SU764716A1

SU764716A1 - Exothermal process control method

Info

Publication number: SU764716A1
Application number: SU782656857A
Authority: SU
Inventors: Владимир Александрович Кондратюк; Раиса Михайловна Коровина; Владимир Александрович Лукашин; Виктор Иванович Сахненко; Николай Васильевич Лобанов
Original assignee: Ленинградский Ордена Трудового Красного Знамени Технологический Институт Им. Ленсовета
Priority date: 1978-08-22
Filing date: 1978-08-22
Publication date: 1980-09-23

Description

Изобретение относится к области управления непрерывными процессами химической технологии и касается, в частности, способа iperynHpoBaHHH температуры экзотермических процессов (например хлорирование, нитрирование, сульфирование), который может применяться в химической, фармацевтической, лакокрасочной, нефтехимической и других отраслях промышленности.The invention relates to the field of control of continuous processes of chemical technology, and relates, in particular, to the iperynHpoBaHHH method of temperature of exothermic processes (e.g. chlorination, nitration, sulfonation), which can be used in chemical, pharmaceutical, paint, varnish, petrochemical and other industries.

Иэвестен способ управления реактором путем изменения подачи реагента в зависимости от температуры дзеакци- 15 онной массы с коррекцией по величине отношения производных количества тепла, выделяющегося в реакторе, и количества тепла, выделяющегося в ре акторе, по температуре [1].There is a known method of controlling the reactor by varying the supply of the reagent depending on the temperature of the reaction mass with correction in terms of the ratio of the derivatives of the amount of heat released in the reactor and the amount of heat released in the reactor with respect to temperature [1].

уровня реакционной массы, отвода жидкого и газового продуктов [2].the level of the reaction mass, the removal of liquid and gas products [2].

Недостатком известного способа явля ется то, что в нем не учитывается тепловой эффект побочных реакций, что снижает производительность реактора при управлении процессом на границеустойчивости.The disadvantage of this method is that it does not take into account the thermal effect of side reactions, which reduces the productivity of the reactor when controlling the process at the bordersustainability.

Цель изобретения - обеспечить максимальную производительность реактора при оптимальном расходе реагентов за счет.повышения точности регулирования.The purpose of the invention is to ensure maximum reactor productivity at an optimal consumption of reagents due to the increased accuracy of regulation.

/Для этого скорость вращения_мешалки изменяют в зависимости от^-величины отношения производных от количества выделившегося тепла в реакторе и количества отведенного тепла из реактора по температуре в 20 реакторе, при этом количество выНаиболее близким по технической. делившегося тёпла определяют по сущности к изобретению яьяяется способ концентрациям побочных продуктов в управления экзотермическим процессом в реакторе путем изменения скорости вращения мешалки в зависимости от и. суммы сигналов вязкости и уровня реакционной массы, подачи исходного реагентов и хладагента в реакторе в за-:· висимости от температуры рёакционной массы и суммы сигналов вязкости и жидком и газовом продуктах, количество отведенного тепла вычисляют по уровню реакционной массы, скорости вращения мешалки, перепаду температур на стенке реактора, температуре и расходу газового продукта./ For this vrascheniya_meshalki speed varies depending on ^- the ratio of the derivatives of the amount of heat evolved in the reactor and the amount of heat retracted from the reactor at a temperature in the reactor 20, the amount of the technical vyNaibolee. the divided heat is determined essentially by the invention, a method is found for the concentration of by-products in controlling the exothermic process in the reactor by changing the rotation speed of the mixer depending on and. the sum of the signals of viscosity and the level of the reaction mass, the supply of the starting reagents and refrigerant in the reactor, depending on: · the temperature of the reaction mass and the sum of the signals of viscosity and liquid and gas products, the amount of heat removed is calculated by the level of the reaction mass, speed of rotation of the mixer, temperature difference on the wall of the reactor, temperature and gas flow rate.

Для химических реакторов, в которых осуществляются экзотермические про764716 цессы, наличие различных возмущений . (изменение температуры и расхода хладагента, изменение· количества поступающего реагента,' а также условий протекания реакции и ее температуры) может вывести в неустойчивую область.For chemical reactors in which exothermic processes are carried out, there are various disturbances. (a change in temperature and flow rate of the refrigerant, a change in · the amount of the incoming reagent, as well as the conditions of the reaction and its temperature) can lead to an unstable region.

Для того, необходимо ловия:In order to catch:

чтобы процесс был устойчив, ί выполнение следующего усотв dQ _ВЫд <ГГ ^> dT ’ производная по температуре от величины теплоотвода из реактора;that the process is stable, ί next execution usotv dQ d _YOU ^<YY> dT 'of the temperature derivative of the magnitude of heat removal from the reactor;

производная по температуре от количества тепла, выделяющегося в реакторе. Q_0TB и Q_BblA определяются из следующих выражений:temperature derivative of the amount of heat generated in the reactor. Q _0TB and Q _{BblA are} determined from the following expressions:

'^Oe».A'4 ^vP·«, ^С _а*Ач1^уР θοτβ где V' ^O e .A'4 ^v P · ", ^C _a * Ach1 ^at P θοτβ where V

Я где <ЗТI where <ST

Значения п< п« >The values of n <n «>

объем реактора, м³; тепловой эффект основной реакции, ккал х х кг*^< · моль~1 ;reactor volume, m ³ ; thermal effect of the main reaction, kcal x x kg * ^< · mol ~ 1;

тепловой эффект побочных реакций, ккал х х кг'/ моль'¹;, коэффициент теплопередачи, ккал · м'-² г·*⁴ х град^_<; константы скорости, прямой и побочных реакций, г*;thermal effect of side reactions, kcal x x kg '/ mol'¹;, heat transfer coefficient, kcal · m'- ² g · * ⁴ x deg ^{_ <} ; rate constants, direct and adverse reactions, g *;

концентрация побочных продуктов, кг . моль X хм'³;concentration of by-products, kg mol X hm '³;

концентрация целевого продукта, кг · моль х хм*³; ^г поверхность теплообмена, 2 м ;the concentration of the target product, kg · mol x hm * ³ ; ^g heat exchange surface, 2 m;

температурный перепад по поверхности теплообмена реактора,°C; количество тепла, отводимого с газовым _ потоком, ккал •г-⁴ .temperature difference over the heat exchange surface of the reactor, ° C; the amount of heat removed with the gas _ stream, kcal • g- ⁴ .

Запас тепловой устойчивости экзотермического процесса определяется величиной коэффициента р> -' . При β> 1 50 '•изотермический процэсс устойчив, при |6 е 1 находится на границе тепловой^ устойчивости, при |Ъ < 1 процесс неустойчив. На величину коэффициента тепловой устойчивости наряду с изменением расхода хладагента, его температуры, поверхности теплообмена, расхода компонентов, температуры реакционной массы оказывает влияние и скорость вращения мешалки. С увеличением скорости вращёния мешалки соответствующим 60 образом возрастает и значение коэффициента теплоотдачи со стороны реакционной массы, что в свою очередь, сказывается на значении коэффициента теплопередачи.' С увеличением скорос25 ^КЦ’^Кт ^СЦ atThe stock of thermal stability of the exothermic process is determined by the value of the coefficient p> - '. For β> 1 50 '• the isothermal process is stable, for | 6 e 1 it is on the boundary of thermal stability, for | b <1 the process is unstable. The value of the coefficient of thermal stability along with a change in the flow rate of the refrigerant, its temperature, heat exchange surface, flow rate of the components, temperature of the reaction mixture is also affected by the speed of rotation of the mixer. With an increase in the speed of rotation of the mixer, the value of the heat transfer coefficient from the side of the reaction mass increases correspondingly 60, which in turn affects the value of the heat transfer coefficient. ' With increasing speed 25 ^K C ' ^K t ^S C at

ОТХ 2~ ти вращения мешалки увеличивается коэффициент теплопередачи, что ведет к увеличению коэффициента тепловой устойчивости, так как возрастает 0_от6 числитель коэффициента тепловой устойчивости.OTX 2 ~ of the rotation of the mixer increases the heat transfer coefficient, which leads to an increase in the coefficient of thermal stability, since the numerator of the coefficient of thermal stability increases from 0 to ₆ .

Таким образом, по знаку и величине коэффициента тепловой устойчивости можно управлять процессом, воздействуя на скорость вращения мешалки реактора.Thus, by the sign and value of the thermal stability coefficient, it is possible to control the process by influencing the speed of rotation of the reactor mixer.

Максимальная производительность реактора достигается тем, что регулирующее воздействие осуществляется изменением скорости вращения мешалки, что не нарушает материального баланса реактора, позволяя сохранять подачу исходных реагентов на ранее заданном оптимальном уровне, и обеспечения условия протекания процесса на границе тепловой устойчивости. Работа реактора в этом режиме достигается тем, что рассчитывается коэффициент |i и в' соответствии с его знаком и величиной корректируется регулирующее воздействие. Сигнал коррекции направлен на такое изменение Структуры регулятора температуры, чтобы, воздействуя на скорость вращения мешалки, обеспечить стабилизацию температурного режима в реакторе на границе тепловой устойчивости.The maximum performance of the reactor is achieved by the fact that the regulatory effect is carried out by changing the speed of rotation of the mixer, which does not violate the material balance of the reactor, allowing you to maintain the supply of the starting reagents at a predetermined optimal level, and to ensure the conditions of the process at the boundary of thermal stability. The operation of the reactor in this mode is achieved by calculating the coefficient | i and, in accordance with its sign and magnitude, the regulatory action is corrected. The correction signal is aimed at such a change in the structure of the temperature controller, so that, acting on the speed of rotation of the mixer, to ensure stabilization of the temperature in the reactor at the boundary of thermal stability.

На чертеже представлена схема реализации способа управления экзотермическим непрерывным процессом.The drawing shows a diagram of a method for controlling an exothermic continuous process.

Реактор 1 с рубашкой 2 оснащен мешалкой 3 с электродвигателем 4, г трубопроводами 5 и 6 подачи исходных компонентов в реактор, перетоком 7, вытяжной системой 8 .и трубопроводом 9 подачи хладагента в рубашку. Температуру в реакторе измеряют первичным преобразователем 10 со вторичным прибором 11. Расход хладагента, поступающего в рубашку, измеряют первичным преобразователем 12 и прибором 13. Термопарами 14 и 15 и вторичным прибором 16 определяют перепад температуры на стенке реактора. Для определения поверхности теплообмена в реакторе служит уровнемер 17 со вторичным прибором 18. Расход газообразных продуктов реакции измеряют первичным преобразователем 19 и вторичным прибором 20, а температуру -термопарой 21 и прибором 22. Концентрация целевого продукта определяется первичным преобразователем 23 и прибором 24. Концентрация побочных продуктов в жидкой и газовой фазах определяются Соответственно первичными преобразователями 25 и 26 со вторичными приборами 27 и 28. В блоке 29 определяют произведение температурного перепада на поверхность теплообмена. В блоке рассчитывается значение коэффициента теплопередачи, исходя из значения расхода хладагента и скорости вращения мешалки, которая измеряется при65 борОм 31. В блоке 32 определяют количество тепла, отводимого через рубашку реактора. В блоке 33 рассчитывают энтальцию газового потока, отводимого вытяжной системой реактора, значение которой суммируют в блоке 34 с количеством отводимого тепла из реактора. В блоке 35 дифференцируют суммарное количество отводимого тепла по • температуре в реакторе. В блоке 36 у рассчитывают количество тепла, выделившегося в хоДе реакции получения целевого продукта с учетом его концентрации и температуры реакционной массы. В блоке 37 рассчитывают количество выделившегося тепла в ходе образования побочного продукта в жидкой фазе с учетом его концентрации и температуры реакционной массы. В блоке 38 ’определяют количество тепла, выделившегося в результате образования газообразного побочного продукта с учетом его концентраций в газовой фазе и ее температуры. Общее количество тепла, выделившегося в ходе реакции, рассчитывают в блоке 39 (сумматор) , а дифференцируют его значение по температуре реакционной массы в блоке 40. Сигналы с блоков 35 и 40 поступают в блок деления 41 для определения -значения и знака коэффициента тепловой устойчивости с целью корректировки параметров регулятора 42 переменной структуры.The reactor 1 with jacket 2 is equipped with a stirrer 3 with an electric motor 4, g pipelines 5 and 6 for supplying the initial components to the reactor, overflow 7, exhaust system 8. and a pipeline 9 for supplying refrigerant to the jacket. The temperature in the reactor is measured by the primary transducer 10 with the secondary device 11. The flow rate of the refrigerant entering the jacket is measured by the primary converter 12 and the device 13. Thermocouples 14 and 15 and the secondary device 16 determine the temperature difference on the wall of the reactor. To determine the heat transfer surface in the reactor, a level gauge 17 with a secondary device 18 is used. The flow rate of gaseous reaction products is measured by the primary converter 19 and the secondary device 20, and the temperature is measured by the thermocouple 21 and the device 22. The concentration of the target product is determined by the primary converter 23 and the device 24. The concentration of by-products in the liquid and gas phases are determined respectively by primary converters 25 and 26 with secondary devices 27 and 28. In block 29, the product of the temperature difference by erhnost heat. In the block, the value of the heat transfer coefficient is calculated based on the value of the refrigerant flow rate and the stirrer rotation speed, which is measured at 65 boron 31. In block 32, the amount of heat removed through the reactor jacket is determined. In block 33, the enthalpy of the gas stream removed by the exhaust system of the reactor is calculated, the value of which is summed in block 34 with the amount of heat removed from the reactor. In block 35, the total amount of heat removed is differentiated by temperature in the reactor. In block 36, the amount of heat released in the course of the reaction to obtain the target product is calculated taking into account its concentration and temperature of the reaction mixture. In block 37, the amount of heat generated during the formation of a by-product in the liquid phase is calculated taking into account its concentration and the temperature of the reaction mixture. In block 38 ’, the amount of heat released as a result of the formation of a gaseous by-product is determined taking into account its concentration in the gas phase and its temperature. The total amount of heat released during the reaction is calculated in block 39 (adder), and its value is differentiated by the temperature of the reaction mass in block 40. The signals from blocks 35 and 40 are sent to the division unit 41 to determine the value and sign of the thermal stability coefficient c the purpose of adjusting the parameters of the controller 42 variable structure.

Способ осуществляется следующим /образом.The method is as follows / as follows.

По данным, о расходе хладагента, уровне реакционной массы, перепаде температур на стенке реактора, скорости вращения мешалки, а также о расходе и температуре газообразных продуктов, которая поступает с приборовAccording to the data on the flow rate of the refrigerant, the level of the reaction mass, the temperature difference on the wall of the reactor, the speed of rotation of the stirrer, as well as the flow rate and temperature of the gaseous products that comes from the devices

13,. 16, 18, 20, 22 и 31, в блоке 34 формируется значение Q_OTB .thirteen,. 16, 18, 20, 22 and 31, in block 34, a Q _OTB value is generated.

Значение Q вид. Формируют в сумматоре 39 на основании концентраций делового продукта, побочного продукта и отходящих газов, измеряемых приборами 24, 27 и 28, а тепловые эффекты реакций рассчитываются в блоках 36, 37 и 38. В блоках дифференцирования 35 и 40 формируют производные οΐ Q_OTB и Q_BblA по температуре в реакторе. От блоков дифференцирования знаd0_OTB ^0выд·. . _ чения ———и——— поступают на блок деления 41, с выхода которого снимаетсй значение коэффициента л.— ¹ й0_выд Q value view. They are formed in adder 39 based on the concentrations of the business product, by-product and exhaust gases measured by devices 24, 27 and 28, and the thermal effects of the reactions are calculated in blocks 36, 37 and 38. Derivatives οΐ Q _OTB and Q are formed in differentiation blocks 35 and 40 _BblA temperature in the reactor. From differentiation blocks, know 0 _O TB ^ 0out ·. . _ Cheniya --- --- and fed to dividing unit 41, which is removed from the output value of the coefficient ^Leningrad-1 d0 _vyd

Сигнал поступает на изменение параметров регулятора 42 переменной структуры, на который также подается с прибора 11 текущее значение температуры в реакторе. Выходной сигнал регулятора 42-поступает на двигатель мешалки реактора, изменяя скорость ее враще_гния.The signal is applied to change the parameters of the controller 42 of a variable structure, to which the current temperature value in the reactor is also supplied from the device 11. The output of the regulator 42 is supplied to the reactor stirrer motor by changing the rotation speed of its Nia _g.

Использование предлагаемого способа управления позволяет проводить тех· нологический процесс при максимальной производительности на границе тепловой устойчивости в условиях наличия всевозможных возмущений, при этом производительность реактора повышает-.. ся на 10-15%. Экономический эффект от использования данной системы управления за счет обеспечения максимальной производительности реактора р расчете на 1 т готового продукта роставляет 175 руб. и'при готовой . . программе в 200 т составит 35000 руб.Using the proposed control method allows carrying out the technological process at maximum productivity on the border of thermal stability under the conditions of the presence of various disturbances, while the reactor productivity increases by 10-15%. The economic effect of using this control system by ensuring maximum reactor productivity p per 1 ton of the finished product is 175 rubles. and when ready. . the 200 ton program will amount to 35,000 rubles.

Claims

The invention relates to the field of control of continuous processes in chemical technology and, in particular, relates to a method for controlling the temperature of exothermic processes (for example, chlorination, nitration, sulfonation), which can be used in the chemical, pharmaceutical, paintwork, petrochemical and other industries. A known method of controlling a reactor is by varying the supply of reagent depending on the temperature of the reaction mass with a correction by the value of the ratio of the derivative of the amount of heat in the reactor and the amount of heat released in the reactor by the temperature of 1. Closer to the technical level. SUMMARY OF THE INVENTION The criocT controls an exothermic process in a reactor by varying the rotation speed of the stirrer as a function of t. the sum of viscosity signals and the level of the reaction mass, the supply of the initial reagents and coolant in the reactor, depending on the temperature of the reaction mass and the sum of the viscosity signals and the level of the reaction mass, removal of liquid and gas products 2. The disadvantage of the known method is that it does not take into account the thermal effect of side reactions, which reduces the productivity of the reactor when managing the process at the stability boundary. The purpose of the invention is to ensure maximum reactor performance with optimal consumption of reagents, thereby increasing the accuracy of the controlled. / For this, the rotational speed of the agitator is changed depending on the relative value of the derivative of the amount of heat released in the reactor and the amount of heat removed, according to the reactor temperature, the amount of heat released is determined by the concentration of by-products in the liquid and gas products. , the amount of heat removed is calculated from the level of the reaction mass, the rotation speed of the stirrer, the temperature difference across the reactor wall, the temperature and the flow rate of the gas product. For chemical reactors in which exothermic processes are carried out, the presence of various disturbances (change in temperature and consumption of chla agent, change in the amount of incoming reactant, as well as the conditions of the reaction and its temperature) can lead to an unstable region. In order for the process to be stable, the following condition must be met: QOTB 0out. dT dT dOpT where is the derivative with respect to temperature dt pe of the magnitude of the heat removal from the reactor; derived from the temperature of the thermal energy generated in the reactor Values and are determined from the following expressions: ° 8xA H-p-yC 2: q, -V. -. Yag and with K-F-it-i O volume of the reactor. - thermal effect of the main reaction, kcal x X; thermal effect of side reactions, kcal x x. coefficient of heat-2. r -Y dacha, kcal m X hail rate constants, direct and side reactions g - concentration of by-products, kg. mol X X concentration of the target product, kg mol x Heat exchange surface ftt - temperature difference over the heat exchange surface of the reactor, C; otkhg the amount of heat removed by the gas flow, kcal-g The thermal stability margin of the ex MjivecKoro process is determined by the nd1 coefficient b - (. At p, the thermal process is stable, ip | i is at the boundary of thermal stability, at jb 1 npoqecc is unstable The value of the heat stability coefficient along with the change in coolant flow rate, its temperature, heat exchange surface, flow rate of components, temperature of the reaction mass is influenced by the rotation speed of the agitator. Correspondingly, the value of the heat transfer coefficient on the side of the reaction mass increases, which, in turn, depends on the value of the heat transfer coefficient. As the agitator speed increases, the heat transfer coefficient increases, which leads to an increase in the heat stability coefficient, as the QQTB increases the numerator of the heat resistance coefficient Thus, by the sign and magnitude of the thermal stability coefficient, the process can be controlled by affecting the rotational speed of the reactor agitator. The maximum productivity of the reactor is achieved by the fact that the regulating effect is carried out: by changing the rotational speed of the agitator, which does not violate the material, the reactor, keeping the supply of initial reagents at a previously specified optimal level, and ensuring the condition of the process at the boundary of thermal stability. The operation of the reactor in this mode is achieved by the fact that the coefficient | b is calculated and the regulating influence is corrected in accordance with its sign and value. The correction signal is aimed at changing the structure of the temperature regulator so that, by acting on the rotational speed of the mixer, stabilization of the temperature regime in the reactor at the thermal stability boundary will be achieved. The drawing shows a scheme for implementing a method for controlling an exothermic continuous process. The reactor 1 with jacket 2 is equipped with a stirrer 3 with an electric motor 4, g pipelines 5 and 6 of supplying the initial components to the reactor, flow 7, exhaust system 8., And pipe 9 of the refrigerant supply to the jacket. The temperature in is measured by the primary converter 10 with the secondary device 11. The flow rate of the refrigerant entering the jacket is measured by the primary converter 12 and the device 13. Thermocouples 14 and 15 and the secondary device 16 determine the temperature difference on the reactor wall. To determine the heat exchange surface in the reactor, a gauge 17 with a secondary device 18 serves. The flow rate of the gaseous reaction products is measured by the primary converter 19 and the secondary device 20, and the temperature of the thermocouple 21 and the device 22. The concentration of the target product is determined by the primary converter 23 and the device 24. Concentration by-products in the liquid and gas phases are determined by primary transducers 25 and 26 with secondary devices 27 and 28. In block 29, the product of the temperature differential is determined a heat exchange surface. In block 30, the value of the heat transfer coefficient is calculated based on the coolant flow rate and the rotational speed of the stirrer, as measured by instrument 31. In block 32, the amount of heat removed through the jacket of the reactor is determined. In block 33, the enthalation of the gas stream discharged by the exhaust system of the reactor is calculated, the value of which is summed up in block 34 with the amount of heat removed from the reactor. In block 35, the total amount of heat removed is differentiated by temperature in the reactor. In block 36: calculate the amount of heat released in the hoi reaction to obtain the desired product, taking into account its concentration and temperature of the reaction mass. In block 37, the amount of released heat is calculated during the formation of a by-product in the liquid phase, taking into account its concentration and temperature of the reaction mass. In block 38, the amount of heat released as a result of the formation of a gaseous by-product, taking into account its concentrations in the gas phase and its temperature, is determined. The total amount of heat released during the reaction is calculated in block 39 (adder), and its value is differentiated by the temperature of the reaction mass in block 40. The signals from blocks 35 and 40 go to block 41 to determine the -value and sign of the coefficient of thermal stability the purpose of adjusting the parameters of the controller 42 of the variable structure. The method is carried out as follows. According to the data on the refrigerant consumption, the level of the reaction mass, the temperature difference on the reactor wall, the rotational speed of the stirrer, and the flow rate and temperature of the gaseous products that come from the devices 13, .16, 18, 20 , 22 and 31, in block 34, the value of QQTB is formed. The value of Q and, is formed in the adder 39 based on the concentrations of the whole product, by-product and off-gas measured by instruments 24, 27 and 28, and the thermal effects of the reactions are calculated in blocks 36 , 37 and 38, in blocks of differentiation 35 and 40 form the derivatives with respect to temperature in the reaction of the blocks of differentiation of the value of the residual radiation density. -, Cheni ---- and --- go to blo. The dividing rate is 41, from which the value of the coefficient is removed. The output is sent to a change in the parameters of the variable structure regulator 42, to which the current temperature in the reactor is also fed from the device 11. The output signal of the regulator 42 Enters the reactor agitator engine, changing its rotational speed. Using the proposed control method allows the process to run at maximum performance at the thermal stability boundary under the conditions of various disturbances of naltgchi, while increasing the reactor performance, from LQ- 15%. The economic effect of using this control system by ensuring the maximum reactor performance per 1 ton of finished product is 175 rubles. and the finished program .. a 200-ton program will be 35,000 rubles. The invention The method of controlling the exothermic process in a continuous reactor by changing the rotational speed of the agitator, measuring the temperature n the level of the reaction mass, the rotational speed of the agitator, discharging the liquid and gaseous products, so that maximizing reactor productivity with optimum reagent consumption by increasing the control accuracy, the rotational speed of the agitator is changed depending on the ratio of derivatives to the amount of precipitate to degus heat la in the reactor and the amount of heat removed. From the reactor, according to the temperature in the reactor, the amount of heat released is determined from the concentrations of by-products in the liquid and gas products, and the amount of heat removed is calculated from the level of the reaction mass, the rotation speed of the stirrer, the temperature difference on the reactor wall, temperature and flow rate gas product. Sources of information taken into account in the examination 1. USSR author's certificate 525463, cl. B 01 J 1/00, 1975.

2. USSR author's certificate 465215, cl. At 01 J 1/00, 1973.

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