EP0426652A1 - Procédé exempt de chlore pour le blanchiment de pâtes cellulosiques - Google Patents

Procédé exempt de chlore pour le blanchiment de pâtes cellulosiques Download PDF

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Publication number
EP0426652A1
EP0426652A1 EP90890291A EP90890291A EP0426652A1 EP 0426652 A1 EP0426652 A1 EP 0426652A1 EP 90890291 A EP90890291 A EP 90890291A EP 90890291 A EP90890291 A EP 90890291A EP 0426652 A1 EP0426652 A1 EP 0426652A1
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Prior art keywords
ozone
pulp
mass
bleaching
containing gas
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Granted
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EP90890291A
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German (de)
English (en)
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EP0426652B1 (fr
EP0426652B2 (fr
Inventor
Wilfried Rückl
Walter Dr. Dipl.-Ing. Peter
Friedrich Kurz
Alfred Schrittwieser
Manfred Schneeweisz
Herbert Sixta
Gerhard Götzinger
Anton Höglinger
Peter Hendel
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Lenzing AG
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Lenzing AG
Chemiefaser Lenzing AG
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Priority claimed from AT0249489A external-priority patent/AT404740B/de
Application filed by Lenzing AG, Chemiefaser Lenzing AG filed Critical Lenzing AG
Publication of EP0426652A1 publication Critical patent/EP0426652A1/fr
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    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21H—PULP COMPOSITIONS; PREPARATION THEREOF NOT COVERED BY SUBCLASSES D21C OR D21D; IMPREGNATING OR COATING OF PAPER; TREATMENT OF FINISHED PAPER NOT COVERED BY CLASS B31 OR SUBCLASS D21G; PAPER NOT OTHERWISE PROVIDED FOR
    • D21H17/00—Non-fibrous material added to the pulp, characterised by its constitution; Paper-impregnating material characterised by its constitution
    • 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
    • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
    • D21C9/10—Bleaching ; Apparatus therefor
    • D21C9/147—Bleaching ; Apparatus therefor with oxygen or its allotropic modifications
    • D21C9/153—Bleaching ; Apparatus therefor with oxygen or its allotropic modifications with ozone

Definitions

  • the invention relates to a method for bleaching pulps, in particular synthetic fiber pulps, for. Hardwood pulps with starting cap values of 15-1, preferably 4-1, or paper pulps, e.g. Softwood pulp, with initial cap values up to 30, preferably up to 10, using ozone, in which a pulp suspension is at a temperature of 15-80 ° C, preferably 40-70 ° C, and at a pH of 1-8, preferably 2-3 , is brought into contact with an ozone-containing gas with vigorous stirring or mixing, the ozone-containing gas containing 20-300 g / m3, preferably 50-150 g / m3, of ozone and at most 2% by mass, preferably 0.05-0 , 5 mass%, ozone, based on dry cellulose, is used.
  • ozone in which a pulp suspension is at a temperature of 15-80 ° C, preferably 40-70 ° C, and at a pH of 1-8, preferably 2-3 , is brought into contact with an o
  • HC high consistency
  • LC low consistency
  • HC ozone bleaching is carried out at consistencies above 25%, generally 35 - 40%.
  • a method of the type mentioned is known from US Pat. No. 4,080,249.
  • the stirring energy is preferably at most 18 kWh / t cellulose suspension.
  • the size of the bubbles of the ozone-containing gas should not exceed 3 mm.
  • material densities between 1 and 2% are described in all examples, so it is clearly an LC method.
  • the object of the invention is to use the method mentioned at the beginning in the medium consistency range (MC), and of course good results are to be achieved in comparison with LC technology.
  • the pulp suspension has a consistency of 3-20% by mass, preferably 5-20% by mass, in particular 7-15% by mass, and in that the ozone-containing gas contains a Pressure of 1-15 bar, preferably 1.1-10 bar, is introduced into the pulp suspension.
  • the medium consistency range offers the advantage that the reaction vessels can be made smaller in comparison to the LC technology, but that on the other hand no expensive dewatering devices like the HC technology are necessary.
  • the required mixing energy is lower than with LC.
  • the reaction of the ozone with the pulp is more homogeneous than with HC.
  • the cellulose damage - measured by the viscosity and the DP distribution - even at very low kappa values - is significantly less than with HC and at least comparable to LC.
  • the specific ozone consumption (O3 consumption per eliminated kappa point) is significantly lower than with LC.
  • Existing systems are relatively easy to convert: apart from pH-controlled acidification (which would also be required for LC and HC), only an investment in an MC pump and an MC mixer is required. Waste water recirculation and reuse of the reaction waste gases with a residual ozone content is possible, so that the process is environmentally friendly Lich works. Overall, the process is very economical (required mixing energy, amount of ozone used and necessary devices).
  • a further advantage is obtained if the method according to the invention is used as an ozone stage in a multi-stage bleaching process. Because most stages that do not use ozone bleaching (e.g. oxygen bleaching) mostly work in the MC range, the pulp consistency no longer needs to be changed between the individual stages, so that the overall process becomes more economical.
  • ozone bleaching e.g. oxygen bleaching
  • MC pulp can also be successfully treated directly with an ozone-containing gas, provided that this gas is under pressure and at the same time is stirred or mixed vigorously. This eliminates the need to dilute and dewater the pulp suspension as provided for in AT-PS 380 496 (see page 3, lines 19-20 and 35-36).
  • the volume ratio gas: liquid is 1: 0.5-1: 8, preferably 1: 1-1: 6.
  • Cooled compressors preferably water ring pumps, are preferably used to compress the ozone-containing gas.
  • a high-shear mixer is preferably used for vigorous stirring or mixing.
  • High-shear mixers are known and are currently used for a wide variety of applications, for example for the production of dispersions for paints (DE-A 24 06 430) position of PVC resin powder (US-A 3 775 359) and for the production of semi-solid emulsions (US-A-3 635 834). It is also known to use them for cellulose suspensions (JP-A 6 309 9389).
  • a high-shear mixer has plates with elevations that are spaced a certain distance apart. This means that there is no grinding, but an intimate mixing.
  • the process is carried out several times in succession, with an alkaline extraction being carried out in between if necessary.
  • the alkaline extraction can be carried out using oxygen or peroxide. In practice, this multiple procedure can be ensured simply by removing part of the pulp behind the reactor and feeding it back to the high-shear mixer, so that a cycle results.
  • the process is carried out after an oxygen and / or peroxide-enhanced extraction, optionally followed by an alkaline peroxide stage, and / or that a peroxide stage or an alkaline extraction follows.
  • Oxygen can also be used in the peroxide stage.
  • the wastewater filtrate obtained in the treatment with ozone is at least partially supplied to the pulp suspension before it is brought into contact with the ozone-containing gas, the acid required for the desired pH value also being present together with the wastewater filtrate. especially sulfuric acid. Since the wastewater filtrate is acidic, acid can be saved in this way; at the same time the wastewater filtrate is put to good use, so that it does not have to be disposed of or discharged in an environmentally harmful manner.
  • hardwood pulps with initial kappa values of 15 to 1 or from 4 to 1 are subjected to the process according to the invention, kappa values of 12 to 0.5 or 1.5 to 0.5 are achieved.
  • An initial whiteness of 50-80% or 70-80% is increased to at least 65-90% or 75-90%.
  • the molecular weight distribution of synthetic fiber pulps can be determined.
  • the viscosity, DP distribution and reactivity required for the further use of the pulps, measured on the filter value are obtained.
  • FIGS. 1a and 1b show systems which are suitable for carrying out the method according to the invention.
  • pulp feed for ozone bleaching from one of the preceding bleaching stages, such as oxygen and / or peroxide bleaching, with subsequent alkaline extraction.
  • Acidic wastewater filtrate 14 which is obtained at the end of the ozone bleaching stage, is added to the pulp suspension in order to adjust the consistency and to use the residual acid content.
  • a pH-regulating acid addition 2 is carried out, which defines the pH.
  • the pulp suspension is conveyed by an MC pump 3 into an MC mixer 4, which is preferably a high-shear mixer.
  • Gas 7 containing ozone is compressed in a compressor 8 and introduced into the MC mixer 4 under pressure. An intimate, rapid mixing of the suspension and the ozone-containing gas 7 takes place in the MC mixer 4.
  • reaction tube 5 a reactor which is designed as a reaction tube 5.
  • a return 9 in the form of a tube and a pump
  • the pulp suspension is provided in order to subject the pulp suspension to the process according to the invention several times if necessary.
  • FIGS. 1a and 1b The incorporation of the fumigated stock suspension in conventional bleaching towers 10 is shown in FIGS. 1a and 1b. According to the invention, this is not absolutely necessary.
  • the pressurized gas stock suspension with or without throttle 6 is conveyed into the bleaching tower 10, where a subsequent reaction can still take place.
  • the pressure has been released in the area of the material discharge, and the exhaust gas is discharged via an exhaust gas disposal 11.
  • the relaxed pulp suspension is mixed with dilution water 12 and discharged from the bleaching tower 10 to the washing filter 13.
  • the resulting waste water filtrate 14 is fed to the pulp feed 1 via a waste water return line 15.
  • the gassed material suspension coming from the reaction tube 5 is thrown over the throttle 6 passed and then expanded to atmospheric pressure in a degassing device 16.
  • the material is discharged into the bleaching tower 10 also by adding dilution water 12.
  • the low-ozone exhaust gas is also conducted via an exhaust gas disposal system, for example a catalytic or thermal ozone destruction device.
  • the oxygen produced in the waste gas disposal 11 can be used in an oxygen bleaching stage and the excess oxygen can be returned to the ozone generator after corresponding cleaning steps. If the oxygen is not used in an oxygen bleaching stage, it can be completely recycled after the necessary cleaning steps.
  • Waste water and exhaust gas recirculation can also save a lot of energy, especially at high process temperatures.
  • the residence time of the pulp suspension in the reaction tube 5 and in the bleach tube 10 is in any case less than 3 h, normally less than 1 h, preferably even less than 5 min.
  • a beech synthetic fiber pulp or spruce paper pulp is subjected to ozone bleaching according to the invention after conventional oxygen extraction reinforced with peroxide.
  • the bleached pulp has the following key figures: Kappa: 0.9 delta kappa: 1.85 O3 consumption / delta kappa: 0.91 White: 83.5% delta white: 7.5% Viscosity: 214 mP delta viscosity: 41 mP
  • the bleached pulp has the following key figures: Kappa: 1.25 delta kappa: 1.65 O3 consumption / delta kappa: 0.95 White: 82.5% delta white: 6.5 Viscosity: 227 mP delta viscosity: 28 mP
  • the pulp has the following key figures: Kappa: 1.9 Viscosity:. 255 mP Whiteness: 76%
  • the bleached pulp has the following key figures: Kappa: 1.1 delta kappa: 0.9 O3 consumption / delta kappa: 1.25 White: 82.0% delta white: 6.0% Viscosity: 218 mP delta viscosity: 37 mP
  • Example 3 The same pulp as in Example 3 is subjected to ozone bleaching with the following parameters: Pressure: 5.0 bar Fabric density: 10.7% Temperature: 23 ° C pH: 2.5 spec. O3 insert: 1.6 g / kg spec. O3 consumption: 1.2 g / kg Response time: 120 s Mixing time: 120 s Ozone concentration in fresh gas: 83.2 mg / Nl Ozone concentration in the exhaust gas: 21 mg / Nl V g / V l : 1: 2.6 (at 5 bar) Speed of the high-shear mixer: 3200 / min
  • the bleached pulp has the following key figures: Kappa: 0.60 delta kappa: 1.3 O3consumption / delta kappa: 0.91 Whites: 86.3% delta white: 10.3% Viscosity: 228 mP delta viscosity: 27 mP
  • Examples 5 and 6 below relate to spruce paper sulfite pulps.
  • the raw material had the following key figures: Kappa (Tappi 236 os-76): April 20 Viscosity: 1500 mPa s ⁇ 10 Whiteness (Elrepho): 49.7% Rip length (24 ° SR): 8900 m Rip length (41 ° SR): 9200 m WRA (24 ° SR): 1143 mNm / m WRA (41 ° SR): 1010 mNm / m Burst strength (24 ° SR): 4.4 kg / cm2 Burst strength (41 ° SR): 4.2 kg / cm2
  • EOP-Z1-PE1-Z2-PE2 EOP-Z1-PE1-Z2-PE2
  • EOP alkaline oxygen treatment reinforced with peroxide
  • Z ozone treatment
  • PE alkaline peroxide treatment
  • H2O2 insert 2.0% dry fabric
  • O2 insert 2 bar
  • Fabric density 10% Residence time: 3 h
  • Temperature: 80 ° C The following pulp parameters were obtained: Kappa: 6.6 Whiteness: 75.5%
  • WRA 810 mNm / m (24 ° SR); 1057 mNm / m (37 ° SR) Burst strength: 3.3 kg / cm2 (24 ° SR); 3.5
  • ozone level - 1 Z1
  • the parameters of the first ozone bleaching and the characteristics of the pulp after the first ozone bleaching were as follows: parameter V1 V2 V3 Fabric density (%) 8.5 8.2 9 Pressure (bar) 5.6 5.6 5.6 Temperature (° C) 20th 31 44 PH value 2.5 2.5 2.5 2.5 Mixing time (s) 15 15 15 Response time (s) 120 120 120 Speed (/ min) 3200 3200 1500 spec. Use of ozone (kg / t) 1.85 1.78 1.94 spec.
  • Viscosity (mPas10) 679 581 631 e) PE2 level The parameters of the second alkaline peroxide treatment and the characteristics of the pulp after the treatment were as follows: parameter V1 V2 V3 NaOH use (%, based on dry cellulose) 0.7 0.7 0.7 H2O2 use (%, based on dry cellulose) 0.5 0.5 0.5 0.5 Fabric density (%) 10th 10th 10th Temperature (° C) 65 65 65 65 Kappa 0.6 0.6 0.6 Whiteness (%) 90.6 90.0 90.0 Viscosity (mPas10) 650 583 577 Tear length (° SR) m 7600 (20) 7900 (21) 7500 (20) (° SR) m 8000 (34) 8200 (36) 8000
  • Example 5 The same raw material as in Example 5 (spruce paper sulfite pulp) was subjected to the bleaching sequence EOP-Z-PE for lower demands on the degree of whiteness.
  • the conditions (V4, V5) of the final bleaching (PE) were varied with the aim of achieving whiteness greater than 85% with the highest possible strength values.
  • the EOP bleaching was carried out as in Example 5.
  • ozone bleaching Z
  • the parameters of ozone bleaching and the characteristics of the pulp after ozone bleaching were as follows: parameter Fabric density (%) 12 Pressure (bar) 6.2 Temperature (° C) 24th PH value 2.5 Mixing time (s) 15 Response time (s) 120 MC mixer speed (/ min) 1700 specific use of ozone (kg / t) 2.62 specific ozone consumption (kg / t) 2.37 V1 / V g 2.56 Kappa 3.7 delta kappa / O3 consumption 1.22 Viscosity (mPas10) 771 Whiteness (%) 75.7 c) PE level
  • parameter V4 V5 NaOH use %, based on dry cellulose
  • 2.5 2.5 H2O2 use %, based on dry cellulose
  • the strength values of the three-stage bleached cellulose essentially correspond to that of the five-stage bleached cellulose. This is an indication that the strength properties of the cellulose are not impaired when sequentially using small specific amounts of ozone, but very high degrees of whiteness can nevertheless be achieved.
  • a spruce kraft pulp was subjected to two different bleaching sequences according to the invention after conventional oxygen extraction.
  • the pulp had the following key figures: Kappa: 16 White: 37.7 Tear length: 10.5 km (17 ° SR) 10.7 km (21 ° SR) WRA: 1666 mNm / m (17 ° SR) 1620 mNm / m (21 ° SR) Relative initial strength: 7.42 kPam2 / g (17 ° SR) 7.13 kPam2 / g (21 ° SR)
  • the pulp had the following properties: parameter Z1-EO-Z2-P Z1-EOP-Z2-P according to Z1 Kappa 12 12 White 41 41 before Z2 Kappa 7 6 White 62 65 according to Z2 Kappa 4th 3.5 White 78 80 after P (fully bleached) White 85 87 Tearing length (km) 9.8 (15 ° SR) 9.7 (15 ° SR) 10.9 (23 ° SR) 10.6 (22 ° SR) Relative initial strength (kPa m2 / g) 7.0 (15 ° SR) 7.4 (15 ° SR) 7.5 (23 ° SR) 7.6 (22 ° SR) WRA (mNm / m) 1816 (15 ° SR) 1780 (15 ° SR) 1580 (23 ° SR) 1610 (22 ° SR)
  • the process conditions of the Z1 stage, the EO stage and the Z2 stage were identical to those of Example 7.
  • the reaction conditions of the D stage were as follows: Fabric density: 10 - 12% Temperature: 70 ° C Active chlorine: 1%
  • the pulp had the following properties: parameter Z1-EO-Z2-D according to Z1 Kappa 12 White 41 before Z2 Kappa 7 White 62 according to Z2 Kappa 4th White 78 to D (fully bleached) White 89 Tearing length (km) 9.8 (15 ° SR) 11.0 (24 ° SR) Relative initial strength (kPa m2 / g) 7.2 (15 ° SR) 7.5 (24 ° SR) WRA (mNm / m) 1820 (15 ° SR) 1520 (22 ° SR)
  • Examples 7 and 8 show that there are no differences in the strength properties between unbleached or chlorine-bleached pulp on the one hand and, according to the invention, chlorine-free bleached pulp on the other hand.

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  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Wood Science & Technology (AREA)
  • Paper (AREA)
  • Polysaccharides And Polysaccharide Derivatives (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
EP90890291A 1989-10-30 1990-10-30 Procédé exempt de chlore pour le blanchiment de pâtes cellulosiques Expired - Lifetime EP0426652B2 (fr)

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
AT0249489A AT404740B (de) 1989-10-30 1989-10-30 Verfahren zum chlorfreien bleichen von zellstoffen
AT2494/89 1989-10-30
AT249489 1989-10-30
AT258889 1989-11-10
AT258889 1989-11-10
AT2588/89 1989-11-10

Publications (3)

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EP0426652A1 true EP0426652A1 (fr) 1991-05-08
EP0426652B1 EP0426652B1 (fr) 1994-05-11
EP0426652B2 EP0426652B2 (fr) 2001-11-14

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EP90890291A Expired - Lifetime EP0426652B2 (fr) 1989-10-30 1990-10-30 Procédé exempt de chlore pour le blanchiment de pâtes cellulosiques

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US (1) US5346588A (fr)
EP (1) EP0426652B2 (fr)
JP (1) JP2995422B2 (fr)
AR (1) AR243946A1 (fr)
AT (1) ATE105599T1 (fr)
AU (1) AU636173B2 (fr)
BG (1) BG51052A3 (fr)
BR (1) BR9005476A (fr)
CA (1) CA2028788C (fr)
DE (1) DE59005677D1 (fr)
DK (1) DK0426652T3 (fr)
ES (1) ES2023623T3 (fr)
FI (1) FI102194B1 (fr)
GR (1) GR910300078T1 (fr)
HR (1) HRP930459B1 (fr)
HU (1) HU205175B (fr)
LV (1) LV10513B (fr)
NO (1) NO176975B (fr)
PH (1) PH30483A (fr)
PT (1) PT95718B (fr)
RO (1) RO107715B1 (fr)
SI (1) SI9012041B (fr)
TR (1) TR24891A (fr)
UA (1) UA27098A1 (fr)
YU (1) YU47233B (fr)

Cited By (17)

* Cited by examiner, † Cited by third party
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EP0511433A1 (fr) * 1991-04-30 1992-11-04 Kamyr, Inc. Blanchiment à l'ozone de pâte à moyenne concentration
EP0517691A1 (fr) * 1991-06-07 1992-12-09 Kamyr, Inc. Blanchiment à l'ozone à moyenne concentration
WO1993000470A1 (fr) * 1991-06-27 1993-01-07 A. Ahlstrom Corporation Procede de blanchiment a l'ozone
WO1993000482A1 (fr) * 1991-06-24 1993-01-07 Den Norske Stats Oljeselskap A.S Plateforme offshore demontable
WO1993012287A1 (fr) * 1991-12-09 1993-06-24 Institut National Polytechnique De Toulouse (I.N.P.T.) Procede de fabrication de pate a papier blanchie
EP0581631A1 (fr) * 1992-07-31 1994-02-02 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Traitement sélectif de pâte avec de l'ozone
EP0588704A2 (fr) * 1992-09-15 1994-03-23 Canadian Liquid Air Ltd Air Liquide Canada Ltee Récupération de gaz riche en oxygène provenant de procédés de blanchiment avec ozone
WO1994010378A1 (fr) * 1992-10-26 1994-05-11 Sca-Wifsta-Östrand Ab Procede de blanchiment de pate alcaline au sulfate
WO1994013393A1 (fr) * 1992-12-07 1994-06-23 Kamyr, Inc. Regulation d'un flux d'ozone sous pression vers un reacteur de delignification de pate
WO1994020673A1 (fr) * 1993-03-03 1994-09-15 A. Ahlstrom Corporation Procede de blanchiment de pate au moyen de produits chimiques sans chlorure
WO1994029512A1 (fr) * 1993-06-08 1994-12-22 Kvaerner Pulping Technologies Ab Procede de blanchiment de la pate de cellulose sans produits chimiques chlores
WO1995008021A1 (fr) * 1993-09-15 1995-03-23 Kamyr, Inc. Phase eop pour la blanchiement sans chlorure
EP0677611A1 (fr) * 1994-04-15 1995-10-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé pour réduire la fluorescence de pâtes désencrées
EP0717800A1 (fr) * 1993-09-03 1996-06-26 Union Camp Patent Holding, Inc. Blanchiment d'une p te a papier a concentration moyenne avec de l'ozone, apres decoloration de cette p te a haute concentration avec de l'ozone
WO1997023666A1 (fr) * 1995-12-22 1997-07-03 Lenzing Aktiengesellschaft Corps moules en cellulose et procede de production correspondant
US5770011A (en) * 1995-11-17 1998-06-23 International Paper Company Neutral monoperoxysulfate bleaching process
WO2003048663A2 (fr) * 2001-11-30 2003-06-12 Wedeco Umwelttechnologie Gmbh Procede et dispositif de compression d'un gaz contenant de l'ozone, destine au blanchiment de cellulose a l'ozone

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DE69221385T2 (de) * 1991-05-24 1997-12-11 Union Camp Patent Holding Zweistufiger Reaktor zum Bleichen von Zellstoff und Verfahren zum Bleichen mit Ozon
SE9200183L (sv) * 1992-01-23 1993-07-24 Kamyr Ab Avskiljningsanordning samt foerfarande
US6010594A (en) * 1993-03-03 2000-01-04 Ahlstrom Machinery Corporation Method of bleaching pulp with chlorine-free chemicals wherein a complexing agent is added immediately after an ozone bleach stage
US6045588A (en) 1997-04-29 2000-04-04 Whirlpool Corporation Non-aqueous washing apparatus and method
DE19816925B4 (de) 1998-04-16 2009-12-10 SOCIéTé BIC Handgerät zum Übertragen eines Filmes von einem Trägerband auf ein Substrat
US6773547B2 (en) * 1998-05-08 2004-08-10 American Air Liquide, Inc. Process for the bleaching of low consistency pulp using high partial pressure ozone
US6579412B2 (en) * 1998-05-08 2003-06-17 L'air Liquide - Societe' Anonyme A' Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for ozone bleaching of low consistency pulp
US20050173082A1 (en) * 1998-08-24 2005-08-11 Arbozon Oy Ltd. Bleaching of medium consistency pulp with ozone without high shear mixing
FI981808A (fi) * 1998-08-24 2000-02-25 Crs Reactor Engineering Uk Ltd Menetelmä massan valkaisemiseksi
US7513004B2 (en) 2003-10-31 2009-04-07 Whirlpool Corporation Method for fluid recovery in a semi-aqueous wash process
US7695524B2 (en) 2003-10-31 2010-04-13 Whirlpool Corporation Non-aqueous washing machine and methods
US7300468B2 (en) 2003-10-31 2007-11-27 Whirlpool Patents Company Multifunctioning method utilizing a two phase non-aqueous extraction process
US7739891B2 (en) 2003-10-31 2010-06-22 Whirlpool Corporation Fabric laundering apparatus adapted for using a select rinse fluid
WO2005106105A1 (fr) 2004-04-29 2005-11-10 Unilever N.V. Procede de nettoyage a sec
US7966684B2 (en) 2005-05-23 2011-06-28 Whirlpool Corporation Methods and apparatus to accelerate the drying of aqueous working fluids
US20080177089A1 (en) 2007-01-19 2008-07-24 Eugene Steven Sadlowski Novel whitening agents for cellulosic substrates
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AT380496B (de) * 1984-06-27 1986-05-26 Steyrermuehl Papier Verfahren und reaktor zur delignifizierung von zellstoff mit sauerstoff
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Cited By (30)

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US5411634A (en) * 1991-04-30 1995-05-02 Kamyr, Inc. Medium consistency ozone bleaching
EP0511433A1 (fr) * 1991-04-30 1992-11-04 Kamyr, Inc. Blanchiment à l'ozone de pâte à moyenne concentration
US5411633A (en) * 1991-04-30 1995-05-02 Kamyr, Inc. Medium consistency pulp ozone bleaching
EP0517691A1 (fr) * 1991-06-07 1992-12-09 Kamyr, Inc. Blanchiment à l'ozone à moyenne concentration
WO1993000482A1 (fr) * 1991-06-24 1993-01-07 Den Norske Stats Oljeselskap A.S Plateforme offshore demontable
US5607545A (en) * 1991-06-27 1997-03-04 A. Ahlstrom Corporation Ozone bleaching process utilizing a fluidizing mixer and super-atmospheric pressure
WO1993000470A1 (fr) * 1991-06-27 1993-01-07 A. Ahlstrom Corporation Procede de blanchiment a l'ozone
EP0577157A2 (fr) * 1991-06-27 1994-01-05 A. Ahlstrom Corporation Procédé de blanchiment au peroxyde
EP0577157A3 (fr) * 1991-06-27 1995-04-12 Ahlstroem Oy Procédé de blanchiment au peroxyde.
WO1993012287A1 (fr) * 1991-12-09 1993-06-24 Institut National Polytechnique De Toulouse (I.N.P.T.) Procede de fabrication de pate a papier blanchie
EP0581631A1 (fr) * 1992-07-31 1994-02-02 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Traitement sélectif de pâte avec de l'ozone
EP0971066A1 (fr) * 1992-09-15 2000-01-12 Air Liquide Canada Inc. Récupération de gaz riche en oxygène provenant de procédés de blanchiment avec ozone
EP0588704A2 (fr) * 1992-09-15 1994-03-23 Canadian Liquid Air Ltd Air Liquide Canada Ltee Récupération de gaz riche en oxygène provenant de procédés de blanchiment avec ozone
US5688367A (en) * 1992-09-15 1997-11-18 Canadian Liquid Air/Air Liquide Canada Ltee Method of monitoring and recovering oxygen-rich gas from ozone bleaching
EP0588704A3 (en) * 1992-09-15 1995-12-06 Liquid Air Canada Recovery of oxygen-rich gas from ozone bleaching processes
WO1994010378A1 (fr) * 1992-10-26 1994-05-11 Sca-Wifsta-Östrand Ab Procede de blanchiment de pate alcaline au sulfate
US5364505A (en) * 1992-12-07 1994-11-15 Kamyr, Inc. Pressurized ozone pulp delignification reactor and a compressor for supplying ozone to the reactor
WO1994013393A1 (fr) * 1992-12-07 1994-06-23 Kamyr, Inc. Regulation d'un flux d'ozone sous pression vers un reacteur de delignification de pate
WO1994020673A1 (fr) * 1993-03-03 1994-09-15 A. Ahlstrom Corporation Procede de blanchiment de pate au moyen de produits chimiques sans chlorure
WO1994029512A1 (fr) * 1993-06-08 1994-12-22 Kvaerner Pulping Technologies Ab Procede de blanchiment de la pate de cellulose sans produits chimiques chlores
EP0717800A1 (fr) * 1993-09-03 1996-06-26 Union Camp Patent Holding, Inc. Blanchiment d'une p te a papier a concentration moyenne avec de l'ozone, apres decoloration de cette p te a haute concentration avec de l'ozone
EP0717800A4 (fr) * 1993-09-03 1998-10-28 Union Camp Patent Holding Blanchiment d'une p te a papier a concentration moyenne avec de l'ozone, apres decoloration de cette p te a haute concentration avec de l'ozone
WO1995008021A1 (fr) * 1993-09-15 1995-03-23 Kamyr, Inc. Phase eop pour la blanchiement sans chlorure
US5529660A (en) * 1994-04-15 1996-06-25 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Calude Method of reducing fluorescence in deinked pulp by treating pulp with ozone and a bleaching agent
EP0677611A1 (fr) * 1994-04-15 1995-10-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé pour réduire la fluorescence de pâtes désencrées
US5770011A (en) * 1995-11-17 1998-06-23 International Paper Company Neutral monoperoxysulfate bleaching process
WO1997023666A1 (fr) * 1995-12-22 1997-07-03 Lenzing Aktiengesellschaft Corps moules en cellulose et procede de production correspondant
CN1079848C (zh) * 1995-12-22 2002-02-27 连津格股份公司 纤维素模塑体和它的制造方法
WO2003048663A2 (fr) * 2001-11-30 2003-06-12 Wedeco Umwelttechnologie Gmbh Procede et dispositif de compression d'un gaz contenant de l'ozone, destine au blanchiment de cellulose a l'ozone
WO2003048663A3 (fr) * 2001-11-30 2003-08-14 Wedeco Umwelttechnologie Gmbh Procede et dispositif de compression d'un gaz contenant de l'ozone, destine au blanchiment de cellulose a l'ozone

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CA2028788A1 (fr) 1991-05-01
JP2995422B2 (ja) 1999-12-27
CA2028788C (fr) 1997-04-15
UA27098A1 (uk) 2000-02-28
NO176975B (no) 1995-03-20
LV10513A (lv) 1995-02-20
DE59005677D1 (de) 1994-06-16
ES2023623T3 (es) 1994-08-01
BG51052A3 (en) 1993-01-15
AR243946A1 (es) 1993-09-30
GR910300078T1 (en) 1991-12-10
SI9012041A (en) 1997-08-31
PT95718A (pt) 1991-09-13
SI9012041B (sl) 2000-06-30
US5346588A (en) 1994-09-13
LV10513B (en) 1995-10-20
JPH03152286A (ja) 1991-06-28
HRP930459A2 (en) 1996-04-30
TR24891A (tr) 1992-07-01
FI102194B (fi) 1998-10-30
NO904673D0 (no) 1990-10-29
HUT55847A (en) 1991-06-28
YU47233B (sh) 1995-01-31
DK0426652T3 (da) 1994-06-13
FI905327A0 (fi) 1990-10-29
ATE105599T1 (de) 1994-05-15
EP0426652B1 (fr) 1994-05-11
ES2023623A4 (es) 1992-02-01
HU906923D0 (en) 1991-05-28
AU636173B2 (en) 1993-04-22
FI102194B1 (fi) 1998-10-30
HRP930459B1 (en) 1998-12-31
YU204190A (sh) 1992-07-20
HU205175B (en) 1992-03-30
BR9005476A (pt) 1991-09-17
RO107715B1 (ro) 1993-12-30
EP0426652B2 (fr) 2001-11-14
NO904673L (no) 1991-05-02
PH30483A (en) 1997-05-28
PT95718B (pt) 1997-11-28
AU6455290A (en) 1991-05-02

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