EP2965819A1 - Regulation and/or control of a pulverizing system - Google Patents

Abstract

The invention relates to a method for controlling and / or controlling a comminution system (1) with a mill (2), a classifier (3) and a separator (4) for comminuting a material to be ground, wherein as at least one reference variable of the control and / or control a first derivative of a function that describes the dependence of a first operating parameter of the crushing plant (1) of a second operating parameter of the crushing plant (1) is used.

Description

The invention relates to a method for controlling and / or controlling a comminution system with a mill, a separator and a classifier for comminuting a ground material.

In particular, the invention relates to crushing plants with ball mills for crushing ores. The main disturbances in the control and / or control of such crushing plants are the changes in the grain size composition and the mechanical and physical properties of the inlet material (the ores). The physical and mechanical properties of the ore and the state of the crushing unit change unpredictably, permanently and with different dynamics. The multitude of nonlinear process characteristics and the extreme situations lead to an enormous amount of object control decisions. Depending on the speed and filling volume of the mill, various operating conditions of the mill are possible which determine the work of crushing the material fed into the mill: a cascade operation (without lifting the media), a mixing operation (with rolling of the media and their partial lifting ), a waterfall operation (with predominantly lifting of the bodies), operation at supercritical speed and operation at overload, ie a drum filling operation with orb-ball load of over 50%.

Known methods for controlling and / or controlling such shredding plants are based on the stabilization or regulation of individual process variables. These include, but are not limited to, raw stock flow, a lot of classifier or hydrocyclone overflows, a drum fill volume, a percent solids in the mill spout, a solids content or finished class in the classifier spout and an outlet volume throughput.

Furthermore, the invention relates in particular to the regulation and / or control of crushing plants upstream of the mill crushers for finely crushing regrind, in particular of ore. Breaking and grinding regrind differ in principle not from each other. The goal is always the digestion of the grains of the ground material. The result of the crushing process of ores is a grain having a grain size of, for example, about 5 mm.

The invention has for its object to provide an improved method for controlling and / or controlling a crushing plant with a mill, a separator and a classifier for crushing a ground material.

The object is achieved by the features of claim 1.

Advantageous embodiments of the invention are the subject of the dependent claims.

In the inventive method for controlling and / or controlling a crushing plant with a mill, a separator and a classifier for crushing a material to be ground as at least a reference variable of the control and / or control a first derivative of a function, the dependence of a first operating parameter of the crushing plant described by a second operating parameter of the crushing plant used.

By using a first derivative of at least one function that relates two operating parameters to each other as a reference variable for the regulation and / or control of a crushing plant, changes of at least one operating parameter are systematically used as the basis of the control and / or control. This is advantageous as a Control and / or control concerns just the change of operating parameters and therefore the choice of at least one suitable first derivative as a reference variable of a control and / or control task is particularly well adapted.

An embodiment of the invention provides that a zero point of a first derivative of a function used as a reference variable is defined as at least one nominal value.

As a result, at least one desired value is assigned to one extreme value of an operating parameter as a function of another operating parameter. This is advantageous because such extremes are often the goal of control and / or control, for example, minimum energy consumption, maximum productivity or maximum efficiency.

A further embodiment of the invention provides that at least one manipulated variable is regulated and / or controlled as a function of at least one sign of a first derivative of a function used as a reference variable.

This refinement is advantageous since the sign of a first derivative of a function alone can already be used to deduce the increase or decrease in the function and thus the operating parameter represented by it. This advantageously simplifies the regulation and / or control of a manipulated variable. This simplification has a particularly advantageous effect on the regulation and / or control of a complex system, such as a comminution system with very many different manipulated variables and operating parameters.

• als ein erster Betriebsparameter eine Energieintensität nach Materialzerkleinerung und als ein zweiter Betriebsparameter ein Füllvolumen der Mühle,
• und/oder als ein erster Betriebsparameter eine Motorleistung der Mühle und als ein zweiter Betriebsparameter ein Füllvolumen der Mühle,
• und/oder als ein erster Betriebsparameter ein Verhältnis flüssigen Materials zu Feststoffmaterial in der Mühle und als ein zweiter Betriebsparameter eine Energieintensität nach Materialzerkleinerung,
• und/oder als ein erster Betriebsparameter eine Mühlenproduktivität nach einem Ausgangsmahlgut und als ein zweiter Betriebsparameter eine Motorleistung der Mühle,
• und/oder als ein erster Betriebsparameter eine Mühlenproduktivität nach einem Ausgangsmahlgut und als ein zweiter Betriebsparameter ein Verhältnis flüssigen Materials zu Feststoffmaterial in der Mühle,
• und/oder als ein erster Betriebsparameter eine Mühlenproduktivität nach einem Ausgangsmahlgut und als ein zweiter Betriebsparameter eine Motorleistung des Separators,
• und/oder als ein erster Betriebsparameter eine Mühlenproduktivität nach einer Fertigungsklasse und als ein zweiter Betriebsparameter eine Umlaufbelastung

verwendet werden.A further embodiment of the invention provides that for the regulation and / or control of the productivity of the comminution of the ground material

• as a first operating parameter an energy intensity after material comminution and as a second operating parameter a filling volume of the mill,
• and / or as a first operating parameter an engine power of the mill and as a second operating parameter a filling volume of the mill,
• and / or as a first operating parameter, a ratio of liquid material to solid material in the mill and, as a second operating parameter, an energy intensity after material comminution,
• and / or as a first operating parameter, a mill productivity after a Ausgangsmahlgut and as a second operating parameter, an engine power of the mill,
• and / or as a first operating parameter, a mill productivity after a starting meal and, as a second operating parameter, a ratio of liquid material to solid material in the mill,
• and / or as a first operating parameter, a mill productivity after a Ausgangsmahlgut and as a second operating parameter, an engine power of the separator,
• and / or as a first operating parameter a mill productivity according to a manufacturing class and as a second operating parameter a circulation load

be used.

This embodiment advantageously defines operating parameters which are particularly suitable for controlling and / or controlling the productivity of a comminution of regrind.

A further embodiment of the invention provides that for controlling and / or controlling a pulp density of a classifier outlet of the classifier, a mill productivity after a Ausgangsmahlgut be used as a first operating parameter and a motor performance of the separator as a second operating parameter.

This refinement advantageously defines operating parameters which are particularly suitable for controlling and / or controlling a pulse density of a classifier outlet of a classifier.

A further embodiment of the invention provides that, for controlling and / or controlling the energy requirement of comminuting the ground material as a first operating parameter, the energy requirement for material comminution and as a second operating parameter, a filling volume of the mill and / or a ratio of liquid material to solid material in the mill be used.

This embodiment advantageously defines operating parameters which are particularly suitable for controlling and / or controlling the energy requirement of the comminution of ground material.

A further embodiment of the invention provides that, for controlling and / or controlling an intermediate product quality during comminution of the material to be ground, a mill productivity after Ausgangsmahlgut and / or an application of an intermediate product of a first deposition stage and as a second operating parameter uses a motor power of the separator as a first operating parameter become.

This embodiment advantageously defines operating parameters which are particularly suitable for controlling and / or controlling an intermediate product quality during the comminution of millbase.

Further embodiments of the invention relate to a crushing plant, which has a crushing plant upstream of the mill with at least one crusher for finely crushing the ground material. A first such embodiment provides that for controlling and / or controlling a productivity of the refining process as a first operating parameter, a crusher productivity of at least one crusher according to initial ore and as a second operating parameter a crushing gap size of a crusher of the crusher, and / or as a first operating parameter a Siebklassierungseffektivität at least one screen of the crushing plant and / or an energy intensity of at least one crusher and as a second operating parameter a crusher productivity of at least one crusher be used. A second such embodiment provides that for controlling and / or controlling an overload of the at least one crusher as a first operating parameter, a crusher productivity of the crusher and as a second operating parameter, a crushing gap size of a crusher of the crusher, and / or as a first operating parameter, an energy intensity of Brechers and as a second operating parameter, a crusher productivity of the crusher can be used.

The abovementioned embodiments advantageously define operating parameters which are particularly suitable for controlling and / or controlling a productivity of a refining process of regrind or for regulating and / or controlling an overload of a crusher of a crushing plant.

A further embodiment of the invention provides that at least one operating parameter is determined from measured data which are acquired at regular time intervals. In this case, sliding time average values of measured data are preferably formed from the measured data to determine at least one operating parameter.

This refinement advantageously makes it possible to determine derivations of functions of the operating parameters from differences in measured data acquired in chronological succession. The formation of moving time average values of measured data advantageously smoothes the determined derivatives and, moreover, compensates for measurement errors.

Further embodiments of the invention provide that the mill is a ball mill and / or that the ground material is an ore.

FIG 1

ein Blockdiagramm eines ersten Beispiels einer Zerkleinerungsanlage zur Zerkleinerung eines Mahlgutes und eines Regelungssystems zur Regelung der Zerkleinerungsanlage,

FIG 2

eine Abhängigkeit einer Energieintensität nach Materialzerkleinerung von einer Überlaufdichte eines Klassierers,

FIG 3

eine Abhängigkeit einer Umlaufbelastung einer Zerkleinerungsanlage mit Erz von einer Mühlenproduktivität nach Fertigklasse,

FIG 4

eine Abhängigkeit einer Energieintensität nach Materialzerkleinerung von dem Verhältnis flüssigen Materials zu Feststoffmaterial in einer Mühle,

FIG 5

eine Abhängigkeit einer Mühlenproduktivität nach Ausgangserz von einer Energieintensität nach Materialzerkleinerung,

FIG 6

eine Abhängigkeit eines Füllvolumens einer Mühle von einer Mühlenproduktivität nach Ausgangserz,

FIG 7

eine Abhängigkeit einer Motorleistung einer Mühle von einer Mühlenproduktivität nach Ausgangserz,

FIG 8

eine Abhängigkeit einer Umlaufbelastung von einem Verhältnis flüssigen Materials zu Feststoffmaterial in einer Mühle,

FIG 9

eine Abhängigkeit einer Mühlenproduktivität nach Ausgangserz von einem Verhältnis flüssigen Materials zu Feststoffmaterial in einer Mühle,

FIG 10

eine Abhängigkeit einer Mühlenproduktivität nach Fertigklasse von einer Umlaufbelastung,

FIG 11

eine Abhängigkeit einer Mühlenproduktivität nach Ausgangserz von einer Überlaufdichte eines Klassierers,

FIG 12

eine Abhängigkeit einer Mühlenproduktivität nach Ausgangserz von einer Mühlenproduktivität nach Fertigklasse,

FIG 13

eine Abhängigkeit eines Verhältnisses flüssigen Materials zu Feststoffmaterial in einer Mühle von einer Überlaufdichte eines Klassierers,

FIG 14

eine Abhängigkeit eines Füllvolumens einer Mühle von einem Verhältnis flüssigen Materials zu Feststoffmaterial in der Mühle,

FIG 15

eine Abhängigkeit einer Energieintensität nach Materialzerkleinerung von einem Füllvolumen einer Mühle,

FIG 16

eine Abhängigkeit einer Mühlenproduktivität nach Ausgangserz von einem Anteil der Fertigklasse in einem Klassiererüberlauf,

FIG 17

eine Abhängigkeit einer Überlastung einer Mühle von einer Energieintensität nach Materialzerkleinerung,

FIG 18

eine Abhängigkeit einer Mühlenproduktivität nach Fertigklasse von einer Energieintensität nach Materialzerkleinerung,

FIG 19

eine Abhängigkeit einer Motorleistung einer Mühle von einem Füllvolumen der Mühle,

FIG 20

eine Abhängigkeit einer Mühlenproduktivität nach Ausgangserz von der Überlaufdichte eines Klassierers,

FIG 21

eine Abhängigkeit des Eisengehalts im Zwischenprodukt einer ersten Abscheidungsstufe von einem Anteil der Fertigklasse in einem Klassiererüberlauf,

FIG 22

eine Abhängigkeit des Eisengehalts im Zwischenprodukt einer ersten Abscheidungsstufe von einer Überlaufdichte Rcl des Klassierers,

FIG 23

eine Abhängigkeit des Eisengehalts im Zwischenprodukt einer ersten Abscheidungsstufe von der Motorleistung eines Separators,

FIG 24

eine Abhängigkeit einer Mühlenproduktivität nach Ausgangserz von der Motorleistung eines Separators,

FIG 25

eine Abhängigkeit des Ausbringens Y des Zwischenprodukts einer ersten Abscheidungsstufe von der Trommeldrehzahl eines Separators,

FIG 26

eine Abhängigkeit des Ausbringens Y des Zwischenprodukts einer ersten Abscheidungsstufe von der Überlaufdichte eines Klassierers,

FIG 27

eine Abhängigkeit des Ausbringens Y des Zwischenprodukts einer ersten Abscheidungsstufe von einer Motorleistung eines Separators,

FIG 28

eine Abhängigkeit eines Eisengehalts in den Tailings einer ersten Abscheidungsstufe von der Motorleistung eines Separators,

FIG 29

ein Blockdiagramm eines zweiten Beispiels einer Zerkleinerungsanlage zur Zerkleinerung eines Mahlgutes und eines Regelungssystems zur Regelung der Zerkleinerungsanlage,

FIG 30

eine Abhängigkeit eines Siebunterlaufgewichts von der Brechspaltgröße eines Brechers,

FIG 31

eine Abhängigkeit einer Siebklassierungseffektivität von der Brechspaltgröße eines Brechers,

FIG 32

eine Abhängigkeit einer Siebklassierungseffektivität von der Brecherproduktivität eines Brechers nach Ausgangserz,

FIG 33

eine Abhängigkeit eines Siebüberlaufgewichts von der Brechspaltgröße eines Brechers,

FIG 34

eine Abhängigkeit eines Siebunterlaufgewichts von einer Brecherproduktivität eines Brechers nach Ausgangserz,

FIG 35

eine Abhängigkeit einer Brecherproduktivität eines Brechers nach Ausgangserz von der Nennkorngröße eines Brechprodukts,

FIG 36

eine Abhängigkeit einer Motorleistung eines Brechers von der Brechspaltgröße des Brechers,

FIG 37

eine Abhängigkeit einer Motorleistung eines Brechers von der Brecherproduktivität des Brechers nach Ausgangserz,

FIG 38

eine Abhängigkeit der Energieintensität eines Brechers von der Brecherproduktivität des Brechers nach Ausgangserz,

FIG 39

eine Abhängigkeit der Energieintensität eines Brechers von der Brechspaltgröße des Brechers,

FIG 40

eine Abhängigkeit der Taumelbewegung eines Brechkegels eines Brechers von der Brecherproduktivität des Brechers nach Ausgangserz, und

FIG 41

eine Abhängigkeit der Taumelbewegung eines Brechkegels eines Brechers von einer Nennkorngröße des Brechprodukts.

The above-described characteristics, features and advantages of this invention, as well as the manner in which they are achieved, will become clearer and more clearly understood in connection with the following description of exemplary embodiments, which are explained in more detail in connection with the drawings. Showing:

FIG. 1

a block diagram of a first example of a crushing plant for crushing a ground material and a control system for controlling the crushing plant,

FIG. 2

a dependence of an energy intensity after material comminution of an overflow density of a classifier,

FIG. 3

a dependence of a circulation load of a crushing plant with ore on a mill productivity to finished class,

FIG. 4

a dependence of an energy intensity after material comminution of the ratio of liquid material to solid material in a mill,

FIG. 5

a dependence of a mill productivity on initial ore of an energy intensity after material comminution,

FIG. 6

a dependence of a filling volume of a mill from a mill productivity to initial ore,

FIG. 7

a dependence of a motor power of a mill on a mill productivity to output ore,

FIG. 8

a dependence of a circulation load on a ratio of liquid material to solid material in a mill,

FIG. 9

a dependence of a mill productivity on initial yield of a ratio of liquid material to solid matter in a mill,

FIG. 10

a dependence of mill productivity on finished class of a circulation load,

FIG. 11

a dependence of a mill productivity on initial ore of an overflow density of a classifier,

FIG. 12

a dependence of a mill productivity on initial yield from a mill productivity to finished grade,

FIG. 13

a dependence of a ratio of liquid material to solid material in a mill of an overflow density of a classifier,

FIG. 14

a dependence of a filling volume of a mill on a ratio of liquid material to solid material in the mill,

FIG. 15

a dependence of an energy intensity after material comminution of a filling volume of a mill,

FIG. 16

a dependence of mill productivity on initial ore from a fraction of finished grade in a classifier overflow;

FIG. 17

a dependence of an overload of a mill on an energy intensity after material shredding,

FIG. 18

a dependence of mill productivity on finished grade of an energy intensity after material shredding,

FIG. 19

a dependence of a motor power of a mill on a filling volume of the mill,

FIG. 20

a dependence of a mill productivity on the initial ore of the overflow density of a classifier,

FIG. 21

a dependence of the iron content in the intermediate product of a first deposition stage on a fraction of the finished class in a classifier overflow,

FIG. 22

a dependence of the iron content in the intermediate product of a first deposition stage on an overflow density Rcl of the classifier,

FIG. 23

a dependence of the iron content in the intermediate product of a first deposition stage on the engine performance of a separator,

FIG. 24

a dependence of a mill productivity on the starting ore of the engine power of a separator,

FIG. 25

a dependence of the output Y of the intermediate product of a first separation stage on the drum speed of a separator,

FIG. 26

a dependence of the output Y of the intermediate product of a first deposition stage on the overflow density of a classifier,

FIG. 27

a dependency of the output Y of the intermediate product of a first deposition stage from an engine performance of a separator,

FIG. 28

a dependence of an iron content in the tailings of a first deposition stage on the engine performance of a separator,

FIG. 29

a block diagram of a second example of a crushing plant for the comminution of a material to be ground and a control system for controlling the crushing plant,

FIG. 30

a dependence of a Siebunterlauflauf weight of the crushing gap size of a crusher,

FIG. 31

a dependence of screen classification efficiency on the crushing gap size of a crusher,

FIG. 32

a dependence of a sieve-classifying efficiency on the crusher productivity of a crusher to starting ore,

FIG. 33

a dependence of a screen overflow weight on the crushing gap size of a crusher,

FIG. 34

a dependence of a sieve underflow weight from a crusher productivity of a crusher to initial ore,

FIG. 35

a dependence of a crusher productivity of a crusher on initial ore from the nominal grain size of a crushed product,

FIG. 36

a dependence of an engine power of a crusher on the crushing gap size of the crusher,

FIG. 37

a dependence of a motor power of a crusher on the crusher productivity of the crusher to the output ore,

FIG. 38

a dependence of the energy intensity of a crusher from the crusher productivity of the crusher to the output ore,

FIG. 39

a dependence of the energy intensity of a crusher on the crushing gap size of the crusher,

FIG. 40

a dependence of the tumbling motion of a crushing cone of a crusher on the crushing productivity of the crusher after initial ore, and

FIG. 41

a dependence of the tumbling motion of a crushing cone of a crusher on a nominal grain size of the crushing product.

Corresponding parts are provided in all figures with the same reference numerals.

FIG. 1 shows a block diagram of a first example of a crushing plant 1 for crushing a ground material and a control system 20 for controlling the crushing plant 1, with reference to which various embodiments of the invention will be described. The material to be ground is in each case an ore in these exemplary embodiments.

The crushing plant 1 comprises a mill 2, a classifier 3 and a separator 4.

The control system 20 comprises in each case at least one sensor 21 for a mill productivity Qr according to initial ore, a water consumption Gvm of the mill 2, an engine power Pcl of the classifier 3, a filling volume V of the mill 2, a water consumption Gvk of the classifier 3, an engine power Pdv of the mill 2 , a classifier overflow density Rcl, an engine power Ps of the separator 4, a drum speed n of the separator 4, and an iron content Feg in a tailing of the first deposition stage.

Further, the control system 20 each includes at least one mill productivity regulator Qr according to initial ore, a ratio of W / F liquid material to solid material in the mill 2, iron content Fe in the intermediate product of the first deposition stage, and overflow density Rcl and water consumption Gvk of the classifier 3 ,

In addition, the control system 20 includes a control unit 23 for evaluating measured data of the transducers 21 and for controlling the controller 22.

To regulate the comminution system 1, measured data are recorded regularly by means of the transducers 21, for example at intervals of several minutes. These measurement data are evaluated by the control unit 23 for controlling the controller 22. In this case, moving average values are preferably determined and evaluated from the measured data. For evaluation purposes, functions are described below which describe in each case a dependency of a first operating parameter of the comminuting plant on a second operating parameter of the comminuting system and are selected such that the first derivatives of these functions, in particular the signs of these first derivatives, are suitable reference variables for the control the crushing plant 1 are. The operating parameters are in each case directly or indirectly related to the measured variables detected by the transducers 21, i. an operating parameter either coincides with one of these measured variables or is determined from the measured variables. The basis of the control method are the nonlinear dependencies of the respective operating parameters described by means of the evaluated functions.

The FIGS. 2 to 29 show qualitative graphical representations of such dependencies of two operating parameters of each other, namely the dependencies of an energy intensity E after material crushing (ie energy demand E per mass of ground material in its final quality) of the overflow density Rcl of the classifier 3 ( FIG. 2 ), a circulation load C of the comminution plant 1 with ore from a mill productivity Qgk to finished class ( FIG. 3 ), the energy intensity E after material comminution of the ratio W / F liquid material to solid material in the mill 2 ( FIG. 4 ), the mill productivity Qr according to initial ore of the energy intensity E after material comminution ( FIG. 5 ), of Filling volume V of the mill 2 from the mill productivity Qr to Ausgangsserz ( FIG. 6 ), the motor power Pdv of the mill 2 from the mill productivity Qr to the output rate ( FIG. 7 ), the circulation load C from the ratio W / F of liquid material to solid material in the mill 2 ( FIG. 8 ), the mill productivity Qr according to the starting point of the ratio W / F liquid material to solid material in the mill 2 ( FIG. 9 ), the mill productivity Qgk after finished class of the circulation load C ( FIG. 10 ), the mill productivity Qr according to the initial ore of the overflow density Rcl of the classifier 3 ( FIG. 11 ) and the mill productivity Qgk to finished class ( FIG. 12 ), the ratio W / F of liquid material to solid material in the mill 2 of the overflow density Rcl of the classifier 3 ( FIG. 13 ), the filling volume V of the mill 2 of the ratio W / F liquid material to solid material in the mill 2 ( FIG. 14 ), the energy intensity E after material comminution of the filling volume V of the mill 2 ( FIG. 15 ), the mill productivity Qr after initial yield of a fraction Scl of the finished class in the classifier overflow ( FIG. 16 ), an overload Iper the mill 2 of the energy intensity E after material crushing ( FIG. 17 ), the mill productivity Qgk after finished class of the energy intensity E after material comminution ( FIG. 18 ), the engine power Pdv of the mill 2 of the filling volume V of the mill 2 ( FIG. 19 ), the mill productivity Qr according to the initial ore of the overflow density Rcl of the classifier 3 ( FIG. 20 ), the iron content Fe in the intermediate product of the first deposition stage from the fraction Scl of the finished class in the classifier overflow ( FIG. 21 ), from the overflow density Rcl of the classifier 3 ( FIG. 22 ) and the engine power Ps of the separator 4 ( FIG. 23 ), the mill productivity Qr according to the output rate of the motor power Ps of the separator 4 (FIG. FIG. 24 ), discharging Y of the intermediate product of the first separation stage from the drum rotation speed n of the separator 4 (FIG. FIG. 25 ), from the overflow density Rcl of the classifier 3 ( FIG. 26 ) and the engine power Ps of the separator 4 ( FIG. 27 ) and the iron content Feg in the tailings of the first deposition stage of the engine power Ps of the separator 4 ( FIG. 28 ).

Below are several on the FIGS. 1 to 29 described regulations of sub-processes of comminution of the millbase, which describe both independently and optionally combined with each other embodiments of the invention.

First of all, as a first embodiment of the invention, a regulation of the productivity of the comminution of the material to be ground, taking into account the filling volume V of the mill 2 and the water supply, will be described. Prerequisites for the implementation of this system of productivity are stabilized quality indicators for iron content Fe in the intermediate product of the first deposition stage as well as the iron content in tailings residues, which are tested in real time using indirect indicators.

The diagnosis of the raw ear crushing productivity scheme will be carried out in accordance with the FIGS. 4 to 7 . 9 to 11 . 15 . 19 and 24 shown nonlinear dependencies using a test matrix described below for a regulation of raw material throughput of the mill 2. On the basis of the test matrix, the test is carried out for an ineffective, effective or optimal state of the process control for productivity control, taking into account the water flow in the mill 2 and separator feed according to the following table [1]. Table 1]: DQR / dt + - - dV / dt + - - dE / dt - + + dE / dV + - 0 dPdv / dV - + 0 d (W / F) / dE + - 0 GQF / dPdV - + 0 DQR / d (W / F) - + 0 GQF / Ps - + 0 dQgk / dC - + 0 rating ineffective effectively optimal

Table [1] contains signs of the first derivatives of various operating parameters, each after a time t or according to another operating parameter, the value 0 indicating the disappearance of a first derivative. These signs form the above-mentioned test matrix for controlling the raw material throughput of mill 2. The last line of the table [1] contains the condition evaluation, by means of which the raw-material throughput is regulated. The optimal state is defined by the disappearance of the first derivatives dE / dV, dPdv / dV, d (W / F) / dE, dQr / dP, dQr / d (W / F), dQr / Ps and dQgk / dC. The regulation of the crude throughput of the mill 2 takes place in such a way that the optimum state is achieved or maintained.

In the event of an ineffective condition, the regulators 22 are given the task of reducing the ore feed of the mill 2 by the mill productivity regulator Qr to the starting point, taking into account the reduction in the filling volume V or reducing the water consumption of the mill 2 by the ratio controller 22 W / F liquid material to solid material in the mill 2, taking into account the density increase in the mill outlet or the density reduction in Klassiererauslauf by the overflow density controller Rcl 22 of the classifier 3. Ineffective operation also reduces the iron content Fe in the intermediate product.

In the case of an effective condition, the regulators 22 receive the task of increasing the ore feed of the mill 2 to the mill productivity Qr according to the output ore, taking into account the increase of the filling volume V or increasing the water consumption of the mill 2 by the ratio W controller 22 / F liquid material to solid material in the mill 2, taking into account the density reduction in the mill outlet or the density increase in the classifier outlet by the overflow density controller Rcl of the Classifier 3. In effective operation, the iron content Fe in the intermediate product also increases.

The feed of mill 2 with millbase is stabilized on reaching the optimum parameters dPdv / dQr = 0, dPdv / dF = 0 and dE / dF = 0 for the filling volume V of mill 2 with ore pulp.

The filling volume V is also stabilized taking into account the water flow in the mill 2 when the optimum parameters dE / d (W / F) = 0 and dQr / d (W / F) = 0 are reached.

Stabilization is also made taking into account the circulation load or when the optimal parameters dQgk / dC = 0 are reached.

Stabilization is also possible with optimum charging of the separator 4, which is achieved by dQr / dPs = 0.

In the following, a regulation of the pulse density of the classifier outlet will be described as a second embodiment of the invention. Prerequisite for the diagnosis of the pulp density of the classifier effluent are also in a given range stabilized quality indicators for the iron content Fe in the intermediate product of the first deposition stage and the iron content in waste residues, which are checked in real time using indirect indicators.

The diagnosis of the classifier operation is similar to the productivity control diagnosis described above based on a test matrix, which in this case is based on the in the FIGS. 11, 13 and 22 defined nonlinear dependencies is defined. On the basis of the test matrix, the test is carried out for an ineffective, effective or optimal state of process control for classifying the products in the classifier 3 as a function of throughput, ratio of W / F liquid material to solid material in the mill 2, iron content Fe in the intermediate product of the first Separation stage and yield of intermediate product of the first separation stage according to the following Table [2]. Table [2]: DRCL / dt - + - DQR / dt - + - d (W / F) / dt - - - DFE / dt + - + Qr dop Qr> Qr dop Qr <Qr dop Qr = Qr dop Fe dop Fe> Fe dop Fe <Fe dop Fe = Fe dop rating effectively ineffective optimal

Here and hereinafter the term "dop" is used for an allowed value of a parameter, i. Qr dop and Fe dop respectively denote permitted values of mill productivity Qr according to initial ore and iron content Fe in the intermediate product.

In the case of an ineffective state, the regulators 22 are given the task of increasing the ore feed of the mill 2 by the mill productivity regulator Qr to the starting point, taking into account the increase in the filling volume V or increasing the water consumption of the mill 2 by the ratio ratio controller 22 / F liquid material to solid material in the mill 2, taking into account the density increase in the mill outlet or the density reduction in Klassiererauslauf by the controller 22 for the overflow density Rcl of the classifier 3. Ineffective operation also reduces the iron content Fe in the intermediate product.

In the case of an effective condition, the regulator 22 receives the mill feed ore feeding task 2, the mill productivity Qr according to the output ore, taking into account the reduction of the filling volume V or the reduction of water consumption of the mill 2 by the ratio W controller 22 / F liquid material to solid material in the mill 2, taking into account the density reduction in the mill outlet or the density increase in the classifier outlet by the overflow density controller 22 Rcl of the classifier 3. In effective operation, the iron content Fe in the intermediate product also increases.

The feed of mill 2 with millbase is stabilized when the optimum parameters dQr / dPs = 0 for the density of the classifier effluent and the yield of intermediate product are reached.

In the following, as a third embodiment of the invention, a regulation of the raw material throughput of the mill will be described with optimization of the water flow in the comminution plant. This regulation also requires stabilized quality indicators for iron content Fe in the intermediate product of the first separation stage as well as the iron content in waste residues, which are checked in real time using indirect indicators.

The diagnosis of the classifier operation is based on a test matrix, which in this case is based on the in the FIGS. 4, 8, 9 and 13 defined nonlinear dependencies is defined. On the basis of the test matrix, the test is carried out on an ineffective, effective or optimal state of the process control for controlling the crude throughput taking into account the water flow in the mill 2 according to the following table [3]. Table [3]: DRCL / dt + + 0 DQR / dt - + 0 d (W / F) / dt - - 0 dC / dt - + 0 dE / dt + - 0 C dop C <C dop C <C dop C <C dop (W / F) dop W / F <(W / F) dop W / F <(W / F) dop W / F> (W / F) dop W / F = (W / F) dop Rcl dop Rcl <Rcl dop Rcl> Rcl dop Rcl = Rcl dop rating effectively ineffective optimal

In the following, as a fourth embodiment of the invention, a regulation of the energy demand E in the raw particle size reduction will be described. The diagnosis of the regulation of the energy requirement for raw crushing takes place under the condition of minimizing the energy consumption at given limits of the quality parameters for the iron content Fe of the intermediate product.

The ore processing energy consumption is diagnosed on the basis of a test matrix for energy demand control, which is based on FIGS. 2, 4, 5 . 15 and 18 defined nonlinear dependencies is defined. On the basis of the test matrix, the test is carried out for an ineffective, effective or optimal state of process control for size reduction, product classification and water flow in mill 2 according to the following table [4]. Table [4]: dE / dt + - + DRCL / dt + - - DQR / dt + - + dE / d (W / F) - + 0 dE / dV - + 0 dQgk / dt + + + Qgk dop Qgk> Qgk dop Qgk <Qgk dop Qgk = Qgk dop E dop E <E dop E> E dop E> E dop rating effectively ineffective optimal

In the case of an ineffective state, the regulators 22 are given the task of increasing the ore feed of the mill 2 by the mill productivity regulator Qr to the starting point, taking into account the increase in the filling volume V or increasing the water consumption of the mill 2 by the ratio controller 22 W / F liquid material to solid material in the mill 2 taking into account the density increase in the mill outlet or the density reduction in the classifier outlet by the overflow density controller 22 Rcl of the classifier 3. Inefficient operation also reduces the iron content Fe in the intermediate product.

In the case of an effective condition, the regulator 22 receives the mill feed ore feeding task 2, the mill productivity Qr according to the output ore, taking into account the reduction of the filling volume V or the reduction of water consumption of the mill 2 by the ratio W controller 22 / F liquid material to solid material in the mill 2, taking into account the density reduction in the mill outlet or the density increase in Klassiererauslauf by the controller 22 for the overflow density Rcl of the classifier 3. In effective operation also increases the iron content Fe in the intermediate product.

Feeding of mill 2 with regrind and water supply is stabilized when the optimum parameters dE / dV = 0 and dE / d (W / F) = 0 for the filling volume V are reached.

In the following, as a fifth embodiment of the invention, a regulation of the intermediate product quality in the raw particle size reduction will be described. The diagnosis of the regulation of the intermediate product quality is based on the minimization of the energy consumption at predetermined limits of the quality parameters for the iron content Fe of the intermediate product.

The diagnosis of intermediate ore grade quality is based on a quality control inspection matrix, which is based on the quality control matrix FIGS. 21 to 24 . 26 and 27 defined nonlinear dependencies is defined. On the basis of the test matrix, the test is carried out for an ineffective, effective or optimal state of quality control according to the following table [5]. Table [5]: DRCL / dt + - + dscl / dt - + - dQ / dt - + - DFE / dt - + - GQF / dPs + - 0 dS - + - dY / dPs + - 0 rating effectively ineffective optimal

In the event of an ineffective condition, the regulators 22 are given the task of reducing the ore feed of the mill 2 by the mill productivity regulator Qr to the starting point, taking into account the reduction in the filling volume V or reducing the water consumption of the mill 2 by the ratio controller 22 W / F liquid material to solid material in the mill 2, taking into account the density increase in the mill outlet or the density reduction in Klassiererauslauf by the overflow density controller Rcl 22 of the classifier 3. Ineffective operation also reduces the iron content Fe in the intermediate product.

In the case of an effective condition, the regulators 22 receive the task of increasing the ore feed of the mill 2 to the mill productivity Qr according to the output ore, taking into account the increase of the filling volume V or increasing the water consumption of the mill 2 by the ratio W controller 22 / F liquid material to solid material in the mill 2, taking into account the density reduction in the mill outlet or the density increase in Klassiererauslauf by the controller 22 for the overflow density Rcl of the classifier 3. In effective operation also increases the iron content Fe in the intermediate product.

The feeding of mill 2 with regrind and water supply is stabilized when the optimum parameters dQr / dPs = 0 and dY / dPs = 0 are reached.

Embodiments of the above-mentioned exemplary embodiments of the invention for controlling a comminution installation 1 will be described below by way of example.

In the following, cooperative algorithms for minimizing the energy demand in filling the mill 2 with ore and for regulating the water supply to the mill 2 will be described. In the control sequence, the control circuits for the ore have priority (s. FIGS. 5, 7, 8 . 15 . 24 ) in front of the control circuits for the water supply in the mill 2 and the classifier 3 (s. FIGS. 8, 9 . 11 ).

The criterion of the control according to a first algorithm is the minimization of the energy requirement at optimum filling volume V of the mill 2 with raw ore (s. Figures 5 . 15 ).

The raw ash crushing productivity control is diagnosed by controlling the raw material throughput of mill 2 on the basis of the dependencies according to table [1], with which the effectiveness test (ineffective, effective, optimal state) of process control and throughput control taking into account the water flow in the Mill 2 and the loads of the separator 4 are performed.

First, the control and diagnosis of the flow rate control will be listed taking into consideration the minimization of the energy consumption in the regulation of the optimum filling volume V of the mill 2. In this case, a setting value for the change of the ore mass in the mill 2 is changed in consideration of the change of the filling volume V of the mill 2 and the energy requirement (energy intensity) E according to the following equation: $$\mathrm{Qn}=\mathrm{Qlauf}+/-\left(\mathrm{dE}/\mathrm{dV}\right)\mathrm{dq}$$

• Qlauf: aktueller Einstellwert des Durchsatzes;
• Qn: neuer Einstellwert;
• dq: Schritt der Vergrößerung/Verringerung der Einstellung;
• dE=Elauf-Evor: Anstieg/Änderung des Energiebedarfs E;
• dV=Vlauf-Vvor: Anstieg/Änderung des Füllvolumens V;

dabei werden hier und im Folgenden die Bezeichnung "lauf" für einen aktuellen Wert eines Parameters und die Bezeichnung "vor" für einen dem aktuellen Wert zeitlich vorhergehenden Wert des jeweiligen Parameters verwendet.The following designations were used:

• Qlauf: current set value of the throughput;
• Qn: new setting value;
• dq: step of increasing / decreasing the setting;
• dE = Elauf-Evor: increase / change in energy demand E;
• dV = Vlauf-Vvor: increase / change of the filling volume V;

Here, and in the following, the term "run" is used for a current value of a parameter and the term "before" for a value of the respective parameter which precedes the current value.

The key to the effectiveness diagnosis of the controller according to equation [6] is the sign of the derivative dE / dV in the control of the feed of the mill 2.

• im Falle eines uneffektiven Zustands der Steuerung nimmt dE/dV einen positiven Wert an, was auf den Anstieg des Energiebedarfs E und eine Verringerung des Roherzdurchsatzes hinweist;
• im Falle eines effektiven Zustands nimmt dE/dV einen negativen Wert an, was auf die Verringerung des Energiebedarfs E und einen Anstieg des Roherzdurchsatzes hinweist;
• im Falle eines optimalen Zustands verschwindet dE/dV, was auf den optimalen Energiebedarf E und den optimalen Roherzdurchsatz unter Berücksichtigung des Füllvolumens V hinweist.

On the basis of the test matrix according to Table [1] and the diagrams of the static characteristics, the effectiveness of the process control is evaluated according to three states:

• in the case of an ineffective state of the control dE / dV assumes a positive value, which indicates the increase of the energy demand E and a reduction of the Roherz's rate;
• in the case of an effective state, dE / dV assumes a negative value, indicating the reduction in energy demand E and an increase in raw-material throughput;
• in the case of an optimal state, dE / dV disappears, which indicates the optimum energy requirement E and the optimum raw-material throughput, taking into account the filling volume V.

As the key element of the control for analyzing the operating conditions of the pulverizer 1, in the equation [6], instead of the derivative dE / dV, other discharges defining the change of the productivity of the mill according to Table [1] can be used. The set value of the flow rate according to equation [6] is calculated on the basis of the moving average values of the process test parameters (Elauf, Evor, Qr before, Qr run, Vlauf, Vvor) changed in decency of, for example, eight to ten minutes.

wobei Qr ein einen Eingangswert von Qr bezeichnet.If the moving average Qr satisfies the optimization condition Qr = Qr opt with Qmin <Qropt <Qmax in the period of eight to ten minutes, where Qropt is an optimum value of Qr, then the moving average values Elauf every eight to ten minutes, efore; Qr before, Qr run: Vlauf, Vvor; Pdv running, Pdv before tested. The increase in throughput is checked according to the following equation, $$\mathrm{dQr}=\mathrm{Qr\; a\; run}-\mathrm{Qr\; one\; in\; front}$$

where Qr indicates an input value of Qr.

Analogously, an analysis of the technological comminution situation taking into account the change of the parameters is carried out every eight to ten minutes. On the basis of this analysis, the search of the new set value Qr is performed taking into account the signs of the derivatives dQr / dt, dE / dt, dE / dV.

1. a) wenn dQr>O, dE<0, dE/dV> 0 (uneffektiver Betrieb), wird der Einstellwert für dQr ein gemäß folgender Gleichung verringert: $$\mathrm{Qr\; ein}=\mathrm{Qr\; ein\; lauf}-\left(\mathrm{dE}/\mathrm{dV}\right)\mathrm{dq}$$
   
2. b) wenn dQr<O, dE>0, dE/dV< 0 (effektiver Betrieb), wird der Einstellwert wird gemäß folgender Gleichung erhöht $$\mathrm{Qr\; ein}=\mathrm{Qr\; ein\; lauf}-\left(-\mathrm{dE}/\mathrm{dV}\right)\mathrm{dq}$$
   
3. c) wenn dE/dV=0, so bleibt die Einstellung auf dem bisherigen Wert, wodurch das optimale Füllvolumen V der Mühle 2 definiert wird. Der Durchsatz wird dabei auf dem optimalen Wert stabilisiert gemäß $$\mathrm{Qr\; ein}=\mathrm{Qr\; ein\; lauf}$$
   

As an example of the diagnosis, the crushing behavior with respect to the change in the flow rate setting in the ineffective, effective and optimum state is considered taking into account the energy demand E and the filling volume V:

1. a) if dQr> O, dE <0, dE / dV> 0 (ineffective operation), the set value for dQr is decreased according to the following equation: $$\mathrm{Qr\; on}=\mathrm{Qr\; a\; run}-\left(\mathrm{dE}/\mathrm{dV}\right)\mathrm{dq}$$
   
2. b) if dQr <O, dE> 0, dE / dV <0 (effective operation), the set value is increased according to the following equation $$\mathrm{Qr\; on}=\mathrm{Qr\; a\; run}-\left(-\mathrm{dE}/\mathrm{dV}\right)\mathrm{dq}$$
   
3. c) if dE / dV = 0, the setting remains at the previous value, whereby the optimum filling volume V of the mill 2 is defined. The throughput is stabilized at the optimum value according to $$\mathrm{Qr\; on}=\mathrm{Qr\; a\; run}$$
   

1. a) Wenn der vorherige letzte Wert der Ableitung dE/dt des Energiebedarfs E nach der Zeit gemäß $$\mathrm{Elauf}\le \mathrm{E}*\min +\left[{\mathrm{k}}_{\mathrm{1}}\mathrm{E}*\mathrm{min\; dE}/\mathrm{dV}\right]\mathrm{mit}\mathrm{0},\mathrm{05}\le {\mathrm{<figure-callout\; id="1"\; label="k"\; filenames="imgf0006.png"\; state="\{\{state\}\}">k</figure-callout>}}_{\mathrm{1}}\le \mathrm{0},\mathrm{1}$$
   
   
   negativ oder Null war, wobei E*min den letzten vorhergehenden gleitenden Mittelwert der Zerstörungsenergie bezeichnet, aber im aktuellen Schritt eine Vorzeichenänderung der Ableitung dE/dV gemäß $$\mathrm{Elauf}>\mathrm{E}*\min +\left[{\mathrm{k}}_{\mathrm{1}}\mathrm{E}*\mathrm{min\; dE}/\mathrm{dV}\right]$$
   
   
   stattgefunden hat, so ändert sich in diesem Fall auf der Basis der Gleichungen [11], [12] das Vorzeichen der Ableitung dE/dV im zu kontrollierenden Zeitabschnitt von einem positiven zu einem negativen Wert. Bei dieser Betriebsweise wird die Effektivität der Mahlung bei Minimierung des Energiebedarfs E erhöht. Das bedeutet, dass die Optimierungszone für das Füllvolumen V der Mühle 2 gefunden und die Minimierung des Energiebedarfs E zur Zerstörung des Erzes mit den vorhandenen mechanischen und physikalischen Eigenschaften erreicht wurde. Die Überprüfung der gefundenen Optimierungszone unter Berücksichtigung des letzten Einstellwertes für die Erzaufgabe in die Mühle 2 wird im Verlauf von beispielsweise ein bis drei Prüfzeitabschnitten durchgeführt, wobei der Qr-Einstellwert nicht geändert wird.
2. b) Wenn sich die Effektivität der Mahlung verringert und dabei ein Anstieg des Energiebedarfs E gemäß $$\mathrm{Elauf}\ge \mathrm{E}*\min +\mathrm{0},\mathrm{1}\mathrm{E}*\min$$
   
   
   festgestellt wird, ist es erforderlich, die Ursache für die Betriebsverschlechterung zu ermitteln, was wiederum auf der Basis von Ableitungen erfolgt:
   • Wenn dQr>0, dPdV/dV>0, dE/dV<0, ist die Mühle unterbelastet; dann wird eine Erhöhung des Einstellwertes für den Durchsatz um einen Wert dQr 2, der kleiner als ein Anfangsschritt dQr 1 ist, durchgeführt. Es wird ein Modus der langsamen Annäherung an die Optimierungszone mit dQr 2<dQr 1 unter Verwendung einer kleineren Einstellungsänderung des Erzdurchsatzes eingeführt, zum Beispiel gemäß dQr 2=k₂ dQr mit 0,2 ≤ k₂ ≤ 0,5. Dann wird der neue Einstellwert gemäß $$\mathrm{Qr\; ein}=\mathrm{Qr\; ein\; lauf}-{\mathrm{<figure-callout\; id="2"\; label="k"\; filenames="imgf0001.png"\; state="\{\{state\}\}">k</figure-callout>}}_{\mathrm{2}}\mathrm{dQr\; ein}$$
     
     
     ermittelt.
   • Wenn sich der Durchsatz verringert, d.h. dQ<O, dP/dV<0, dE/dV>0, kann sich die Mühle 2 unmittelbar vor der Überlastung oder im Bereich der Überlastung befinden. In diesem Fall wird eine Verringerung des Einstellwertes um einen Wert dQr 2, der ebenfalls kleiner als ein Anfangsschritt dQr 1 ist, durchgeführt, zum Beispiel gemäß dQr 2=k₃ dQr 1 mit 0,2 ≤ k₃ ≤ 0,5. Dann wird der neue Einstellwert gemäß $$\mathrm{Qr\; ein}=\mathrm{Qr\; ein\; lauf}-{\mathrm{<figure-callout\; id="3"\; label="k"\; filenames="imgf0001.png"\; state="\{\{state\}\}">k</figure-callout>}}_3\mathrm{dQr\; ein}$$
     
     
     ermittelt. Gleichung [15] bewirkt, dass die Mühle 2 den bezüglich des Füllvolumens V uneffektiven Zerkleinerungsmodus verlässt.

If a change in the physical and mechanical properties of the raw ore (eg increase in ore strength, deterioration of grindability, increase in grain size) results in an increase in energy demand E and a reduction in raw core throughput Qr, it is necessary to determine the cause of the productivity reduction. It is determined in which characteristic area E (V) (s. FIG. 15 ) the crushing operation is in relation to the charging parameters (underload, overload or optimum mill charge):

1. a) If the previous last value of the derivative dE / dt of the energy demand E after the time according to $$\mathrm{Elauf}\le \mathrm{e}*\min +\left[{\mathrm{k}}_{\mathrm{1}}\mathrm{e}*\mathrm{min\; dE}/\mathrm{dV}\right]\mathrm{With}\mathrm{0}.\mathrm{05}\le {\mathrm{<figure-callout\; id="1"\; label="k"\; filenames="imgf0006.png"\; state="\{\{state\}\}">k</figure-callout>}}_{\mathrm{1}}\le \mathrm{0}.\mathrm{1}$$
   
   
   was negative or zero, where E * min denotes the last preceding moving average of the destruction energy, but in the current step a sign change of the derivative dE / dV according to $$\mathrm{Elauf}>\mathrm{e}*\min +\left[{\mathrm{k}}_{\mathrm{1}}\mathrm{e}*\mathrm{min\; dE}/\mathrm{dV}\right]$$
   
   
   In this case, on the basis of the equations [11], [12], the sign of the derivative dE / dV in the time period to be controlled changes from a positive to a negative value. In this mode of operation, the effectiveness of the grinding is increased while minimizing the energy requirement E. This means that the optimization zone for the filling volume V of the mill 2 found and the minimization of the energy demand E to destroy the ore with the existing mechanical and physical properties has been achieved. The check of the found optimization zone taking into account the last setting value for the ore feed into the mill 2 is carried out in the course of, for example, one to three test periods, wherein the Qr set value is not changed.
2. b) If the effectiveness of the grinding decreases and thereby an increase in the energy demand E according to $$\mathrm{Elauf}\ge \mathrm{e}*\min +\mathrm{0}.\mathrm{1}\mathrm{e}*\min$$
   
   
   is determined, it is necessary to determine the cause of the deterioration of the operation, again on the basis of derivatives:
   • If dQr> 0, dPdV / dV> 0, dE / dV <0, the mill is underloaded; then an increase in the set value for the flow rate by a value dQr 2 which is smaller than an initial step dQr 1 is performed. A mode of slow approximation to the optimization zone with dQr 2 <dQr 1 is introduced using a smaller ore change in the ore flow, for example according to dQr 2 = k ₂ dQr where 0.2 ≤ k ₂ ≤ 0.5. Then the new setting value becomes $$\mathrm{Qr\; on}=\mathrm{Qr\; a\; run}-{\mathrm{<figure-callout\; id="2"\; label="k"\; filenames="imgf0001.png"\; state="\{\{state\}\}">k</figure-callout>}}_{\mathrm{2}}\mathrm{dQr}$$
     
     
     determined.
   • As the throughput decreases, ie, dQ <O, dP / dV <0, dE / dV> 0, the mill 2 may be just prior to congestion or in the area of congestion. In this case, a reduction of the set value by a value DQR 2, which is also smaller than an initial step DQR 1, carried out, for example, according DQR 2 = k ₃ DQR 1 with 0.2 ≤ k ≤ 0.5 _3. Then the new setting value becomes $$\mathrm{Qr\; on}=\mathrm{Qr\; a\; run}-{\mathrm{<figure-callout\; id="3"\; label="k"\; filenames="imgf0001.png"\; state="\{\{state\}\}">k</figure-callout>}}_3\mathrm{dQr}$$
     
     
     determined. Equation [15] causes the mill 2 to leave the crushing mode ineffective with respect to the filling volume V.

entspricht, dann befindet sich das System im Stabilisierungsmodus. Qr ein opt bezeichnet dabei die vom Bediener festgelegte Einstellung.When a set value given by an operator in the control of local control instruments has the following condition $$\mathrm{Qr\; a\; run}\le \mathrm{Qr\; an\; opt}$$

corresponds, then the system is in stabilization mode. Qr An opt designates the setting specified by the operator.

FIG. 29 shows a block diagram of a second example of a crushing plant 1 for crushing a ground material and a control system 20 for controlling the crushing plant 1, based on which further embodiments of the invention will be described. The ground material is also an ore in each of these embodiments.

As in the in FIG. 1 As shown in the first example, the crushing plant 1 comprises a mill 2, a classifier 3 and a separator 4, the classifier 3 and the separator 4 in FIG FIG. 29 not shown again. In addition, the includes in FIG. 29 crusher 1 shown one of the mill 2 upstream crusher 5 for finely crushing the ore.

The crushing plant 5 comprises a plurality of bunkers 6, a plurality of metering devices 7, a plurality of crushers 8, a plurality of screens 9, an intermediate storage 10, a metering device 11, a circulation load belt 12 and a conveyor belt 13.

The control system 20 comprises in each case at least one sensor 21 for a material stock H1 to H4 in each bunker 6, a metering speed nd1 to nd4 of each meter 7, an engine output N1 to N4 of each breaker 8, an energy intensity E1 to E4 of each crusher 8, a crushing gap size B1 to B4 of each crusher 8, a tumbling motion n1 to n4 of a crushing cone of each crusher 8, a mesh opening size L1 to L4 of each screen 9, a screen overflow weight T1 to T4 of each screen 9, a screen underpass weight C1 to C4 of each sieve 9, a sieve-classifying efficiency Esib1 to Esib4 of each sieve 9, an ore weight Qz of the sieve underflow after a center breaking, an ore weight Qg of the sieve overflow after a center breaking, a nominal grain size d of a crushing product, an ore weight of the mill-fed ore for detecting a mill productivity Qr according to the starting ore and the engine power Pdv of the mill 2.

In addition, the control system 20 comprises at least one regulator B of bunker feed B, the metering speed nd1 to nd4 of each meter 7, the engine power N1 to N4 and energy intensity E1 to E4 of each breaker 8, the tumbling motion n1 to n4 of a crushing cone of each crusher 8, the sieve opening size L1 to L4 of each sieve 9, and the mill productivity Qr to starting ore (mill feed of ore).

In addition, the control system 20 includes a control unit 23 for evaluating measured data of the transducers 21 and for controlling the controller 22. The control unit 23 is supplied with a predefinable desired grain size dsoll.

The control of the refining process is carried out with a control of the size of the crusher, energy characteristics and crushing zone productivity, adjusted to the productivity of the mill 2 in the crushing area and taking into account the size of the final crushing product and the productivity of the mill 2. Line measurement of a grain size of the final product used and realized a real-time control of technological parameters of the crushing processes (productivity, particle size of the crushing products, crushing stage, energy characteristics, efficiency of the classification with the sieve). A part of these parameters is measured directly, the remaining part is calculated.

The aim of the control is to maximize the throughput of the entire crushing plant 1 and minimize the energy used with stable grain composition of the final product to a minimum grain size of the crushed product in the nominal limits with maximum possible productivity of the refining process and maximum productivity of the mill 2 of the first crushing stage of To achieve refurbishment. For this purpose, the processes of crushing, screening and grinding of the ore are coordinated and optimized taking into account random changes in the strength properties of the ore, the grain size of the products after a center breaking and the embedding of the intermediate storage 10. Here, similar to the embodiments described above dependencies different Operating parameters used.

The FIGS. 30 to 41 show qualitative graphical representations of such dependencies of two operating parameters from each other, namely the dependencies of a Siebunterlaufgewichts C1 of the crushing gap size B1 of a crusher 8 ( FIG. 30 ), a sieve classification efficiency Esib1 of the crushing gap size B1 of a crusher 8 ( FIG. 31 ) and from the crusher productivity Q1 of a crusher 8 to the output ore ( FIG. 32 ), a screen overflow weight T1 of the crushing gap size B1 of a crusher 8 ( FIG. 33 ), a wire underrun weight C1 from a crusher productivity Q1 of a crusher 8 to starting ore ( FIG. 34 ), a crusher productivity Q1 of a crusher 8 to initial ore of the nominal grain size d of the crushed product ( FIG. 35 ), the engine power N1 of a crusher 8 from the crushing gap size B1 of the crusher 8 (FIG. FIG. 36 ) and from the crusher productivity Q1 of the crusher 8 to the output ore ( FIG. 37 ), the energy intensity E1 of a crusher 8 from the crusher productivity Q1 of the crusher 8 to Ausgangsserz ( FIG. 38 ) and the crushing gap size B1 of the crusher 8 (FIG. FIG. 39 ), as well as the tumbling motion n1 of a crushing cone of a Crusher 8 from the crusher productivity Q1 of the crusher 8 to Ausgangsserz ( FIG. 40 ) and the nominal grain size d of the crushed product ( FIG. 41 ). It shows FIG. 34 the dependence of a Siebunterlaufgewichts C1 of the crusher productivity Q1 of a crusher 8 to Ausgangsserz for two different Siebergergangsbreiten, the lower function graph depicting the dependency for a larger Siewerksgangsbreite. FIG. 37 shows the dependence of the engine power N1 of a crusher 8 from the crusher productivity Q1 of the crusher 8 to the output ore for four different crusher gap sizes B1 of the crusher 8, the four function graphs representing dependencies for increasing crushing gap size B1 from left to right.

In the following, embodiments of the invention for controlling the crushing plant 5 will be described. The regulation takes place in each case using at least one of the three control circuits described below.

A first control loop for regulating the crushing plant 5 optimizes the productivity of the ore crushing process with sizes of the underflow of the sieve which are stabilized in nominal limits with maximum permissible sieving efficiency. The control of the productivity of the crushing process is based on the dependencies shown in FIGS. 30 to 41, 5 and 7.

• Eine Einspeisung von Erz zu Brechern 8 wird erhöht:
  • bei negativen Ableitungswerten der Produktivität Q1 bis Q4 und negativen Ableitungswerten der Korngröße d des Brecherzes nach der Zeit (s. FIG 35);
  • bei positiven Ableitungswerten der Klassierungseffizienz Esib1 bis Esib4 und negativen Ableitungswerten der Größe B1 bis B4 des Brechspalts nach der Zeit (s. FIG 31);
  • bei negativen Ableitungswerten der Umlauflast T1 bis T4 und negativen Ableitungswerten der Größe B1 bis B4 des Brechspalts nach der Zeit (s. FIG 33);
  • bei negativen Ableitungswerten der Leistung N1 bis N4 des Elektromotors des Brechers und negativen Ableitungswerten der Beschickung Q1 bis Q4 des Brechers nach der Zeit (s. FIG 37);
  • bei negativen Ableitungswerten des Energiebedarfs N1 bis N4 des Brechers und positiven Ableitungswerten der Größe B1 bis B4 des Brechspalts nach der Zeit (s. FIG 39);
  • bei negativen Ableitungswerten der Produktivität Q1 bis Q4 des Brechers und negativen Ableitungswerten der Pendelfrequenz n1 bis n4 des Kegels nach der Zeit (s. FIG 40).

The control unit 23 is supplied with measurement data acquired by the transducers 21. The control unit 23 determines from these measurement data instantaneous values of first derivatives for in the FIGS. 30 to 41 . 5 and 7 displayed functions. The controllers 22 are controlled as follows as a function of these determined values of first derivatives by the control unit 23 as follows:

• A feed of ore to breakers 8 is increased:
  • with negative derivative values of the productivity Q1 to Q4 and negative derivative values of the grain size d of the crushing ore after the time (s. FIG. 35 );
  • for positive derivative values of the classification efficiency Esib1 to Esib4 and negative derivative values of the size B1 to B4 of the refractive index after the time (see FIG. FIG. 31 );
  • for negative derivative values of the circulation load T1 to T4 and negative derivative values of the size B1 to B4 of the refractive gap after the time (see FIG. FIG. 33 );
  • for negative derivative values of the power N1 to N4 of the electric motor of the crusher and negative derivative values of the charge Q1 to Q4 of the crusher after the time (see FIG. FIG. 37 );
  • for negative derivative values of the energy demand N1 to N4 of the crusher and positive derivative values of the size B1 to B4 of the crushing gap after the time (see FIG. FIG. 39 );
  • for negative derivative values of the productivity Q1 to Q4 of the crusher and negative derivative values of the pendulum frequency n1 to n4 of the cone after time (see FIG. FIG. 40 ).

• bei positiven Ableitungswerten der Produktivität Q1 bis Q4 und positiven Ableitungswerten der Korngröße d des Brecherzes nach der Zeit (s. FIG 35);
• bei negativen Ableitungswerten der Klassierungseffizienz Esib1 bis Esib4 und positiven Ableitungswerten der Größe B1 bis B4 des Brechspalts nach der Zeit (s. FIG 31);
• bei positiven Ableitungswerten der Umlauflast T1 bis T4 und positiven Ableitungswerten der Größe B1 bis B4 des Brechspalts nach der Zeit (s. FIG 33);
• bei positiven Ableitungswerten der Leistung N1 bis N4 des Elektromotors des Brechers und positiven Ableitungswerten der Beschickung Q1 bis Q4 des Brechers nach der Zeit (s. FIG 37);
• bei positiven Ableitungswerten des Energiebedarfs N1 bis N4 des Brechers und negativen Ableitungswerten der Größe des Brechspalts B1 bis B4 nach der Zeit (s. FIG 39);
• bei positiven Ableitungswerten der Produktivität Q1 bis Q4 des Brechers und positiven Ableitungswerten der Pendelfrequenz n1 bis n4 des Kegels nach der Zeit (s. FIG 40).

The feed to the crusher is reduced:

• at positive derivative values of the productivity Q1 to Q4 and positive derivative values of the grain size d of the crushing ore after the time (s. FIG. 35 );
• for negative derivative values of the classification efficiency Esib1 to Esib4 and positive derivative values of the size B1 to B4 of the refractive index after the time (see FIG. FIG. 31 );
• at positive derivative values of the circulation load T1 to T4 and positive derivative values of the size B1 to B4 of the refractive gap after the time (s. FIG. 33 );
• at positive derivative values of the power N1 to N4 of the electric motor of the crusher and positive derivative values of the charge Q1 to Q4 of the crusher after the time (s. FIG. 37 );
• for positive derivative values of the energy demand N1 to N4 of the crusher and negative derivative values of the size of the crushing gap B1 to B4 after the time (see FIG. FIG. 39 );
• with positive derivative values of the productivity Q1 to Q4 of the crusher and positive derivative values of the pendulum frequency n1 to n4 of the cone after the time (s. FIG. 40 ).

The feed process for comminution to crusher feed is stabilized when the following optimum parameters for zero values of derivatives are reached: dCi / dBi = 0 (s. FIG. 30 ), dEsibi / dQi = 0 (s. FIG. 32 ), dEi / dQi = 0 (s. FIG. 38 ), respectively for i = 1, ..., 4.

Given the fact that the ores have different chemical and mineral properties and different strengths, resulting in a different throughput of the mill 2 for the final class, we take as the standard situation of the process "breaking - sieving - storage - grinding" the processing of the starting mineral ,

During the processing of the ore mineral, the break occurs only through the cone with regulation of the gap size. In the case of the change of the mineral with high strength in the crushing process, together with the change of the crushing gap of a crusher 8 and the pendulum frequency of the crushing cone of the crusher 8 is controlled with ensuring the minimum possible sizes of the crushing product. In other words, normally only the crushing gap sizes B1 to B4 are regulated and, in addition to a predefinable ore strength, the pendulum frequencies of the crushing cone of the crushers 8 are additionally controlled.

Breaking with predetermined minimum crushing gap sizes B1 to B4 is also useful in the case of limited space for the storage of the product in the intermediate storage 10. If a mineral with lower strength passes into the crushers 8, there is the possibility of increasing the nominal grain size d of the crushing product to increase the productivity of the crushing process. This may be necessary for the filling of the intermediate storage 10 up to a certain level, if the stock of crushing material in the intermediate storage 10 is below a predetermined value. Here, an increase in the nominal grain size d less hard ore is tuned to a desired productivity of the mill 2. In this case, an increase in the sieve opening sizes L1 to L4 is required in order to bring ore of the underflow into the intermediate store 10. In the case of technical impossibility of controlling the sieve opening sizes L1 to L4, the productivity optimization control system restricts the size of the crushed product in accordance with the maximum sieve classification efficiencies Esib1 to Esib4 depending on the crusher productivity Q1 to Q4 of a crusher 8 after starting ore (see FIG. FIG. 32 ).

A second control circuit controls overloading of the technological crushing and screening process using calculated overload factors to prevent overloading of the crushers 8 with respect to the power and material level in the aggregate. Overloading of a crusher 8 in terms of power consumption may occur if the input exceeds a permissible value defined by the desired grain size and ore strength properties and gap width. To overload a crusher 8 in relation to the amount of material occurs when the amount of feed material per time exceeds a maximum allowable throughput through the crusher 8 at a given crushing gap size B1 to B4.

In case of overload or fault of a crusher 8, the overload operation in real-time operation by means of relation characters of the corresponding derivatives dCi / dBi (s. FIG. 30 ) and dEi / dQi (s. FIG. 38 ) for i∈ {1, ..., 4}, so that dCi / dBi <0 and dEi / dQi> 0.

In case of overload and disturbance of a screen 9, the overload operation in real time operation by means of relation characters of the corresponding derivative dEsibi / dQi for i∈ {1, ..., 4} (s. FIG. 32 ), so that dEsibi / dQi <0 holds.

Upon reaching a stable borderline complex overall overload criterion according to Ipi> Ipi dop, where Ipi denotes a calculated criterion of overload, the crusher feed progressively decreases until a stable change in the signs of the above derivatives.

A third control circuit optimizes the productivity of the milling process of the starting ore at a stabilized nominal particle size d of the intermediate within specified limits, taking account of the ore strength as a function of the first derivatives of the functions mentioned below.

• bei negativen Werten der Ableitungen der Produktivität und positiven Werten der Zerkleinerungsenergie nach der Zeit (s. FIG 5) ;
  oder
• bei einem positiven Wert der Ableitung dPdv/dQr (s. FIG 7).

The feeding of feed material into the mill 2 is increased:

• with negative values of the derivatives of the productivity and positive values of the comminution energy after the time (s. FIG. 5 );
  or
• at a positive value of the derivative dPdv / dQr (s. FIG. 7 ).

• bei positiven Werten der Ableitungen der Produktivität und negativen Werten der Zerkleinerungsenergie nach der Zeit (s. FIG 5) ;
• bei einem negativen Wert des Verhältnisses der Ableitung dPdv/dQr (s. FIG 7).

The feeding of feed material into the mill 2 is reduced:

• with positive values of the derivatives of the productivity and negative values of the comminution energy after the time (s. FIG. 5 );
• at a negative value of the ratio of the derivative dPdv / dQr (s. FIG. 7 ).

Feeding of feed into mill 2 is stabilized upon reaching dPdv / dQr = O.

While the invention has been further illustrated and described in detail by way of preferred embodiments, the invention is not limited by the disclosed examples, and other variations can be derived therefrom by those skilled in the art without departing from the scope of the invention.

Claims (13)

Method for controlling and / or controlling a crushing plant (1) with a mill (2), a classifier (3) and a separator (4) for comminuting a material to be ground, wherein as at least one reference variable of the control and / or control a first derivative of a Function which describes the dependence of a first operating parameter of the comminution plant (1) on a second operating parameter of the comminution plant (1) is used. Method according to claim 1,
characterized in that as at least one reference value defines a zero of a first derivative used as a reference variable of a function. Method according to one of the preceding claims, characterized in that at least one manipulated variable is regulated and / or controlled as a function of at least one sign of a first derivative of a function used as a reference variable. Method according to one of the preceding claims, characterized in that for the regulation and / or control of the productivity of the comminution of the ground material as a first operating parameter, an energy intensity (E) after material comminution and as a second operating parameter a filling volume (V) of the mill (2), and / or as a first operating parameter an engine power (Pdv) of the mill (2) and as a second operating parameter a filling volume (V) of the mill (2), and / or as a first operating parameter a ratio (W / F) of liquid material to solid material in the mill (2) and as a second operating parameter an energy intensity (E) after material comminution, - and / or as a first operating parameter, a mill productivity (Qr) after a Ausgangsmahlgut and as a second operating parameter an engine power (Pdv) of the mill (2), and / or as a first operating parameter a mill productivity (Qr) after a starting meal and as a second operating parameter a ratio (W / F) of liquid material to solid material in the mill (2), - and / or as a first operating parameter, a mill productivity (Qr) after a Ausgangsmahlgut and as a second operating parameter, an engine power (Pdv) of the separator (4), and / or as a first operating parameter a mill productivity (Qgk) according to a production class and as a second operating parameter a circulation load (C) are used. Method according to one of the preceding claims, characterized in that for controlling and / or controlling a pulp density of a Klassiererauslaufs of the classifier (3) as a first operating parameter mill productivity (Qr) after Ausgangsmahlgut and as a second operating parameter, an engine power (Ps) of the separator (4) can be used. Method according to one of the preceding claims, characterized in that for controlling and / or controlling the energy demand of the comminution of the ground material as a first operating parameter, an energy requirement (E) after material crushing and as a second operating parameter, a filling volume (V) of the mill (2) and / or a ratio (W / F) of liquid material to solid material in the mill (2) are used. Method according to one of the preceding claims, characterized in that for controlling and / or controlling an intermediate quality in the comminution of the ground material as a first operating parameter mill productivity (Qr) after Ausgangsmahlgut and / or application (Y) of an intermediate product of a first deposition stage and as a second operating parameter, an engine power (Ps) of the separator (4) can be used. Method according to one of the preceding claims,
the crushing plant having a crushing plant (5) upstream of the mill (2) with at least one crusher (8) for finely crushing the ground material and at least one sieve (9) for sieving the crushed material to be ground,
characterized in that for controlling and / or controlling a productivity of the refining process as a first operating parameter, a crusher productivity (Q1 to Q4) of at least one crusher (8) according to initial ore and, as a second operating parameter, a crushing gap size (B1 to B4) of a crusher's crusher gap (B1 to B4) 8), and / or as a first operating parameter a Siebklassierungseffektivität (Esib1 to Esib4) at least one sieve (9) and / or an energy intensity (E1 to E4) of at least one crusher (8) and as a second operating parameter crusher productivity (Q1 to Q4 ) of at least one crusher (8) can be used. Method according to one of the preceding claims,
the crushing plant having a crushing plant (5) upstream of the mill (2) with at least one crusher (8) for finely crushing the ground material,
characterized in that for controlling and / or controlling an overload of the at least one crusher (8) as a first operating parameter, a crusher productivity (Q1 to Q4) of the crusher (8) and as a second operating parameter a crushing gap size (B1 to B4) of a crushing gap of Crusher (8), and / or as a first operating parameter an energy intensity (E1 to E4) of the crusher (8) and as a second operating parameter a crusher productivity (Q1 to Q4) of the crusher (8) are used. Method according to one of the preceding claims,
characterized in that at least one operating parameter of measurement data is determined, which are recorded at regular time intervals. Method according to claim 10,
characterized in that, to determine at least one operating parameter, sliding temporal average values of measured data are formed from the measured data. Method according to one of the preceding claims,
characterized in that the mill (2) is a ball mill. Method according to one of the preceding claims,
characterized in that the ground material is an ore.

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