System of automatic temperature profile support in reactor |
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IPC classes for russian patent System of automatic temperature profile support in reactor (RU 2326424):
                        
 System of engine fuel supply / 2325547
System of engine fuel supply consists of fuel tank wherein the following is installed: a level meter connected to the inlet of a "fuel-water" level regulator, and a control valve to flow out commodity water; the said valve is connected to a control outlet of the regulator. The level meter is made as two sensors of the fuel level, located in a portion of the lowest allowable fuel level mainly at opposite sides of the tank and one water level sensor located at the flow out level. The control valve is assembled so as to provide a positive feedback with the regulator upon receiving a signal on water presence and a negative feedback when there is no signal entry. At the moment of a positive feedback and water flow out the regulator is programmed to let out not more than 100 kg of fuel.
 Method of controlling process of thermal destruction of petroleum residues in pipe furnace / 2318858
Method according to invention determines pressure gradients at exit and entrance in each section of the furnace and real gradient is compared to projected gradient, after which, depending on disagreement value, this value is diminished via variation of fuel consumption in corresponding furnace burner. Projected gradient is calculated using formula: ΔPi=k(L1+b)n, wherein ΔPi is pressure gradient in i-th section of coil, %; k, b, n are coefficients depending on conversion value, nature of raw material, and projected quality of final thermal destruction products; and L1 reduced length of coil from its beginning to i-th measurement point, %.
 Separator / 2314876
The invention is pertaining to the devices for purification of the gas flow from the solid and liquid particles and may be used in the different branches of industry and at the enterprises of the agro-industrial complex at operation of the pneumatic actuators, pneumatic installations, and also in need of usage in the production processes of the air and other gases. The separator is supplied with the automatic control system connected to the electrical slide valves connected with the inlet fitting pipe, the purified gas outlet fitting pipe and the fitting pipe for withdrawal of the separated particles. The separator also is supplied with the sensors of the temperature, humidity and pressure disposed on the inlet and outlet fitting pipes, the sensor of the level of the separated particles allocated in the lower part of the storage bin, the sensor of the gas flow speed connected to the gas flow speed controller. The sensors and the rotary valve drive are connected to the automatic control system. The technical result of the invention is automation of purification of the polluted gas flow from the solid and liquid particles at the heightened purification efficiency.
 Method of control over the process of decomposition of the aluminate solution in the alum earth production / 2310607
The invention is pertaining to the field of nonferrous metallurgy and may be used to control the inertia processes, the outlet parameter of which is nonlinearly, predominantly extremely, linked with the inlet parameters. The method to control the process of decomposition of the aluminate solution in production of the alum earth exercised in the battery of the sequentially connected apparatuses- decomposers supplied with the devices of cooling of the source aluminate solution and the decomposing pulp, the devices of separation of the decomposing pulp at the battery outlet into the large-sized production fraction and small-sized fraction in compliance with the dimension of the solid particles in the pulp, with feeding of the source aluminate solution into the head decomposer, and the small-sized fraction and the part pf the large-sized fraction - in the capacity of the streams of the seed - in the decomposers of the head part of the battery provides for measurements of the consumption of the aluminate solution inlet stream, measurement of the consumption of the seed stream, the temperature of the aluminate solution and the pulp, contents of the aluminum oxide and the caustic alkali in the aluminate solution, contents of the particles of the preset class in the commercial hydroxide, stabilization of consumption of the seeds streams, the temperature of the aluminate solution and the decomposing pulp and alterations on each step of the control of the preset stabilizing values. The preset for stabilization at each step of the control values of the consumption of the seed streams and the temperature of the inlet aluminate solution and the decomposing pulp are determined by means of the approximated mathematical model consisting of in series connected the linear dynamic link, which inlets are the measured values of all indicated parameters, and the linear static link determining the predictable value of the speed of fluctuation of the contents of the particles of the preset size in the commercial hydroxide, average and centered the measured values of all parameters, depending on which and on the predictable value of the speed of fluctuation of the contents of the particles of the preset size determine and set the given for stabilization on that step of control the values of the parameters. The invention allows to maintain the quality of the ready product - the contents of the preset fraction of aluminum hydroxide.
 Method for moisture stabilization of dairy butter / 2302108
Continuous action butter machine includes seasoning reservoirs, churning machine with mixer and normalizing component batching pump. At outlet of continuous action butter machine, value of expected butter moisture deviation is determined from a formula. Churning machine mixer rotation frequency is controlled together with feeding of normalizing component depending on deviation of moisture from given value with consideration of value of expected component.
 Device of the automatic control over the reactor of the semi-continuous operation / 2299094
The invention is pertaining to the field of the control over the reactor of the semi- continuous operation (RSCO) at the variable consumption of the liquid batched component. The device contains the service tank for the liquid batched component, the reactor supplied with the stirrer, the coiled pipe and the jacket, the heat converter located in the reactor, the level sensor mounted in the service tank, the electro-pneumatic digital transducers intended for control over the pneumatic drives of the cut-off and discharge valves, the static power supply. The device is additionally supplied with the static three-channel power source, the pressure and consumption sensors arranged on the pressure branch pipe of the batcher and the electro-conductivity in the reactor, the meters of the frequency and voltage of the power delivered to the engines of the batcher and the stirrer, and also the power consumed by the consumption indicator, the microprocessor controller intended for implementation of the functions of the cascade system of the temperature stabilization of the reaction mass in the reactor and the program-pulse-revercive system making regulation of the rate of rotation of the engine of the stirrer, and also forming the control actions delivered to the electro-pneumatic transducers and through the static three-channel power supply - to the engines of the batcher, the stirrer and the consumption meter. The technical result of the invention is reduction of the batching duration, the increased production of the target product, improvement of the product quality ratings.
 Method for stabilizing of butter moisture normalization process / 2298918
Method involves regulating rotational frequency of churn mixer and feeding normalizing component depending on butter moisture content deviation from predetermined value; changing cream churning temperature depending on changing of butter moisture content deviation from predetermined value. When butter moisture content is below predetermined value, cream temperature is changed by value equivalent to normalizing component dosing value. When butter moisture content is above predetermined value, cream temperature is changed by value equivalent to butter moisture content deviation from predetermined value. Method allows butter yield to be increased to more than 180 kg per working shift.
 Method for automatically controlling thermal processing of concrete under conditions of open construction site / 2297025
Method includes heating of placed mixture, measurement of temperature of mixture, limiting of temperature of surface layer of mixture, exposure of concrete till achievement of required hardness, measurement of temperature of outer air and wind speed. Then, temperature-time schedule of thermal processing of concrete is formed and required minimal electric power for realization of thermal processing process is determined in accordance to generated temperature-time graph. Energy provision of construction area is realized in accordance to preliminarily set conditions of consumption of electric power and realization of temperature-time schedule of thermal processing of concrete.
 Method of controlling cyclohexanol or cyclohexanone production processes / 2296741
Invention relates to production of cyclohexanol or cyclohexanone via hydrogenation of phenol or benzene with hydrogen in presence of catalyst and diluent followed by hydration in case of using benzene as starting material. Process is characterized by that hydrogen and benzene or hydrogen and phenol preheated in heat exchanger, provided with condensate intake control circuit, and circulation gas are supplied to vaporizer and preheater, provided with heating steam consumption control circuits, through supply lines provided with shutoff valves. Phenol or benzene and circulation gas, as well as heating steam and condensate consumptions are specified and adjusted. Preheated mix is then fed into separator to separate gas from liquid phase, which is removed, while remaining gas mixture is sent to hydrogenation reactors comprising temperature control zones and heat-extracting tube-type condensers and provided with phenol or benzene, hydrogen and condensate control circuits, temperature sensors connected to controllers to adjust consumptions of phenol or benzene, hydrogen and condensate, and wherein diluent volume level compared to that of catalyst is controlled and hydration temperature is measured. Resulting product enters cooler and then separation column provided with cyclohexanol or cyclohexanone recovery level control and adjusting, wherefrom it is directed to gas circulation line comprising cooler, separator, and compressor equipped with pipelines with circulation gas consumption control circuits.
 Device for automatic control over semi-continuous action reactor / 2294556
Device contains controlled object itself with heat-exchanging devices in form of serially connected coat and coil, mixer with motor, unloading valve, devices for measuring temperature of reaction mass, flow of dosed component, rotation speed of mixer motor, adaptive block for reaction mass temperature controller, with adaptive compensators of perturbations, adjusting valve in the line for feeding dosed component into reactor, controllable mixer drive, consisting of motor and static block for controlling its speed. Branch pipe for feeding dosed component from repository vessel is connected serially through controlling valve and flow meter to force branch pipe, lowered below the mirror of reaction mass, directly into mixer operation zone. Output from flow meter of dosed component through integrator is connected to block for controlling rotation speed of mixer motor. Device additionally contains microprocessor controller, frequency meter for measuring rotation speed of mixer, electro-pneumatic analog transformer, positioned near the drive of controlling valve, adaptive controllers and compensators for considering oscillations of reaction mass temperature and flow of dosed component.
 The method of obtaining cyclic anhydrides or aliphatic nitriles, the method of obtaining maleic anhydride and a method of producing acrylonitrile and methacrylonitrile / 2058978
The invention relates to a method for producing a cyclic anhydride or a nitride of hydrocarbon and oxygen-containing gas in the presence of an appropriate catalyst, in particular to a method of reducing or eliminating the risk of explosion or fire in the headspace of the reactor system, in which there is a formation of the anhydride, or nitrile of hydrocarbon and oxygen
 The way to produce succinic anhydride / 2058311
The invention relates to a method for obtaining succinic anhydride used in the production of pharmaceuticals, insecticides, as a hardener of epoxy resins, in analytical chemistry
 The way to produce succinic anhydride / 2044731
The invention relates to a method for producing succinic anhydride, which can find application in the chemical industry
 The method of obtaining anhydride, endo-norbornene-2,3-dicarboxylic acid / 2032682
The invention relates to anhydrides of dibasic acids, in particular to an improved method for producing anhydride, endo-norbornene-2,3-dicarboxylic acid, which is used for the synthesis of unsaturated polyesters, alkyd resins
 System of automatic temperature profile support in reactor / 2326424
Invention relates to the chemical industry, particularly to the automatic control systems and can be used for temperature support of the reaction mixture in chemical reactors. The system of automatic temperature profile support in the reactor with distributed constants in maleic anhydride production contains two control systems: cascade automatic control system (ACS) of coolant temperature control in the reactor and ACS of benzene-air mixture fed to the reactor where the correction signal is inleted according to reaction mixture temperature. The correction signal represents the sum of the signals about reaction mixture temperature in the measurement points positioned along the reactor height multiplied to the weight factor determined intuitively or from optimization problem solution. Then the correction signal is compared with assignment signal on the functional generator serving as algebraic adder. The invention allows to increase the temperature support accuracy in the reactor at maleic anhydride production.
 2,4,6-phenyl-substituted cyclic ketoenols / 2353615
Described are 2,4,6-phenyl-substituted cyclic ketoenols of formula
Maleic anhydride purification method / 2399618
Method of purifying maleic anhydride involves heating molten initial crude product to 60-65°C and then cooling to 53-54°C and filtering at temperature of 51.5-53°C. Filtration is carried out on a filter with hole size of 0.01-0.05 mm and the molten mass is thermally processed in an atmosphere of dry inert gas or in sealed conditions in an atmosphere of dry inert gas.
Method of producing maleic anhydride and catalyst used therein (versions) / 2421452
Invention relates to a method of producing maleic anhydride in a fluidised bed by oxidising material which contains C4 hydrocarbons with molecular oxygen or oxygen-containing gas in a reactor with a fluidised bed at reactor temperature 325-500°C in the presence of a catalyst capable of working in the fluidised bed, containing mixed oxides of vanadium and phosphorus, wherein the catalyst is prepared as follows: (a) preparation of a catalyst precursor containing mixed vanadium and phosphorus oxide; (b) packing the catalyst precursor; (c) crushing the catalyst precursor to particles whose average size is less than one micrometre in diametre; (d) moulding particles which are capable of working in the fluidised bed, with bulk density greater than or equal to 0.75 g/cm3 from the packed crushed catalyst precursor; and (e) annealing said particles in boiling conditions, where output of the maleic anhydride is increased by adding a compensating catalyst into the reactor with the fluidised bed, wherein said compensating catalyst contains alkyl ether of orthophosphoric acid of formula (RO)3P=O, where R is hydrogen or C1-C4 alkyl and at least one R is C1-C4 alkyl, where the compensating catalyst is prepared by saturating the catalyst obtained according to steps (a) to (e) with alkyl ether of orthophosphoric aid. The invention also discloses a method of improving operation of the mixed vanadium-phosphorus oxide catalyst for producing maleic anhydride from butane in a fluidised bed. The invention also relates to a catalyst capable of working in the fluidised bed, for producing maleic acid by oxidising material which contains C4 hydrocarbons.
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FIELD: physics; operation. SUBSTANCE: invention relates to the chemical industry, particularly to the automatic control systems and can be used for temperature support of the reaction mixture in chemical reactors. The system of automatic temperature profile support in the reactor with distributed constants in maleic anhydride production contains two control systems: cascade automatic control system (ACS) of coolant temperature control in the reactor and ACS of benzene-air mixture fed to the reactor where the correction signal is inleted according to reaction mixture temperature. The correction signal represents the sum of the signals about reaction mixture temperature in the measurement points positioned along the reactor height multiplied to the weight factor determined intuitively or from optimization problem solution. Then the correction signal is compared with assignment signal on the functional generator serving as algebraic adder. The invention allows to increase the temperature support accuracy in the reactor at maleic anhydride production. EFFECT: increasing of the temperature support accuracy in the reactor. 2 cl, 2 dwg
The invention relates to a system for automatic high-precision maintaining the temperature in the reactor at one or another of its coordinate (for example, the length or height), i.e. to the system automatic precision maintaining its temperature profile (fields). Such objects are called objects with distributed parameters (PPR). While accurately maintaining the temperature profile as in statics and dynamics depends on the quality in the reactor product or intermediate, with attendant economic consequences. Known reactors, in which the temperature of the reaction mixture is maintained at a predetermined value through a single billing system. For example, in the semi-continuous reactor steps in the production of the PTS-60 (Voronezh-Tambov stabilizer) this is done by stabilizing the temperature in the reactor by the change of the flow of combusted natural gas in a furnace, in which the reactor, i.e. by changing the number of the heat carrier heating the reactor (see schedule production PTS-Novomoskovsk 60 JSC "Combine of organic synthesis" (COP)). In a continuous reactor in the production of oxalic acid from ethylene glycol (see regulation for production of oxalic acid from the same plant - KOS) this is done by stabilizing the temperature in the reactor by changing the supply temperatures is enta shirt ("bath") reactor. And in the first and second cases, the temperature in the reactor is measured only at one point. It is considered that due to the stirring reaction mixture temperature at all points of the reactor will be the same and equal to the temperature measured, i.e. the reactor in this case is the object with lumped parameters. Similar schemes maintain the temperature in the reactor, i.e. its support by creating a single ASR can be found, for example, in the books: 1. Automatic control in the chemical industry. Ed. Agudama. - M.: Chemistry, 1987. S-132. 2. Sinski F. automatic control of chemical processes. - M.: Chemistry, 1974. S. When small volumes of the reaction mixture at a sufficiently vigorous stirring the same parameters inside the reactor well run, that is, indeed, in these cases, the reactor can be mistaken for the object with lumped parameters and can be used to maintain the temperature inside the reactor single billing system. When the requirements that provide the same parameters inside the reactor, the temperature values at a single regulation at different points of the reactor are different, which can lead to poor product quality. While trying to find such a point set and a temperature sensor in the reactor, which as much as possible to ensure the best management of the process at this point. Insufficient quality of regulation, even if the condition on the concentration parameters of the reactor may, for example, due to the large inertsionnosti temperature measurement. In this case, to improve the quality of resorting to the creation of complex control systems, such as cascading billing system, by introducing an additional inner loop temperature control in the "Bane" of the reactor and introducing corrective signal for the temperature of the external circuit is the temperature inside the reactor, or combined systems, or systems with automatic change of settings (see, for example, the system of temperature regulation in the books: 1. Manusov E.B. Control and regulation of technological processes of paint and varnish industries. M.: Khimiya, 1977. P.50-57. 2. Automatic control in the chemical industry. Ed. Agudama. - M.: Chemistry, 1987. P.132-133). At the same time, there are reactors with a marked rassredotochivshey parameters, for example, the height of the reactor. They should clearly be attributed to the objects with distributed parameters (PPR). Such objects include, for example, the reactor in the production of maleic anhydride (MA) JSC "Combine of organic synthesis" (KOS) whenmost, for which a new system of automatic maintenance of temperature profile. Production MA at JSC Novomoskovsk KOS is based on a continuous vapor-phase catalytic oxidation of benzene with oxygen in the reactor (contact phone) on a stationary catalyst (see Moldovan BV, Kernos UD Maleic anhydride and maleic acid. L.: Chemistry, 1976. - 88 C.). At the exit of the reactor get maleina-air mixture (MVS) with a certain amount of maleic anhydride, which then allocate desublimate, distillation and subsequent crystallization. The main reaction for the catalytic oxidation of benzene in MA is with great heat:
Schematic of the reactor and the existing regulatory systems shown in figure 1, showing: 1 - reactor (contact); 2 - steam generator; 3 - stirrer; 4, 5, respectively, flow regulators benzene and condensate; 6 - ratio controller benzene-air; 7 - temperature controller; 8 - meter temperature - thermocouple; 9 - temperature control devices salts (6 pieces); 10 - temperature control devices benzole-air mixture (10 PCs). Letter designations devices 4-10 taken in accordance with GOST 21.404-85 "denote the conditional instrumentation and automation in the schema. For removal of heat of reaction in astronom space circulates the molten salt, the heat from which, in turn, is due to complete evaporation of the condensate in the steam generator 2, embedded in the Central part of the contact device and forming together the bath reactor. The temperature in the bath varies from 280 to 325°and is not less than 3-6 points along the height of the contact apparatus. In the Central part of the apparatus, the flow of salts is directed upward, which is provided by a propeller stirrer 3, surrounded by the above-mentioned steam generator, and the external side from top to bottom due to gravity flow (see figure 1). The top of the reactor 1 into the tube space, filled with a catalyst, served benzole-air mixture (BVS). Thus, the inner part of the reactor consists of a direct-flow shell-and-tube heat exchanger with 9142 tubes with a diameter of 30×1.8 mm and a length of 3500 mm In the catalyst bed height up to 3150 mm, the temperature of the reaction mixture varies from 200 to 480°C. the Last measured 10 thermocouples installed in a spiral at a depth of from 100 to 3000 mm In the operation position of thermocouple is adapted to better control the temperature distribution in the catalyst layer, and at least two thermocouples installed in the zone "hot spot". The desired temperature profile, from the accurate maintenance of which depends on the product yield of the reaction is AI, provided by regulation of the ratio of benzene to air in BVS and temperature "baths" by changing the supply of condensate to the steam generator. At the present time (see regulation for production of maleic anhydride KOS, Novomoskovsk, 1987) maintaining the temperature profile in the reactor are at a temperature of "hot spots", i.e. the point with the highest temperature of the reaction mixture at the height of the reactor, the component of order 480°C. In all other points along the height of the reactor temperature is controlled and its value by 10 points total order: 200°s at a height of 100 mm; 300° - under 265 mm; 400° - at 430 mm; 460° - at 600 mm; 400° - if 800 mm; 370° - if 1000 mm; 350° - at 1400 mm; 340° - at 1800 mm; 325° - at 2300 mm and 310° - at 2900 mm Thus, the "hot spot" is somewhere between the 3rd and 4th points of temperature measurement, and profile control is conducted on the 4-th point by building ASR ratio benzole-air mixture (BVS)fed to the reactor, the change in the amount of supplied air regulator 6 (FFC) (see figure 1) for a given "host" expense benzene (flow regulator benzene 4 (FC)) and by setting the ratio depending on the temperature of the "hot spots" (the dotted line to the regulator 6 (FFC) from the 4th point of the temperature profile MVS). To maintain the profile also use the second system is to him - system cascade temperature control "baths". As the refrigerant used salt (in the reactor, they are loaded preset number (mass)), giving, in turn, the heat of reaction for the condensation of the steam generator, located at the centerline (in the middle) of the reactor, turning it into steam. The temperature of the salts according to the height of the reactor remains relatively constant (varying from 250°at the entrance to approximately 325°With output). This allows us to use to maintain the profile of salts cascading billing system 3 point temperature profile (only temperature profile of the refrigerant measured by the devices 9 in 6 points: 1-I am at a height of 100 mm; 2-I - 430 mm; 3-I - 800 mm; 4-I - 1400 mm; 5-I - 2300 mm and 6-I - 2910 mm), using information from thermocouple 8 controller 7 (TC) external circuit ACP. As the inner loop of the cascade billing temperature salt is used, the flow control condensate (see figure 1) regulation 5 (FC). During operation it was discovered that when using these two standard systems of regulation of the quality management process (due to the complexity of chemical reactions and the complexity of the process) low and even worse than that which can be achieved through manual control by intuition apparatchiks. In addition, it supported manually ratio BVS status is made about 1:35÷ 1:40 (1 part of benzene, the rest is air), which is far from possible lower limit of 1:28 and below (up to the lower explosive limit of 1:24), which is the maximum content of MA (about 74%) in the MAM. Thus, the application of the known systems described above, i.e. the creation of a single ASR ratio BVS with correction for the temperature of a hot spot in the reactor (prototype) together with cascading billing temperature of the refrigerant in the "bath" does not give the desired effect. Moreover, the low quality of the product (malaina-air mixture (MVS) of a given concentration and a given quality at the outlet of the reactor) results in failure of the single ASR temperature of the "hot spot" and hand the management of the process by maintaining the ratio of BVS (so the line job ratio controller 6 (FFC) at a temperature of 4-th point of the profile MVS shown in figure 1 by the dotted line) on the intuition of the operator. The purpose of this invention is the creation of automatic control systems, providing the MAM of a given concentration and a given stability in automatic mode, i.e. systems that can provide a predetermined temperature profile along the height of the reactor as in statics and dynamics. For this purpose it is offered instead of a single ASR ratio BVS-corrected temperature "hot spots" in re chore to enter into this single ASR ratio correction signal from the system optimal collect measurement data about the temperature profile along the height of the reactor. The last signal is generated as follows (see figure 2). Figure 2 adopted the same conventions as in figure 1, with additional designations: 11, 12, 13 - functional signal Converter temperatures, meaning the conversion of which is explained in the inscription above the Converter. Full Ki
where Tisignal proportional to the temperature value in the i-th measurement point of the temperature over the height of the reactor is given by the temperature control devices 10 (TI), ki- damnosus the th coefficient of the i-th transducer 11 (0≤ ki≤1), and their value is determined in such a way as to give the maximum value of the I signal, i.e. based on the solution of optimization problem:
where → read as "should", / - "subject", Ω - the constraints imposed on the solution of the problem (beyond the signal change Tithe limits of variation of the parameters of the transfer functions of Withe limits of variation of values of Kiand others). The resulting solution of this optimization problem, the weighting coefficients Toitake into account the dynamics of change in temperature, as the optimization criteria I values of Tiwill depend on the parameters of the transfer functions of Wiby respective temperature channels (i) depending on the control actions (U) the ratio of the BVS (UC) and its quantity (UQ), which is reflected in (1) showing the dependence of Tias a function of In some cases, instead of finding wholesale the normal values For i* by solving the optimization problem (1) their values are chosen intuitive way, which makes the optimal system for collecting measurement information in intuitive, and the control system - in an intuitive control system (see the Posts SHE My brain. - M.: Sinteg, 2001. - 164 S.). Note also that in the particular case of the reference signal System temperature profile by introducing a correction in the ACP ratio BVS signal system optimal collect measurement data about the temperature profile of the reaction mixture at the height of the reactor shown in figure 2, was simulated on the computer by MATLAB in the SIMULINK system. The simulation showed the stability of the temperature profile as in statics and in dynamics in comparison with its maintenance by the existing system - the system changes the ratio BVS temperature "hot spots" (see figure 1). This suggests the possibility of reducing the ratio of BVS towards the lower limit, i.e. to the possibility of maintaining it level 1:28 that, in turn, will significantly increase the content of the MA output MVS from the reactor. Currently, the authors are engaged in the issue outside the rhenium of the proposed system on the reactor in the production of maleic anhydride KOS-based modules LOLICON-TM and multi-channel device MIP-S. 1. The system of automatic maintenance of temperature profile in the reactor with distributed parameters in the production of maleic anhydride by creating two control systems - cascade automatic regulation system (ASR) refrigerant temperature in the reactor and ASR ratio benzole-air mixture fed to the reactor, with the introduction of a correction signal according to the temperature of the reaction mixture, characterized in that as a correction signal using the signal generated as the sum of the signals of the temperature of the reaction mixture at the measurement points of the temperature over the height of the reactor, multiplied by weighting factors determined intuitively or as a result of solving optimization problems, and then compared with the reference signal on functional Converter that performs the function of the algebraic adder. 2. The system of automatic maintenance of temperature profile in the reactor with distributed parameters in the production of maleic anhydride according to claim 1, characterized in that in the particular case of the reference signal on the functional Converter may be zero.
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