EP0082869A1 - Procede de commande de melange - Google Patents

Procede de commande de melange

Info

Publication number
EP0082869A1
EP0082869A1 EP82902168A EP82902168A EP0082869A1 EP 0082869 A1 EP0082869 A1 EP 0082869A1 EP 82902168 A EP82902168 A EP 82902168A EP 82902168 A EP82902168 A EP 82902168A EP 0082869 A1 EP0082869 A1 EP 0082869A1
Authority
EP
European Patent Office
Prior art keywords
agitator
stirring
viscosity
stirred
torque
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP82902168A
Other languages
German (de)
English (en)
Inventor
Dieter Kupka
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Publication of EP0082869A1 publication Critical patent/EP0082869A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • G—PHYSICS
    • G01—MEASURING; TESTING
    • G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
    • G01N11/00—Investigating flow properties of materials, e.g. viscosity, plasticity; Analysing materials by determining flow properties
    • G01N11/10—Investigating flow properties of materials, e.g. viscosity, plasticity; Analysing materials by determining flow properties by moving a body within the material
    • G01N11/14—Investigating flow properties of materials, e.g. viscosity, plasticity; Analysing materials by determining flow properties by moving a body within the material by using rotary bodies, e.g. vane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/20—Measuring; Control or regulation
    • B01F35/21—Measuring
    • B01F35/212—Measuring of the driving system data, e.g. torque, speed or power data
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/80—Forming a predetermined ratio of the substances to be mixed
    • B01F35/82—Forming a predetermined ratio of the substances to be mixed by adding a material to be mixed to a mixture in response to a detected feature, e.g. density, radioactivity, consumed power or colour
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • G—PHYSICS
    • G05—CONTROLLING; REGULATING
    • G05D—SYSTEMS FOR CONTROLLING OR REGULATING NON-ELECTRIC VARIABLES
    • G05D24/00—Control of viscosity
    • G05D24/02—Control of viscosity characterised by the use of electric means
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • B01J2219/00094—Jackets
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00168—Controlling or regulating processes controlling the viscosity

Definitions

  • the invention relates to a method for controlling stirring processes, in particular a method for regulating the power consumed by a stirrer in a stirred tank, taking into account the properties of the respective stirrer, a method for determining the viscosity of a stirrer in a stirred tank, the agitator at a given speed gives a torque dependent on the viscosity of the material to be mixed, and a method for controlling the stirring parameters of a stirring process in a mixing container equipped with a stirrer by means of an electronic data processing device.
  • stirring processes are used to manufacture chemical products. These stirring processes, which can take several hours or even days, require a considerable amount of energy both for the agitator drive and for the supply of heat or cooling of the material to be stirred in exothermic processes.
  • the power required for the agitator drive depends on the one hand on the speed of the agitator and on the other hand on the viscosity of the material to be stirred.
  • the viscosity of the material to be stirred changes during the various phases of the stirring process. The stirring process is only maintained if the agitator operates at a given minimum speed for a given viscosity of the material to be stirred.
  • the stirring processes are usually controlled by time-dependent program circuits.
  • the energy supply required for the maintenance of the process, in particular the agitator output, is controlled according to a time program gained from experience. Since one essentially has to fall back on average values and maintain a sufficient safety distance from the minimum power required for maintaining the stirring process, such a control cannot bring about an optimal use of energy. If the stirring processes are carried out at a constant speed of the agitator, the speed must be designed in such a way that it satisfies the most unfavorable conditions, that is to say corresponds to the highest power required at one point in time of the stirring process or possibly the highest speed required at another point in time.
  • stirrer works with an unnecessarily high power consumption, but in addition the stirrer or its drive motor and gear unit must be designed for a relatively high permanent load, which means the material and construction effort as well as this Manufacturing costs can be increased.
  • the object of the invention is in particular to provide a method for controlling stirring processes by means of which the deficiencies set out above are remedied.
  • the fiction, modern method is intended in particular a substantial savings • tion of zuge ⁇ the agitator during a stirring process resulted enable drive power by the rotational speed of the stirrer is controlled so that the agitator just only that optimum performance outputs required for the stirring process still keep going.
  • an automatic control of all stirring parameters with optimized total power consumption in the course of the stirring process is to be achieved.
  • the method according to the invention for regulating the power consumed by the agitator in the agitator tank, taking into account the properties of the respective agitated material is characterized in that first of all the optimal power consumption of the agitator is determined empirically for the respective agitated material, which is given for a given Viscosity value of the material to be stirred, which depends on the respective stirring phase, ensures that the stirring process in the respective stirring phase is maintained with minimal energy expenditure. Furthermore, the viscosity of the material to be stirred is continuously determined in the course of the entire stirring process.
  • the speed or the torque of the agitator is then readjusted on the basis of the respectively determined viscosity values of the agitated material until the power consumed by the agitator corresponds to the empirically determined optimum power consumption.
  • the invention is therefore based on the idea that the speed of the agitator is controlled depending on the viscosity of the material to be stirred that it is just sufficient to keep the stirring process going.
  • the invention therefore also provides a method for the continuous determination of the viscosity of the material to be stirred in a stirred container in the course of the stirring process, which makes the use of conventional viscosity measuring devices superfluous.
  • the process according to the invention for the continuous measurement of the viscosity of the material to be stirred is characterized by the following process steps:
  • the method according to the invention thus makes it possible to continuously determine the viscosity of the material to be stirred in the course of the stirring process solely on the basis of the measured speed of the agitator and the torque with which the agitator is driven, and on the basis of the easy-to-determine specific weight of the material to be stirred the dependence of the Reynold number on the Nus number known from empirical research.
  • the calculations required in the course of taking place after OF INVENTION ungsdorfen process running viscometers' ty bestircnung by successive approximation can easily communicate an appropriate data processing means are performed.
  • Microprocessor or microcomputer systems are particularly suitable which, in addition to the ongoing calculation of the viscosity of the agitator, can take over all other control and monitoring functions of the agitator system.
  • a method for controlling the stirring parameters of a stirring process by means of an electronic data processing device is created, which according to the invention is characterized in that the stirring parameters, in particular the composition of the material to be stirred, such as temperature and pressure in the stirring container, are entered at the beginning of the stirring process via a data input station the data processing device can be entered; the data processing device controls directions depending on the entered data, which determine the parameters, in particular special inlet valves for loading the stirred tank with the components to be stirred, heating device of the stirred tank and pressure control; the data processing device, taking into account the stirring parameters from the measured rotational speed of the agitator and the torque emitted by the latter, taking advantage of the empirically determined dependency between Reynold number and Nusselt number, the viscosity of the material to be stirred continuously
  • the torque or the speed of the agitator is controlled so that the power consumption of the agitator is equal to an empirically determined optimum power consumption, at which the maintenance of the ongoing stirring process is still guaranteed for the calculated viscosity value.
  • This method enables the automatic control of the entire stirring process, starting with the input of the mixture of items to be stirred at an input station of the data processing device, e.g. via a keyboard until the stirring process is reached, which is achieved when a predetermined period of time has expired or when a specific setpoint value for the viscosity of the material to be stirred has been reached.
  • the data processing device performs all monitoring functions which ensure safe operation of the stirring system.
  • FIG. 1 shows a schematic view of a stirring system which is suitable for carrying out the method according to the invention, with the mixing container shown in vertical axial section and in plan view;
  • FIG. 2 shows a flowchart of a subroutine for calculating the viscosity of the material to be stirred via successive approximation; and 3 shows a flow chart of a complete control program for explaining the method according to the invention.
  • the generally cylindrical stirrer tank 10 shown schematically in vertical axial section and in plan view in FIG. 1 has an agitator with coaxial stirrer shaft 12 and stirrer blades 14 arranged at a distance therefrom.
  • the agitator shaft 12 is driven at its upper end by an agitator drive 16 which is installed in a housing 18 and, in addition to the drive motor, comprises a gear.
  • the agitator shaft 12 is rotatably supported in a main bearing 20 at the upper end of the agitator tank 10.
  • the housing 18 is also rotatably mounted on the stirred tank 10. It has a radially outwardly projecting arm 22, which is supported on one of two pressure cells 24, 26 arranged opposite one another, which are rigidly connected to the mixing container 10.
  • the torque transducers 24, 26 allow the torque delivered by the agitator drive to the agitator elle to be measured in both directions of rotation.
  • the stirred tank 10 has on its upper side two inlet steps 28, 30 which have different cross-sections. Vo the inlet port 28, 30, an inlet valve 32 and 34 is arranged.
  • the inlet valves 32, 34 are provided with a suitable actuator for automatic remote control.
  • the stirring container 10 is surrounded by a heating jacket 40 over most of its height.
  • the temperature inside the stirred container 10 is monitored by a thermometer 42 which is arranged on the underside of the stirred container and penetrates the heating jacket 40.
  • a fill level detector 44 is also arranged on the outer wall of the stirred tank 10.
  • a digital data processing device 46 is provided, which is shown only schematically in FIG. 1 as a housing with a digital display and with an input keyboard.
  • the data processing device 46 is connected via a plurality of lines to the pressure cells 24, 26, the valves 32, 34, the agitator 16, the level indicator 44, the heating jacket 40, the Thermome 42 and the outlet valve 38.
  • the subroutine shown in Fig. 2 enables the ongoing determination of the viscosity of the material to be stirred in the stirred tank based on the measurement of the torque given by the agitator drive to the agitator shaft and the speed of the agitator, which is preferably photoelectrically attached to the agitator shaft 12 Slotted or perforated disc and a photodetector arrangement fastened to the container wall and interacting with this disc is measured.
  • the subroutine shown in FIG. 2 is used to calculate the viscosity of the material to be stirred by a method of successive application. This calculation is based on generally known physical laws, from which the dependency of the viscosity of the material to be stirred results on the individual stirring parameters.
  • the viscosity ⁇ is a function of the speed n de
  • ⁇ F (n, Ne, Re, Md, d, o)
  • an estimated approximate initial value of the viscosity is first entered into the data processing device on the basis of empirical values, for example by means of a keyboard or another data input station. This is shown in Fig. 2 as the initial step 100 of the sub-program.
  • the speed n of the agitator and its torque Md measured. Since the stirrer diameter d and the viscosity of the material to be stirred are known for a given stirring process, the Reynoldzah Re can now be measured according to the following relationship:
  • ⁇ is the approximate starting value of the viscosity
  • the factor 60 is based on the speed n in revolutions / minute.
  • the calculation of the Reynold number Re is indicated in FIG. 2 as sub-program step .106. Subsequent to the calculation d Reynold number Re, the Nusselt number Ne is determined in step 108.
  • An associated torque Mdx_i.d of the agitator can in turn be calculated from the Nusselt number using known physical laws according to the following relationship:
  • step 110 This calculation is shown in FIG. 2 as subroutine step 110.
  • step 112 it is then checked whether the torque Md thus calculated corresponds to the actual torque Mdgern of the agitator measured in step 104 g r . This will generally not be the case based on the rough estimate of the initial viscosity value entered in step 100, and then in step 114 the assumed initial value of viscosity will be corrected by a step of a predetermined size in the appropriate sense.
  • the subroutine then returns to step 104 and repeats steps 104 to 112, and so often, until the check carried out in this step 112 matches the measured torque value with the calculated torque value Md_.
  • the initial size of the viscosity specified in the immediately preceding calculation of the torque Md R then corresponds to the actual value of the viscosity of the material to be stirred.
  • the viscosity ⁇ of the material to be stirred has thus been found and can be displayed in step 116 on a display panel and, at the same time or alternatively, can be stored in a work register of the data processing device in order to control the optimum speed n of the agitator in FIG. 3 shown ste er program to be used.
  • the data processing device preferably contains a microprocessor, a working memory, a data memory and a program memory, which comprises a fixed program memory part and a programmable program memory part.
  • the control and monitoring functions which are required for each stirring process are stored in the fixed program memory part, while specific program steps which are adapted to the agitator used, the individual stirring parameters, etc. are stored in the programmable program memory part.
  • the individual stirring parameters can be entered via an input keyboard, a program card or the like. be entered into the programmable program memory part.
  • the method begins with the start step 200 shown in FIG. 3, after which it is checked in step 202 whether the previously entered stirring program should be repeated. If the Progra is not to be repeated, the new stirring parameters are entered in step 204, in particular the composition of the material to be stirred, temperature profile during the entire stirring process
  • step 204 it is then checked whether the entire stirring process should run automatically. If not, the necessary control functions are set manually in step 208. If automatic operation is desired, the stirring process is started in step 210. In step 212, the specific weight o of the material to be stirred is then calculated from the composition entered in step 204. Step 21 is then followed as program step 214 by the subroutine shown in FIG. 2 with subroutine steps 100 to 116, ie the viscosity ⁇ of the material to be stirred is measured.
  • step '216 the torque value MD is obtained from the data memory , which corresponds to the calculated viscosity value ⁇ .
  • the setpoint Md ,, of the agitator torque ⁇ is the value that is required to maintain the agitation process with minimal energy consumption of the agitator drive.
  • the dependency of this torque setpoint on the various viscosity values was previously determined empirically and stored in the data memory. This dependency is the same for all stirring processes and therefore only needs to be determined once.
  • step 218 it is then checked whether the g 3 measured torque Mdgern with the target value
  • Mdsol, l of the torque matches. If there is a match, readjustment of the agitator is not necessary. If there is no match, the speed n of the agitator is readjusted in a suitable sense by a predetermined step in step 220. By adjusting the speed, the torque of the agitator increases or decreases, depending on whether the speed has been increased or decreased. Subsequent to the readjustment of the speed of the agitator, the viscosity ⁇ is then again calculated first, and the associated target torque is fetched from the data memory and then again in step 218 with the measured torque compared.
  • the speed is readjusted in the program loop formed from steps 214 to 220 until in step 218 agreement between the measured torque and the setpoint torque of the agitator is determined.
  • the stirring system works with minimal energy consumption of the agitator, in which maintenance of the stirring process is just guaranteed.
  • the agitator works with optimal power consumption during the entire agitating process, which means that savings of up to 40% can be achieved compared to operation at constant speed.
  • the entire stirring system can be designed for a significantly low permanent load.
  • step 222 After a correspondence between the measured torque and the setpoint torque of the agitator has been determined in step 218, it is checked in step 222 whether a program-controlled automatic temperature changeover should take place. Possibly. it is then checked in step 224 whether the viscosity value calculated in step 214 is one in which a temperature changeover is provided in the stirring program. Possibly. the temperature is then readjusted in step 226 in accordance with the temperature jump seen before in the stirring process, whereupon the Progra returns to step 214.
  • step 228 checks whether the stirring process should be ended by the viscosity value of the material to be stirred being a predetermined value * r l . ,__-, • has reached. If this is not the case, a check is carried out in step 230 as to whether the stirring process should be ended by expiry of a predetermined stirring time. When the intended stirring process time has elapsed, the stirring process is ended in step 232. If the intended stirring process has not expired, the program returns to step 214. If the check at step 228 shows that the stirring process should be ended when the intended final value ⁇ f ..
  • step 234 it is checked in step 234 whether the viscosity value determined in step 214 with the desired final value ⁇ f . matches. If this is the case, the program proceeds to the end step 232 mentioned above. If the final viscosity value is • not reached, however, various monitoring functions of the stirring system are carried out in step 236. After the monitoring functions have ended, the program returns to step 214.
  • the program steps 204, 210, 212, 214, 216, 220, 226, 232 and 236 shown in FIG. 3 are subroutines, of which only one, namely the program step 214, has been explained in detail with reference to FIG. 2.
  • program step or subroutine 204 e.g. B. queried the Tas tur of the data processing device, or who read the appropriate program carrier. The read data is then transferred to the main memory of the data processing device.
  • program step or subroutine 212 the average specific weight of the material to be stirred is calculated from the composition of the stirred tank filling entered in step 204, and the result is stored in order to remain available for the entire stirring process.
  • the program step or the lower program 236 also has special features. In it, the signals from the thermometer and the level indicator 44 and other signals are monitored which are important for the operational safety of the stirring system, in particular the barrier pressure of the agitator bearing 2, the temperature of this agitating bearing and the current consumption of the agitator drive. If one of the monitored signals indicates a malfunction, the stirring system can be stopped automatically to remedy the situation.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Physics & Mathematics (AREA)
  • Physics & Mathematics (AREA)
  • Health & Medical Sciences (AREA)
  • Automation & Control Theory (AREA)
  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Biochemistry (AREA)
  • General Health & Medical Sciences (AREA)
  • Immunology (AREA)
  • Pathology (AREA)
  • Organic Chemistry (AREA)
  • Mixers Of The Rotary Stirring Type (AREA)

Abstract

Le procédé permet une commande automatique au moyen d'un dispositif électronique de traitement de données (46), de tous les paramètres d'un procédé de mélange dans un récipient de mélange (10) muni d'un agitateur. La puissance absorbée est réglée en fonction de la viscosité du produit à mélanger mesurée de façon continue pour que l'action de mélange soit tout juste maintenue. La mesure continue de la viscosité du produit est effectuée par une approximation successive basée sur les valeurs mesurées du couple de rotation de l'agitateur et du nombre de tours de l'agitateur, ainsi qu'à partir de la relation empirique entre le nombre de Reynolds et le nombre de Nusselt. Pour calculer le nombre de Reynolds on prend d'abord une valeur de viscosité basée sur l'expérience; ensuite on calcule, à partir du nombre de Nusselt qui fait partie du nombre calculé de Reynolds, la valeur du couple de rotation de l'agitateur correspondant à la viscosité estimée. Cette valeur est comparée avec le couple de rotation effectif. Si les deux valeurs du couple de rotation divergent, on corrige la viscosité estimée jusqu'à coïncidence des valeurs.
EP82902168A 1981-07-04 1982-07-05 Procede de commande de melange Withdrawn EP0082869A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3126552 1981-07-04
DE3126552A DE3126552A1 (de) 1981-07-04 1981-07-04 "verfahren zur steuerung von ruehrprozessen"

Publications (1)

Publication Number Publication Date
EP0082869A1 true EP0082869A1 (fr) 1983-07-06

Family

ID=6136191

Family Applications (1)

Application Number Title Priority Date Filing Date
EP82902168A Withdrawn EP0082869A1 (fr) 1981-07-04 1982-07-05 Procede de commande de melange

Country Status (3)

Country Link
EP (1) EP0082869A1 (fr)
DE (1) DE3126552A1 (fr)
WO (1) WO1983000101A1 (fr)

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DE3707745C2 (de) * 1987-03-11 1999-07-22 Buehler Ag Verfahren und Anlage zur Steuerung der Vermahlung einer teigig-pastösen Masse
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DE4127873C2 (de) * 1991-08-22 1995-02-23 Reimelt Dietrich Kg Kneteinrichtung für eine zu knetende Masse
FR2680887A1 (fr) * 1991-08-30 1993-03-05 Cappelletto Renzo Dispositif de regulation de vitesse destine notamment aux malaxeurs, et nouveau malaxeur destine notamment a la fabrication de sable de fonderie.
DE4212937C2 (de) * 1992-04-18 1994-04-14 Walter Stahl Mischer
DE4401679C2 (de) * 1994-01-21 1996-04-18 Janke & Kunkel Kg Rührgerät mit einer Haltevorrichtung
DE9412699U1 (de) * 1994-08-05 1995-12-07 Liebherr Mischtechnik Gmbh Ringtragzwangsmischer
DE10066151B4 (de) * 2000-09-27 2010-10-07 Gako Konietzko Gmbh Verfahren zum Betrieb eines programmgesteuerten Rührwerks und programmgesteuertes Rührwerk
DE10049002C2 (de) * 2000-09-27 2003-05-22 Albrecht Konietzko Programmgesteuertes Rührwerk
DE102004017442B4 (de) * 2004-04-02 2006-07-20 Technische Universität Dresden Verfahren und Vorrichtung zum Rühren von nichtleitenden Flüssigkeiten in Behältern
US20060058427A1 (en) * 2004-09-15 2006-03-16 O'neill Julia C Power-controlled bonding of resin or (co)polymer powder and flake materials
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DE102010014239B4 (de) * 2010-04-01 2012-09-13 Ksb Aktiengesellschaft Verfahren und Vorrichtung zur Herstellung von Biogas
US10265668B2 (en) * 2016-01-29 2019-04-23 Sartorius Stedim Biotech Gmbh Mixing methods
DE102019132715B4 (de) * 2019-12-02 2024-03-14 Ika - Werke Gmbh & Co. Kg Rührgerät
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Also Published As

Publication number Publication date
WO1983000101A1 (fr) 1983-01-20
DE3126552A1 (de) 1983-01-20

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