Method of automatic control of ion-exchange sorption of amino acids from waste water |
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IPC classes for russian patent Method of automatic control of ion-exchange sorption of amino acids from waste water (RU 2379107):
 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.
 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.
 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 for performing ion-exchange sorption of molybdenum on anionite vp-1 an / 2437841
To realise the method, an initial sorbent - anionite VP-1 An is divided into two fractions according to particle size, where the division boundaries are selected such that the coarse and fine fractions have equal effective weight. The treated stream of molybdenum stream is first passed through a fixed layer of the coarse fraction, and the stream combined on the target component is passed through a fixed layer of the fine fraction.
 Method for automated oils mixing management, said oils being manufactured from oil product, by means of forming mixing timetables in real time / 2246984
Method is based on use of computer system, including an optimizer, tables for selection of goal function, block for determination of optimization method. Database for recording inputted information and received results is used as well as block for importing data concerning initial state of reservoir fleet and mixing task. Graphic user interface is used to indicate and alter current data during creation of timetable, parameters for optimizer adjustment and indication of textual and graphical system reports. Block for controlling trustworthiness of initial data for forming the best timetable, block for generation of optimization task matrix and block for interpretation of results of optimization task solution are used. Data concerning amount of components, admixtures and product oils in all mixing reservoirs at the moment of beginning of timetable creation, concerning planned tasks for readiness of product oils at certain time moment in accordance to shipment graph, concerning mixing receipts and certification time for each oil, concerning mixing time and readjustment of mixing reservoir during transfer from one oil type to another, concerning speed of feeding of each component and admixture from appropriate reservoirs, concerning configuration of area of mixing and amount of mixing reservoirs are all transferred to computer system from data import block. After check of physical possibility, linear programming matrix is generated for use by optimizer, which automatically selects an optimization method for determination of the best timetable, which is interpreted in form of series of mixing of given product oils, beginning and ending time for each mixing, transfer of each component and admixture from appropriate reservoirs for mixing of each oil, beginning and ending time for feeding of prepared oil directly after mixing and certification into appropriate product reservoir, time of switching feeding of component after filling of one component reservoir to another by results interpretation block.
 Method for automatic controlling of continuous malting process / 2248390
Method involves providing continuous malting process in rotating drum; measuring and stabilizing temperature of malt by changing air flow rate for cooling of grain under germination procedure; additionally measuring malt moisture content and regulating it depending on changing of malt moisture content as compared to set values by changing water supply for grain moistening during germination process; also, regulating water supply for cooling air and correcting changing of air flow rate for cooling of grain under germination process depending on changed temperature of malt as compared to set values.
Method of automatically governing biotechnological process / 2248399
Invention concerns governing periodical air-intake biotechnological process carried out in bioreactor. Method comprises measuring oxygen content in effluent gas, working volume of culture medium, concentration of biomass, and concentration of intermediate product of its vital activity. Measured parameters allow specific oxygen consumption rate and velocity of intermediate product concentration change to be determined to enable regulation of feeding air used in aeration, supplying nutritional medium, and agitating culture medium. Moreover, temperature of culture medium, temperature of supplied and withdrawn cooling agent, and consumption of the latter are measured to use these parameters for determining biomass heat release rate and velocity of intermediate product amount change. The two latter parameters enable regulation of feeding air used in aeration and supplying nutritional medium. The following characteristics are thus improved: elevating power by 8.1%, maltase activity by 7.9% and resistance by 7.4%.
 Method for automatically starting manufacturing plants operating with use of brief processes / 2252916
Automatic starting of manufacturing plant is realized according to predetermined algorithm with use of controller on base of microprocessor system. At first preset flow rates of components in starting pipelines of reactor, of plug or of sanitary system are set with use of flow rate regulators. Then operation mode of said regulators is changed to automatic one. Then flows of components are fed with the aid of cut off valves controlled by means of controller. Conditions simulating hydrodynamic mode of plant are realized in starting pipelines at time moment of feeding components.
 Automatic control apparatus for process of concrete heat treatment in thermo-active forms / 2256209
Apparatus includes heaters for heating placed concrete mixture, pickups for detecting concrete mixture temperature, temperature regulator that limits temperature of surface layer of concrete and in addition it includes pickups for detecting temperature of outer air and wind speed, pickups for detecting concrete temperature in zones of its contact with heaters, concrete strength pickup and second temperature regulator. First temperature regulator controls temperature of heat transfer agent of outer board and second temperature regulator controls temperature of inner board.
 Control method for high-viscous oil product discharge from railroad tank cars / 2257327
Method involves determining temperature of outer tank car wall by measuring thereof in lower tank car case portion, which is the nearest to tank car bottom; comparing the measured temperature with one estimated from heat calculations performed with the use of control computer. The temperature is calculated from well-known correlations with taking into consideration previously measured temperature of ambient air and wind velocity, technical characteristics of tank cars, physical properties of oil product to be discharged and air.
 Method for automatic control of sugar liquoring process and system for automatic control of realization of this method / 2260832
Method for automatic controlling of sugar liquoring process in horizontal sectional liquoring continuous-action mixer and accumulating mixer includes changing flow of liquoring solution with consideration of liquoring concentration in accumulating mixer. Into sections, where concentration of dry substances does not exceed 18%, lime milk is fed, flow of which is adjusted so, that pH of liquoring in this sections was 10,8-11,2, and stop of sugar feeding into liquoring mixer is performed when liquoring level in accumulating mixer reaches certain level. System for automatic control of sugar liquoring process in horizontal sectional liquoring continuous-action mixer and accumulating mixer includes level sensor in accumulating mixer, mounted in said mixer, liquoring concentration sensor and liquoring solution feeding adjuster into first section of liquoring mixer. Each section of liquoring mixer, except last one, is provided with branch pipe for feeding lime milk, pH indicator and dry substances concentration indicator. Also, system is provided with serially connected valve for stopping sugar feed into liquoring mixer and adjuster, input of which is connected to level indicator, mounted in accumulating mixer, while the latter is connected to liquoring solution feeding adjuster into first section via set-point device, connected to concentration sensor. Use of device allows to increase efficiency of sugar purification due to forming of favorable conditions for decomposition of reducing substances during liquoring. Containment level of reducing substances in sugar liquoring is decreased in 1,4-1,4 times.
 Method to control the process of production of polyethers and demulsifying agents on their base / 2265030
The invention is pertaining to the field of chemical industry, in particular, to the methods of control over the chemical-technological processes of production of polyethers and demulsifying agents on their basis. The method of control over process of production of the alkaline polyethers and demulsifying agents is conducted in the mixers and in the reactor-etherificator at realization of reaction of the oxypropropylation and oxyethylation with utilization of the allocated zones of regulation and contours of circulation of the reaction mixture. Conduct corrective actions of control over the steam and a condensate consumption moisture and at that additionally install a can with a bubbler for a polyether and a detector of methanol consumption, a reactants stirring device, sensor units of consumptions, measuring tools and other equipment. For production of demulsifying agents from polyethers use cans with stirring devices with measurers and batchers components, screens for removal salts and the mechanical impurities, connected by corresponding pipelines with formation of contours of circulation of the reaction mixture equipped by means of measuring and control. The technical result is formation of the interrelated process control of production of polyethers and demulsifying agents. The invention allows to reduce power inputs and to expand the assortment of the produced products.
 Process for automatic control of sugar clarification and automatic control system for performing the same / 2267149
Method for automatic control of clarification of sugar by means of sugar-containing solution in successively joined auger and horizontal sectional clarifying agitator at supplying sugar to auger comprises steps of controlling flow rate of sugar-containing solution to clarifying agitator depending upon concentration of dry matters in clarified product; supplying to auger catholyte with pH 10 - 11.5 and feeding to first section of clarifying agitator milk of lime; controlling flow rate of catholyte in such a way that in those section of clarifying agitator where clarifying process is going on for 4 - 6 min concentration of dry matters is in range 12 -18% and controlling flow rate of milk of lime in such a way that pH in the same section is in range 10.8 - 11.5; supplying sugar- containing solution to next sections of clarifying agitator along motion direction of sugar in it; measuring concentration of dry matters in order to control flow rate of sugar-containing solution in last section of clarifying agitator. Automatic control system for controlling clarification of sugar in successively joined auger and horizontal sectional agitator includes circuit for stabilizing concentration of dry matters of clarified product with use of pickup for measuring concentration of dry matters. Auger is provided with branch pipes for feeding catholyte into it. Clarifying agitator includes branch pipe for feeding lime of milk to first section. Pickup for measuring concentration of dry matters is arranged in last section of clarifying agitator. System includes in addition circuit for controlling quality of clarification having pickups for measuring pH and concentration of dry matters, both placed in one section of clarifying agitator and pickup for measuring catholyte flow rate; regulators and valves. One valve is mounted inline for feeding milk of lime and other valve is mounted inline for feeding catholyte.
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FIELD: chemistry. SUBSTANCE: 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. EFFECT: invention increases accuracy of control and minimises energy and material costs. 1 dwg
The present invention relates to methods and systems for automatic process control of ion exchange sorption of target components from the wastewater and can be used in chemical, food and other industries. A known method for automatic control and regulation of the content of surfactants in aqueous process solutions [an Application for a patent of the Russian Federation 2000127702, CL. G01N 33/18, 35/00, Publ. 01.27.2003], including the control and regulation of the content of surfactants in aqueous solution cleanser. The disadvantage of this method is the lack of automatic control methods target component that does not provide operational regulatory process. The known method for automatic process control of wastewater treatment in the device [RF Patent 94015544, MKI C02F 3/02, Appl. 27.04.1994, publ. 10.04.1996,] including control of concentrations of ingredients wastewater flow measurement of liquid solutions and their level in the tanks. The disadvantage of this method is the low precision, since it does not provide control of the target component in the wastewater inlet and the exhaust regenerating solution. The closest in technical essence and the achieved effect to the present invention is a method of controlling inoome the major water purification installation [A.S. 1389838, MKI B01J 47/02, Appl. 12.06.1986, publ. in B. I., 1988, No. 15], including the control and regulation of the flow of regeneration solution and the treated water. The disadvantage of this method is the low precision, since it does not provide control of all operating parameters of the equipment and their changes depending on the selected criteria. An object of the invention is to improve the accuracy of the control and regulation of the operating parameters of the equipment depending on the selected criteria. The technical object of the invention is achieved by a method for automatic process control of ion exchange sorption of amino acids from wastewater, including the control of concentrations of ingredients wastewater flow measurement of liquid solutions and their level in the tanks, what's new is that advanced in the automatic mode in the source water measure the acidity level and maintain it at the required level, the source water is fed into the first ion-exchange column filled with sulfonic cation exchanger, and produce control over its consumption, which adjust to the optimum filtration rate in the first ion-exchange column and when reaching the residual concentration of the target component in the form of amino acids, the corresponding point "breakthrough", make the inclusion of a slave is that the second ion-exchange column, filled with sulfonic cation exchanger, by direction of the flow of treated water from the first ion exchange columns in the second ion-exchange column with simultaneous filtration of treated water through the first and second columns, thus provide measurements of the concentration of the target component in the form of amino acids at the output of the first and second columns and achieve the concentration of the target component in the form of amino acids at the output of the first column equal to the concentration at the inlet in the first column, switch it on regeneration, which includes stages of displacement acidic wastewater and desorption, and when you reach the result of filtering the waste water through the second column the residual concentration of the target component in the form of amino acids, the corresponding point "breakthrough", make the inclusion of the third ion exchange columns filled with sulfonic cation exchanger, by direction of the flow of treated water from the second ion exchange column in the third column with simultaneous filtration of treated water through the second and third columns, and the displacement of acidic wastewater remaining in each of the three columns after sorption, carried out by feeding them in preheated distillate in the direction opposite to the direction of flow of water by sorption, and the output of each of the three columns measure kislotno the ü distillate, level which is judged about the end of phase displacement and the early stage of desorption, which is carried out by filtering the pre-heated Stripping solution through the layer of sulfonic cation exchanger in each of the three columns with monitoring and controlling the flow desorbing solution to the optimal filtration rate during desorption, and after passing through the Stripping solution through each of three ion exchange columns, select it in the form of acidic concentrated eluate and stop stage desorption upon reaching the initial values of acidity Stripping solution, and after the first regeneration column and displacing the Stripping solution of the distillate, it is included in the work for the implementation of the sorption in the second column on the stage of recovery and the achievement of in the treated water during the filtration process in the third column of the residual concentration of the target component in the form of amino acids corresponding to the point "breakthrough", and the information about the course of the process of ion exchange sorption of amino acids from wastewater is transferred from the sensors to the control level in the source water tanks, distillate and Stripping solution, the pH of the source water and the flow in the ion exchange column, the temperature of the distillate and Stripping solution, the concentration of the target komponentov the source water and the water at the outlet of ionoobmennyh columns and flow through the secondary devices, in microprocessor and digital to analog converters of the actuators to change the operating parameters of the equipment depending on the selected criteria. The technical result is to increase the accuracy of the control and regulation of the operating parameters of the equipment depending on the selected criteria. The drawing shows the diagram of a method for automatic process control of ion exchange sorption of amino acids from wastewater. The diagram of a method for automatic process control of ion exchange sorption of amino acids from waste water include ion exchange columns (adsorbers) vertical type 1, 2, 3, the capacity of the water source 4, tanks for distillate 5 and regenerating solution 6 with heating elements respectively 7 and 8, control valves 9-26. The diagram of a method for automatic process control of ion exchange sorption of amino acids from wastewater also includes a line 27 to the filing of the original water in the ion exchange column 1, line 28 supply of treated water in the ion exchange column 2, line 29 supply of treated water in the ion exchange column 3, line 30 removal waste water, line 31, 32, 33 supply of distillate in ion-exchange columns 1, 2 and 3, line 34 removal of distillate from the ion exchange columns 1, 2 and 3, lines 35, 36, 37 feed regenerating solution, respectively in ion to the h-1, 2 and 3, line 38 of the spent regenerating solution from the ion exchange columns 1, 2 and 3, lines 39, 40, 41 feed partially processed water from the ion exchange column 1 in the ion exchange column 2, of the ion exchange columns 2 ion exchange column 3 from the ion exchange columns 3 in the ion exchange column 1, level sensors 42, 43, 44, respectively, in the source water tanks 4, distillate 5 and regenerating solution 6, the sensors acidity 45-51, respectively in the source water when it is fed through the ion exchange columns 1, 2 and 3, in the distillate, removed from the ion exchange columns 1, 2 and 3, the spent regenerating solution from the ion exchange columns 1, 2 and 3, the temperature sensors 52, 53, respectively, of the distillate in the tank 5 and regenerating solution in the vessel 6, the sensors, the concentration of the target component 54-57, respectively, in the source water and treated water at the outlet of the ion exchange columns 1, 2, 3, sensors 58-72 flow, secondary devices 73-100, the microprocessor 101, the digital-analog converters 102-121, actuators 122-141. Method for automatic process control of ion exchange sorption of amino acids from wastewater is as follows. Wastewater containing in its composition of the target component in the form of amino acids (for example, 20 g/l methionine), various salts (for example, 200 g/l of sodium sulfate) and other components, adultsa in the capacity of 4, in which the transmission of the correction signal from the microprocessor 101 to the Executive mechanism 130 regulating valve 9 is supported by a valid source water controlled by the sensor 42. Also in the tank 4 is controlled by a sensor 45 and is supported by adding the appropriate reagents (acids) necessary level of acidity (e.g., pH 1÷2). From the tank 4 through line 27 source water transmission correction signal from the microprocessor 101 to the Executive mechanism 129 regulating valve 15 is fed to the ion exchange column 1 filled with sulfonic cation exchanger, with the highest selectivity, kinetic permeability and dynamic activity in relation to the target component in the form of amino acids (for example, a cation exchanger KU-5 polycondensation type, which has at sorption from aqueous salt solutions industrial wastewater highest selectivity towards methionine). While using flow sensors 58 and 60, respectively, at the outlet from the tank 4 and in line 27 is a control flow of the source water, which is regulated by the transfer of the correction signal from the microprocessor 101 to the Executive mechanism 129 regulating valve 15, to ensure optimal filtration rate during sorption (for example, 3000 l/h·m2 ). In ion-exchange column 1 is filtered water, but when you reach a certain residual concentration of the target component in the form of amino acids (for example, equal to the content of methionine 0.5 g/l), which corresponds to the point of "breakthrough" and is monitored by the sensor to the concentration of the target component 55 is included in the next ion exchange columns 2 through the direction of flow of the treated water from the ion exchange column 1 column 2 transfer adjustment signal from the microprocessor 101 to the Executive mechanism 125 regulating valve 19. In this case, the wastewater is filtered through two pre-connected columns 1 and 2. At the same time being measured by sensors 55 and 56 of the concentration of the target component in the form of amino acids (e.g. methionine) respectively output from columns 1 and 2. The removal of waste water thus produced on line 30 sending a corrective signal from the microprocessor 101 to the Executive mechanism 125 for switching control valve 19. Upon reaching the concentration of the target component in the form of amino acids (e.g. methionine) at the outlet of column 1 controlled by the sensor 55 is equal to the concentration at the inlet controlled by the sensor 54 (i.e., there is complete saturation in column 1), the switch to the subsequent stage when the latter is tion and desorption (i.e. on its regeneration). To prevent contamination deformiruemogo methionine sodium sulfate displacement of acidic waste water remaining in the tube 1 after sorption by filing its distillate from the tank 5 by the transfer of the correction signal from the microprocessor 101 to the Executive mechanism 127 regulating valve 12. The distillate passes through the layer of sulfonic cation exchanger in the opposite direction during sorption and at the outlet of the ion exchange columns 1, it measures the acidity using the sensor 46, and then it is removed through line 34. The distillate is fed to the ion exchange column 1, heated in the vessel 5 to the required temperature (for example, 70-80°C), controlled by the sensor 52 and supported on a given level of transmission of the correction signal from the microprocessor 101 to the Executive mechanism 132 of the heating element 7. In the tank 5 by the transfer of the correction signal from the microprocessor 101 to the Executive mechanism 131 of the control valve 10 is also supported by the necessary level of distillate, as measured by the sensor 43. After exclusion from the system of distillate in the ion exchange column 1 filter deformirujuschij solution (for example, hot (t=70°C) 1% solution of caustic soda containing 25-30 g/l methionine), pre-heated in the vessel 6 by sending a corrective signal with high performance embedded is Sora 101 Executive mechanism 134 of the heating element to a specified temperature level (for example, 50-60°C). In the tank 6 is also supported by the measured sensor 44 required level Stripping solution sending a corrective signal from the microprocessor 101 to the Executive mechanism 132 regulating valve 11. Submission of the Stripping solution in the ion exchange column 1 is the transmission from the microprocessor 101 to the Executive mechanism 128 of the control valve 18. While using flow sensors 69, 59 and 72, respectively, at the outlet from the tank 6, the inlet and outlet of the ion exchange column 1 is the control flow of a Stripping solution, which is governed by the transfer of the correction signal from the microprocessor 101 to the Executive mechanism 128 of the control valve 18, to ensure optimal filtration rate during desorption (for example, 2500 l/h·m). After passing the solution through ionoobmennoe column 1 he was cast in the form of acidic concentrated eluate at a given value of pH (e.g. pH 5.5-7), controlled by the sensor 49, and by transmitting the correction signal from the microprocessor 101 to the Executive mechanism 123 of the regulating valve 20 is removed in line 38, from which on cooling to room temperature, then stands crystalline target component in the form of amino acids (e.g. methionine in the amount of 75-80% of the sorbed). In the uneasy regenerating solution is performed by transmitting correction signals from the microprocessor 101 to the Executive mechanism 127 control valve 12 for supplying to the ion exchange column 1 distillate. At the end of the neutral displacement of the target component (e.g., methionine) pH of the eluate increases dramatically and quickly reaches the original value (for example, pH 12÷12,5). For example, while the remaining methionine desorbed in the form of methionate and together with the mother liquor, obtained by filtration of the crystalline methionine used for desorption in the next cycle. Simultaneously with the desorption is carried out regeneration of methionine (translation in sodium form). The purity of the selected crystalline methionine was characterized by the content of the main product and sodium sulfate (according to TU on methionine), as well as the data obtained by the elemental analysis of the product on the carbon, sulfur and nitrogen. At the same time after switching of the column 1 on the regeneration raw water line 28 is supplied in the following ion-exchange column 2 and at the same time using flow sensors 58 and 64, respectively, at the outlet from the tank 4 and in line 28 is the control over its consumption, which is controlled by the actuator 126 and the valve 16. Filtering in the ion exchange column 2 is also made to advances in water with a specific residual concentration of the target component in the form of amino acids (for example, equal to the content of methionine 0.5 g/l), which corresponds to the point of "breakthrough" and controlled using the Attica concentration of the target component 56, is the involvement of ion-exchange columns 3 through the direction of flow of the treated water from the ion exchange column 2 column 3 by means of the actuator 141 and the valve 22. Waste water, as in the first case, also filtered through two pre-connected columns 2 and 3. At the same time being measured by sensors 56 and 57 of the concentration of the target component in the form of amino acids (e.g. methionine) respectively output from columns 2 and 3. While the removal of waste water is produced on line 30 through the switching valve 22 of the actuator 141. Upon reaching the concentration of the target component in the form of amino acids (e.g. methionine) at the outlet of column 2, is equal to the concentration at the inlet (full saturation), respectively, controlled by sensors, the concentration of the target component 56 and 54, it switches to the next stage of displacement and desorption (i.e. regeneration). The displacement of acidic waste water remaining in the tube 2 after sorption by filing it heated to the required temperature (for example, 70-80°C), controlled by the sensor 52, the distillate from the tank 5 by the transfer of the correction signal from the microprocessor 101 to the Executive mechanism 122 of the regulating valve 13. At the outlet of the ion exchange columns 2 distillate change aetsa acidity using sensor 47, and then it is removed through line 34. After exclusion from the system of distillate in the ion exchange column 2 filter deformirujuschij solution (for example, hot (t=70°C) 1% solution of caustic soda containing 25-30 g/l methionine), pre-heated in the vessel 6 to a specified temperature level (e.g., 50÷60°C). Submission of the Stripping solution in the ion exchange column 2 is the transmission from the microprocessor 101 to the Executive mechanism 124 regulating valve 21. While using flow sensors 69, 63 and 71, respectively, at the outlet from the tank 6, the inlet and outlet of the ion exchange columns 2 is a control flow of a Stripping solution, which is governed by the transfer of the correction signal from the microprocessor 101 to the Executive mechanism 124 regulating valve 21, to ensure optimal filtration rate during desorption (for example, 2500 l/h·m2). After passing the solution through ionoobmennoe column 2 he was cast in the form of acidic concentrated eluate at a given value of pH (e.g. pH 5.5÷7), controlled by a sensor 50, and by transmitting the correction signal from the microprocessor 101 to the Executive mechanism 140 control valve 23 is removed in line 38. Stage desorption stop when reaching the acidity of the original value, then Khujand who are ousting of regenerating solution in the distillate. The displacement of regenerating solution in the distillate carry out the transfer of the correction signals from the microprocessor 101 to the Executive mechanism 122 of the control valve 13 for submission to the ion exchange column 2 distillate. At the same time after switching of the column 2 on the regeneration raw water line 29 is supplied in the following ion-exchange column 3 and at the same time using flow sensors 58 and 67, respectively, at the outlet from the tank 4 and in line 29 is controlled by the flow rate, which is controlled by the actuator 141 and the valve 17. Filtering in the ion exchange column 3 is also made to advances in water with a specific residual concentration of the target component in the form of amino acids (for example, equal to the content of methionine 0.5 g/l), which corresponds to the point of "breakthrough" and controlled by means of the sensor the concentration of the target component 57, after which it re-occurs, including ion-exchange columns 1, which passed the stage of displacement and desorption (i.e. the process of regeneration). The flow of the treated water from the ion exchange column 3 refer to the column 1 by transmitting the correction signal from the microprocessor 101 to the Executive mechanism 136 regulating valve 25. The waste water thus filtered through two connected columns 3 and 1. At the same time Khujand is realized measurement using sensors 57 and 55 of the concentration of the target component in the form of amino acids (for example, methionine) respectively output from columns 3 and 1. While the removal of waste water is produced on line 30 by transmitting the correction signal from the microprocessor 101 to the Executive mechanism 136 regulating valve 25. Upon reaching the concentration of the target component in the form of amino acids (e.g. methionine) at the outlet of column 3, is equal to the concentration at the inlet (full saturation), respectively, controlled by sensors, the concentration of the target component 57 and 54, it switches to the next stage of displacement and desorption (i.e. regeneration). The displacement of acidic waste water remaining in the tube 3 after sorption by filing it heated to the required temperature (for example, 70-80°C), controlled by the sensor 52 distillate from the tank 5 by the transfer of the correction signal from the microprocessor 101 to the Executive mechanism 138 of the control valve 14. At the outlet of the ion exchange columns 3 in the distillate is measured acidity with the help of the sensor 48, which is then removed through line 34. After exclusion from the system of distillate in the ion exchange column 3 filter deformirujuschij solution (for example, hot (t=60-70°C) 1% solution of caustic soda containing 25-30 g/l methionine), pre-heated in the vessel 6 to a specified temperature level (for example, 70-80°C). Submission Stripping solution ionoobmennoi column 3 is the transmission from the microprocessor 101 to the Executive mechanism 137 regulating valve 24. While using flow sensors 69, 66 and 68, respectively, at the outlet from the tank 6, the inlet and outlet of the ion exchange columns 3 is a control flow of a Stripping solution, which is governed by the transfer of the correction signal from the microprocessor 101 to the Executive mechanism 137 regulating valve 24, for optimum filtration rate during desorption (for example, 2500 l/h·m2). After passing the solution through ionoobmennoe column 3 he was cast in the form of acidic concentrated eluate at a given value of pH (e.g. pH 5.5÷7), controlled by a sensor 51, and by transmitting the correction signal from the microprocessor 101 to the Executive mechanism 135 control valve 26 is removed in line 38. Stage desorption stop when reaching the acidity of the original value, followed by the displacement of regenerating solution in the distillate. The displacement of regenerating solution in the distillate carry out the transfer of the correction signals from the microprocessor 101 to the Executive mechanism 138 of the control valve 14 for submission to the ion exchange column 3 of distillate. Thus, continuous scheme of ion-exchange columns 1, 2, 3 provides that when the output of the adsorber 1 concentration of methionine 0.5 g/l to him podshoev aetsa 2nd adsorber etc. In turn fully saturated ion-exchange columns are switched for the next stage of displacement and desorption, i.e. each individual adsorber operates on a closed cycle: sorption → displacement of acidic wastewater → desorption and activation of cation exchanger → the displacement of regenerating solution → sorption etc. The information about the flow of a process of ion exchange sorption of amino acids from wastewater is transferred from the sensors through the secondary devices 73-100 in the microprocessor 101, which generates correction signals through d / a converters 102-121 the actuators 122-141 to change the operating parameters of the equipment depending on the selected criteria. The proposed method for automatic process control of ion exchange sorption of amino acids from wastewater has advantages due to the fact that the additional measurement modes and change operating parameters of the equipment depending on the selected criteria can improve the control accuracy and to minimize energy and material costs. Method for automatic process control of ion exchange sorption of amino acids from wastewater, including the control of concentrations of ingredients wastewater flow measurement of liquid solutions and their level in the tank, characterized in that it further in the car is aliceson mode in the source water measure the acidity level and maintain it at the required level, the source water is fed into the first ion-exchange column filled with sulfonic cation exchanger, and produce control over its consumption, which adjust to the optimum filtration rate in the first ion-exchange column, and when reaching the residual concentration of the target component in the form of amino acids corresponding to the point "breakthrough", switch on the second ion-exchange column filled with sulfonic cation exchanger, by direction of the flow of treated water from the first ion exchange columns in the second ion-exchange column with simultaneous filtration of treated water through the first and second columns, thus provide measurements of the concentration of the target component in the form of amino acids at the output of the first and second columns and when reaching the concentration of the target component in the form of amino acids at the output of the first column equal to the concentration at the inlet in the first column, switch it on regeneration, which includes stages of displacement acidic wastewater and desorption, and when you reach the result of filtering the waste water through the second column the residual concentration of the target component in the form of amino acids corresponding to the point of breakthrough, make the inclusion of the third ion exchange columns filled with sulfonic cation exchanger, by direction of the flow of treated water from the second and Normanni column in the third column with simultaneous filtration of treated water through the second and third columns, thus the displacement of acidic wastewater remaining in each of the three columns after sorption, carried out by feeding them in preheated distillate in the direction opposite to the direction of flow of water by sorption, and the output of each of the three columns measure the acidity of the distillate, which is judged on the completion of phase displacement and the early stage of desorption, which is carried out by filtering the pre-heated Stripping solution through the layer of sulfonic cation exchanger in each of the three columns with monitoring and controlling the flow of Stripping solution to the optimal filtration rate during desorption, and after passing through the Stripping solution through each of three ion exchange columns select it in the form of acidic concentrated eluate and stop stage desorption upon reaching the initial values of acidity Stripping solution, and after the first regeneration column and displacing the Stripping solution of the distillate, it is included in the work for the implementation of the sorption in the second column at the stage of regeneration and achievement in the treated water during the filtration process in the third column of the residual concentration of the target component in the form of amino acids corresponding to the point "breakthrough", and the information about the course of the process of ion exchange is the sorption of amino acids from wastewater is transferred from the sensor level control in tanks source of water, distillate and Stripping solution, the pH of the source water and the flow in the ion exchange column, the temperature of the distillate and Stripping solution, the concentration of the target component in the source water and the water at the outlet of the ion exchange columns, and flow through the secondary devices, a microprocessor and a digital-analog converters actuators to change the operating parameters of the equipment depending on the selected criteria.
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