in a narrow temperature range 65 - 75oC. Concentration nerazlochennom of cumene hydroperoxide at the outlet of the reactor unit of the mixing is determined by the difference between the temperature T1 at the inlet and outlet specially installed mini-reactor (calorimeter). In the reactor displace water in the amount of 100 to 500 kg/h, which is determined by the value of RA is them out of the circuit after mixing products of the decomposition of water and the residence time of the products in the mini-reactor 7 - 8 minutes of the Management process of decomposition of the CCP through the relationship of the values T1 and T2 in such a way that the value of T2 is maintained at 0.2 to 3oWith higher than T1 . To prevent the occurrence of unwanted side reactions during the distillation of the reaction products put acetone in front of the apparatus to the evaporation of the acetone is ammonia in a molar ratio of H2SO4: NH3equal to from 1 : 1 to 1 : 2. 1 table, 2 Il.

The invention relates to the field of petrochemical synthesis, in particular to a method for production of phenol, acetone and alpha-methylstyrene Kukolnik method.

The method consists of two stages: the first is the oxidation of cumene with oxygen to cumene hydroperoxide (CHP), the second acid-catalyzed decomposition of the CCP to phenol and acetone. Decomposition of the CCP, along with the target products is phenol, acetone and alpha-methylstyrene, formed a certain amount of unusable products, the so-called "phenolic resins", the number of which is largely determined by the way in which the process of decomposition of the CCP and ranges from 50 - 60 kg/t in the best technology and up to 120 - 180 kg/t of phenol in traditional technologies [1].

To date, this research effort were not, and often more important indicator of industrial production of phenol and acetone is to increase productivity of existing process units. At the same time to solve the issues of maintaining high selectivity of the process and increase productivity failed.

The closest in technical essence (prototype) is the solution laid down in the flowsheet decomposition of the CCP, protected by a U.S. patent [4] and implemented on phenolic plant of the General Electric company in mount Vernon (United States).

Decomposition of technical CCP are in accordance with the scheme shown in Fig. 1.

The process is carried out in two stages.

The first stage is the decomposition of the CCP, which is carried out in three series set the reactor, and reaction heat is removed by cooling water in the tube space of the reactor and the circulation of the products of decomposition through the above reactor block with frequency 10 to 25 relative to the supplied CCP.

To increase the selectivity of the process in circulating products of decomposition served an additional amount of water and acetone, the latter depending on the load on the CCP serves to determine CCP - quantity of acetone and the number of technical GPK, t/h;

[CCP] is the concentration of CPC in the technical code of civil procedure, wt. share.

This technique is very important to maintain the selectivity of the process, which is determined also strictly maintained the temperature range in each of the three reactors 1-A, B, C 50 - 62oC, 62 - 57oC and 57 50oC, respectively, the conversion of CCP in 30 - 60%, 25 - 50% and 30 to 10%, respectively.

Since the reaction of the decomposition of the CCP is emitting a very large amount of heat applied to the reactor with a total surface area of heat transfer at least 30 - 35 m21 ton of 100% of the CCP. Common, given the extremely high risk decomposition reaction of the CCP, to design devices with a specific surface area of not less than 45 - 60 m21 tonne supplied 100% of the CCP.

Managing the stages of decomposition of the CCP is through the value of the temperature difference at the inlet and outlet specially installed on the output line of products from the reaction block mini-reactor 3 (calorimeter), and the stated size range is 4 - 16oC, which determines the concentration nerazlochennom CCP at the exit of the reactor R-1C from 0.6 to 2.3% wt

In the above Endpattern 45 - 2 min).

The second stage is the decomposition of dicumylperoxide cumene (DCT) is performed sequentially in two devices 4 and 7, representing the reactors displacement, and in the first of them is served aqueous ammonia to translate parts of sulfuric acid in NH4HSO4. Thus, the decomposition of the DCT is binary catalyst (H2SO4+ NH4HSO4) with strict maintenance of a ratio of the latter, and the temperature is 90 - 110oC in the apparatus 7. Heating products in the heat exchanger 6.

The decomposition of the CCP in reactors 1-A, B, C is carried out under atmospheric pressure, the DCT decomposition in the reactor 4 is carried out under atmospheric pressure, and the reactor 7 under a pressure of at least 2 ATM.

In the apparatus 8 is evaporation from the products of decomposition parts of acetone, which after condensation in the apparatus 10 as recycling is fed from the tank 10 by pump 11 in the reactor block decomposition of the CCP.

The above scheme shows the best current consumption. However, it has some serious drawbacks:

1) the use of reactors of large volume and large surface heat transfer (more than 50 m2/1 t of 100% notelist and installation;

2) the presence of 4 reactor operating at atmospheric pressure, leads to the necessity of using an additional pump 5 for supplying the reaction mass decomposition in the reactor DCT transformation (reactor 7), operating at elevated temperatures (greater than 90oC) and the resulting high pressure to prevent boiling acetone, having a boiling point (56oC) at atmospheric pressure;

3) in the reactor 4 is maintained at low temperatures due to the presence in the products of a sufficiently large number nerazlochennom CCP (0.5 to 2%), unsafe failure to comply with the ratio of H2SO4: NH4HSO4;

4) the exact dosage low flow water solutions of ammonia and H2SO4difficult and, as a consequence, this leads either to the formation of dimers of alpha-methylstyrene and complex phenols (if neonatally H2SO4), or to decrease the conversion of DCT (if preneutralization H2SO4). In both cases, the yield of the target products is reduced and accordingly increases the output of the waste - "phenolic resins";

5) due to the presence in the products of decomposition of H2SO4and NH4HSO4by evaporation of the acetone in the apparatus 8 is policereported in the specified device is largely occurring adverse reactions with formation of by-products and reduce the selectivity of the process. The above nepodozirana NH4OH sharply exacerbated the situation, resulting in the loss of up to 10 - 20 kg feedstock per 1 t of phenol (yield alpha-methylstyrene is reduced from 80% to 60% of theoretical.);

6) the reactor 7 at a very weak acid catalyst (H2SO4+ NH4HSO4) leads to the necessity of the use of technology for reactor decay DCT large volume (0.8 m3/1 t supplied technical CCP);

7) managing the process of decomposition of the CCP through the value of T ensures the safety of the process, however, does not provide selective reaction of decomposition of the DCT, because the analytical determination of GLC method of composition of the products (at the reactor exit 7) is a long procedure that will take several hours, whereas the fluctuation modes due to changes in load, changes in the composition of the catalyst occurs much more often and faster.

8) submission of acetone in the node decomposition of the CCP on the above algorithm leads to significant energy consumption for its condensation and the use of devices with large surface heat transfer, which also requires high capital investment for the purchase of equipment and its installation.

The aim of the present invention is as the expense of reductions in the volume of equipment in the construction of new facilities, simplifying technology while maintaining high selectivity of the process.

A schematic diagram is shown in Fig. 2.

Stage of decomposition of the CCP and CSD are sequentially merged in the reactor under the same pressure. The reaction of the decomposition of cumene hydroperoxide proceeds emitting extremely high amount of heat (380 kcal/kg), which is equivalent to raising the temperature to 700oC decomposition in the adiabatic reactor. To remove a specified amount of heat in industrial conditions, because the decomposition of cumene hydroperoxide takes place in a very short period of time (from 1 minute to 3 - 5 min) extremely important process parameter is the distribution of the total conversion of the CCP in each of the reactors. The distribution of the degree of conversion of the CCP in the reactor determines not only the process, but its effectiveness from the point of view of capital costs for construction of new and renovation of existing facilities.

For removal of the heat of decomposition of the CCP is in the products obtained by the decomposition of technical CCP and circulating through the reactor 1 - A, B, C, and the ratio of circulation of these products in relation to the supply of those is ashed which is determined depending on the number of technical GPK, supplied to the decomposition according to the following algorithm:

GAC= GCCP0,125[CCP] + (35/GCCP[CCP]),

where

GCCP, GAC- quantity supplied to the decomposition of technical CCP and acetone, t/h; [CCP} - concentration of CPC in the technical code of civil procedure, wt. share.

The decomposition process of the CCP is implemented in such a way that the conversion of CCP reactor 1 - A, B, C was 62 - 75%, 80 - 94%, 90 - 98% respectively. The temperature in said reactor is maintained in a well-defined range: reactor 1-A 57 - 82oC, 1-B - 65 - 82oC, 1-C 57 - 70oC.

The CPC concentration in the reactor exit 1 - C is maintained in the range of 0.1 to 0.45 wt.%, preferably 0.2 to 0.4 wt.%. at the same time, decomposition of the CCP in one pass is 17 to 28 hours as reactors are applied heat exchangers with a total specific surface 17 of 25 m3/1 t 100% CCP.

The decomposition products from the reactor 1-C through the heater 6 is transferred directly into the tube space of the reactor 7, where the DCT transformation and dimethylphenylcarbinol (DMPC) in the target products.

In the product line after the reactor 1-C water in an amount to provide 98% DCT transformation and DMPC in reaka management process decomposition DCT and DMFC after the point of mixing water with the products of decomposition in parallel with the second thread is set mini-reactor (calorimeter) largest temperature difference T2 , at the inlet and the outlet of which is set and controlled (supported) the temperature in the reactor 7. The temperature adjustment mode is cancelled by the magnitude of the temperature difference T = T1-T2 in the first and second calorimeter, and the value T is maintained in the range of 0.2 - 3oC.

To eliminate chemical losses during the Stripping of acetone on the entry of products into the evaporator is supplied alkaline agent in an amount to provide a translation of H2SO4neutral salts (sulfates), and as a neutralizing agent may be used Na2CO3, NH4OH, NaOH, but preferably aqueous ammonia, the concentration of 1 - 10% wt.

The present invention allows to solve several problems;

1) virtually no capital expenditure increases the performance of the existing equipment in 2 - 2.5 times. However, despite the significant intensification of the process, the selectivity of the process remains at maximum (output alpha - methylstyrene is 78 - 80% of theoretical.);

2) capital investment in the construction of new facilities is reduced in 2 - 2.5 times due to:

a) the reaction of decomposition of the CCP in reactors with low specific surface heat transfer (17 - 25 is R>
b) the reaction of decomposition of the DCT in one reactor instead of two by combining reactors in one unit operating at the same pressure;

C) the intensification of the process by the reaction of decomposition of the CCP under strictly defined conversion CCP, the multiplicity of circulation, temperature, and the temperature in each reactor is maintained at 10 to 15oC higher than in the prototype.

3) Energy costs for the process are reduced by reducing the number of recycle acetone and exclusion from the process circuit of the pump 5.

4) simplified procedure of decomposition of the DCT by eliminating the supply of ammonia and feed instead of the last of the water to regulate the acid-catalytic properties of H2SO4;

5) simplified procedure of decomposition due to the management process on the value of T = T1-T2 , which allows you to automatically maintain the high selectivity of the process at the stage of decomposition of the CCP, and at the stage of decomposition of the DCT;

6) neutralization of H2SO4before the acetone evaporator eliminates the leakage of unwanted side effects.

Along with the above new technology solves environmental pollutants 1-A, B, C, and the first reactor DCT decomposition, are excluded from the scheme.

Example 1 (comparative prototype). In the reactor unit consisting of three tubular reactors type total 10,08 m3continuously served the technical hydroperoxide cumene following composition, % wt.:

The cumene hydroperoxide - 82,500

The cumene - 12,721

Dimethylphenylcarbinol - 4,326

The acetophenone - 0,453

In the reactor, where circulating decomposition products, is served acetone in the number 5492 kg/hour and 16 kg/h of water. For the decomposition of used reactors with a total surface heat transfer 1254 m2that corresponds to the value of specific surface area of heat transfer for 1 tonne of 100% of cumene hydroperoxide 58 m2/t CCP.

The residence time in the reactor for the decomposition of the CCP 74 seconds. The temperature at the outlet of each of the three reactors installed in series respectively supported 58oC, 55oC, 50oC. Conversion of CCP to the outlet of each reactor is maintained at 38%, 73%, 85% respectively. The value of the differential temperature Delta T1 in the mini - reactor is maintained 5,6oC. At the inlet of the CCP in the reactor for the decomposition of the latter is mixed with the reaction mass decay in the ratio of 1 : 16 (kr is xida hydroperoxide is carried out in two sequential reactors displacement, the temperature in the first reactor is maintained at a low 58oC, in the second 93oC. In the first reactor eviction is served aqueous ammonia in the number of 33.8 kg/HR concentration of 5 % wt. so that the degree of neutralization of sulfuric acid to translate the latter into ammonium bisulfate was 50%.

The decomposition of the CCP in three reactors mixing and DCT in two reactors displacement is carried out at different pressure - atmospheric in the reactor for the decomposition of the CCP and the first reactor decomposition of the DCT, and 3 to 5 ATM. in the second reactor for the decomposition of the DCT,

The residence time in the reactor for the decomposition of the DCT is 420 seconds in the reactor 4 and 2030 seconds in the reactor 7.

Submission of acetone in the node decomposition GPC is carried out by Stripping of the reaction mass decomposition in a special apparatus operating under vacuum.

As a result of all reactions in the above reactors, receive: phenol - 13174,5 kg/h (output 99,2%); acetone - 8084,5 kg/h (output 98.9 per cent); alfamethylstyrene 54,4 kg/t of phenol, (exit alpha-methylstyrene 73,4 % of theoretical per filed DMFC); exit phenolic resin 59.2 kg/t of phenol; the consumption of IPA 1333 t phenol

Example 2. The example illustrates the increase in the manufacturer schemes operate under the same pressure, why all the reactors are connected in the upper part between itself and the total system pressure is 4 kg/cm2.

In the reactor for the decomposition of the CCP serves 60 t technical cumene hydroperoxide composition defined in example 1. Decomposition of technical GPC is carried out with quadratische circulation 26 and the temperature at the outlet of the reactor 68oC, 67oC and 60oC, respectively, to maintain them in the conversion of CCP 62%, 94%, 98%, respectively.

Node decomposition of the code of civil procedure of the apparatus of the Stripping of acetone from the reaction mass decomposition of the latter served in a number 6890 kg/h defined by the formula:

GAC= GCCP0,125 [CCP] + (35/GCCP[CCP]),

where

CAC, GCCP-quantity of acetone and technical GPK, t/h; [CCP] is the concentration of cumene hydroperoxide in the technical hydroperoxide, wt.share.

In the mini - reactor site decomposition is supported by the magnitude of the temperature difference T1 = 0,4oC.

In the supply line of products in the decomposition reactor DCT water quantity 482 kg/HR so that the concentration of the latter in the decomposition products at the outlet of the reactor is 1,63% wt. and time decomposition of the DCT is 485 seconds.

At the point poleca the value of the temperature difference T2 on the output. Moreover, the control process is carried out in terms of the absolute temperature difference T = T1-T2 = 0,65oC.

To eliminate chemical losses of target products in the machine Stripping of acetone in a line of input products in the specified device is served aqueous ammonia concentration of 5% wt. in the amount of 145 kg/hour.

The result: phenol - 30431,2 kg/hour (yield of 99.5%); acetone - 18769,7 kg/hour (yield 98.5 per cent); alfamethylstyrene 58,5 kg/t of phenol (yield alpha-methylstyrene 79.9 % of theoretical per filed DMFC); exit phenolic resin 54,2 kg/t of phenol; the consumption of IPA 1388 t of phenol.

Example 3. The example illustrates the process in the reactor reduced volume, reduced surface heat transfer and correspondingly low specific surface heat transfer.

The process is conducted as described in example 2 scheme. However, for apparatus used in example 3: the volume of the reactor system decomposition CCP 2.8 times; surface heat transfer within the same system and 3.5 times; specific surface heat transfer 3.4 times; the volume of the reactor system decomposition DCT 3 times less than those described in example 1.

In the reactor for the decomposition of the CCP pod is 26. In a circulating circuit composed of a reactor for the decomposition of the CCP, served 9.3 kg/hour of sulfuric acid. Decomposition of technical GPC is carried out at temperatures at the exit of the reactor 79oC, 75oC and 69oC, respectively, to maintain them in the conversion of CCP 77%, 96%, 98%, respectively.

Node decomposition of the code of civil procedure of the apparatus of the Stripping of acetone served recycle acetone in the number 4312 kg/h, which is determined by the formula indicated in example 2.

The residence time of the reaction products in the reactor for the decomposition of the DCT is 638 seconds.

The result: phenol - 13185,3 kg/h (output 99,4%); acetone - 8075,4 kg/h (output 98,8%); alfamethylstyrene 58,02 kg/t of phenol (yield alpha-methylstyrene 79.9% of theoretical per filed DMFC); exit phenolic resin 55,03 kg/t of phenol; the consumption of IPA 1329 so on phenol.

In the mini - reactor site decomposition is supported by the magnitude of the temperature difference T1 = 0,34oC.

The absolute value of the temperature difference T = T1-T2 = 0,66oC.

To eliminate chemical losses of target products in the machine Stripping of acetone in a line of input products in the specified device is served aqueous ammonia concentration of 5% wt. of 63 kg/hour, Theimer illustrates the process in the reactor, where the specific surface area of heat transfer is defined as 25 m2per ton of 100% of the CCP.

In the reactor for the decomposition of the CCP serves 26 t technical hydroperoxide caiola composition defined examples 1. The multiplicity of circulation is 26. In a circulating circuit composed of a reactor for the decomposition of the CCP is served 9.3 kg/hour of sulfuric acid. Decomposition of technical GPC is carried out at temperatures at the exit of the reactor 67oC, 66oC and 61oC, respectively, to maintain them in the conversion of CCP 62%, 87%, 94%, respectively.

Node decomposition of the code of civil procedure of the apparatus of the Stripping of acetone served recycle acetone in the number 4312 kg/h composition defined by the formula indicated in example 2.

The residence time of the reaction products in the reactor for the decomposition of the DCT is 640 seconds.

The result: phenol - 13188,5 kg/h (output 99,3%); acetone - 8078,9 kg/h (output 98.9 per cent); alfamethylstyrene 58,5 kg/t of phenol (yield alpha Mediterra 79.9% of theoretical per filed networking initiatives hosted by diff); exit phenolic resin 53,9 kg/t of phenol; the consumption of IPA 1328 t of phenol.

In the mini - reactor site decomposition is supported by the magnitude of the temperature difference T1 = 1,26oC. In a mini-reactor, the prescribed ass feedC.

The absolute value of the temperature difference T = T1-T2 = 0,72oC.

To eliminate chemical losses of target products in the machine Stripping of acetone you a line of input products in the specified device is served aqueous ammonia concentration of 5% wt. of 63 kg/hour, so that the degree of translation of the acid in the ammonium bisulfate in the acetone evaporator is 200%.

Example 5. The example illustrates the high selectivity of the process when the load changes on the node decomposition technical CCP.

In the reactor for the decomposition of the CCP serves 22 t technical cumene hydroperoxide composition defined in example 1. The multiplicity of circulation is 26. In a circulating circuit composed of a reactor for the decomposition of the CCP, served 7,2 kg/hour of sulfuric acid. Decomposition of technical GPC is carried out at temperatures at the exit of the reactor 72oC, 78oC and 67oC, respectively, to maintain them in the conversion of CCP 65%, 92%, 97%, respectively.

Node decomposition of the code of civil procedure of the apparatus of the Stripping of acetone served recycle acetone in the number 4192 kg/h composition defined by the formula indicated in example 2.

The residence time of the reaction products in the reactor for the decomposition of the DCT is T1 = 0,82oC.

In the mini-reactor, established after the supply of water in the reaction products at the outlet of the circulation loop, the magnitude of the temperature difference is 1,68oC.

The absolute value of the temperature difference T = T1-T2 = 0,86oC.

To eliminate chemical losses of target products in the machine Stripping of acetone in a line of input products in the specified device is served aqueous ammonia concentration of 5% wt. in the amount of 48 kg/hour, so that the degree of translation of the acid in the ammonium bisulfate in the acetone evaporator is 200%.

The result: phenol - 11156,4 kg/h (output 99,4%); acetone - 6815,7 kg/hour (yield 98.5 per cent); alfamethylstyrene to 58.1 kg/t of phenol (yield alpha-methylstyrene 79.9% of theoretical per filed networking initiatives hosted by diff); exit phenolic resin 55,14 kg/t of phenol; the consumption of IPA 1328 t phenol

Example 6. The example illustrates the high selectivity of the process when the load changes on the node decomposition technical CCP.

In the reactor for the decomposition of the CCP serves 35 t technical cumene hydroperoxide composition defined in example 1. The multiplicity of circulation is 26. In a circulating circuit composed of a reactor for the decomposition of the CCP, served 11,80 kg/hour of sulfuric acid. RAOC, respectively, to maintain them in the conversion of CCP to 70%, 93%, 97%, respectively.

Node decomposition of the code of civil procedure of the apparatus of the Stripping of acetone served recycle acetone in the number 4821 kg/h composition defined by the formula indicated in example 2.

The residence time of the reaction products in the reactor decay DCT 487 seconds.

In the mini - reactor site decomposition is supported by the magnitude of the temperature difference T1 = 0,64oC. In a mini-reactor, established after the supply of water in the reaction products at the outlet of the circulation loop, the magnitude of the temperature difference is 1.92oC.

The absolute value of the temperature difference T = T1-T2 = 1,27oC.

To eliminate chemical losses of target products in the machine Stripping of acetone in a line of input products in the specified device is served aqueous ammonia concentration of 5% wt. in the amount of 80 kg/hour, so that the degree of translation of the acid in the ammonium bisulfate in the acetone evaporator is 200%.

The result: phenol - 17751 kg/h (output 99,4%); acetone - 10906 kg/hour (yield of 99.1%); alfamethylstyrene to 58.6 kg/t of phenol (yield alpha-methylstyrene 79.9 % of theoretical per filed networking initiatives hosted by diff); exit phenolic resin 54,1 the sa with the composition of the technical code of civil procedure, supplied to the node decomposition.

In the reactor for the decomposition of the CCP serves 35 t technical gasoperated cumene, of the following composition, %:

The cumene hydroperoxide is 91.5

The cumene - 2,0

Dimethylphenylcarbinol - 5,5

The acetophenone - 1,0

The multiplicity of circulation is 26. In the circulation loop is served 9.3 kg/hour of sulfuric acid. Decomposition of technical GPC is carried out at temperatures at the exit of the reactor 71oC, 67oC and 61oC, respectively, to maintain them in the conversion of CCP to 75%, 94%, 98%, respectively.

Node decomposition of the code of civil procedure of the apparatus of the Stripping of acetone served recycle acetone in the number 4444 kg/h composition defined by the formula indicated in example 2.

The residence time of the reaction products in the reactor for the decomposition of the DCT is 640 seconds.

In the mini - reactor site decomposition is supported by the magnitude of the temperature difference T1 = 0,49oC. In a mini - reactor, established after the supply of water in the reaction products at the outlet of the circulation loop, the magnitude of the temperature difference at 1.38oC.

The absolute value of the temperature difference T = T1-T2 = 0,89oC.

To eliminate chemical losses of target products in apparel 5% wt. of 63 kg/hour, so that the degree of translation of the acid in the ammonium bisulfate in the acetone evaporator is 200%.

The result: phenol - 14610,2 kg/h (output 99,3%); acetone - 8972,3 kg/h (output 98.9 per cent); altmeister 56,6 kg/t of phenol (yield alpha-methylstyrene 79.9% of theoretical per filed networking initiatives hosted by diff); exit phenolic resin 62,51 kg/t of phenol; the consumption of IPA 1335 t of phenol. The results are shown in the table.

Method for production of phenol, acetone and a-methylstyrene acid decomposition of technical cumene hydroperoxide in three reactors installed in series mixing for the decomposition of cumene hydroperoxide at high pressure and temperature to feed them in acetone and the mixture containing dicumylperoxide that is decomposed in the reactor displacement with the addition of water, followed by neutralization products of decomposition, evaporation and recycling of acetone in a reactor mixing and subsequent separation of the reaction products, characterized in that the decomposition of cumene hydroperoxide and dicumylperoxide coming together with the technical hydroperoxide and optionally produced from cumene hydroperoxide and dimethylphenylcarbinol in the reactor mixing, carried out at the same tablesave addiction

< / BR>
where GGPTO, GandC- the amount fed to the decomposition of technical CCP and acetone, t/h;

[CCP] is the concentration of CPC in the technical code of civil procedure, wt. share

keep the temperature in the first reactor of a mixture of 57 82oWith the second 65 - 82oAnd in the third 57 - 67oWith a total specific surface 17 of 25 m2per 1 ton of 100% of the CCP with the conversion of cumene hydroperoxide in the first reactor of a mixture of 62% and 75%, in the second 80 - 94% and in the third 90 - 98%, maintain the temperature difference between the calorimeter installed at the outlet of the third reactor mixing 1 to 3oWith serving water in line in front of the reactor displacement for the decomposition of dicumylperoxide providing water concentration in the reaction products of 1,3 - 2.0 wt.%, maintain a temperature difference of 1 to 3oWith the calorimeter installed on the system before the reactor displacement after the point of water supply, maintain the temperature difference between the temperature in the calorimeter 0.2 to 3oFrom serving in the line of reaction products in front of the apparatus to the evaporation of the acetone aqueous ammonia with a concentration of 1 to 10 wt.% in quantities that ensure the transfer of sulphuric acid in high salt.

 

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21 cl, 14 tbl, 153 ex

FIELD: industrial inorganic synthesis.

SUBSTANCE: aqueous carbamate solution leaving urea recovery section at a certain temperature is decomposed by indirect heat exchange with flowing heat carrier having specified temperature. Temperature difference between aqueous carbamate solution and heat carrier is thus decreased to a value not exceeding 70°C, preferably to a value within a range of 20-40°C. Aqueous carbamate solution, prior to be fed into decomposition apparatus, is preheated in heat exchanger by stream produced in evaporation zone containing ammonia and carbon dioxide in vapor phase.

EFFECT: increased efficiency of apparatuses designed for decomposition of recycled carbamate solution.

6 cl, 2 dwg

FIELD: organic chemistry, biochemistry, medicine, pharmacy.

SUBSTANCE: invention relates to new aminobenzophenones of the formula (I):

or their pharmaceutically acceptable salts. These compounds elicit properties of inhibitors of cytokines secretion, in particular, 1β-interleukin (IL-1β) and tumor necrosis α-factor (TNF-α) and to secretion of polymorphonuclear superoxide that are useful for treatment of inflammatory diseases, for example, skin diseases, such as psoriasis, atopic dermatitis. In the formula (I) R1 is taken among the group consisting of halogen atom, hydroxy-, mercapto-group, trifluoromethyl, amino-group, (C1-C3)-alkyl, (C2-C3)-olefinic group, (C1-C3)-alkoxy-, (C1-C3)-alkylthio-, (C1-C6)-alkylamino-group, (C1-C3)-alkoxycarbonyl, cyano-group, carbamoyl, phenyl or nitro-group under condition that when R1 means a single substitute then it at ortho-position, and when R1 means more one substitute then at least one substitute of R1 is at ortho-position; R2 means one substitute at ortho-position being indicated substitute is taken among the group consisting of (C1-C3)-alkyl, (C1-C3)-alkoxy-group; R3 means hydrogen, halogen atom, hydroxy-, mercapto-group, trifluoromethyl, amino-group, (C1-C3)-alkyl, (C2-C3)-olefinic group, (C1-C3)-alkoxy-, (C1-C3)-alkylthio-, (C1-C6)-alkylamino-group, (C1-C3)-alkoxycarbonyl, phenyl, cyano-, carboxy-group or carbamoyl; R4 means hydrogen atom or (C1-C3)-alkyl; Q means a bond or -SO2-; Y means (C1-C15)-alkyl, (C3-C10)-carbocyclic group or phenyl being each of them can be substituted optionally with one or some similar or different substitutes designated by the formula R5; R5 means halogen atom, (C1-C4)-alkyl, amino-, (C1-C3)-alkoxy-group, (C1-C3)-alkoxycarbonyl or -COOH; X means oxygen or sulfur atom. Also, invention relates to a pharmaceutical composition and to a method for treatment and/or prophylaxis of inflammatory diseases.

EFFECT: valuable medicinal properties of compounds and composition.

9 cl, 2 sch, 2 tbl, 29 ex

FIELD: organic chemistry, medicine, pharmacology.

SUBSTANCE: invention relates to new derivatives of carbamic acid esters of the general formula (I):

and their pharmaceutically acceptable salts eliciting activity with respect to metabotropic glutamate receptors mGlu of group I that can be used for treatment of acute and/or chronic neurological disorders. In the general formula (I) R1 means hydrogen atom or (C1-C7)-alkyl; R2 and R2' mean independently of one another hydrogen atom, (C1-C7)-alkyl, (C1-C7)-alkoxy-group, halogen atom or trifluoromethyl; X means oxygen (O), sulfur (S) atom or two hydrogen atoms not forming a bridge; A1/A2 mean independently of one another phenyl or 6-membered heterocycle comprising 1 or 2 nitrogen atom; B represents group of the formula:

wherein R3 means (C1-C7)-alkyl and others; Y means -O-, -S- or a bond; Z means -O- or -S-; or B means 5-membered heterocyclic group of formulae: (a) , (b) , (c) or (d) . Also, invention relates to methods for preparing compounds and to a medicinal agent based on thereof.

EFFECT: improved preparing methods, valuable medicinal properties of compounds.

22 cl, 1 tbl, 2 sch, 78 ex

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