EP0947625A1 - Procédé et appareil de contrÔle et l'optimisation du procédé de la récupération des substances chimiques pendant la production de cellulose - Google Patents

Procédé et appareil de contrÔle et l'optimisation du procédé de la récupération des substances chimiques pendant la production de cellulose Download PDF

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Publication number
EP0947625A1
EP0947625A1 EP99105545A EP99105545A EP0947625A1 EP 0947625 A1 EP0947625 A1 EP 0947625A1 EP 99105545 A EP99105545 A EP 99105545A EP 99105545 A EP99105545 A EP 99105545A EP 0947625 A1 EP0947625 A1 EP 0947625A1
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EP
European Patent Office
Prior art keywords
chemical
model
spectra
parameters
pcn
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Granted
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EP99105545A
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German (de)
English (en)
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EP0947625B1 (fr
Inventor
Herbert Dr. Furumoto
Andreas Dr. Kemna
Uwe Dr. Lampe
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Siemens AG
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Siemens AG
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    • 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
    • D21C7/00—Digesters
    • D21C7/12—Devices for regulating or controlling
    • 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
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters

Definitions

  • the invention relates to a process control method and for process optimization of chemical recovery using in the manufacture of pulp at least one state model and / or process model.
  • the invention relates to a device for Execution of the procedure.
  • pulping is done by boiling wood chips using appropriate cooking chemicals either in in a continuous or in a discontinuous process.
  • the cellulose boiling with sulfate or sulfite exclusion usually a recovery process for the Cooking chemicals.
  • the process control in the recovery of the cooking chemicals is difficult because important quality parameters of the cooking chemicals - for example, in the case of sulfate digestion, the active alkali concentration, sulfidity, sulfate content, sulfur content, Na 2 S, Na 2 SO 4 , Na 2 CO 3 , Na 2 O, CaO, NaOH, NaCl, K 2 CO 3 , CaCO 3 , Ca (OH) 2 and for sulfite digestion, for example, the chemicals SO 2 , HSO 3 - , SO 3 - , S 2 O 3 - , SO 4 - , MgO , Active MgO, burnt MgO - only be measured in the laboratory with a time delay. For this reason, an interim faulty production cannot be excluded. In order to avoid the risk of incorrect production, the production process is therefore usually operated with a greater margin of safety with regard to the quality of the cooking chemicals than would actually be necessary.
  • DE 195 10 009 A1 discloses a method for the process control of a paper machine. Selected spectral parameters are used for the measurement of product quality parameters. Neural networks that have been trained on the product parameters measured in the laboratory are used specifically for process control in the headbox of a paper machine. Furthermore, DE 195 10 008 A1 discloses a process control process in pulp and paper production in which spectral parameters of different wavelengths are derived for determining the starting materials and for evaluating the quality of the raw materials. Correction signals for the system-related regulating or control devices are also to be determined, in particular with neural networks. With this method, the measurement signal is recorded directly on the raw material Wood ", such as wood chips or wood fibers, or directly on the raw material Waste paper ".
  • DE 36 16 051 A1 discloses a method for controlling the digestion of lignocelluloses using FTIR spectroscopy. By measuring in the MIR (M ittleren I nf r arot) range of Restligninanteil and the concentration of the cooking chemicals is determined, for example, the content of free SO 2 in the sulphite cooking.
  • MIR M ittleren I nf r arot
  • an incinerator is from DE 42 21 404 A1 for the waste liquor of a pulp cooker with a control device known for the combustion air at which the amount at the temperature of a waste liquor atomized in the system Dependency on a measure of the ash quality like this takes place that the combustion products of the waste liquor as far as possible large amounts of hydratable starting materials for the Recovery of digestion chemicals included.
  • the task is in a method of the aforementioned Art according to the invention with the features of claim 1 solved, with advantageous developments in the dependent Claims are specified.
  • the associated device is in single property claim specified.
  • the method with acquisition of the continuous spectra can alternatively be used for the sulfite or sulfate process.
  • spectroscopic measurements are carried out specifically on the chemical streams of the recovery system, ie in the sulfate digestion, for example on the soda melt after the recovery kettle, in the green, white and black liquor, and in the sulfite digestion, for example in the ash stream or on the ash or in the cooking liquids, carried out.
  • absorption, emission and / or luminescence spectroscopy in the spectral range from 0.1 ⁇ m to 400 ⁇ m, preferably between 0.4 ⁇ m and 100 ⁇ m, can advantageously be used.
  • the continuous spectra are evaluated with suitable calculation methods and allow a statement about the expected chemical composition of the cooking liquid.
  • the process can be intervened to regulate, for example by changing the air distribution in the recovery boiler, the CaO supply in the so-called caustifier, by adding so-called Make-up chemicals and by regulating the mixing ratio of black liquor, white liquor and dilution water.
  • the improved chemical recovery is special advantageous for pulp production with a smoothing the quality of the cooking liquid on high Level. This will increase the yield and production volume, a reduction in chemicals and / or Use of energy as well as the saving of auxiliary materials in the bleaching stage following the pulp production reached.
  • the invention is compared to the state stated at the outset the technology in essential points, such as in particular Measurement site, the measurement method, the processing of the spectra and the Modeling, further developed.
  • Raman spectra can also be measured in addition to absorption, emission or luminescence spectra.
  • the excitation for luminescence can take place, for example, through the irradiation of electromagnetic radiation, for example UV radiation, or through a specific chemical reaction such as chemiluminescence; on the other hand, the emission is excited, for example, by irradiation with electrons.
  • FTIR Fourier transform infrared spectroscopy
  • the state models for calculating the quality parameters can with a sufficiently large number of data based of neural networks, fuzzy systems, multilinear regression models or combinations thereof.
  • Alternative to purely data-driven models are also Combined models possible, where additional analytical Knowledge is brought in.
  • process models can also be constructed using the same means become.
  • a model validity check integrated in the spectrum preprocessing ( Novelty detection ) according to the older, unpublished DE 196 322 45 A1 can indicate the need for a new training phase in good time in the ongoing process.
  • FIG 1 the structure of a continuously working Chemical preparation shown, in the present Connection the measuring point scheme is clarified.
  • a well-known stove for the production of pulp by cooking raw materials, especially in the form of Wood chips, in a suitable cooking liquid.
  • At 11 is the inlet for the wood in the stove 10, with 12 the feed line for the cooking liquid and with 13 designated the outlet for the finished pulp.
  • the cooker 10 close a blow tank 14 and several washers 15, 15 ', 15' 'with assigned filtrate tanks 16, 16', 16 ''. From The finished pulp is output to the washer.
  • the filtrate is passed through at least one unit 17, advantageously units 17, 17 ', 17'', ... for multi-stage evaporation, into a so-called black liquor tank 18 and from there into a recovery tank 20 for cooking chemicals.
  • the recovery boiler 20 the non-recyclable waste liquors, referred to as black liquor, are to be burned and the recyclable cooking chemicals are to be recovered.
  • the fly ash is removed via an electric filter 21.
  • the soda melt accumulating at the bottom of the recovery boiler 20 flows into a melt-dissolving tank 22. This is followed by a green liquor clarifying tank 23 and a causticizing system in which chemical conversion reactions for the extraction of caustic take place.
  • This system essentially consists of an extinguishing tank 24, several individual caustifiers 25, 25 ', 25'', a white liquor clear tank 26 and a cooking liquor tank 27.
  • the system for caustification is assigned a scrubber 28 with filter 29 and a lime kiln 30. The lime burned there is returned to the extinguishing tank 24.
  • the mode of operation of the staggered caustifiers 25, 25 ', 25''and25''' is clear from the partial illustration according to FIG.
  • the measured spectra are processed by signal preprocessing smoothed and standardized. Then a disassembly in the main components and / or the identification more important Peaks occur. From the main components you can then with models, e.g. using methods of multilinear regression, the concentrations of the following quantities are calculated: Effective alkali, sulfidity, carbonate, sulfate and thiosulfate.
  • a regulatory intervention is at various points in the Recovery process conceivable, e.g. by replenishing Chemicals, by temperature variations or by Changes in the Circulations.
  • 31 characterizes the course of an IR spectrum of cooking liquid in the wavenumber range 1500 to 900 cm ⁇ 1 .
  • measurements can also be carried out in other wavenumber ranges.
  • the chemical concentrations describing the chemical recovery process are in particular the active alkali concentration, the sulfidity, the sulfate content and the content of Na 2 S, Na 2 CO 3 and NaOH used.
  • the MgO Concentration divided into so-called burnt MgO and active MgO.
  • 40A and 40B each represent a relevant state model of the cooking chemicals, from which their properties, such as the concentration, are calculated.
  • the essential quality parameters for the cooking liquid to be prepared can be derived from this.
  • PCA principal component analysis
  • PLS PLS method
  • the state model 40A or 40B can but possibly alone from the continuous spectra determined parameters PC1 to PCn are formed.
  • the model 40A or 40B can e.g. advantageously by a neural network should be formed.
  • a neural network should be formed.
  • Figure 6 is a process model for chemical recovery designated by the sulfate process at 50. Entered are discrete physical and chemical properties, e.g. Temperature, pH and Pressure and the state variables of the cooking liquid as an output of the state models, for example according to FIGS. 4 or 5.
  • the process models can also be used only with those from the Characteristics determined continuous spectra formed become.
  • a corresponding process model 60 is special in FIG specified for the sulfite process. Unless discrete physical and / or chemical properties are used in addition to the optical spectrum, for example the flows and / or temperatures are given, which is shown in Figure 6. The pH value during sulfite digestion can be entered.
  • the process model according to FIG. 6 can also be used as dynamic process model 70 can be designed.
  • the input variables are here according to the input variables in FIG. 6 in each case at discrete times k, ..., (k-n). The same applies to the chemical concentration.
  • Out of it Dynamic process model 70 determines the chemical concentration at future times (k + 1.
  • FIG. 9 Process generally designated 80, which is the current Process state based on the spectra with 81 results.
  • the process model is denoted here by 82, from which the data is converted into a Unit to be given to cost function 83, the same time with data for costs and prices from unit 84 is applied.
  • An optimizer 85 determines the Actuating variables 86, which are fed back into the process model 82 and continue to be the optimal manipulated variables 87 for process control. These can also be switched via a switch 88 Plant operators can be switched through.
  • a unit 91 for Pre-processing and compression for the spectra of the entire spectrum 90 serves, from which e.g. the parameters PC 1 to PC 10 are calculated.
  • the main component analysis used for this is from a suitable number of spectra, for example between three and ten spectra, so-called scores, for the purpose of data reduction educated. From this, the input variables PC1, ..., PCn in particular of the model calculated according to FIG. 4.
  • the parameters PC1 to PCn flow into the state model 93 and in the process model 94, whereby here additionally discrete physical and / or chemical properties and the process description the state model for Complement the process model. From the state model 93, the product properties the cooking chemicals and from the process model 94 derived the product properties of the cooking liquid. Now all chemical additives can be calculated and in Optimized to achieve the desired cost savings.
  • Figure 12 shows how with appropriate evaluation and optimization software using a computer that the computer 105 from Figure 1 can be intervened in an existing process control system becomes.
  • Optimized manipulated variables can be generated a known automation device 100 as a process control system charge that with the actual system for Implementation of the process interacts.
  • the existing chemical recovery facilities through several spectrometers 101 to 103 and an associated, optimization program implemented as software, that runs on the computer 105, added.

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EP19990105545 1998-03-31 1999-03-18 Procédé et appareil pour le contrôle et l'optimisation du procédé de la récupération des substances chimiques pendant la production de cellulose Expired - Lifetime EP0947625B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE1998114385 DE19814385C1 (de) 1998-03-31 1998-03-31 Verfahren und Vorrichtung zur Prozeßführung und zur Prozeßoptimierung der Chemikalienrückgewinnung bei der Herstellung von Zellstoff
DE19814385 1998-03-31

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EP0947625A1 true EP0947625A1 (fr) 1999-10-06
EP0947625B1 EP0947625B1 (fr) 2014-08-13

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001059437A1 (fr) * 2000-02-07 2001-08-16 Alberta Research Council Inc. Determination des proprietes d'une solution ou d'un solide par l'application des rapports raman
US6774992B1 (en) 1997-03-10 2004-08-10 Alberta Research Council Inc. Determination of the property of a solution or solid using raman ratios
WO2009139714A1 (fr) 2008-05-13 2009-11-19 Soottech Aktiebolag Procédé pour la mesure de conditions dans un four de chaudière de production d'énergie utilisant un souffleur de suie
WO2010128354A1 (fr) * 2009-05-06 2010-11-11 Abb Research Ltd Procédé et système d'optimisation en ligne d'un digesteur discontinu de pâte à papier
WO2020234511A1 (fr) * 2019-05-17 2020-11-26 Andritz Oy Détermination du taux de réduction d'une chaudière de récupération
CN116859830A (zh) * 2023-03-27 2023-10-10 福建天甫电子材料有限公司 用于电子级氟化铵生产的生产管理控制系统

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10126251A1 (de) * 2001-05-29 2003-01-23 Buehler Ag Online-Prozessüberwachung und Online-Prozessmodelierung
US7149649B2 (en) 2001-06-08 2006-12-12 Panoratio Database Images Gmbh Statistical models for improving the performance of database operations
DE102007036383A1 (de) * 2007-07-31 2009-02-05 Voith Patent Gmbh Verfahren zum Steuern der Aufschlussdauer eines Sulfitaufschlusses für Hochausbeute-Faserstoffe
DE102012202111A1 (de) * 2012-02-13 2013-08-14 Krones Ag Verfahren zur Steuerung und/oder Regelung von Filteranlagen zur Ultrafiltration

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WO1984004552A1 (fr) * 1983-05-18 1984-11-22 Weyerhaeuser Co Analyseur de carbonate/sulfure et procede de regulation
US4536253A (en) * 1981-09-25 1985-08-20 Kemotron A/S Process for controlling the properties of white liquor
EP0210745A2 (fr) 1985-07-22 1987-02-04 Avondale Industries, Inc. Dispositif pour détacher automatiquement des barres de transfert d'une presse transfert
DE4221404A1 (de) * 1991-07-02 1993-01-14 Siemens Ag Verbrennungsanlage fuer die ablauge eines zellstoffkochers mit einer regeleinrichtung fuer die verbrennungsluft
DE3233428C1 (de) 1982-09-09 1993-04-29 Maschinenfabrik Müller-Weingarten AG, 7987 Weingarten Beschickungs- und Entnahmevorrichtung insbesondere an Pressen
JPH05321183A (ja) * 1992-05-18 1993-12-07 Toshiba Corp 回収ボイラの燃焼制御装置
US5364502A (en) * 1992-07-08 1994-11-15 Pulp & Paper Research Institute Of Canada Control of recovery boiler operation by IR spectroscopy
DE4408447A1 (de) 1994-03-12 1995-09-14 Mueller Weingarten Maschf Transporteinrichtung
EP0672480A1 (fr) 1994-03-12 1995-09-20 Maschinenfabrik Müller-Weingarten AG Système de transport
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US5616214A (en) * 1995-09-12 1997-04-01 Pulp And Paper Research Institute Of Canada Determination of sodium sulfide and sulfidity in green liquors and smelt solutions
WO1998010137A1 (fr) * 1996-09-03 1998-03-12 Fisher-Rosemount Systems, Inc. Procede et appareil pour controler l'efficacite d'un processus de caustification
EP0847818A1 (fr) 1996-12-14 1998-06-17 Müller Weingarten AG Presse de transfert

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DE3504486A1 (de) * 1985-02-09 1986-08-14 Oskar Dipl.-Holzw. Dr. 2057 Reinbek Faix Verfahren zur kontrolle des sulfitaufschlusses von lignocellulosen mit hilfe der ftir-spektroskopie
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US4536253A (en) * 1981-09-25 1985-08-20 Kemotron A/S Process for controlling the properties of white liquor
DE3233428C1 (de) 1982-09-09 1993-04-29 Maschinenfabrik Müller-Weingarten AG, 7987 Weingarten Beschickungs- und Entnahmevorrichtung insbesondere an Pressen
WO1984004552A1 (fr) * 1983-05-18 1984-11-22 Weyerhaeuser Co Analyseur de carbonate/sulfure et procede de regulation
EP0210745A2 (fr) 1985-07-22 1987-02-04 Avondale Industries, Inc. Dispositif pour détacher automatiquement des barres de transfert d'une presse transfert
DE4221404A1 (de) * 1991-07-02 1993-01-14 Siemens Ag Verbrennungsanlage fuer die ablauge eines zellstoffkochers mit einer regeleinrichtung fuer die verbrennungsluft
JPH05321183A (ja) * 1992-05-18 1993-12-07 Toshiba Corp 回収ボイラの燃焼制御装置
US5364502A (en) * 1992-07-08 1994-11-15 Pulp & Paper Research Institute Of Canada Control of recovery boiler operation by IR spectroscopy
US5378320A (en) * 1992-07-08 1995-01-03 Pulp & Paper Research Institute Of Canada Control of recausticizing system operation by IR spectroscopys
DE4408447A1 (de) 1994-03-12 1995-09-14 Mueller Weingarten Maschf Transporteinrichtung
EP0672480A1 (fr) 1994-03-12 1995-09-20 Maschinenfabrik Müller-Weingarten AG Système de transport
EP0693334A1 (fr) 1994-06-16 1996-01-24 Maschinenfabrik Müller-Weingarten Ag Système de transport
DE19510008A1 (de) * 1995-03-23 1996-09-26 Siemens Ag Verfahren und Vorrichtung zur Prozeßführung bei der Zellstoff- und/oder Papierherstellung
US5616214A (en) * 1995-09-12 1997-04-01 Pulp And Paper Research Institute Of Canada Determination of sodium sulfide and sulfidity in green liquors and smelt solutions
WO1998010137A1 (fr) * 1996-09-03 1998-03-12 Fisher-Rosemount Systems, Inc. Procede et appareil pour controler l'efficacite d'un processus de caustification
EP0847818A1 (fr) 1996-12-14 1998-06-17 Müller Weingarten AG Presse de transfert

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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6774992B1 (en) 1997-03-10 2004-08-10 Alberta Research Council Inc. Determination of the property of a solution or solid using raman ratios
WO2001059437A1 (fr) * 2000-02-07 2001-08-16 Alberta Research Council Inc. Determination des proprietes d'une solution ou d'un solide par l'application des rapports raman
WO2009139714A1 (fr) 2008-05-13 2009-11-19 Soottech Aktiebolag Procédé pour la mesure de conditions dans un four de chaudière de production d'énergie utilisant un souffleur de suie
US8584540B2 (en) 2008-05-13 2013-11-19 Soottech Aktiebolag Method for measuring conditions in a power boiler furnace using a sootblower
WO2010128354A1 (fr) * 2009-05-06 2010-11-11 Abb Research Ltd Procédé et système d'optimisation en ligne d'un digesteur discontinu de pâte à papier
WO2020234511A1 (fr) * 2019-05-17 2020-11-26 Andritz Oy Détermination du taux de réduction d'une chaudière de récupération
CN116859830A (zh) * 2023-03-27 2023-10-10 福建天甫电子材料有限公司 用于电子级氟化铵生产的生产管理控制系统
CN116859830B (zh) * 2023-03-27 2024-01-26 福建天甫电子材料有限公司 用于电子级氟化铵生产的生产管理控制系统

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Publication number Publication date
DE19814385C1 (de) 1999-10-07
EP0947625B1 (fr) 2014-08-13

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