EP0445321A1 - Procédé de fabrication de pâte dans un lessiveur en continu - Google Patents

Procédé de fabrication de pâte dans un lessiveur en continu Download PDF

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Publication number
EP0445321A1
EP0445321A1 EP90104231A EP90104231A EP0445321A1 EP 0445321 A1 EP0445321 A1 EP 0445321A1 EP 90104231 A EP90104231 A EP 90104231A EP 90104231 A EP90104231 A EP 90104231A EP 0445321 A1 EP0445321 A1 EP 0445321A1
Authority
EP
European Patent Office
Prior art keywords
production
quality measure
pulp
cellulose
quality
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.)
Granted
Application number
EP90104231A
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German (de)
English (en)
Other versions
EP0445321B1 (fr
Inventor
Herbert Dr. Ing. Furumoto
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.)
Siemens AG
Original Assignee
Siemens AG
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 Siemens AG filed Critical Siemens AG
Priority to AT90104231T priority Critical patent/ATE106477T1/de
Priority to DE59005944T priority patent/DE59005944D1/de
Priority to EP90104231A priority patent/EP0445321B1/fr
Publication of EP0445321A1 publication Critical patent/EP0445321A1/fr
Application granted granted Critical
Publication of EP0445321B1 publication Critical patent/EP0445321B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C3/00—Pulping cellulose-containing materials
    • D21C3/22—Other features of pulping processes
    • D21C3/228—Automation of the pulping processes
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C3/00—Pulping cellulose-containing materials
    • D21C3/22—Other features of pulping processes
    • D21C3/24—Continuous processes

Definitions

  • the invention relates to a method for pulp production by continuous cooking of wood.
  • continuous wood pulp mass is processed continuously in the continuous pulp production.
  • This is continuously conveyed through the digestion chemicals in a heated digester and at the end of which, after the desired removal, at least the so-called lignin in the form of pulp is continuously removed.
  • a continuous cooker is usually a lying or sloping, isothermal reactor.
  • This can also consist of several tanks connected in series, which are filled with digestion chemicals and through which the wood chips flow with the help of conveyors, e.g. Screw conveyors or conveyor belts.
  • the invention has for its object to provide a method for pulp production by continuous boiling of wood.
  • FIG. 1 shows an inclined, continuous cellulose cooker ZK as an example.
  • the wood to be digested is fed to this through a wood chip feed HE, preferably in the form of an aqueous, pulpy mass flow, via a controllable entry lock ES.
  • This entry lock preferably contains a feed screw ZS with adjustable speed nl.
  • the stove is filled with an alkali, which enables the pulp to be disintegrated from the wood composite by chemically removing the lignin contained in the wood.
  • the digestion chemicals have a concentration C and are kept in a chemical tank TA. In order to maintain a desired digester fill level L, the chemicals are fed to the cellulose digester ZK via a line CU.
  • a heat exchanger CA fed with live steam FD is preferably used for preheating.
  • preheated fresh chemicals are preferably fed continuously to the reactor in order to maintain a desired concentration and a desired fill level.
  • waste liquor is preferably continuously withdrawn via a take-off point AB, which is usually located inside the reactor, and a discharge line LA.
  • this live steam FD can be supplied at various points, only a few supply points being shown as examples in the figure.
  • FIG. 1 shows a speed-adjustable conveyor belt TB and the conveying direction F of the mass flow through the reactor by means of arrows, for example.
  • the wood pulp paste that is entered is converted into pulp with a quality that can be specified as possible by continuous cooking.
  • the pulp produced is continuously removed from the stove via a pulp discharge ZA.
  • a discharge lock A which in turn contains a speed-adjustable discharge screw AS, is preferably used for this purpose.
  • the quality of the pulp to be produced depends on a large number of process parameters, which can also be used as control variables for influencing the course of the cooking process if the machine is designed appropriately for mechanical engineering.
  • the speed of the cooking process is influenced on the one hand by the concentration C of the chemicals supplied to the cooker ZK from the tank TA.
  • Another influencing variable is the average amount of liquid digestion chemicals in the reactor. The more the digester is filled with the digestion liquor, the longer the wood pulp pulp is exposed to the influence of the chemicals during its continuous passage, and the faster the process of pulping takes place.
  • the amount of chemicals therein is determined by the alkali level L, also called the degree of digester filling.
  • a desired temperature inside the cooker ZK is generally set by supplying appropriately preheated fish steam FD. If necessary, this is introduced into the cooker at different points, for example at the upper end. Furthermore, you can adjust the temperature the digestion liquor supplied to the cooker from the tank TA and / or the wood chip mass flow HE supplied via the entry lock ES are preheated using the live steam FD. In the figure, a heat exchanger CA for heating chemicals is provided as an example.
  • Another important factor influencing the cooking process is the throughput speed of the wood chip mass flow through the reactor. In the reactor shown by way of example in the figure, this is determined in particular by the speed n1 of the feed screw ZS. As a rule, the speeds n1, n2 and n3 of the feed screw, the conveyor belt and the discharge screw are matched to one another in a suitable manner by means of a speed profile.
  • the boiling temperature T is best suited as a control variable for influencing the continuous boiling. This is the best way to control the process so that the desired pulp quality is produced with the greatest possible throughput. If this goal is not met, the pulp quality actually achieved may drop sharply. For example, a double loss can occur if the throughput speed of the wood chip mass flow is too low compared to the other process parameters. On the one hand, the system is not fully utilized and therefore the maximum possible production volume is not achieved. On the other hand, the wood chips are exposed to the influence of the pulping chemicals for too long, so that there are also losses in the quality and yield of the pulp.
  • Too much boiling produces a lot of pulp, but of lower quality, ie with a large number of short and fragile fibers.
  • the cooking temperature as a manipulated variable according to the invention, it is possible to react to fluctuations in the other process variables in such a way that the fluctuations in the pulp quality are at least temporary or slight after a disturbance has occurred.
  • a quality measure Q * corresponding to the desired pulp quality is specified, the setpoint of the associated optimal cooking temperature T * is determined by means of a process model, and this is then set in particular by transferring the setpoint to a lower-level cooking temperature control.
  • the process model preferably determines the cooking temperature T * cyclically at fixed time intervals with the aid of the current values of the process parameters involved. For this purpose, the actual values of the chemical concentrations C, the degree of filler L and the production quantity are preferably taken into account.
  • process constants are included in the model, the current values of which depend on the technology of the process, in particular on the chemical digestion process used and the type of cooker. The digestion process is largely determined by the type of digestion chemicals used, while the type of digester depends on the mechanical engineering conditions of the plant.
  • the value of the yield Y as a quality measure Q is also a statement about the internal quality of the pulp produced.
  • the cellulose quality that can be produced in each case can be influenced particularly simply and effectively in a first approximation in the method for cellulose production according to the invention.
  • a quality measure Q * is a known parameter.
  • a known parameter is, for example, the so-called "kappa number”. This is a measure of the residual concentration of lignin in the pulp produced. If the kappa number is large, only a small amount of digestion of the wood pulp used is achieved, for example, because the cooker throughput is too high. High residual lignin concentrations in the pulp result in low paper quality after they have been processed into paper, for example. If, on the other hand, a lower value, for example the kappa number, is achieved at a lower, optimal throughput, this indicates a high digestion of the wood chip mass used.
  • the current values of the chemical concentrations, the degree of filling of the cooker and the production quantity are fed to the process model as input variables.
  • the actual values of the chemical concentration C and the fill level L of the cooker can be influenced by additional subordinate control loops so that they no longer represent strongly fluctuating disturbance variables for the process model and assume almost constant, predetermined values.
  • the respective production volume is preferably preset to a value to be compatible with the desired pulp quality, in particular by specifying corresponding values for the speeds n1, n2 and n3 of the means ZS, TB and AS to maintain the mass flow through the cooker.
  • the process model i.e. with control laws dependent on the above process variables, the cooking temperature T in the interior of the continuous cooker is tracked as the main control variable.
  • the use of a process model, in particular stored in a program-controlled automation system for real-time management of technical processes, has the particular advantage that complex control laws that take into account a large number of influencing variables can be used for the process simulation.
  • Such tax laws generally do not represent a mathematically exact representation of the dynamic mode of operation of the technological process to be controlled Rather, it is usually an empirical relationship between the main process variables, found in particular through process observation.
  • the process model in the present process for pulp production thus links the quality measure Q * , the chemical concentration C, the degree of filler L, the production quantity and technology-dependent process constants to the control variable cooking temperature.
  • the measured variable of the speed n1 of the feed screw ZS in the wood chip feed lock ES can be used as a measure of the current production quantity. Furthermore, the measured quantity of the alkali level in the interior of the cooker can be used particularly advantageously for the current cooker fill level L.
  • a large number of process constants are preferably taken into account as "gain factors".
  • the first is the production constant a. This describes the relationship between the achievable production volume and the feed speed of the wood chips, which is particularly dependent on the mechanical engineering conditions of the system.
  • a second process constant is the activation energy E. This depends on the particular chemical digestion process, i.e. especially of the chemicals contained in the digestion solution.
  • the so-called impact factor k can also be taken into account. This represents a process speed constant which describes the gain factor between the achievable digestion speed on the one hand and the present cooking temperature and the chemical concentration on the other.
  • the three process constants above are just a selection. Particularly in the case of more extensive process models, and thus taking into account a large number of control laws, it is necessary to provide a larger number of process constants as gain factors.
  • the cooking temperature T * associated with a predetermined target value of the quality measure Q * is determined with the aid of the process model.
  • the process model M is preferably supplied with the actual values of the essential process parameters, for example the chemical concentration C, the production quantity n and the degree of filler L.
  • the model M is adapted to the current values of the respective process constants, for example the activation energy E, the production constant a and the impact factor k.
  • the process model M independently simulates, in the manner of a controller, the relationship between the preset value Q * for the desired size of the quality measure and the temperature setpoint T * acting on the cooker as a manipulated variable.
  • the determined value of the cooking temperature T * is preferably set by comparison with the current actual value T in an additional, subordinate temperature controller TR by means of direct intervention on the live steam supply FD.
  • Such a method according to the invention for pulp production is particularly applicable when the process model can be designed in such a way that it approximates the behavior of the stove for all possible working points, ie in the entire available control room, with sufficient accuracy.
  • the technological behavior of a ZK pulp cooker is strongly non-linear.
  • the process model M can only describe the relationship between the input variable Q * and the desired manipulated variable T * with sufficient accuracy in a section which is preferably in the middle of the overall working range. If the cooker is thus operated in an operating point lying outside this optimal range, the actual quality value Q of the pulp actually produced at the cooking temperature T specified by the model M may deviate considerably from the specified nominal value Q * .
  • a further control device for the quality measure which, in the event of deviations in the setpoint and actual value of the quality measure, tracks the cooking temperature in such a way that the deviation disappears as far as possible.
  • FIG. 3 shows a possible exemplary embodiment for this.
  • the control device QR forms a setpoint T * 1 for the subordinate temperature controller TR, which, after comparison with the actual temperature value T, processes it into an actuating signal for the live steam supply FD.
  • the cooking temperature setpoint T * formed by the process model M from the setpoint Q * is used for setting the operating point of the temperature controller TR.
  • the temperature controller is precontrolled as optimally as possible with the aid of the process model M, so that only slight deviations in the quality measure have to be compensated for with the aid of the control device QR.
  • a further possibility is shown by means of FIG. 4, in spite of the inventive determination of the cooking temperature setpoint T * with the aid of the process model M, to compensate for deviations between the setpoint and actual value of the quality measure.
  • an adaptation of the process model is preferably carried out cyclically and / or when very large deviations occur between the setpoint and actual value of the quality measure.
  • This is a new one in relation to the current working point of the pulp cooker Alignment of the process model, ie a new standardization.
  • At least one of the process constants of the process model is preferably redetermined with the aid of the same control laws as stored in the model and the actual value of the quality measure actually achieved at the current cooking temperature.
  • this represents an exact or sufficiently precise relationship between the process control variable Q and the control variable cooking temperature T, at least for a certain period of time and / or until strong operating point deviations occur when the pulp cooker is operating.
  • the process model M is thus expanded to an adaptable process model AM by means AD for model adaptation.
  • the adaptation values are preferably supplied with the actual values of the quality measure Q and the cooking temperature T. This updates at least one of the process constants at certain time intervals.
  • the production constant a, the activation energy E and the impact factor k are available for this. It has been found that the impact factor k is particularly well suited to be used to adapt the process model by constant updating.
  • the updated value of k is supplied to the model M by the adaptation means AD.
  • the yield Y of pulp produced can serve as a quality measure.
  • the actual value of the yield is preferably simulated at least with the aid of leaching analysis means.
  • a measuring point SA for specromic leaching analysis is shown as an example on the leaching discharge line LA.
  • the actual value of the yield can also be determined directly on the cellulose discharge line ZA following the discharge lock A.
  • the sizes pulp mass flow m Z and pulp consistency C Z are preferably determined.
  • the mass flow ⁇ A of the lye in the discharge line LA and the so-called dry content TS of the lye are preferably determined.
  • the dry matter content indicates the amount of extracted wood substance, in particular the lignin components, based on the amount of lye.
  • the dry content TS thus results
  • the actual value of the yield Y can be determined with the aid of an empirical equation which depends on quantities which are preferably obtained as measured values by analyzing the waste liquor removed from the cooker and analyzing the wood chip stream fed to the cooker. It follows With The measured variables Meß A , TS can be determined by leaching analysis, and ⁇ H , ⁇ by analysis of the wood chip mass flow supplied.
  • the actual value of the yield Y is thus dependent on the measured values of the hydraulic module X a and the dry content TS of the waste liquor.
  • the speed n of the means for supplying wood is available as a measured variable, then according to a third embodiment this value can also be used to simulate the actual yield value.
  • the wood feed means used are the feed screw ZS shown in the process image of FIG. 1 in the entry lock ES, the conveyor belt TB inside the cooker and the discharge screw AS in the discharge lock A at the end of the cooker. Since the speeds n1, n2, n3 of these three transport means are preferably adapted to one another via a speed profile, it is sufficient to use the speed n1 of the feed screw ZS as the speed n of the wood feed means. The production quantity is also affected via this size.
  • the yield is simulated with the aid of the speed n of the wood feed means, the dry content TS of the waste liquor and the mass flow ⁇ A of the waste liquor.
  • This relationship has the particular advantage that the G1. 7 and 9 still necessary analysis of the supplied wood chip mass flow is replaced by the much simpler use of the speed n of the wood feed means.
  • hydromodule X a is available as a measurement or calculation variable according to G1.
  • 9 is available for replication of the actual yield value, this is fed to the replication agent NQ as input variables together with the dry matter content TS of the waste liquor as shown in FIG. 6.
  • the speed n of the wood feed means is available as a measured variable and thus the actual yield value according to G1. 12 are simulated, so the illustration in FIG 7 are the replica agent NQ n sizes accordance with TS and m A as a measuring or calculation values supplied.
  • the yield Y can also serve as a quality measure for use as an input variable for the process model. If the lignin residue concentration in the manufactured pulp, referred to as the kappa number, is used for this purpose, the actual value of the lignin concentration can be determined by direct or indirect pulp analysis.

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EP90104231A 1990-03-05 1990-03-05 Procédé de fabrication de pâte dans un lessiveur en continu Expired - Lifetime EP0445321B1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
AT90104231T ATE106477T1 (de) 1990-03-05 1990-03-05 Verfahren zur herstellung von zellstoff in einem kontinuierlichen kocher.
DE59005944T DE59005944D1 (de) 1990-03-05 1990-03-05 Verfahren zur Herstellung von Zellstoff in einem kontinuierlichen Kocher.
EP90104231A EP0445321B1 (fr) 1990-03-05 1990-03-05 Procédé de fabrication de pâte dans un lessiveur en continu

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP90104231A EP0445321B1 (fr) 1990-03-05 1990-03-05 Procédé de fabrication de pâte dans un lessiveur en continu

Publications (2)

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EP0445321A1 true EP0445321A1 (fr) 1991-09-11
EP0445321B1 EP0445321B1 (fr) 1994-06-01

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AT (1) ATE106477T1 (fr)
DE (1) DE59005944D1 (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19510008A1 (de) * 1995-03-23 1996-09-26 Siemens Ag Verfahren und Vorrichtung zur Prozeßführung bei der Zellstoff- und/oder Papierherstellung
WO1999028548A1 (fr) * 1997-11-26 1999-06-10 Siemens Aktiengesellschaft Dispositif de commande pour lessiveur fonctionnant en continu pour la production de cellulose
DE19752442A1 (de) * 1997-11-26 1999-08-26 Siemens Ag Steuereinrichtung für einen kontinuierlich arbeitenden Kocher zur Herstellung von Zellstoff
EP0854953B1 (fr) * 1995-10-09 2000-02-09 Siemens Aktiengesellschaft Procede pour determiner la fin de cuisson de la cellulose et dispositif pour commander le temps de cuisson lors de la cuisson dans un reacteur
WO2002016690A1 (fr) * 2000-08-22 2002-02-28 Siemens Aktiengesellschaft Procede de controle de processus lors de la production de pate de cellulose
DE10350075A1 (de) * 2003-10-27 2005-06-09 Siemens Ag Verfahren und Vorrichtung zur Prozessführung bei der Zellstoffkochung
CN102094344A (zh) * 2010-12-08 2011-06-15 陕西科技大学 一种废纸碎解方法

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2714235C (fr) 2010-04-27 2014-01-07 Centre De Recherche Industrielle Du Quebec Procede et systeme pour stabiliser la densite seche des copeaux de bois devant alimenter un processus de raffinage des copeaux

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3322616A (en) * 1963-07-12 1967-05-30 Honeywell Inc Pulp digester control apparatus
US3941649A (en) * 1972-07-14 1976-03-02 Mo Och Domsjo Aktiebolag Process for obtaining a predetermined Kappa number in sulfate pulping
US4239590A (en) * 1979-01-11 1980-12-16 Kamyr, Inc. Method of maintaining uniformity of fibrous material fed to a continuous digester
EP0110683A1 (fr) * 1982-11-24 1984-06-13 The Babcock & Wilcox Company Détermination du degré de cuisson dans un digesteur au sulfite pour délignification
DE3525248A1 (de) * 1985-07-15 1987-01-15 Herbert Dr Ing Furumoto Verfahren zur steuerung und optimierung von reaktionen
DE3641785A1 (de) * 1986-03-31 1987-10-08 Wolfen Filmfab Veb Verfahren zur herstellung von zellstoff
DE3927183A1 (de) * 1988-08-17 1990-02-22 Kajaani Electronics Verfahren zur steuerung des alkalischen kochens von zellulosehaltigem material

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3322616A (en) * 1963-07-12 1967-05-30 Honeywell Inc Pulp digester control apparatus
US3941649A (en) * 1972-07-14 1976-03-02 Mo Och Domsjo Aktiebolag Process for obtaining a predetermined Kappa number in sulfate pulping
US4239590A (en) * 1979-01-11 1980-12-16 Kamyr, Inc. Method of maintaining uniformity of fibrous material fed to a continuous digester
EP0110683A1 (fr) * 1982-11-24 1984-06-13 The Babcock & Wilcox Company Détermination du degré de cuisson dans un digesteur au sulfite pour délignification
DE3525248A1 (de) * 1985-07-15 1987-01-15 Herbert Dr Ing Furumoto Verfahren zur steuerung und optimierung von reaktionen
DE3641785A1 (de) * 1986-03-31 1987-10-08 Wolfen Filmfab Veb Verfahren zur herstellung von zellstoff
DE3927183A1 (de) * 1988-08-17 1990-02-22 Kajaani Electronics Verfahren zur steuerung des alkalischen kochens von zellulosehaltigem material

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19510008A1 (de) * 1995-03-23 1996-09-26 Siemens Ag Verfahren und Vorrichtung zur Prozeßführung bei der Zellstoff- und/oder Papierherstellung
US6398914B1 (en) 1995-03-23 2002-06-04 Siemens Aktiengesellschaft Method and device for process control in cellulose and paper manufacture
EP0854953B1 (fr) * 1995-10-09 2000-02-09 Siemens Aktiengesellschaft Procede pour determiner la fin de cuisson de la cellulose et dispositif pour commander le temps de cuisson lors de la cuisson dans un reacteur
WO1999028548A1 (fr) * 1997-11-26 1999-06-10 Siemens Aktiengesellschaft Dispositif de commande pour lessiveur fonctionnant en continu pour la production de cellulose
DE19752442A1 (de) * 1997-11-26 1999-08-26 Siemens Ag Steuereinrichtung für einen kontinuierlich arbeitenden Kocher zur Herstellung von Zellstoff
DE19752442C2 (de) * 1997-11-26 2000-05-25 Siemens Ag Steuereinrichtung für einen kontinuierlich arbeitenden Kocher zur Herstellung von Zellstoff
WO2002016690A1 (fr) * 2000-08-22 2002-02-28 Siemens Aktiengesellschaft Procede de controle de processus lors de la production de pate de cellulose
DE10350075A1 (de) * 2003-10-27 2005-06-09 Siemens Ag Verfahren und Vorrichtung zur Prozessführung bei der Zellstoffkochung
CN102094344A (zh) * 2010-12-08 2011-06-15 陕西科技大学 一种废纸碎解方法
CN102094344B (zh) * 2010-12-08 2012-07-25 陕西科技大学 一种废纸碎解方法

Also Published As

Publication number Publication date
DE59005944D1 (de) 1994-07-07
ATE106477T1 (de) 1994-06-15
EP0445321B1 (fr) 1994-06-01

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