Highly selective method for production of phenol and acetone (process fan 98)

 

(57) Abstract:

The invention relates to the production of phenol and acetone by decomposition of technical cumene hydroperoxide (CHP). The decomposition of the CCP to phenol, acetone and methylsterol is carried out in the presence of sulfuric acid so that the rate of heat release and the rate of heat removal is balanced in each of the three reactors installed in series and decomposition of GIC flows in almost isothermal conditions: 47-50oWith in the first reactor, 50-48oWith the second reactor and 48-50oC in the third reactor. Accordingly, the conversion of CCP reactor maintained within the range of 43-50%, 67-73% 78-82%. The concentration of sulfuric acid at the stage of decomposition of the CCP is 0,018 at 0.020 wt.%. The decomposition of the CCP carried out in a reaction medium containing equimole number of phenol and acetone, 10-12 wt.% cumene and 5-8 wt.% additional input acetone per technical CCP. In the second stage of the process perform the decomposition of dicumylperoxide (DCT) and dimethylphenylcarbinol (DMPC) in multiple reactor displacement in non-isothermal mode at a controlled rise in temperature from 120 to 146oC. the Depth of the DCT transformation and DMFC regulate by changing the temperature Control is carried out installed in each of the sections of the reactor thermocouple and the resulting temperature profile is compared with tempera - cultural profile of the kinetic model on the basis of the values of T in each of the sections of the reactor. According to the results of the variance adjustment process mode. The result is improved economic performance, reduced consumption of raw materials. table 2., 4 Il.

This invention relates to the field of petrochemical synthesis, in particular to a method for production of phenol, acetone and alpha-methylstyrene (AMS) Kukolnik method. The process involves a few basic steps that determine its selectivity:

1. The oxidation of cumene (IPA) oxygen to cumene hydroperoxide (CHP);

2. Acid (using H2SO4) decomposition obtained CCP;

3. Separation of the products of decomposition of the CCP method multistage rectification.

This invention relates to a process of acid decomposition of the CCP and, in particular:

to improve expenditure process indicators - reduction of consumption of raw materials;

to improve the security of decomposition of the CCP due to the equality of rates of heat generation and heat removal;

reduction of steam consumption and the new principle of control the second stage of the process - turning dicumylperoxide (DCT) and dimethylphenylcarbinol (DMPC);

reduce chemical losses of target products at the time of their separation, d is the production of phenol and acetone by acid decomposition of technical cumene hydroperoxide (CHP). The main difference between the methods is in the use of various reaction medium in which the reaction is carried out, and the mode of removal of a significant amount of heat (380 kcal/kg), generated by decomposition of the CCP.

As a reaction medium, in the processes which achieved the best selectivity is used equimolar mixture of phenol and acetone, which is added from 15 to 30 Rel.% acetone per technical GPC [U.S. Patent 5530166, 1996; U.S. Patent 4358618, 1982]. This allows to achieve high selectivity in the process, often defined by the amount of yield valuable by-product of alpha-methylstyrene (AMS), which is formed from dimethylphenylcarbinol (DMPC) present in the technical cumene hydroperoxide. The release of AMC [U.S. Patent 5530166, 1996; U.S. Patent 4358618, 1982] reached about 80%.

According to the method of heat released during the decomposition of the CCP, the processes are divided into:

1. The process of evaporation of acetone [U.S. Patent 2663735, 1953] and return last in the reactor;

2. The process with the removal of the heat of the cooling water.

Adiabatic decomposition of 100% of the CCP under the influence of an acid catalyst temperature increases priblizitelino hazardous processes, and, accordingly, the issue of combining the speed of heat dissipation and heat removal is an important task of the safety improvement process.

In [U.S. Patent 2663735, 1953], where the heat of reaction is given by evaporation of the acetone, the process of heat generation and heat removal fully combined. The amount of emitted during decomposition 1 t GPK heat completely removed 2,2 - 3,0 t fed to the reactor acetone. The vaporized acetone is condensed outside the reactor and continuously returned to him. Due to this, the reactor operates in the desired from the standpoint of security mode thermal stability. However, the mode of thermal stability is achieved only under conditions of very high compared with other processes, the concentration of sulfuric acid is 0.12 to 0.13 wt.% (this is a forced measure, as supplied to the decomposition products in such large quantities of acetone dramatically reduces the activity of sulfuric acid, which is a catalyst for the decomposition of the CCP). The result of the high concentration of acid is the low yield of the target products and the high content of trace contaminants (to 0.15 wt. %), such as oxide mesityl, hydroxyacetone, 2-methylbenzofuran, greatly reducing the quality of the phenol. Required from the point of view of chemistry Ijima, because of a sharp reduction in the degradation rate of the CCP begins its accumulation in the lower part of the reactor with subsequent thermal explosion. I.e., lowering the concentration of sulfuric acid reactor enters the mode of thermal instability. In fact, the process has a thermal resistance only under conditions of high concentrations of sulfuric acid, but the latter leads to a low selectivity of the process, i.e. the principle of thermal stability (security) and the principle of achieving high selectivity are interconnected in an insoluble contradiction in the process with the evaporating acetone.

In patents [U.S. Patent 5530166, 1996; U.S. Patent 4358618, 1982 ; U.S. Patent 5254751, 1993] heat of reaction is removed repeatedly circulating through the heat exchangers products of the reaction, the reaction mass decomposition - PMP), cooled by water. The heat exchangers, the number of which, as a rule, from two to six, are essentially reactors, which is the decomposition of the CCP. What is the composition of the reaction medium, the range of acid concentration, temperature profile, and, accordingly, the distribution of the conversion of CCP reactor depends on what type of process is thermally stable (i.e., safe) is consequently established reactors, and the greater the temperature difference between the first and second reactors, the lower thermal stability of the process. In fact, the more neizotermichnost is the decomposition of the CCP, the process stronger moves in a more dangerous mode.

The closest technical solution and achieve practical results of the present invention is a process patent [U.S. Patent 5530166, 1996], which is taken as a prototype.

In [U.S. Patent 5530166, 1996] decomposition of the CCP and the DCT is performed in two stages, with the reactor for the decomposition of the CCP reactors mixing and reactor conversion DCT (reactor displacement) are running at the same increased pressure from 2 to 10 ATM (Fig. 1).

The decomposition of the CCP and CSD is in equimole mixture of phenol-acetone containing up to 12 wt.% cumene. To reduce the acid properties of sulfuric acid and, correspondingly, increase the yield of the target products (phenol, acetone and AMS) in the reaction medium additionally served acetone algorithm

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

where GAC. GCCP- costs of additional acetone and technical CCP, respectively, kg h;

[CCP] is the concentration of CPC in technical Budgeting CCP depending on the load is maintained in the first reactor 62-75%, in the second 87-94%, in the third 94-98%, and the temperature, respectively, 67-79oC, 78-67oC and 69-60oC. the Above algorithm filing an additional amount of acetone, the temperature distribution and conversion of CCP reactor allows to operate the process in a wide range of loads.

The CPC concentration at the outlet of the reactor stage 1 is 0.14-0.43 wt.%, which corresponds to the value of T1in the calorimeter, which manage the first stage of the process, equal 1-3oC.

In the decomposition reactor DCT serves water in an amount to provide a concentration of water in the reaction products of 1,3-2.0 wt.%. Control of the reactor of the second stage is carried out through the difference of the temperatures T2equal to 1-3oC calorimeter installed in the line before the reactor decomposition of the DCT. In the reactor, decomposition of the DCT process is isothermal and at different loads supported by various temperature from 94oC at low loads to 99oC under high loads. The management process as a whole (1 and 2 stage) through the value of the temperature difference between the two available in the scheme by the calorimeters, and the specified value of the temperature difference pok is Ki acetone in-line flow before the evaporator is fed ammonia to sulfuric acid in a neutral salt (NH4)2SO4. As a result, in the process reach a high enough output AMS 78,8-79,6 theory.%.

The aim of the present invention is to obtain a higher yield of the target products by increasing the release of the AMC to the level of 85-87% and reduce chemical losses in columns separation of the products of decomposition, increase the security of the process by carrying out the decomposition of the CCP in conditions close to isothermal, reducing energy costs in the process by reducing the number of recycled acetone and heat recovery reactor decomposition of the DCT and DMFC, achieve constant DCT conversion in the second stage of the process when changing loads and fluctuations in operating parameters, the selective reduction of losses at the stage of separation of the products of decomposition.

This goal is achieved through changes in the composition of the reaction medium in comparison with the prototype, changes in temperature conditions in the first and second stages, changes in the conversion of CCP in reactors 1 stage of change algorithm to control the reactor in the second stage of the process (Fig.2).

The decomposition process of the CCP and CSD in this invention is carried out as in the prototype in two stages.

Persitara - of sulfuric acid. The amount of sulfuric acid is maintained in strict correlation with respect to the amount supplied to the decomposition of technical CCP so that its concentration in the reaction medium was not lower than 0,018 wt.% and not more than 0.02 wt.% in the calculation of the reaction mass decomposition. The content of cumene in technical CCP is 10-12 wt.% in the calculation of the technical CCP.

At the first stage of the process served the additional amount of acetone in the amount not exceeding 8 Rel.% in the calculation of the number of submitted technical CCP. The number of additional fed acetone is maintained within narrow limits from 5 to 8 Rel.% in the calculation of the technical code of civil procedure, which enables to achieve the desired magnitude of conversion of CCP at variable loads and fluctuations of the operating parameters. The rate of heat removal and heat dissipation in each of the three reactors installed in series were balanced so that the decomposition of the CCP with the simultaneous synthesis of DCT proceeded in nearly isothermal conditions in the first 47-50oC, in the second - 50-48oC and in the third 48-50oC conversion of CCP reactor 42-50%, 67-73% 78-82%, respectively. The temperature in said reactor is implemented in terms close to isothermal. The above distribution of the transformation of the CCP and the reactor temperature allows for a certain speed of decomposition of the CCP to equalize the heat release rate and the rate of heat removal. This allows you to make the process much more secure because only balanced by warm at all points of the reactor processes classified as safe.

The exception in the reactor zones with increased temperature observed by traditional methods of decomposition [U.S. Patent 5530166, 1996; U.S. Patent 4358618, 1982; U.S. Patent 2663735, 1953], leads to the additional advantage of reducing the rate of formation of unwanted side products (AMS dimers and complex phenols), which improves the selectivity of the stage of decomposition of the CCP and, consequently, of the whole process.

The second stage of the process is carried out in multiple reactor displacement. The concentration of acid in the second stage of the process is supported 0,09-0,10 wt. % (based on the reaction mass decomposition. Decomposition of the DCT and dimethylphenylcarbinol (DMPC) in the second stage is carried out under non-isothermal controlled rise in temperature from 120 to 146oC and control the depth into the translation of sulfuric acid in NH4HSO4when variable loads, and temperature control is carried out by installing in each of the sections of the reactor thermocouple, and the resulting temperature profile is compared with the desired kinetic model of the temperature profile on the basis of the values of T in each of the sections of the reactor, and on the basis of these deviations adjustment of the amount advanced in the reactor water temperature and degree of translation of sulfuric acid in NH4HSO4and the reaction is stopped by cooling and neutralization when 0,05-0,01 wt.% DCT in the reaction mass decomposition remains neprevzaidennymi.

In the reactor flows through the main reaction is the transformation of the DCT to phenol, acetone and AMS and side - turning DMFC in AMS, which is a valuable byproduct of the process, because it can be either converted into cumene and, accordingly, returned to the process at the stage of receipt of code of civil procedure, or may be provided as a commercial product.

Along with the target products of the process - phenol, acetone and AMS in the reactor are formed of undesirable by-products - AMS dimers and complex phenols.

It is believed that the formation of by-products flows through Klah is th link of AMC with education carbocation A

< / BR>
and the subsequent transformation of A complex phenols and dimers AMC:

< / BR>
Our studies have shown that reactive particle is not above Carbonia-ion, and formed oxanabol ion:

< / BR>
when interacting with whom phenol and DMFC formed dimers AMC and complex phenols. I.e. reactive particle is not AMC, and the molecule DMFC.

We established the mechanism of the reaction was allowed to take another look at the conditions of the reaction conversion DMPC in the reactor DCT.

In fact, the process sets the balance

< / BR>
On the specified position of the equilibrium between 1 and 2 reactive and directionspanel particles, as shown by our studies, is affected by two key factors - the structure of the solvent (in relation to the process of the reaction medium composition and temperature. Found theoretical evidence for the reaction mechanism has allowed to establish the conditions under which the equilibrium is shifted in the direction of the target product - AMS.

Offset the above balance has reduced the number neprevyshenie DMFC 3-4 times, reduce the formation of unwanted POI process. Simultaneously with the above-mentioned decrease in the number DMFC at the exit of the reactor DCT allows to reduce the number of unwanted side products formed in the columns of the separation of the products obtained from 15-17 kg/t of phenol up to 8-10 kg of phenol, which is equivalent to reducing the consumption of IPA 7-8 kg/so

In the process of our research, it was found that thermal effect decomposition of the DCT is 214 kcal/kg found Using thermal effect of the reaction was proposed to carry out the process of decomposition of the DCT non-isothermal manner, as shown in Fig. 3.

Depending on the amount of heat obtained by the decomposition products in heater H-2 (see process flow of Fig. 2), the temperature profile in the reactor DCT may have a fundamentally different nature, i.e. isothermal, non-isothermal and intermediate between the above two modes, as shown in Fig. 3.

The final output of the AMS, despite the equality of the temperatures at the outlet of the reactor for the case of T-1 and T-2 and for the case of T-2 and T-3, in which the average temperature in the reactor are the same, turn out significantly different. The worst results are obtained for the case of T-1, where the temperature in the reactor is prakticheskie results (output AMS about 85-87 theory.%), when the process is non-isothermal manner (curve T-2). Mode T-3, in which the average temperature equal to the average temperature regime T-2, out intermediate between isothermal and non-isothermal process results output AMS about 78-80 theory.%.

Maintain a consistently high output AMS in the reactor DCT in each of its sections is mounted thermocouple and the resulting temperature profile is compared with the optimal temperature profile obtained in the developed kinetic model. The deviation of the temperature profile at the incomplete transformation DCT or DCT conversion exceeds the maximum in the reactor changes the concentration of water in order to return runaway temperature profile in the initial state, as shown in Fig. 4.

In "hard" mode 2 in the reactor served an additional amount of water, which reduces the acidic properties of the catalyst and reduces the temperature profile in the direction of the optimum.

When the incomplete DCT transformation (mode 3) in the reactor reduces the amount of water in it and increases the temperature in the heater installed before the reactor DCT. This allows to increase the speed R is th 1 corresponds to the optimal curve changes in the concentration of da (Fig. 4B, curve 1), "hard" mode meets the curve 2, "soft" mode - curve 3.

Distinctive features of the developed process from prototype [U.S. Patent 5530166, 1996] are:

1. The decomposition process of the CCP in the reactor mixing is carried out at the expense of balanced speed heat generation and heat removal, i.e., in conditions very close to isothermal, thus ensuring that the process is in a safe environment;

2. The process of decomposition of the DCT in the reactor displacement is carried out under non-isothermal controlled rise in temperature from 120 to 146oC and control the depth of the DCT transformation and DMFC by simultaneous changes in the concentration of water in the products of decomposition, temperature and degree of translation of sulfuric acid in NH4HSO4when variable loads, and temperature control is carried out by installing in each of the sections of the reactor thermocouple, and the resulting temperature profile is compared with the desired kinetic model of the temperature profile on the basis of the values of T in each of the sections of the reactor, and on the basis of these deviations adjustment of the amount advanced in the reactor water temperature and degree of translation sulfuric Ki is and reactor decomposition of the DCT and DMFC reduced energy costs in the process;

4. Due to changes in the composition of the reaction medium and changes the control algorithm reactor in the second stage of the process yield valuable by-product of AMS increases up to 85-87 theory.%.

The advantages and differences of the developed technology are demonstrated by examples 1-11 (summary table examples table. 1).

Example 1 (comparative prototype).

In the reactor unit consisting of three series-connected reactors, tubular type, at high pressure 2-10 bar served 72 t/h technical CCP the following composition, wt.%:

the cumene hydroperoxide - 82,9

the cumene to 12.0

dimethylphenylcarbinol - 4.2V

the acetophenone - 0,6

demolitioned - 0,3

In recirculating flow decomposition products are also continuously fed acetone in accordance with the stated algorithm in the number 9976 kg/h ( ~ 12,16% of the amount of the CCP).

As a result of introducing into the reactor an additional amount of acetone, the reaction medium has a composition characterized by a molar ratio of phenol : acetone : cumene, equal to 1 : 1,42 : 0,22.

In recirculating flow decomposition products are also continuously fed sulfuric acid at a rate of 21 kg/h (the content of reaction what about the second 89,6%, in the third of 94.5%, and the temperature, respectively, to 75.8oC, 72,4oC and 63,1oC.

The CPC concentration at the outlet of the reactor 1 stage is to 0.21 wt.%, which corresponds to the value of T1in the calorimeter, which is controlled by the first stage of the process, 1.59oC.

The decomposition formed in the circuit DCT is carried out in adiabatic two-reactor displacement. In the line feeding the feedstock into the reactor decomposition of the DCT is continuously fed water in the amount of 716,6 kg/HR so that the concentration at the outlet of the reactor was 1.91 wt.%.

In the decomposition reactor DCT supported the same composition as the reaction medium, i.e., the ratio of phenol : acetone : cumene, as in a reactor for the decomposition of the CCP.

Control of the reactor of the second stage is conducted through the difference of the temperatures T2equal to 1.34oC calorimeter installed in the line before the reactor decomposition of the DCT. In the reactor, decomposition of the DCT process is isothermal at a temperature of 99oC. Management process in General (1 and 2 stage) through the value of the temperature difference between the two available in the scheme of the calorimeters, the specified amount of time and decomposition of the CCP in the reaction medium acetone is excreted in the evaporator, established after the reactor decomposition of the DCT. Whisked into the evaporator and condensed in the refrigerator acetone is sent to recycling to the stage of decomposition of the CCP.

To reduce non-selective loss of target products (phenol and AMC) in the evaporator is fed an aqueous solution of ammonia for translation of sulfuric acid in a neutral salt (NH4)2SO4.

The release of AMC after the stage of decomposition is 78,6 theory.%.

Example 2.

Technical CCP composition shown in example 1, in the amount of 72 t/h is fed to the stage of decomposition performed, as given in the description of the process diagram above.

The decomposition of the CCP is carried out in a reaction medium containing equimole amount of acetone and phenol, 12% of cumene and 8 Rel.% added acetone per technical CCP. In the reaction medium is supported by the molar ratio of phenol : acetone : cumene, equal to 1 : 1,28 : 0,22.

The consumption of sulfuric acid is 16.6 kg/h, the concentrations of sulfuric acid in the reaction mass corresponds to at 0.020 wt.%.

Conversion of CCP is maintained in the first reactor of 50%, in the second 69,0%, in the third 81,16%, and the temperature, respectively, 48,2oC; 48,3oC and 49,1approvedat in multiple reactor non-isothermal displacement in a controlled rise in temperature from 120 to 137oC, equipped with a system for independent force maintain the desired temperature in each of the sections.

In the line feeding the feedstock into the reactor decomposition of the DCT is continuously fed water in the amount of 418,9 kg/HR so that the concentration at the outlet of the reactor amounted to 1.4 wt.%. and an aqueous solution of 5% ammonia in the amount of 57.5 kg/hour, in order to provide a degree of translation of sulfuric acid in NH4HSO4equal to 50%.

Additionally entered on the stage of decomposition of the CCP in the reaction medium acetone is excreted in the evaporator, established after the reactor decomposition of the DCT. Whisked into the evaporator and condensed in the refrigerator acetone is sent to recycling to the stage of decomposition of the CCP. To reduce non-selective loss of target products (phenol and AMC) in the evaporator of the distillation of additional cumene is fed an aqueous solution of ammonia for translation of sulfuric acid in a neutral salt (NH4)2SO4.

The release of AMC after the stage of decomposition is 85.6 theory.%.

Example 3.

The decomposition process of the CCP is carried out analogously to example 2 with the difference that the decomposition is served technical CCP the following composition. wt.%:

the cumene hydroperoxide - 90,3
It is maintained in the first reactor 49,6%, the second - 67.0 per cent, in the third - 78,9%, and the temperature, respectively, 48,5oC; 49,5oC and 50.0oC.

Decomposition of the DCT is carried out in multiple reactor non-isothermal displacement in a controlled rise in temperature from 120 to 143oC, equipped with a system for independent force maintain the desired temperature in each of the sections.

In the line feeding the feedstock into the reactor decomposition of the DCT is continuously fed water in the amount of 198,7 kg/HR so that the concentration at the outlet of the reactor amounted to 1.4 wt. % aqueous solution of 5% ammonia in the number of 60.3 kg/h in order to provide a degree of translation of sulfuric acid in NH4HSO4equal to 50%.

The release of AMC after the stage of decomposition was 85.1 theory.%.

Example 4.

The process is carried out analogously to example 2 with the difference that in the circulating stream of decomposition products is served 15,1 kg/hour of sulfuric acid, which leads to reduction of its concentration in the reactor for the decomposition of the CCP to 0,018 wt. % (based on the reaction mass decomposition.

Conversion of CCP is maintained in the first reactor to 48.8% in the second 67.0 per cent, in the third of 79.6%, and the temperature, respectively, 48,40oC; 49,1oC and 49.9oC.

oC, equipped with a system for independent force maintain the desired temperature in each of the sections.

The release of AMC after the stage of decomposition is 85,8 theory.%.

Example 5.

The decomposition of the CCP carried out analogously to example 2 with the difference that the decomposition is carried out in a reaction medium, in which is supported the molar ratio of phenol : acetone : cumene, equal to 1 : 1,19 : 0,22, which corresponds to 5 Rel.%. added to acetone in the calculation of the technical CCP.

The concentration of sulfuric acid in the reaction mass corresponds 0,018 wt. % (based on the reaction mass decomposition.

Conversion of CCP is maintained in the first reactor to 50.0% in the second 68,8%, in the third 81,7%, and the temperature, respectively, 47,0oC; 48,3oC and 48,9oC.

Decomposition of the DCT is carried out in multiple reactor non-isothermal displacement in a controlled rise in temperature from 120 to 135oC, equipped with a system for independent force maintain the desired temperature in each of the sections.

The release of AMC after the stage of decomposition is 85,7 theory.%.

Example 6.

The decomposition of the CCP carried out analogously to example 4 differs in the first reactor to 44.0%, in the second 67.0 per cent in the third 77,1%, and the temperature, respectively, 50,0oC; 50,0oC and 48.6oC.

Decomposition of the DCT is carried out in multiple reactor non-isothermal displacement in a controlled rise in temperature from 120 to 137oC, equipped with a system for independent force maintain the desired temperature in each of the sections.

The release of AMC after the stage of decomposition is 85.6 theory.%.

Example 7.

The decomposition of the CCP carried out analogously to example 4 with the difference that the material is 54 t/h, i.e. 25% less than in the prototype.

Conversion of CCP is maintained in the first reactor to 50.0% in the second 72,9%, in the third 81,9%, and the temperature, respectively, 50,0oC; 49,2oC and 49.0oC.

Decomposition of the DCT is carried out in multiple reactor non-isothermal displacement in a controlled rise in temperature from 120 to 137oC, equipped with a system for independent force maintain the desired temperature in each of the sections.

The release of AMC after the stage of decomposition is 85,5 theory.%.

Example 8.

The decomposition of the CCP carried out analogously to example 4 with the difference that the reaction mass decomposition of the CCP is I DCT amounted to 2.0 wt.%.

The process of decomposition of the DCT is carried out under non-isothermal controlled rise in temperature from 129 to 146oC.

The release of AMC after the stage of decomposition is 87,0 theory. %.

Example 9.

The decomposition of the CCP carried out analogously to example 7 with the difference that the reaction mass decomposition of the CCP before the supply of raw materials to the DCT decomposition is introduced 629,0 kg/h of water so that its concentration in the reactor decay DCT amounted to 1.7 wt.%.

The process of decomposition of the DCT is carried out under non-isothermal controlled rise in temperature from 125 to 142oC.

The release of AMC after the stage of decomposition makes 86.4 theory.%.

Example 10.

The decomposition of the CCP carried out analogously to example 2 with the difference that the reaction mass decomposition of the CCP before the supply of raw materials to the DCT decomposition is introduced 886,0 kg/h of water so that its concentration in the reactor decay DCT amounted to 2.0 wt.%. The process of decomposition of the DCT is carried out under non-isothermal controlled rise in temperature from 129 to 146oC.

The release of AMC after the stage of decomposition is 86,8 theory.%.

Example 11.

The decomposition of the CCP carried out analogously to example 9 with the difference that in the reaction mass of restore decomposition of the DCT was 1.7 wt%. The process of decomposition of the DCT is carried out under non-isothermal controlled rise in temperature from 125 to 142oC.

The release of AMC after the stage of decomposition is 86,3 theory.%.

Highly selective method to produce acetone and phenol by acid digestion of technical cumene hydroperoxide (CHP) in the three reactors installed in series mixing at an elevated pressure of 2 to 10 atmospheres and elevated temperature flow in the reactor an additional amount of acetone per filed code of civil procedure, the decomposition of dicumylperoxide (DCT) in the reactor displacement at a temperature of 94 - 99oC, decomposition of the CCP largest T1= 1 - 3oC, control of reactor decay DCT largest T2= 1 - 3oC calorimeter installed before the reactor decomposition of the DCT, and maintaining the temperature difference T1and T2between calorimeters 0.2 to 3oC, characterized in that the decomposition process of the CCP is carried out so that the heat release rate and the rate of heat removal in each of the three reactors installed in series were balanced so that the decomposition of the CCP with the simultaneous synthesis of DCT proceeded in an almost isothermal conditions 47 - 50otoruses 43 - 50, 67 - 73 and 78 - 82%, respectively, and the concentration of sulfuric acid in the first stage of the process is supported 0,018 at 0.020 wt.%, and in the second stage - 0,09 - 0,10 wt.% in the calculation of the reaction mass and the decay of the CCP and DCT is carried out in a reaction medium containing equimole number of phenol and acetone, 10 - 12 wt.% cumene and 5 - 8 Rel.% additional input acetone in the calculation of the technical code of civil procedure, and the decomposition of the DCT and dimethylphenylcarbinol (DMPC) in the second stage is carried out in multiple reactor non-isothermal displacement in a controlled rise in temperature from 120 to 146oC and control the depth of the DCT transformation and DMFC by simultaneous changes in the concentration of water in the products of decomposition, temperature and degree of translation of sulfuric acid in NH4HSO4when variable loads, and temperature control is carried out by installing in each of the sections of the reactor thermocouple and the resulting temperature profile is compared with the desired kinetic model of the temperature profile on the basis of the values of T in each of the sections of the reactor and on the basis of these deviations adjustment of the amount advanced in the reactor water temperature and degree lane who,05 - 0.01 wt.% DCT in the reaction mass decomposition remains neprevzaidennymi.

 

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