Method of regulating thermal decomposition of oil residues in tube furnaces |
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IPC classes for russian patent Method of regulating thermal decomposition of oil residues in tube furnaces (RU 2367679):
       
 Method for operating mode of caprolactam production / 2366651
Invention refers to the method for operating mode of caprolactam production from benzene carried out in the plant with one process line including the stations of benzene hydrogenation with hydrogen, cyclohexane oxidation with oxygen, cyclohexanone rectification, oximation, cyclohexanone oxim rearrangement to caprolactam, neutralisation of the reaction mixture with ammonia and mixing of caprolactam. The said stations are connected with pumps, pipelines with sensors and valves for consumption control of benzene, hydrogen, cyclohexanone, hydroxylamine sulphate and oleum, sensor of acid value and pH-metre of caprolactam. The said line contains additionally the second process line of caprolactam production from phenol including the stations of phenol hydrogenation with hydrogen, dehydrogenation of cyclohexanol with circulation circuit including: pump - station of cyclohexanol dehydrogenation - station of cyclohexanone rectification - pump, station of cyclohexanone rectification, oximation with hydroxylamine sulphate, rearrangement of cyclohexanon oxim to caprolactam and neutralisation of the reaction mixture with ammonia connected by pumps and pipelines with sensors and valves for control of benzene, hydrogen, cyclohexanone, hydroxylamine sulphate and oleum consumption, sensor of acid value and pH-metre of caprolactam and contains the device of benzene-phenol ratio connected with stations of benzene and phenol hydrogenation, oxidation and dehydrogenation; device of cyclohexanone distribution to the oximation stations connected with rectification stations and (through the cyclohexanone mixing tank) with the oximation stations; device of crystalline caprolactam switch-over to liquid caprolactam connected with caprolactam mixer, concentrator of crystalline caprolactam and tank of liquid caprolactam. The total caprolactam capacity, benzene-phenol ratio, cyclohexanone distribution to oximation stations, shipping of crystalline and liquid caprolactam to customers are set up; the consumption of benzene, phenol, hydrogen, cyclohexanone, hydroxylamine sulphate and oleum are corrected with corresponding valves.
 Production area environmental control device / 2363031
Invention relates to instrument making and can be used to control production area environments. Proposed device comprises regulator unit, control unit, temperature pickup, noise and illumination pickups. It also includes transducers of signals generated by the temperature, noise and illumination pickups. It incorporates setters of maximum and minimum tolerable temperatures, maximum tolerable noise and maximum tolerable illumination. The device includes comparator for every aforesaid setter and logical elements for every aforesaid controlled parametre. It incorporates the 1st , 2nd, 3rd and 4th logical elements, read-only memories for all controlled parametres, shift registers and counters of all aforesaid parametres. In compliance with this invention, the proposed device additionally comprises I/O units, communication unit, satellite receiver unit, power supply monitor, power buffer, ADC, real-time clock unit, RAM, nonvolatile memory unit. It incorporates, further on, real-time clock storage battery, relative humidity pickup with amplifier, airflow speed pickup with amplifier, environment heat load intensity pickup with amplifier, carbon oxide concentration pickup with amplifier, sulfur oxide concentration pickup with amplifier, nitrogen oxide concentration pickup with amplifier, ozone concentration pickup with amplifier, town gas concentration pickup with amplifier, power supply voltage pickup with amplifier and power supply.
 Method for control of potassium chloride preparation / 2359909
Invention can be used in the process of potassium chloride preparation by the method of solution-crystallisation. The method for the control of the aforesaid process by the way of input water flow varying includes: 1) the adjustment of water flow fed into crystallisation alkali liquor depending on potassium chloride concentration in the liquor and water consumption for washing of crystallisation apparatus; 2) detection of the temperature, density and consumption of alkali liquor. The said measurements allow to determine the sodium chloride content in the alkali liquor. The crystallisation water consumption is calculated on the basis of the obtained data according to proposed equation; the calculated values are input as assignment to the system of water consumption control.
 Control of process of production of loose form of powdery choline chloride from its aqueous solution / 2356907
Invention is related to automation of technological processes and may be used in automation of process of production of loose form of powdery choline chloride from its aqueous solution. In method that provides for use of crushed and fractionated dry sugar beet pulp as active adsorbent, its mixing with previously heated aqueous solution of choline chloride, and then drying in vibration dryer by superheated steam of atmospheric pressure, separation of spent superheated steam flow into the main one, sent to vibration dryer with creation of recirculation circuit, and additional one sent for reheating of choline chloride prior to its supply for mixing, the novelty is the fact that superheating of atmospheric pressure steam is done with heating steam, at that heating steam is produced by means of steam generator with electric heating elements, feed pump and safety valve, heating steam condensate produced in this process after superheating and condensate produced during heating of aqueous solution of choline chloride is taken to condensate collector, and then in mode of closed circuit is supplied in steam generator, at that flow rate of crushed and fractionated dry pulp is measured, as well as aqueous solution of choline chloride coming for mixing, flow rate and temperature of superheated steam upstream vibration dryer, choline chloride temperature before and after its heating, pressure of choline chloride after heating, temperature and humidity of mixture of crushed and fractionated dry pulp and aqueous solution of choline chloride prior to supply for drying, amplitude and frequency of oscillations in gas-distributing grid of vibration dryer, flow rate and humidity of powdery choline chloride after drying, level of condensate in steam generator and pressure of heating steam, at that flow arte of dry sugar beet pulp after fractionation is used to set flow rate of heated choline chloride coming for mixing, and flow rate and humidity of prepared mixture of crushed and fractionated dry pulp and aqueous solution of choline chloride prior to supply for drying, flow rate and humidity of powdery choline chloride after drying are used to determine amount of evaporated moisture in vibration dryer, which is used to establish flow rate of superheated steam in the main circuit of recirculation, and its temperature is established by current value of temperature of mixture of crushed and fractionated dry pulp and aqueous solution of choline chloride by setting of specified capacity of steam generator affecting power of electric heating elements, at that in case condensate level in steam generator falls below specified value, condensate is supplied from condensate collector, and when pressure of steam in steam generator reaches upper limit value, steam pressure is released through safety valve, if flow rate of mixture of crushed and fractionated dry pulp and aqueous solution of choline chloride deviates prior to supply for drying to the side of increase from specified value, at first frequency is increased, and then amplitude of oscillations in gas-distributing grid of vibration dryer, if flow rate of mixture of crushed and fractionated dry pulp and aqueous solution of choline chloride deviates to the side of reduction from specified value, at first frequency is reduced, and then amplitude of oscillations in gas-distributing grid of vibration dryer, current values of temperature and flow rate of choline chloride prior to heating are used to set flow rate of spent superheated steam in additional recirculation circuit, at that temperature of choline chloride after heating is used to set specified pressure of choline chloride at the inlet to mixer.
 Method of controlling process of sylvinite ore dissolution / 2352385
Invention relates to technique of controlling processes of sylvinite ores dissolution and can be used in production of potassium chloride by dissolution-crystallisation method. Method of controlling processes of sylvinite ores dissolution includes regulation of ore supply depending on content of useful component in input flows, measuring ready solution temperature and determining sodium chloride content in solution by calculation method. Additionally determined are density, temperature and consumption of dissolving solution, content of sodium chloride in it is determined by content of useful component, density and temperature. Ore supply is calculated according to suggested equation and calculated value is given as task to system of weigher control.
 Automated method of controlling and managing process for preparing sugar syrup mixture for crystallisation by cooling / 2342438
Proposed automated method of controlling and managing the process of preparing sugar syrup mixture for crystallisation by cooling makes provisions for regulating the volumetric discharge of water entering the mixer and the level of sugar syrup in it. Regulating the level of the sugar syrup in the vertical mould is achieved by acting on the adjustable-frequency electric drive of the sugar syrup pump. Periodically using the lab the density of the ready sugar syrup is controlled at the exit from the mixer. The active electrical power which is used in the electric motor of the sugar syrup pump, the temperature and pressure differential of the sugar syrup mixture, coming from the mixer and water at the entrance of the mixer are all measured. The water-mass density is calculated by its temperature and the density of the sugar syrup mixture by its pressure differential. Afterwards the volume flow rate is worked out by the measured volume flow rate of water, by the estimated value of the density of water and sugar syrup mixture and by the density of ready sugar syrup measured in the laboratory. The dependency ratio of the active electric power from the volume rate of flow of the sugar syrup mixture and the differential in its pressure N=α1Q3 УΔPy+α2QyΔPy , where N - active electric power; QY - volume rate of flow of sugar syrup mixture entering the mixer; ΔPY - pressure differential of the sugar syrup mixture; α1, α2 - coefficients. The obtained plot is used for future calculations of volume rate of flow of sugar syrup mixture only with measured values of active electric power and pressure differential of the sugar syrup mixture. The current task of the regulator of the volumetric water discharge is determined on the basis of measured values of this output, estimated values of the density of sugar syrup mixture, water and volume rate of flow of the sugar syrup mixture, the determined value of density of ready sugar syrup mixture and the task of the regulator calculated in the previous control step. The solid content of the original sugar syrup mixture is controlled - by its temperature and density in the ready sugar syrup mixture. This invention makes it possible to reduce the loss of sugar from molasses due to a more qualitative stabilisation of the density of molasses on its exit from the mixer.
 Work environment remote control device / 2335795
Device contains control unit, temperature sensor, noise sensor and luminance sensor, temperature, noise and luminance signal converter per each sensor, boundary value generator per each controlled factor, comparator per each generator of maximum permissible values of measured temperature, noise, luminance, logic elements per each controlled factor, read-only storage per each controlled factor, shift registers, value counter of each controlled factor, control unit and generator. Besides, device contains relative humidity detector, air speed transducer and pulse number sensor, signal converters of relative humidity, air speed and pulsation factor per each sensor, boundary value generator per each additional controlled factor, comparator per each generator of each additional controlled factor, logic elements per each controlled factor, read-only storage per each controlled factor, shift registers, counter of maximum relative humidity, counter of minimum relative humidity, counter of air speeds, counter of pulsation factors.
 Work environment remote control device / 2335794
Device contains control unit, temperature sensor, noise sensor and luminance sensor, temperature, noise and luminance signal converter per each sensor, boundary value generator per each controlled factor, comparator per each generator of maximum permissible values of measured parameters, logic elements per each controlled factor, read-only storages per each controlled factor, four shift registers, counter of maximum temperature, counter of minimum temperature, noise counter, luminance, control unit and generator. Besides, device contains chemical sensor with converter, chemical concentration generator, logic element of maximum chemical concentrations, read-only storage of maximum chemical concentrations, shift register, counter of maximum chemical concentrations.
 Air humidity detector / 2332701
Invention can be applied for automated systems of microclimate control in closed warehouse space for improving accuracy of heat and humidity calculation in controlled variable air medium. Detector contains temperature sensor, relative humidity and atmospheric pressure detectors, temperature converter to air vapour pressure, and computing unit. Using of converter and atmospheric pressure detector allows for increased accuracy of humidity detection. Invention provides automated real-time humidity and increased accuracy of humidity detection.
 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.
Coke reinforced with carbon fibre, obtained on retarded coking installation / 2343133
Coke is formed with combined coking of mixture of small amount of cut carbon fibres and heavy residues of oil or coal tar and pitch processing, obtained by mixing carbon fibres or stabilised precursor fibres for formation of carbon fibres with flow of supplied raw material for method of retarded coking, coking of said mixture on known retarded coking installation and burning of obtained coke. Raw material consists of group of residues with high content of aromatic compounds after distillation in vacuum, light cracking, catalytic cracking in pseudoliquified layer, thermal cracking, pyrolysis of ethylene or soft pitches, produced by coal coking or distillation of coal residues with high content of aromatic compounds. Coke is applied in polygranulated amorphous or graphitised carbon materials, containing at least 70% wt, of carbon, in particular, in coal electrodes and in connected with them connecting elements (nipples), fine-grained graphites and reactor graphites, in bricks for blast furnaces or cathodes and anodes for electrolysis of melted aluminium salts.
 Method for retarded coking of oil residues and coking reactor / 2339674
Method includes heating of source raw material, mixing it with a re-circulator - heavy gas-oil of coking in a cube part of a rectification column, heating of produced secondary raw material to coking temperature and coking in a reactor with withdrawal of steam-gas products of coking, their cooling and separation in a cyclone with extraction of steam and liquid phases; at that, the steam phase if withdrawn into the concentration part of the rectification column for separation, while a liquid part is withdrawn directly from the cyclone into the reactor. The reactor for implementation of the suggested method includes a cylinder case with sleeves of secondary raw material input and withdrawal of steam-gas products of coking, at the upper portion of the cylinder the cyclone is installed, the inter-circular space of which is connected with the steam-gas withdrawal sleeve, while the lower part of the cyclone is connected with the reactor cavity; at that the cyclone is equipped with a sleeve for input of a cooling jet.
 Low-sulphur oil coke's producing method / 2338771
Method for producing low-sulphur oil coke lies in the fact that initial raw materials are made from oil chemistry and/or oil processing residue using mixer, which contain 5-15% of asphalt, and light fraction of slow coking liquids. Raw materials are heated in furnace convection coils and then mixed with vapour gases leaving the slow reactor in the still section of the rectifying column. Secondary raw materials enter furnace through transfer lines, whereinto some part of preheated light fraction of slow coking liquids is supplied via inlet point, and then they are heated up to the coking temperature and enter slow coking reactor through mixing point. The rest of light fraction of slow coking liquids is supplied to the above mixing point or directly to this reactor, and the total quantity of light fraction of slow coking liquids which is fed to secondary raw materials' inlet point prior to its heating up to coking temperature and to the mixing point before slow coking reactor or directly to this reactor is 10-20%.
Petroleum cokemaking method / 2331663
Invention refers to oil refining, in particular, to petroleum cokemaking by method of delayed coking. Proposed is a petroleum cokemaking method that includes tar cocking at the first flow with making of common sulphur coke and heavy gas oil of delayed tar cocking. Then heavy gas oil of delayed cocking is subjected to mixture with heavy pyrolysis gum and heavy gas oil of catalytic cracking at % mass rate (60-65):(15-20):(15-20), obtained mixture being coked in the second flow to make the target low-sulfur coke.
 Method of low-sulphur oil coke production / 2330872
Invention refers to petrochemical industry, particularly to treatment of black oil in the process of delayed coking. The method of low-sulphur oil coke production is performed by means of delayed coking of a mixture consisting of petrochemical and/or oil processing black oil; at that 10-25% of a hydro refined gasoline fraction of liquid coke products, preliminary heated up to 200-300°C, is added into black oil or into the mixture.
Method of obtaining coke from petrochemical and oil refining residue / 2330056
Invention pertains to the technology of recycling petroleum residues of petrochemical and/or oil refining in a slow coking process, and can be used for improving properties of the obtained petroleum coke. The petroleum coke is obtained by mixing three or more residues of petrochemical and/or oil refining with subsequent slow coking. The said mixture contains not more than 5·105 oligomer particles/cm3, with cross sectional area of more than 1000mkm2, and particles, with cross sectional area in the range of 0.5÷10 mkm2, the fraction of which is not less than 60% of the overall quantity of particles in the mixture.
 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, %.
 Reactor for processing coking petroleum processing waste into liquid fuel and coke / 2315079
Invention relates to apparatuses for isolation of hydrocarbon fractions of liquid fuel and coke from straight-run goudron and acid sludges, aged mazuts, oil slimes, and can be used to utilize indicated wastes. Reactor for isolation of hydrocarbon fractions of liquid fuel and coke from subquality coking products and petroleum processing wastes comprises upright cylindrical body 1 with plane bottom 2 provided with external heater 3 having central opening 21 with connecting pipe 22; feedstock receiver 5 secured to drive shaft 4; perforated sparkling tube 6 rigidly connected to feedstock receiver 5; and knife 7 mounted on shaft 4 before sparkling tube in the direction of rotation of shaft 4 and in parallel to bottom 2 and tube 5. Perforations of sparkling tube 6 are made in the form of through grooves 11 along cylindrical surface of tube 6 and are positioned over plane gutter 12. Sparkling tube 6 bears rod 13 for longitudinal displacement. Rod 13 supports scrappers 16. Body 1 accommodates direct (9) and back (10) pushers of rod 13. Feedstock receiver 5 and sparkling tube 6 are provided with screens 24 and 25. Cutting edge of knife 7 is made in the form of equal-sided corner prominences. Hub 19 with radial inclined blades 20 is attached to lower part of shaft 4 and connecting pipe 22 is provided with radial counterblades.
 Method of speeded down carbonization / 2314333
Method comprises preliminary heating of initial raw material, mixing it with the carbonization gas oil, supplying the mixture to the intermediate tank, heating the raw material up to the temperature of carbonization, and carbonizing it in the carbonization chamber to produce carbon and carbonization distiller. The distiller is supplied to the bottom section of the rectification tower in which it is separated into gas, gasoline, and light and cubic carbonization gas oils. The other heated hydrocarbon raw material is additionally supplied to the bottom section of the rectification tower. The concentration of sulfur in the material is higher than that in the initial raw material . The cubic gas from the rectification tower is carbonized by a known method to produce coke and distiller which is supplied to the bottom section of the rectification tower. The initial raw material can be mixed with the light or heavy carbonization gas oil.
Petroleum coke production process / 2296151
Invention aims at simultaneously producing petroleum coke with low and high contents of volatiles, which coke, after calcination, can be used to manufacture anodes or graphitized products. Process of producing petroleum coke through retarded coking of petroleum residues comprises supplying feedstock to coke chamber at 475-485°C, coking during 14 to 36 h, discharging resulting coke by drilling central well in the coke bulk and cutting coke of the top part of chamber until it is completely emptied at a depth 4-5 m, discharged coke is removed from under the chamber and after that cutting of coke is continued in the lower part of chamber until it is also completely emptied. Thereafter, coke discharged from the top part of chamber and coke discharged from the lower part of chamber are stored separately. The former contains at least 15% volatiles and is used as substitute of sintering and thinning components in coal coking charge in blast furnace coke production and the latter contains no more than 11% volatiles.
 Plant for trapping hydrocarbons from coking reactors / 2255793
Proposed plant includes reservoir for receiving the products heating the coking reactors with piping system equipped with pumps discharging non-conditioned oil products and pipe lines discharging gas for rectification or sprinkling into scrubber for steaming and cooling the coke at discharge of gas into atmosphere and drainage of water condensate into disposal system through hydraulic seal; hydraulic seal is connected via vibrating sieve with near-reactor coke accumulator combined with gravity filter; above-sieve part of vibrating sieve is connected with near-reactor coke accumulator and under-sieve part is connected via gravity filter with deepened circulating water reservoir or with disposal system. Proposed plant makes it possible to return some components of water condensate and cool coke at simultaneous discharge of them to disposal system.
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FIELD: oil-and-gas production. SUBSTANCE: method involves measurement of a temperature parametre, comparison the actual temperature parametre with a given parametre and, depending on the difference value, reduction of this value by changing flow of fuel to burners of the corresponding section coil pipe of the furnace. The temperature parametre used is the temperature profile along the coil pipe and the given temperature profile for each section of the coil pipe is calculated using the formula EFFECT: reduced coking of the coil pipe of the furnace and longer time between repairs of the installation, of which the furnace is a component part. 2 tbl
The invention relates to the field of oil refining, in particular to a method of regulation of the process of thermal decomposition in multi-section tubular furnace. A known method of regulating the heating process and the cracking temperature of the product at the exit of the furnace coil (Smidovich EV Technology of oil and gas processing, part 2, M, Chemistry, 1968, p.86-95). The disadvantage of this method is the lack of control and regulation of the heat supply by the length of the coil (in sections), which causes the danger of coking of the furnace coil and reducing turnaround installation. There is a method of regulation of the process of thermal decomposition of oil residue in the furnace, including the measurement of the actual pressure gradient between the inlet and outlet of each section of the furnace and its comparison with the set with a subsequent decrease in the magnitude of the error by changing the fuel to the burners of the relevant section (U.S. Pat. Of the Russian Federation No. 2318858, op. 10.03.2008, BI No. 7). The disadvantage of this method is the high complexity of the hardware design when implementing method. The closest to the technical nature of the claimed object is a method of regulating thermal regime of the process of obtaining coke in the reactor delayed coking unit depending on the temperature difference of the input in re ctor and vapor outlet thereof by measuring the temperature difference of the raw material at the exit and entrance of each section of the furnace, which compared with calculated and depending on the magnitude of the error change the outlet temperature of each section of the furnace by changing the fuel to the relevant section. Calculated values of the temperature along the length of the coil set for a given temperature difference of the input to the reactor and the vapor outlet thereof and coefficients depending on the nature of the raw material, the temperature of the feedstock at the inlet and outlet of the furnace (A.S. No. 1778134, op. 30.11.92, BI No. 44). The disadvantage of this method is that when the regulation process, first, it is not considered the ultimate value of the conversion of raw materials in one pass, which for visbreaking is 8% (the sum of the output gas and gasoline), and for delayed coking of 7.5 to 12.5% (the sum of the output gas and gasoline), whereas in the known method, this value is 11÷47%. Secondly, when calculating the temperature in a known way using the indicator Δt, which distorts the results of the calculations, as it is used as a constant value, but actually is a variable value and temperature-dependent vapor at the outlet of the reactor, which varies from the beginning to the end of the coking cycle at 40-90°C. furthermore, the temperature of the raw material at the exit and entrance of each section are also variables, which increases the stabilization time of the system and reduces to the number of the regulation. These deficiencies increase the risk of coking of the furnace coil and shorten the duration of a continuous run of installation. The technical result, which is aimed invention is to reduce coking of the furnace coil by improving the quality of regulation of the process of thermal decomposition of oil residue in the furnace coil when receiving products of the required quality. This technical result is achieved in that in the method of regulation of the process of thermal decomposition of petroleum residues in the coil of the furnace, including the measurement of the temperature parameter, comparing the actual temperature of the parameter with the given and depending on the magnitude of the error decreases this value by changing the fuel to the burners of the relevant section of the coil of the furnace, according to the invention as a temperature setting using the temperature profile along the length of the coil, and a specified temperature profile for each section of the furnace coil is calculated by the formula
where t is the relative temperature along the length of the coil, %; k - conversion of raw materials (gas + gasoline, % of raw materials; L - the length of the coil from its beginning to the i-th measuring points, % of total length of the coil of the furnace; a - factor formula; j - the index of the coefficient. efficient formulas and ijhas the following value: for visbreaking
for delayed coking unit
and is determined by the least squares method. Using the temperature profile as measured parameter eliminates variables (Δt, the temperature of the raw material at the exit and entrance at the boundaries of the sections and operative to control and regulate the process of thermal decomposition of petroleum residues in sections in accordance with a specified temperature profile along the length of the coil when receiving products of the required quality and thereby reduce the danger of coking of the furnace coil. The method of regulating thermal decomposition of oil residue in the furnace is as follows. After start-up and warm-up of the technical system at the starting gas in the multicell furnace instead of starting product is served raw material composition (a mixture of tar with thinners, turbulization) under pressure furnace pump, which takes place pipe camera convection and enters the pipe chamber radiation, where it is heated by radiation of the flame of the burning fuel mixture (fuel, air, steam)coming out of the burners located in the furnace. As you progress through the coil of the furnace temperature rises to the temperature of decomposition of si is rd (420-430°C), the volume of the vapor phase increases, respectively, increases the rate of flow increases the temperature in the coil section, the structure of the flow inside the coil also changes and moves from the homogeneous liquid to two-phase (gas - liquid). When the temperature level flow 460-500°C feedstock decomposes more intensively with the formation of low molecular weight components (gas, gasoline, light and heavy gas oils), the volume of flow increases according to the exponential dependence, respectively, increases the flow rate and temperature increases in the current section (section) pipe. In this regard, the magnitude of the temperature difference characterizes the performance of the processes of raw material inside the pipe, which is the result of heat to the flow on this section of the coil of the furnace. In fact, the measured temperature profile is compared with the set and depending on the magnitude of the error this value is reduced by changing the flow rate of fuel to the burners of the relevant section of the coil. The control system must be implemented in hardware, such as programmable logic controllers. The coking of the i-th section of the furnace coil is accompanied by a decrease in the conversion of raw materials, which causes the control system switching control is of less significant value of the coefficient a ijbelonging to a lower value conversion. This is correction of the temperature profile in a softer mode, so it isn't an excessive increase in the fuel supply to the burners of this section and, therefore, prevents further coking of this section and the entire coil of the furnace and increases the duration of continuous run setup. Given the temperature profile of each coil section of the furnace is calculated by the formula above, with coefficients that set the pre-calculation and experimental way. These coefficients depend on the nature of raw materials, given the conversion of raw materials and quality of products of thermal decomposition, as well as from the material design of the coil of the furnace. The absolute value of the temperature profile in sections determined by multiplying the relative (%) profile (gradient) temperature total temperature gradient (°C) coil current installation. The following are specific examples of implementation of the proposed method. Raw tar with a density of 960 kg/m3, cocking behavior 10%, the nominal viscosity at 80°C. WU80°C=80. The raw material is subjected to high temperature heating and cracking in laboratory flow-through installation, which includes: raw material tank, tank pad, gas oil, pump, furnace with coil h is atemperature heating raw materials, valve-pressure regulator, reactor delayed coking unit with electric heating, refrigerating condenser, distillate receiver, gas watch, electrical equipment, control and measuring devices, in particular, at the inlet and outlet of the coil of the furnace, reactor pressure gages are installed. For option at the stage visbreaking cracking temperature in the furnace was 480-490°C, a pressure of 2 MPa. The reactor of the scheme off. Conversion of the raw material (decomposition) is determined by the sum of the output gas and gasoline as a percentage of raw materials. For option delayed coking temperature in the furnace was 480-490°C, a pressure of 2 MPa in the reactor temperature 420-450°C, a pressure of 0.3 MPa. According to the results of experiments data were obtained: ITC distillate, gas composition, material balance, conversion, quality, balance +180°C (boiler fuel), the quality of coke (volatile solids), on which the calculations of industrial furnaces processes visbreaking and delayed coking units at different predetermined conversion of the feedstock in a furnace with a recirculation ratio of 1.2 (Kp=1, 2) upon receipt of the products of a given quality. In table 1 and table 2 shows the experimental and calculated data. From table 1 (examples 1, 2, 3) shows that to improve the quality of balance (+180°C) viscosity breaking by reducing the viscosity from WU80°C=38 to the standard to the more fuel (WU 80°C≤16) it is necessary to increase the conversion of raw materials into the furnace coil from 2.8 to 5.5% (gas + gasoline), while the temperature gradient in the furnace coil increases 1.3 times. From table 2 (columns 5, 6; examples 1, 2, 3) shows that in this case, when the application of the proposed method continuous run of a coil of the furnace is increased by 10-28% (relative) compared to the prototype (column 4). From table 1 (examples 4, 5, 6) also shows that to improve the quality of coke by reducing the content of volatile substances from 9-10 7-8%, it is necessary to increase the conversion of raw materials into the furnace coil from 6 to 10% (gas + gasoline), while the temperature gradient in the furnace coil increases 1.6 times. From table 2 (columns 5, 6; examples 4, 5, 6) shows that in this case, when the application of the proposed method continuous run of a coil of the furnace is increased by 14-26% (relative) compared to the prototype (column 4). Discrepancies between the data presented in table 1 and calculated by the proposed formula, does not exceed 5 Rel.%.
Thus, the proposed method of control of the process allows to minimize coking furnace coil in the processes of thermal decomposition of the oil residue after receipt of the products of the specified quality and to increase the duration of continuous mileage furnace at 10-28% (relative) when visbreaking and 14-26% (relative) during coking. The process control method of thermal decomposition of petroleum residues in the coil of the furnace, including the measurement of the temperature parameter, comparing the actual temperature of the parameter with the specified and, depending on the magnitude of the error, reducing this value by changing the fuel to the burners of the relevant section of the coil of the furnace, characterized in that as the temperature setting using the temperature profile along the length of zaleevich, and the specified temperature profile for each section of the coil is calculated by the formula
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