US20040026051A1 - Environmentally-friendly fiberline for producing bleached chemical pulp - Google Patents
Environmentally-friendly fiberline for producing bleached chemical pulp Download PDFInfo
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- US20040026051A1 US20040026051A1 US10/633,536 US63353603A US2004026051A1 US 20040026051 A1 US20040026051 A1 US 20040026051A1 US 63353603 A US63353603 A US 63353603A US 2004026051 A1 US2004026051 A1 US 2004026051A1
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- pulp
- practiced
- treating
- treatment
- pulping process
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Classifications
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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
- 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
- D21C9/1057—Multistage, with compounds cited in more than one sub-group D21C9/10, D21C9/12, D21C9/16
-
- 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
- D21C9/12—Bleaching ; Apparatus therefor with halogens or halogen-containing compounds
- D21C9/14—Bleaching ; Apparatus therefor with halogens or halogen-containing compounds with ClO2 or chlorites
- D21C9/144—Bleaching ; Apparatus therefor with halogens or halogen-containing compounds with ClO2 or chlorites with ClO2/Cl2 and other bleaching agents in a multistage process
-
- 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
- D21C3/222—Use of compounds accelerating 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
- 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
-
- 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
-
- 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
- D21C9/16—Bleaching ; Apparatus therefor with per compounds
- D21C9/163—Bleaching ; Apparatus therefor with per compounds with peroxides
Definitions
- TCF bleaching no chlorine-containing.chemicals, in particular no chlorine (Cl 2 , or simply designated “C”) or chlorine dioxide (Cl0 2 , or simply “D”), are used in the bleaching of pulp.
- C chlorine
- D chlorine dioxide
- elemental chlorine is eliminated from the bleach plant in favor of more environmentally benign chlorine dioxide.
- TCF bleaching sequences include the use of oxygen gas (0 2 , or simply “0”), ozone gas (0 3 , or simply “Z”), and hydrogen peroxide (H 2 0 2 , or simply “P”), among others, while ECF bleaching sequences also include the use of chlorine dioxide (D).
- TOF and ECF bleaching sequences are susceptible to the damaging effects of the presence of dissolved metal ions such as dissolved iron (Fe), copper (Cu), and manganese (Mn), among others.
- dissolved metal ions such as dissolved iron (Fe), copper (Cu), and manganese (Mn)
- these metals especially, Mn, are recognized as detrimental to the effective treatment of pulp with non-chlorine bleaching agents, most notably, hydrogen peroxide.
- Typical treatments used to minimize the prescience of these metal include acid washing and chelate treatment, for example, using conventional chelating agents EDTA and DPTA, among others.
- kraft process is the “soda” process in which the active pulping chemical is limited to NaOH alone, that is, no sulfur-containing chemicals are used in the pulping process (though some sulfur may be introduced via the wood supply or through oil burned in the mill's boilers).
- the soda process is recognized as producing a somewhat inferior product than the kraft process. That is, the soda process typically produces a pulp having lower yield and strength properties than the kraft process.
- attempts have been made to introduce strength or yield-enhancing additives to the soda process to improve the quality of the pulp produced.
- anthraquinone (AQ) has been introduced with limited success to provide what has been known as the “soda-AQ” process.
- the present invention provides an environmentally-friendly and commercially viable process for producing fully-bleached cellulose pulp from comminuted cellulosic fibrous material.
- One embodiment of the present invention comprises a method of treating a slurry of comminuted cellulosic fibrous material to produce a bleached chemical pulp, comprising or consisting of the following: a) treating the material in a first stage with a gas containing ozone; and b) treating the material in a second stage with a liquid containing chlorine dioxide; wherein between a) and b) the material is treated with an alkaline liquid to raise the pH of the material prior to b) and wherein no washing is performed between a) and b).
- the pH of the material is raised to at least about 6.0, preferably, at least 7.0.
- the present invention may be expressed by the notation (ZEND), where Z represents an acidic treatment with an ozone containing gas, EN is an alkaline neutralization treatment, and D is an alkaline treatment with chlorine dioxide; again, no washing is performed between these treatments.
- the alkaline neutralization treatment, EN performs at least two recognized functions.
- the increase in alkalinity to an approximately neutral pH that is, to a pH of between about 6 and 8, preferably, about 7, solubilizes the products of reaction from the prior Z stage.
- the lignin-containing compounds oxidized in the Z stage are kept in solution by the addition of alkali to the ozonated pulp.
- solubilized compounds are removed in a subsequent washing of the pulp prior to further treatment, according to the present invention, no washing (the term “washing” also includes pressing and thickening) is necessary, and the solubilized lignin-containing compounds are passed to the following alkaline chlorine dioxide treatment.
- the lignin-containing compounds can be subsequently removed in a washing stage following the chlorine dioxide stage.
- the introduction of alkali in the neutralization stage also increases the pH of the pulp to a range that is more compatible with the subsequent alkaline D stage. It is known in the art that it is preferable to initiate the chlorine dioxide treatment in an alkaline state, however, during chlorine dioxide treatment the pH typically drops as acids are formed.
- the alkali introduced in the EN stage offsets the amount of alkali that needs be added to adjust the pH for the D stage.
- the present invention not only is a more effective treatment of the pulp obtained, that is, a more effective removal of chromophoric compounds, but also the need for an expensive washing device is obviated.
- the material is treated in an alkaline chemical pulping process, preferably an essentially sulfur-free pulping process, such as a soda pulping process.
- This alkaline pulping process also preferably includes treatment with a strength or yield enhancing additive such as anthraquinone or polysulfide, or their equivalents or derivatives.
- the preferred additive is anthraquinone, AQ, because AQ has been shown to off-set the reduced yield characterized by the soda process, in comparison to the kraft process.
- the alkaline pulping process preferably includes a bulk delignification stage and the process includes at least one stage prior to or during the bulk delignification stage in which a liquid containing a first level of dissolved organic material is removed from the material and replaced with a second liquid having a lower (e.g. at least 50% lower) level of dissolved organic material, as described in the aforementioned patents (the disclosures of which are hereby incorporated by reference herein).
- the treatment a) is preferably preceded by, c), treating the material with a liquid containing chlorine dioxide followed by d) treating the material with an alkaline liquid.
- the treatment c) is a treatment with chlorine dioxide (D) and d) is a treatment with an alkaline liquid to solubilize and extract (E) the oxidized products produced in c).
- the alkaline liquid in d) is typically sodium hydroxide.
- one preferred embodiment is the bleaching sequence D-E-(ZEND), in which washing is performed before, between, and after the first D and first E stages (as indicated by the hyphens in the bleaching sequence designation) and no washing is performed between the Z, EN and D stages (as indicated by enclosing those symbols within parenthesis without hyphens between them in the bleaching sequence designation).
- the first treatment with the alkaline liquid (E) may also include the presence of oxygen, a peroxide, or both. That is, this stage may also be an E O ,E P or E OP stage.
- Another embodiment of the present invention includes a method for producing bleached chemical pulp from comminuted cellulosic fibrous material comprising the following: a) treating the material in a chemical pulping process in the presence of chemical additive to produce a chemical pulp containing at least some of the additive; b) treating the chemical pulp with at least one elemental chlorine-free bleaching agent to produce a bleached chemical pulp having at least some discoloration due to the presence of the chemical additive; and c) treating the bleached pulp with at least one oxidizing agent to remove the discoloration produced by the presence of the chemical additive.
- the chemical additive used in the pulping process of a) is anthraquinone or its equivalents or derivatives.
- the discoloration of the pulp due to the presence of the additive, typically AQ is characterized by a yellowish or orange tinge to the pulp.
- the at least one bleaching agent used in the treatment b) is preferably one or more of the following bleaching agents: oxygen, chlorine dioxide, sodium hydroxide, ozone, hydrogen peroxide, but most preferably comprises at least chlorine dioxide.
- the oxidizing agent used in c) is typically air, ozone, oxygen, or peroxide, but is preferably an ozone-containing gas.
- a method of ECF treatment of comminuted cellulosic fibrous material comprising the sequence soda/AQ cooking, and then one of D-Ep-(ZEND), or D-E O -(ZEND), or D-E OP -(ZEND).
- the pulp so produced has a brightness of at least 89 or 90% ISO, and a viscosity of over 21 or 22 cP.
- FIG. 1 is a schematic illustration of a complete fiberline of one exemplary embodiment according to the present invention.
- FIG. 2 is a schematic detailed illustration of a subsystem of the fiberline of FIG. 1;
- FIG. 3 is a graph of viscosity versus brightness showing the properties of pulp produced according to the present invention compared to various prior art processes.
- FIG. 4 is a graph like that of FIG. 3 only plotting brightness versus chlorine dioxide consumption.
- FIG. 1 is a schematic illustration of a typical complete environmentaily-friendly and commercially viable fiberline, or cellulose material treatment system, 10 , according to the present invention.
- Comminuted cellulosic fibrous material 11 typically hardwood or softwood chips, though any other form of comminuted cellulosic fibrous material may be treated according to the invention, is introduced to a digester 12 .
- digester 12 may also be a batch digester.
- the pulping process is preferably a sulfur-free alkaline cooking process, preferably a soda/AQ process.
- Caustic soda, or sodium hydroxide is introduced to digester 12 along with the chips via conduit 13 and AQ, or its equivalent or derivative, is introduced via conduit 14 .
- the treated pulp is discharged from the digester into conduit 15 .
- the cooked pulp is typically treated in one or more brownstock washers 16 to recover some of the cooking chemical and to clean the pulp slurry prior to further treatment.
- the cleaned pulp is passed via conduit 17 to optional alkaline oxygen delignification 18 and post oxygen delignificaticn washing 20 via conduit 19 .
- the oxygen treatment is preferably performed in one or two stages at medium consistency, that is, at a pulp consistency between about 8 and 18%.
- the washed pulp, with or without oxygen treatment is passed to further treatment via conduit 21 .
- Conduit 21 introduces the pulp to the first formal bleaching stage 22 , which is preferably an alkaline chlorine dioxide treatment, DO.
- This treatment 22 may be performed at medium consistency or at low consistency, that is, at a pulp consistency between 0.5 to 18%, preferably between about 2-8% (and all other specific narrower ranges within the broad range).
- the treated pulp is then passed via conduit 23 to washer 24 .
- Washer 24 may be any conventional washer, such as a vacuum drum washer, a wash press, a diffusion washer, or a belt washer. Washing in one or more washers 24 may be performed at low or medium consistency as is conventional.
- the washed pulp is passed via conduit 25 to alkaline extraction stage (E) 26 (which may be an E O , E P , or E OP stage) which is a conventional alkaline treatment with sodium hydroxide which solubilizes the products of reaction of stage 22 .
- the pulp from extraction stage 26 is forwarded to another conventional washing stage 28 , similar to stage 24 , via conduit 27 .
- the washed pulp is forwarded to the ozone treatment stage 30 via conduit 29 .
- Treatment stages 30 , 34 and 38 constitute the broadest embodiment of the present invention.
- the pulp preferably at medium consistency (e.g. about 6-18%), though it may be at low (0.5-5%) or high (over 18%) consistency, is treated with an ozone containing gas introduced via conduit 31 .
- This ozone-containing gas typically is generated and introduced using of a carrier gas, for example, oxygen or air, at a concentration greater than 5%, typically between about 5 and 15%. Though this ozone containing gas is typically produced on-site, it may be supplied from an external source.
- the ozone-containing gas is typically provided in a pressurized state to a high-intensity mixer, for example, to an AMZ mixer supplied by Andritz-Ahlstrom Inc.
- the treatment in stage 30 is typically in an acidic environment, typically, at a pH less than 5, preferably a pH between about 2 and 3.
- the treated pulp is passed to alkaline treatment 34 via conduit 32 .
- some de-gassing 33 may be performed after treatment 30 and before treatment 34 , but no washing (which term includes pressing and thickening).
- Alkaline treatment 34 is typically a relatively short exposure of the ozonated pulp to alkali, typically NaOH, introduced via conduit 35 .
- the retention time in treatment 34 is typically less than 30 minutes, preferably less than 15 minutes.
- the treatment 34 neutralizes the acidic pulp discharged from treatment 30 that the products of the reaction in treatment 30 are maintained in a solubilized state.
- the pH in stage 34 is typically between about 6 and 8, preferably about 7.
- these solubilized compounds are not washed out of the pulp after treatment in 34 but are passed directly to alkaline treatment 38 , D 1 , via conduit 36 .
- some degassing 37 may be performed between stages 34 and 38 , if necessary.
- the unwashed pulp introduced to treatment 38 via conduit 36 is treated with chlorine dioxide, Cl0 2 .
- the chlorine dioxide is introduced to the pulp via conduit 39 and a mixer (see mixer 59 in FIG. 2), for example, a conventional high-intensity mixer.
- the treated pulp is then passed via conduit 40 to conventional washing in stage 41 and then, if desired, to further treatment via conduit 42 , for example, to further elememtal chlorine-free bleaching stages (so that the entire treatment of the pulp is ECF), to storage, to stock preparation before a paper machine, if the mill is an integrated paper mill, or to a pulp drier, if the mill is a market pulp mill.
- ECF elememtal chlorine-free bleaching stages
- FIG. 2 illustrates a specific embodiment of stages 30 , 34 and 38 shown in FIG. 1. Structures in FIG. 2 that are similar to those in FIG. 1 are identified with similar reference numbers, but in FIG. 2 the reference numbers are 10 prefaced by the numeral “1”. For example, the conduit 129 in FIG. 2 is essentially the same the as conduit 29 in FIG. 1.
- Pulp from washer 28 in FIG. 1 is introduced to treatment 130 via conduit 129 in FIG. 2.
- Treatment 130 is preferably performed in a mixer 50 to which an ozone-containing gas, typically ozone in an oxygen carrier gas, is introduced via conduit 131 .
- the ozone treatment step is typically performed at a temperature less than 100° C., for example, at a temperature between about 20 and 70° C., depending upon the energy balance of the system.
- the acidic ozone treatment 130 is typically performed at a pH less than 5, preferably, a pH between about 2 and 3. However, the ozone treatment 130 may be performed at a pH of greater than 5, even greater than 7, if ozone decomposition and cellulose damage can be avoided or minimized at such higher pH values.
- the ozonated pulp is discharged from the mixer 50 to conduit 132 . Since the reaction of the ozone with the pulp is very rapid, for example, the reaction may typically take less than 30 seconds, no retention vessel is normally necessary after the mixer 50 and the ozonated pulp may be passed directly to the alkaline neutralization stage 134 . However, if desired, a retention vessel 51 may be used after the mixer 50 . Though not shown in FIG. 2, the pulp may be de-gassed after mixer 50 and before stage 134 .
- the ozone-treated pulp is introduced to alkaline neutralization stage 134 via conduit 132 .
- Treatment 134 is effected by the introduction of alkali, preferably NaOH via conduit 135 , to mixer 52 , again, preferably a high-intensity mixer.
- the alkali in conduit 135 may also be introduced directly to mixer 150 via conduits 62 and 131 . In a specific embodiment of this invention, it may even be possible to eliminate the mixer 52 and introduce both the ozone-containing gas and the alkali to mixer 50 .
- the pulp is discharged to conduit 53 .
- the pulp is retained in this alkaline state, typically at a temperature of between about 20 and 70° C., preferably at a temperature of between about 50 and 70° C., for at least about 15 minutes, preferably at least between about 30 minutes and about 60 minutes.
- This retention can be effected in a conventional retention vessel (not shown) or in a pump feed chute 54 .
- at least some de-gassing 137 of the pulp is effected as the pulp is introduced to feed chute 54 , in any suitable conventional manner.
- the pulp may also be de-gassed in a specially-designed rotary de-gassing device if desired.
- the pulp is pumped to chlorine dioxide treatment 138 via pump 55 .
- the pump 55 may be a de-gassing-type pump from which gas is removed via conduit 56 .
- the pump 55 passes the pulp through conduit 57 to mixer 59 , again, preferably a high-intensity mixer, to which chlorine dioxide is introduced via conduit 139 .
- the pulp in conduit 57 may be heated by introducing steam via conduit 58 .
- the pH of the pulp discharged to vessel 61 is typically at least 5, preferably at least 6. Additional alkali may also be added to the pulp, for example, via conduit 63 .
- the chlorine dioxide is intimately mixed with the pulp in mixer 59 and discharged to retention vessel 61 via conduit 60 .
- the alkaline and chlorinated pulp is retained in conventional retention vessel 61 (e.g. an upflow vessel) for at least 1 hour, typically the pulp is retained for between about 1.5 to 6 hours, preferably between about 2 to 4 hours, at a temperature of between about 20 and 70° C., preferably, between about 50 and 70° C.
- the treated pulp is discharged via conduit 140 to conventional washer 141 , washed, and then forwarded on to further treatment, as discussed previously, via conduit 142 .
- FIG. 3 shows plots 6 f three different treatment scenarios, a D-E op -(ZEND) treatment sequence according to the present invention indicated by reference numeral 70 , and two prior art procedures, D-E op -D-P indicated at 71 , and D-E op p-D indicated at 72 .
- the treatment 70 according to the present invention achieves brightness comparable to that of the procedure 71 , yet with viscosity that is much higher, and in fact comparable to that indicated at 72 .
- the feed pulp before the treatment sequence was LO-SOLIDS® cooked mixed hardwood that was oxygen delignified to a kappa number of 9 , exactly the same feed pulp being used for each of the treatments 70 , 71 , 72 .
- FIG. 4 is a graph of the same pulps and treatment sequences as in FIG. 3, only showing brightness graphed against chlorine dioxide consumption.
- the treatment procedure 73 according to the present invention had brightness comparable to that of the procedure 74 , and much greater than the procedure 75 , with approximately the same (only slightly greater) chlorine dioxide consumption.
- the treatment sequence D-E [typically either E 0 , or E p , or E op ]-(ZEND) according to the invention produces pulp having a brightness of at least 89 or 90% ISO, and a viscosity of at least about 21 or 22 cP.
- the invention includes all specific narrower ranges within the broad ranges recited above.
- a consistency of 6-18% means 6-12%, 8-11%, 9-18%, and all other narrow ranges within the broad range.
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Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10/633,536 US20040026051A1 (en) | 1999-12-02 | 2003-08-05 | Environmentally-friendly fiberline for producing bleached chemical pulp |
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US16753799P | 1999-12-02 | 1999-12-02 | |
US72242000A | 2000-11-28 | 2000-11-28 | |
US10/633,536 US20040026051A1 (en) | 1999-12-02 | 2003-08-05 | Environmentally-friendly fiberline for producing bleached chemical pulp |
Related Parent Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US72242000A Division | 1999-12-02 | 2000-11-28 |
Publications (1)
Publication Number | Publication Date |
---|---|
US20040026051A1 true US20040026051A1 (en) | 2004-02-12 |
Family
ID=26863255
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US10/633,536 Abandoned US20040026051A1 (en) | 1999-12-02 | 2003-08-05 | Environmentally-friendly fiberline for producing bleached chemical pulp |
Country Status (5)
Country | Link |
---|---|
US (1) | US20040026051A1 (fi) |
JP (2) | JP2001200486A (fi) |
CA (1) | CA2327248A1 (fi) |
FI (2) | FI20002647A (fi) |
SE (1) | SE0004438L (fi) |
Cited By (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20060201642A1 (en) * | 2005-03-08 | 2006-09-14 | Andritz Inc. | Methods of treating chemical cellulose pulp |
US20070142926A1 (en) * | 2005-12-21 | 2007-06-21 | Rockwell Automation Technologies, Inc. | Remote monitoring and control of an I/O module |
US20080087394A1 (en) * | 2006-10-11 | 2008-04-17 | Akzo Nobel N.V. | Bleaching of pulp |
DE102007006582A1 (de) * | 2007-02-09 | 2008-09-04 | Hiwin Mikrosystem Corp. | Externes Steuerelement für eine schnell lösbare Vorrichtung eines Linearantriebs |
US20100065233A1 (en) * | 2006-12-13 | 2010-03-18 | Itt Manufacturing Enterprises, Inc. | Method for bleaching chemical paper pulps by final ozone treatment at high temperature |
CN104611972A (zh) * | 2015-02-12 | 2015-05-13 | 北京京诚新星造纸工程技术有限公司 | 一种沙柳浆的二氧化氯漂白工艺 |
ITUB20153369A1 (it) * | 2015-09-03 | 2017-03-03 | Nicholas Iarocci | Filtro di carta per sigarette e blocchetto di fogli da filtro |
US20170306557A1 (en) * | 2004-04-20 | 2017-10-26 | The Research Foundation For The State University Of New York | Methods of producing a paper product |
US10214595B2 (en) * | 2014-06-23 | 2019-02-26 | Api Intellectual Property Holdings, Llc | Nanocellulose compositions and processes to produce same |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US8262856B2 (en) * | 2007-06-18 | 2012-09-11 | Andritz Inc. | Processes and systems for the bleaching of lignocellulosic pulps following cooking with soda and anthraquinone |
KR102223405B1 (ko) * | 2019-04-15 | 2021-03-08 | (주)리아씨엔에프 | 해조류 펄프의 제조 공정을 위한 표백 방법. |
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US4568420A (en) * | 1984-12-03 | 1986-02-04 | International Paper Company | Multi-stage bleaching process including an enhanced oxidative extraction stage |
US4619733A (en) * | 1983-11-30 | 1986-10-28 | Kooi Boon Lam | Pollution free pulping process using recycled wash effluent from multiple bleach stages to remove black liquor and recovering sodium hydroxide from the black liquor |
US4959124A (en) * | 1989-05-05 | 1990-09-25 | International Paper Company | Method of bleaching kraft pulp in a DZED sequence |
US5645687A (en) * | 1995-07-10 | 1997-07-08 | Champion International Corporation | Process for manufacturing bleached pulp with reduced chloride production |
US6019870A (en) * | 1994-05-11 | 2000-02-01 | Elf Atochem S.A. | Process for the preparation of delignified and bleached chemical paper pulps |
Family Cites Families (3)
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JP2002517173A (ja) * | 1991-01-03 | 2002-06-11 | ユニオン キャンプ パテント ホウルディング インコーポレイテッド | 塩素を使用しないリグノセルロースパルプの漂白法 |
JPH11286884A (ja) * | 1998-04-03 | 1999-10-19 | Akio Onda | パルプ蒸解薬液とパルプの製造方法 |
JP2000290887A (ja) * | 1999-04-02 | 2000-10-17 | Oji Paper Co Ltd | リグノセルロースの漂白方法 |
-
2000
- 2000-12-01 SE SE0004438A patent/SE0004438L/ not_active Application Discontinuation
- 2000-12-01 JP JP2000367014A patent/JP2001200486A/ja not_active Ceased
- 2000-12-01 CA CA002327248A patent/CA2327248A1/en not_active Abandoned
- 2000-12-04 FI FI20002647A patent/FI20002647A/fi unknown
-
2003
- 2003-08-05 US US10/633,536 patent/US20040026051A1/en not_active Abandoned
-
2007
- 2007-08-07 FI FI20070590A patent/FI20070590A/fi unknown
-
2009
- 2009-01-09 JP JP2009003068A patent/JP2009074234A/ja active Pending
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
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US4619733A (en) * | 1983-11-30 | 1986-10-28 | Kooi Boon Lam | Pollution free pulping process using recycled wash effluent from multiple bleach stages to remove black liquor and recovering sodium hydroxide from the black liquor |
US4568420A (en) * | 1984-12-03 | 1986-02-04 | International Paper Company | Multi-stage bleaching process including an enhanced oxidative extraction stage |
US4568420B1 (en) * | 1984-12-03 | 1999-03-02 | Int Paper Co | Multi-stage bleaching process including an enhanced oxidative extraction stage |
US4959124A (en) * | 1989-05-05 | 1990-09-25 | International Paper Company | Method of bleaching kraft pulp in a DZED sequence |
US6019870A (en) * | 1994-05-11 | 2000-02-01 | Elf Atochem S.A. | Process for the preparation of delignified and bleached chemical paper pulps |
US5645687A (en) * | 1995-07-10 | 1997-07-08 | Champion International Corporation | Process for manufacturing bleached pulp with reduced chloride production |
Cited By (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9945073B2 (en) * | 2004-04-20 | 2018-04-17 | The Research Foundation For The State University Of New York | Methods of producing a paper product |
US20170306557A1 (en) * | 2004-04-20 | 2017-10-26 | The Research Foundation For The State University Of New York | Methods of producing a paper product |
US20060201642A1 (en) * | 2005-03-08 | 2006-09-14 | Andritz Inc. | Methods of treating chemical cellulose pulp |
US20070142926A1 (en) * | 2005-12-21 | 2007-06-21 | Rockwell Automation Technologies, Inc. | Remote monitoring and control of an I/O module |
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Also Published As
Publication number | Publication date |
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SE0004438L (sv) | 2001-06-03 |
SE0004438D0 (sv) | 2000-12-01 |
JP2009074234A (ja) | 2009-04-09 |
FI20070590A (fi) | 2007-08-07 |
FI20002647A (fi) | 2001-06-03 |
CA2327248A1 (en) | 2001-06-02 |
JP2001200486A (ja) | 2001-07-27 |
FI20002647A0 (fi) | 2000-12-04 |
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