Method for control of operation mode of coke dry-quenching plant and device for its realisation |
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IPC classes for russian patent Method for control of operation mode of coke dry-quenching plant and device for its realisation (RU 2398005):
       
 Hydroformylation process stabilisation / 2388742
Present invention relates to versions of a method of stabilising the hydroformylation process and a device for realising the said method. One version of the method involves reaction of one or more reagents, carbon monoxide and hydrogen in the presence of a hydroformylation catalyst to obtain an exhaust gas stream and a reaction product stream which contains one or more products, in which the method described above is realised at such partial pressure of carbon monoxide that, the rate of reaction increases when partial pressure of carbon monoxide falls, and falls when partial pressure of carbon monoxide increases; and in which the following steps of the process for stabilising the rate of reaction, total pressure, speed of the exhaust gas stream, reaction temperature or combinations thereof are carried out, process steps including at least one of the following process control schemata, selected from: Scheme A: (a1) setting a given total pressure; (a2) determination of total pressure and determination of the difference between the measured total pressure and the given total pressure; and (a3) based on the pressure difference measured at step (a2), manipulation of the stream of incoming gas which contains carbon monoxide in order to balance the measured total pressure to virtually the given total pressure; and Scheme B: (b1) setting a given speed of the exhaust gas stream; (b2) determination of the speed of the exhaust gas stream and determination of the difference between the measured speed of the exhaust gas stream and the given speed of the exhaust gas stream; and (b3) manipulation of the speed of incoming gas which contains carbon monoxide based on the difference in the speed of the exhaust gas stream measured at step (b2) in order to equalise the determined speed of the exhaust gas stream virtually with the given speed of the exhaust gas stream.
 Reagent dosing method and equipment for implementation / 2382813
Group of inventions related to oil industry, to dosing methods and equipment of reagents, such as demulsifying agents and corrosion inhibitors - oil development and preparation at fields and can be used at oil treatment and water preliminary discharge plants. Preliminary equalise pressure in a reagent tank and accompanying oil gas pipeline. Then regulate reagent flow rate, compare measured with flow metre reagent flow rate value in regulator with reagent flow rate target value, and according hose values difference create a control signal to a control valve, installed on pipe connecting nozzle to the tank. Device contains sealed tank with reagent, located over the pipeline top generating line. A section of a smaller diametre with nozzle mounted into the pipeline. The nozzle connected to the tank via pipeline, with reagent flow metre, connected to the regulator, reagent target flow rate signal transferred to the second end it, and outlet connected with control valve, installed on the pipe connecting nozzle to the tank. The reagent tank connected to the accompanying oil gas pipeline with equaliszing line.
 Method of automatic control of ion-exchange sorption of amino acids from waste water / 2379107
Invention relates to a method of automatic control of ion-exchange sorption of amino acids from waste water and can be used in chemical, food and other industries. The method of automatic control of ion-exchange sorption of amino acids from waste water involves controlling concentration of components of waste water, measuring flow of liquid solutions and their level in reservoirs. Information on flow of the process of ion-exchange sorption of amino acids from waste water is sent to sensors for monitoring level in containers of incoming water, distillate and desorbing solution, acidity of incoming water and during its flow into ion-exchange columns, temperature of the distillate and desorbing solution, concentration of the target component in the incoming water and water at the outlet of the ion-exchange columns and flow through secondary devices, a microprocessor and digital-to-analogue converters to actuating mechanisms for changing parametres of operation of the equipment depending on selected criteria.
 Method of controlling process of removing reduced permanganate compounds when using methanol carbonylation technology / 2376276
First version of the method involves the following steps: distillation of a mixture which contains methyl iodide and acetaldehyde in a distillation apparatus in order to obtain an overhead fraction and a residue, measuring density of the said overhead fraction, determination of relative concentration of methyl iodide, acetaldehyde or both in the overhead fraction based on the measured density and regulation of at least one process variable, associated with the said distillation apparatus. As a response reaction to the said measured density or relative concentration calculated from the measured density, the said process variable is selected from heating intensity, column pressure, the composition fed, condensate composition and coefficient of flow reversal.
 Method for definition of moisture condensation conditions in mixing of two air flows and device for its realisation / 2368936
Stated invention is related to method and device, and may be used in the field of automation of mixed air flows parametres control in ventilation systems. Device for method realisation comprises metres of initial values of temperature and moisture content of mixed flows, metre of barometric pressure, outlets of which are connected to inputs of initial parametres processing and setting. Besides outlet of initial parametres processing and setting is connected to inlet of functional converter of temperature differences, and outlet of functional converter is connected with inlet of computing unit. Also outlet of computing unit is connected to inlet of temperature difference sign analysis unit, outlet of which is connected to inlet of outlet signal generator. Device outlet is outlet of outlet signal generator.
 Method of regulating thermal decomposition of oil residues in tube furnaces / 2367679
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
 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.
 Dry coke quenching method / 2391379
Invention can be used in coal-tar industry. Cooled coke unloaded from a coke-cooler plenum 2 through a stop valve 1. Hot gas enters an exhaust heat boiler 7, where it is cooled, from an accumulation chamber 5 through a dust collecting bin 6 and then back to the coke-cooler plenum 2 through an exhaust fan. Excess gas from the vent of the accumulation chamber 4 is cleaned from dust and then fed through a pipe to a raw gas pipe 11, after which it is further cleaned in a mixture with raw gas from dust, ammonia and resinous substances.
 Installation and method of dry coke quenching / 2388789
In coke quenching chamber 1 there performed is dry coke quenching. Circulation of cooling agent in coke quenching chamber 1 is performed by means of circulation system 2 of cooling agent. From continuous coke discharge device 4 there removed is cooling agent along recirculation circuit 5 of cooling agent to circulation system 2 of cooling agent. There also discharged is excess volume of cooling agent from continuous coke discharge device 4 to burner device 10 of additional heat-recovery boiler 6 via pipeline 112.
 Plant and method for coke dry cooling / 2377273
Invention relates to by-product coke industry. Coke dry cooling is carried out in coke drying chamber 1 by passing cooling agent through coke layer. Cooling agent circulation in said chamber is performed by circulation system 2 furnished with exhaust-heat boiler 3 and induced-draft fan 83. Coke is discharged by continuous discharge system 4 coupled with gas mix circulation circuit 6. Cooling agent circulation circuit 5 communicates continuous discharge system 4 with circulation system 2. Extra exhaust-heat boiler 7 communicates with gas mix circulation circuit 6 and cooling agent circulation system 2.
 Gas pumping unit for coke dry quenching plant and method of operating said unit / 2369627
Invention can be used in chemical-recovery industry. Through a feed pipe 19, inert gas is fed into a cooling chamber 3 of a coke dry quenching plant 1, where it exchanges heat with red hot coke. The heated inert gas comes out through a ring opening 20 in the first dust collector 4. Air is fed into a pre-combustion chamber 2 through a nozzle 17. Temperature sensors 10 are fitted on the inner circumference of the coke dry quenching plant 1. The measured value of temperature inside the pre-combustion chamber 2 is sent to an airflow controller 12, which controls volume of air and circulating gas, fed into the furnace.
 Coke dry-quenching chamber / 2330871
Invention can be used in chemical recovery industry. Coke dry-quenching chamber includes prechamber 1, coke cooling zone 2, inclined flue zone 3, with 300-600 mm long overhang. Partitions 4 of inclined flues 3 are made along the total length of coke cooling zone 2, and feeding gate 5 height of inclined flues 3 is equal to the height of the coke cooling zone 2.
 Method for dry cooling of coke and apparatus for performing the same / 2320698
Method involves charging coke into coke-cooler plenum 1 through charging hole 2. During coke cooling process, water boils in water jacket 4 at temperature of 100 C and water steam is delivered due to pressure difference through upper pipe 5 of water jacket 4 into condenser-heater 7 to be condensed. Condenser flows by gravity through pipeline 9 and returns through lower pipe of water jacket 4 into coke-cooler plenum. Heat released from condensed steam heats air running around heat-exchanging surface of condenser-heater 7. Air is delivered by means of fan 11 and is fed to consumer. Cooled coke is discharged through discharging device 3.
 Method dry quenching of coke / 2236436
The invention relates to metallurgy, in particular to the production of coke in coke ovens and dry quenching
 The camera dry quenching of coke / 2178439
The invention relates to coke production and can be used in devices for dry quenching of coke
 Boot device installation dry quenching of coke / 2123024
The invention relates to the coking industry, namely, devices for loading the camera dry quenching of coke
 The dry quenching facility / 2111230
The invention relates to coke production, namely the dry quenching of coke with a continuous discharge is extinguished coke from the camera extinguishing
Method for dry cooling of coke and apparatus for performing the same / 2320698
Method involves charging coke into coke-cooler plenum 1 through charging hole 2. During coke cooling process, water boils in water jacket 4 at temperature of 100 C and water steam is delivered due to pressure difference through upper pipe 5 of water jacket 4 into condenser-heater 7 to be condensed. Condenser flows by gravity through pipeline 9 and returns through lower pipe of water jacket 4 into coke-cooler plenum. Heat released from condensed steam heats air running around heat-exchanging surface of condenser-heater 7. Air is delivered by means of fan 11 and is fed to consumer. Cooled coke is discharged through discharging device 3.
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FIELD: oil and gas production. SUBSTANCE: invention can be used in chemical-recovery industry. Coke is loaded into coke-cooler plenum 8. Circulating gases are removed from coke-cooler plenum 8 with the help of draft system 7 and supplied into waste heat boiler 2. Produced superheated steam is removed from waste heat boiler 2 along steam line 9. Downstream waste heat boiler 2 circulating gases again arrive into coke-cooler plenum 8. In order to control actual flow rate of circulating gases and maintenance of superheated steam temperature at specified level, data obtained from superheated steam temperature sensor 1, sensor 3 of circulating gases temperature at the inlet to waste heat boiler 2, sensor 4 of circulating gases temperature at the outlet from waste heat boiler 2 and sensor 5 of circulating gases flow rate is sent to control unit 6. After processing of obtained data, control unit 6 generates signal of draft system 7 control. EFFECT: invention makes it possible to increase accuracy of superheated steam control and to reduce power inputs. 3 cl, 1 dwg
The technical FIELD The claimed group of inventions relates to the coking industry and can be used in the coke dry quenching facility. The LEVEL of TECHNOLOGY In CDCP coke quenching is carried out by circulating gas which circulates through the path using exhaust device. Parts of the facility are also Luggage coke quenching, cleaning system circulating gases and the boiler. In the chamber of the coke is coke cooling by means of recirculated gases. The boiler is designed to heat the circulating gases that depart from the camera to the quenching. At the output of the boiler to receive superheated steam, which is used for technological needs. A significant portion of energy consumption in the dry quenching of coke is spent on the exhaust system, which ensures the regulation of the flow rate of the circulating gas, so reducing energy consumption can be achieved by optimizing the mode of operation of the facility, which is an important task during its operation. The superheated steam temperature is an important indicator of the operation of the facility and must be maintained at a given level, which is also achieved by optimization of the mode of operation of the facility. Operating experience from CDCP it is known that the temperature of the superheated parasassi flow rate of the circulating gas in the circuit of CDCP, namely, when the flow rate increases circulating gases, the temperature of the superheated steam is reduced, and Vice versa. The flow rate of the circulating gas, which is required to provide a nominal temperature of superheated steam, depends on the load of CDCP on coke, temperature coke and some other parameters. Due to the imperfection of the existing schemes regulating the temperature of superheated steam, in particular, unstable load facility, the superheated steam temperature is changed in an invalid range. In this case, if the temperature of the superheated steam falls below the nominal value, the energy consumption for operation exhaust device increases by a proportional amount. Known methods and devices for regulating the mode of operation of the facility, which differ from each other by a range of measurable indicators and effectiveness of the regulation. CHARACTERISTICS of KNOWN METHODS The known method of regulating the mode of operation of the facility, according to which the temperature control of superheated steam is produced by introducing into a stream of superheated steam cooling agent, in particular feed water (see Kazarnovskaya E.M. temperature control of superheated steam to power steam plants, M., "Metallurgizdat", 1960, p.50-53). The method consists in the fact that the flow of superheated steam is introduced to the cooling gap is surrounding the agent, which is evaporated by the heat of superheated steam mingling with them, and lowers the temperature of the superheated steam at the required value. The disadvantages of this method are: 1. Limited load range of the boiler with a rated temperature of the superheated steam. 2. The instability of the superheated steam temperature. 3. Additional costs associated with the use of equipment required for submission under the pressure of the cooling agent into the superheated steam. 4. The lack of control of the flow rate of the circulating gas for coke quenching, leading to increased energy consumption. The above-mentioned disadvantages associated with ineffective regulation of the mode of operation of the facility, due to lack of item measurable indicators, which do not allow to provide adaptive control of the process of coke. The known method of regulating the mode of operation of the facility, according to which control of the temperature of superheated steam, the temperature of the circulating gas at the inlet to the HRSG to the formulation of the control unit commands theduties device (see A.S. USSR №1017008, publ. 23.03.92, IPC SW 39/02). In a known method further control the pressure of the circulating gases before theduties device. The disadvantages of this method are: 1. N. the stability of the superheated steam temperature. 2. Significant energy costs associated with inefficient working draft. The above-mentioned disadvantages due to the slight dependence of the measured indicator, namely the magnitude of the underpressure before theduties device, the temperature of the superheated steam. At the same time, the magnitude of the value of underpressure before theduties the device is changed during operation of the facility, for example, by the partial blockage by coke oblique moves the camera suppression, which leads to excessive consumption of the circulating gases and, accordingly, increasing energy consumption when carrying out the known method. CHARACTERISTICS of KNOWN DEVICES Know the device controlling the mode of operation of the facility, which is used in the dry quenching of coke containing the sensor temperature of superheated steam, the output of which is connected with a control unit and a system for introducing a cooling agent into the superheated steam (see Kazarnovskaya E.M. temperature control of superheated steam to power steam plants, M., "Metallurgizdat", 1960, p.50-53). The disadvantages of the known devices are: 1. Limited load range of the boiler with a rated temperature of the superheated steam. 2. The instability of the superheated steam temperature. 3. Additional costs associated with the use of equipment is Finance, required for submission under the pressure of the cooling agent into the superheated steam. 4. The lack of control of the flow rate of the circulating gas for coke quenching, leading to increased energy consumption. The above-mentioned disadvantages associated with inefficient temperature control of superheated steam, due to lack of item measurable indicators, which do not allow to provide adaptive control of the process of coke. Know the device controlling the mode of operation of the facility that contains the control unit, the output of which is connected with traducianism device, the sensor of the superheated steam temperature, the output of which is connected to the first input of the control unit, the temperature sensor circulating gases at the inlet to the HRSG, the output of which is connected with the second input of the control unit (see A.S. USSR №1017008, publ. 23.03.92, IPC SW 39/02). In the known device is additionally installed sensor vacuum recirculating gases before theduties device. The disadvantages of the known devices are: 1. The instability of the superheated steam temperature. 2. Significant energy costs associated with inefficient working draft. The disadvantages inherent in the known device, associated with inefficient way of regulating the mode of operation of the facility, which is implemented Dunaevskaya. The above-mentioned disadvantages associated with minor dependence of the measured indicator, namely the magnitude of the underpressure before theduties device, with the temperature of the superheated steam. This is because the vacuum before theduties device may change during operation of the facility for various reasons that are not related to the temperature of superheated steam, for example, by the partial blockage by coke oblique moves the camera extinguishing. This also increases the cost associated with the work of the exhaust device, and the increasing frenzy of coke. The INVENTION The task of the group of inventions is to develop a method and device for its implementation, which are characterized by high accuracy of temperature control of superheated steam and low energy consumption. This object is achieved in that in the known method of regulating the mode of operation of the facility, according to which control of the temperature of superheated steam, the temperature of the circulating gas at the inlet to the HRSG to the formulation of the control unit commands theduties device according to the present method controls the temperature of the circulating gas at the outlet of the boiler, control the actual flow rate of the circulating gas, then the data about the temperature the e circulating gases at the outlet of the boiler, as well as data on the actual consumption of the circulating gases act on the above-mentioned control unit for generating a control command according to which data on a design flow of recirculating gases act on the aforementioned draft device. So the actual flow rate of the circulating gas is provided in accordance with the estimated flow rate of the circulating gas. In the private version of the method for determining the design flow rate of the circulating gases is carried out on the basis of the following dependencies:
where B1- the actual flow rate of the circulating gas, m3/h; In2- estimated flow of circulating gas, m3/h; A, k - values, depending on the design and parameters of the CDCP; Q1the actual heat load of coke dry cooling plant, j/h; Q2- estimated heat load of coke dry cooling plant, j/h; T - the set value of the superheated steam temperature, °C; C1- heat capacity of the circulating gas at the inlet to the HRSG, j/(m3°C); With2- heat capacity of the circulating gas at the outlet of the HRSG is, J/(m3°C); t1- the temperature of the circulating gas at the inlet to the HRSG, °C; t2- the temperature of the circulating gas at the outlet of the boiler, °C. The use of the method of regulating the operation mode of the CDCP is a continuous determination of design flow rate of the circulating gas, which directly affects the value of the superheated steam temperature in the facility and allows you to instantly respond to changes in temperature of superheated steam, due to rapid changes of the flow rate of the circulating gases. The design flow of the circulating gases, calculated on the basis of dependencies (1-5)provides for the maintenance of accurate values of the superheated steam temperature, and can reduce the energy consumption of the facility. A DEVICE FOR IMPLEMENTING the proposed METHOD This object is achieved in that in the known device regulation mode of operation of the facility that contains the control unit, the output of which is connected with traducianism device, the sensor of the superheated steam temperature, the output of which is connected to the first input of the control unit, the temperature sensor circulating gases at the inlet to the HRSG, the output of which is connected with the second input of the control unit according to the present invention the device is provided with a temperature sensor circulating the Azov at the exit of the boiler, the output of which is connected with the third input of the control unit and the sensor of the flow rate of the circulating gas, the output of which is connected with the fourth input of the control unit. The use of control device operation mode CDCP is continuous determination of design flow rate of the circulating gas, which directly affects the value of the superheated steam temperature in facility that allows you to instantly respond to changes in temperature of superheated steam, due to rapid changes of the flow rate of the circulating gas, and also allows to reduce the energy consumption of the facility. Also, using the inventive device is provided, the reduction of coke burn-off due to reduction of air flowing in CDCP at the optimum flow rate of the circulating gas, which allows to increase the yield of coke. DRAWINGS The method of regulating the operation mode of the CDCP and the device for its implementation are explained using the drawing (Figure 1), which is attached to the description of the claimed group of inventions, and by the graph (Figure 2), which is also attached to this description. Thus, figure 2 shows two graphs a and b, which were built on the basis of the dependence of B2=A+kQ2. While graphics And corresponds to the obtained dependence (1) for facility performance 52 t/h (example 3 n the present description), and graphics To match the obtained dependence (1) for facility performance 74 t/h (example 4 of the present description). The IMPLEMENTATION of a GROUP of INVENTIONS The claimed group of inventions, namely, the method of regulating the operation mode of the CDCP and the device for its implementation, was implemented as follows. Each facility has its own individual characteristics, for example, the volume of the chamber, coke quenching, cleaning systems recirculating gases, the type of heat exchange surfaces, etc. that affect the determination of the design flow rate of the circulating gases. So when you start CDCP it is necessary to test its operation in the test mode, which determines the value of the superheated steam temperature and the corresponding values of controllable parameters, and determine the calculated value of the heat load of coke dry cooling plant. Then use statistical methods are set according to (1-5), which are further used in the operation of the facility. When implementing the method for controlling the mode of operation of the facility after determining dependencies (1-5) in the test mode of operation of the coke dry cooling plant is the following sequence of actions: 1. Measured actual flow rate of the circulating gas, B1. 2. Measured f the static heat load of coke dry cooling plant, Q1. 3. On the basis of the dependence (1) is determined by the calculated value of the flow rate of the circulating gas, B2. 4. Compares the values of B1and B2. If they do not match, then using the exhaust device changes the actual flow rate of the circulating gas, which is set to B2. EXAMPLE 1 of the METHOD In CDCP was required to ensure the value of the superheated steam temperature (T). This was used by the claimed method of regulating the mode of operation of the facility. Made a test mode operation of the coke dry cooling plant, which were determined coefficients a and k for the immediate implementation of the proposed method in accordance with dependencies (1-5). According to the claimed method the temperature of the superheated steam was controlled by sensor 1. The temperature of the circulating gas at the inlet to the HRSG 2 was controlled by the sensor 3. With the help of the sensor 4 controlling the temperature of the circulating gas at the outlet of the boiler 2. The actual flow rate of the circulating gas was controlled by sensor 5. The obtained data about the temperature of the circulating gas at the entrance to the boiler 2, the data about the temperature of the circulating gas at the outlet of the boiler 2, the actual flow rate of the circulating gases in the village who fell in the control unit 6 to generate the control commands theduties device 7. Determination of design flow rate of the circulating gas (B2) was carried out on the basis of dependencies (1-5). The above method of regulating the temperature of superheated steam was implemented in the facility. In the chamber of the coke quenching 8 downloaded coke. In the operation of the CDCP actual heat load of coke dry cooling plant has changed over time and differed from the nominal value. Circulating gases, which took away from the camera to the quenching 8 through the exhaust device 7, was admitted to the boiler 2. In which formed the superheated steam, which was given from the recovery boiler 2 steam line 9. Received by the control unit 6 data on a design flow of recirculating gases were received on the draft device 7, which provides the necessary hydraulic mode of operation of the facility. In operation, the CDCP has been a continual change of the controlled parameters which were changed due to cooling of the coke, the magnitude of the loading chamber of the coke quenching 8 and other factors. Data on the indicators that were changed, were transferred to the control unit 6, which has processed the received data to generate control commands for the draft device 7, which can provide optimal and continuous maintenance of the hydraulic regime with the aim of gaining the required temperature of superheated steam, which was given from the recovery boiler 2 steam pipe 9. It should be noted that in the process of CDCP when changing the controlled parameters of the actual flow rate of the circulating gases leads to deviations from the optimum hydraulic regime that, in turn, leads to a change in temperature of superheated steam, the data which is continuously output to the control unit 6. Causing the control unit 6, to maintain the setpoint temperature of superheated steam, produces estimates of the flow rate of the circulating gas to change the actual flow rate of the circulating gas to the calculated value. Thus, the present invention provides an adaptive management process facility. EXAMPLE 2 the implementation of the DEVICE The device for implementing the method for controlling the mode of operation of the facility is intended for use in the dry quenching facility, which contains the camera coke quenching 8, HRSG 2, which is given superheated steam to the steam pipe 9, the cleaning system of the circulating gases and the exhaust device 7. The device is characterized by the presence of the control unit 6, the output of which is connected with traducianism device 7, the sensor 1 temperature of superheated steam, the output of which is connected to the first input of the control unit 6, the sensor 3 temp is the temperature is elevated circulating inlet gas heat recovery boiler 2, the output of which is connected with the second input of the control unit 6. The device also has a sensor 4, the temperature of the circulating gas at the outlet of the boiler 2, the output of which is connected with the third input of the control unit 6, and the sensor 5 of the flow rate of the circulating gas, the output of which is connected with the fourth input of the control unit 6. The device operates as follows. In the chamber of the coke quenching 8 download coke. In the operation of the CDCP actual heat load of coke dry cooling plant changes over time and differs from the nominal value. Circulating gases that depart from the camera to the quenching 8 through the exhaust device 7, enter the HRSG 2, in which the waste heat of the circulating gases. The resulting superheated steam, which is drained from the boiler 2 through the steam pipe 9. After boiler 2 circulating gases were again received into the chamber of the coke quenching 8. In operation, the facility is operational regulation of the actual flow rate of the circulating gases and ensure that the temperature of superheated steam at a given level. For this purpose, the data obtained from the sensor 1 temperature superheated steam, sensor 3 temperature of the circulating gas at the entrance to the boiler 2, sensor 4 temperature circus is stimulating gases at the outlet of the boiler 2 and the sensor 5 flow circulating gases, go into the control unit 6, which processes the received data, then the control unit 6 generates a control signal theduties device 7. This results in maintaining at a given level of the superheated steam temperature when changing the actual heat load of CDCP (Q1), namely decreasing the actual heat load of CDCP (Q1) there is a reduction of the actual flow rate of the circulating gas (B1) to the calculated value of the flow rate of the circulating gas (In2)that maintains the temperature of superheated steam (T) at a given level and reducing energy consumption by optimizing working draft device 7. EXAMPLE 3 of the METHOD In CDCP, the performance of which was 52 t/h Cox was required to ensure the value of the superheated steam temperature of 440°C. this was used by the claimed method of regulating the mode of operation of the facility. The calculated indicators mentioned CDCP were as follows, see table 1.
The nominal value of thermal load of dry coke quenching (Q1) at 100% 18 Gcal/h Made a test mode operation of the facility, the data entered in the log of the tests, including the actual value of the temperature of superheated steam, the temperature of the circulating gas at the inlet to the HRSG (t1), the temperature of the circulating gas at the outlet of the boiler (t2), the actual consumption (B1and the composition of the circulating gases. The composition of the circulating gas was as follows: N2=75,7%, CO=11%, CO2=10%, O2=0,8%, SN4=0,5%, N2=2,0%. Based on these data determined the heat capacity of the circulating gas at the inlet to the HRSG (C1), the heat capacity of the circulating gas at the outlet of the boiler (C2). Table 2 presents the obtained average values pointed to by the x parameter.
Based on the above data defined functional dependence of B2=A+kQ2, which took the following form: B2=4,17·103+4,296×Q2. where the value A=4,17·103[nm3/h], and the value k=4,296 [nm3/Gcal]. Figure 2 above obtained dependence is depicted in the graph of A. In the result set values of the superheated steam temperature (T) when you change the actual heat load of CDCP (Q1strictly remain at a given level is 440°C. Table 3 shows the obtained values of superheated steam and the actual value of the temperature of superheated steam for facility performance 52 t/h
The results of the tests are shown in table 3, indicate that the claimed group of inventions provides increased accuracy maintain the temperature of superheated steam and optimization of energy consumption draught of the device by reducing the actual costs of the circulating gases. EXAMPLE 4 the METHOD In CDCP, the performance of which was 74 t/h Cox was required to ensure the value of the superheated steam temperature 440°Sdla this was used in the claimed method of regulating the mode of operation of the facility. The calculated indicators mentioned CDCP were as follows, see table 4.
The nominal value of thermal load of dry coke quenching (Q1) at 100% 25,84 Gcal/h Made a test mode operation of the facility, the data entered in the log of the tests, including the actual value of the temperature of superheated steam, the temperature of the circulating gas at the inlet to the HRSG (t1), the temperature of the circulating gas at the outlet of the boiler (t2), the actual consumption (B1and the composition of the CID is Wirayuda gases. The composition of the circulating gas was as follows: N2=75,7%, CO=11%, CO2=10%, O2=0,8%, SN4=0,5%, N2=2,0%. Based on these data determined the heat capacity of the circulating gas at the inlet to the HRSG (C1), the heat capacity of the circulating gas at the outlet of the boiler (C2). Table 5 presents the obtained average values of the specified parameters.
Based on the above data defined functional dependence of B2=A+kQ2, which took the following form: B2=6,07·103+4,297×Q2 where the value A=6,07·103[nm3/h], and the value k=4,297 [nm3/Gcal]. Figure 2 above obtained dependence is depicted in the graph Century In the result set values of the superheated steam temperature (T) when you change the actual heat load of CDCP (Q1strictly remain at the specified level. Table 6 shows the obtained values of superheated steam and the actual value of the temperature of superheated steam for facility performance 74 t/h
The results of the tests are shown in table 6, show that C is presented the group of inventions provides increased accuracy maintain the temperature of superheated steam and optimization of energy consumption draught of the device by reducing the actual costs of the circulating gases. 1. The method of regulating the operation mode of the coke dry cooling plant, according to which control of the temperature of superheated steam, the temperature of the circulating gas at the inlet to the HRSG to the formulation of the control unit commands theduties device, wherein controlling the temperature of the circulating gas at the outlet of the boiler, control the actual flow rate of the circulating gas, then the data on the temperature of the circulating gas at the outlet of the boiler, the actual flow rate of the circulating gases act on the above-mentioned control unit for generating a control command according to which data on a design flow of recirculating gases act on the aforementioned draft device. 2. The method of regulating the operation mode of the coke dry cooling plant according to claim 1, characterized in that the determination of design flow rate of the circulating gases is carried out on the basis of the following dependencies: 3. The device controlling the mode of operation of the coke dry cooling plant that contains the control unit, the output of which is connected with traducianism device, the sensor of the superheated steam temperature, the output of which is connected to the first input of the control unit, the temperature sensor circulating gases at the inlet to the HRSG, the output of which is connected with the second input of the control unit, characterized in that the device is provided with a temperature sensor circulating gases at the outlet of the boiler, the output of which is connected with the third input of the control unit and the sensor of the flow rate of the circulating gas, the output of which is connected with the fourth input of the control unit.
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