US3446699A - Method of producing pulps from lignocellulose containing materials - Google Patents

Method of producing pulps from lignocellulose containing materials Download PDF

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Publication number
US3446699A
US3446699A US702483A US3446699DA US3446699A US 3446699 A US3446699 A US 3446699A US 702483 A US702483 A US 702483A US 3446699D A US3446699D A US 3446699DA US 3446699 A US3446699 A US 3446699A
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United States
Prior art keywords
pulp
refining
temperature
defibration
pressure
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Expired - Lifetime
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US702483A
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English (en)
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Arne Johan Arthur Asplund
Rolf Bertil Reinhall
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Valmet AB
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Defibrator AB
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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
    • D21C3/00—Pulping cellulose-containing materials
    • D21C3/22—Other features of pulping processes
    • D21C3/26—Multistage processes
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
    • D21B1/00—Fibrous raw materials or their mechanical treatment
    • D21B1/04—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres
    • D21B1/12—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres by wet methods, by the use of steam
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
    • D21B1/00—Fibrous raw materials or their mechanical treatment
    • D21B1/04—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres
    • D21B1/12—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres by wet methods, by the use of steam
    • D21B1/30—Defibrating by other means
    • D21B1/36—Explosive disintegration by sudden pressure reduction
    • 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
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21D—TREATMENT OF THE MATERIALS BEFORE PASSING TO THE PAPER-MAKING MACHINE
    • D21D1/00—Methods of beating or refining; Beaters of the Hollander type
    • D21D1/20—Methods of refining
    • D21D1/30—Disc mills

Definitions

  • This invention provides a method of producing mechanical and chemo-mechanical or semichemical pulp from lignocellulose containing material.
  • the continuous method of this invention includes the digesting of the material in the presence of sodium sulfite at a temperature of between 140-240" C. at a superatmospheric pressure.
  • the digested material is defibrated in an atmosphere of steam under substantially the same superatmospheric pressure and temperature prevailing in the digester.
  • At least two successive refining zones are provided after the defibrating step. Progressively decreasing superatmospheric pressures are established and maintained in respective successive refining zones after the said defibrating zone. This causes the defibrated pulp to move from the defibrating zone to and through the successive refining zones.
  • a diluting liquid is introduced into the system before each successive zone. This diluting liquid has a temperature below that prevailing in each preceding stage of the operation to gradually reduce the temperature and consistency of the pulp previous to every new refining zone.
  • the starting material such as the wood chips
  • the starting material can be defibrated with low consumption of power, when the difibration is conducted at high temperature and under high pressure such as a temperature between 140 and 240 C. and a corresponding steam pressure.
  • the material is subjected to a further treatment generally defined as the refining process.
  • the defibration may be conducted in the presence of, or without, chemicals or the chips may be decomposed partially by acid or alkaline cooks.
  • the chips may be pretreated by a heating or partial decomposition either in a liquid phase or a vapor phase. In the former case free liquid is removed from chips prior to the defibration; in the latter case no free liquid is present.
  • the defibration is effected immediately after the pre-treatment of the chips and usually at the temperature and under the pressure prevailing in the pre-treatment although it is, of
  • the defibration is carried out at a high concentration amounting to between 25 and 40 percent, which together with the prevailing high temperature rendering the lignine plastic is the main explanation for the low demand on power for effecting the defibration.
  • the refining process may with advantage be conducted in direct sequence to the defibration in such a manner that the defibrated pulp is directly blown into the refining system without collection and dilution in intermediate bins, 'whereby the time interval between the defibration and the refining procedures is reduced to a minimum.
  • the refining process is conducted or at least commenced before the lignine has lost its plastic properties, which results in improved fiber qualities and improved disintegration of the fibers themselves.
  • the refining operation is effected under pressure, but it is obvious that it must be done under less severe conditions than the defibration proper, which means at a lower temperature and with a lower concentration.
  • Purpose of the invention It is thus one main object of the invention to provide a method of producing pulp from lignocellulose containing material which in comparison to the methods hitherto used renders improved quality of the fibers and improved disintegration of the individual fiber.
  • a further object of the invention is to provide a method of producing pulp from lignocellulose containing material which offers possibility of conducting the refining process without additional pumping work.
  • a still further objection of the invention is to provide a method of producing mechanical or semichemical pulp with reduced consumption of power for attaining a predetermined grade of grinding of the defibrated and refined material.
  • the material to be treated is continuously fed through a hopper and a sluice member, for example a so-called cell-feeder 12, to a cooker 14.
  • the material may be constituted by chips of fur wood, for example, which chips have been moistoned with steam and impregnated with an aqueous solution of sodium sulfite having a pH of 6.5 corresponding to kilograms of Na O per ton of chips, calculated as absolutely dry.
  • Fed into the cooker 14 is also steam entering through a pipe 16 so as to create a pressure of 8 superatmospheric atmospheres and a temperature of about 175 C., to exist in the cooker.
  • the chips are treated under a short time, such as five minutes whereupon they are fed at the prevailing temperature and pressure continuously into a defibrator 18, which preferably is of a disc type and driven by an electric motor 20.
  • the defibrator may be of the kind disclosed in the U.S. Patent No. 2,964,250.
  • the chips are decomposed into minor fiber bundles and furthermore individual fibers are set free to some ex- 9 tent.
  • the pulp suspension has a consistency of about per cent when leaving the defibrator 18 and is blown through a throttle or reducing valve 22 and a conduit 24 under utilization of the high pressure prevailing in the defibrator, into a refiner 26 driven by an electric motor 28 and having a lower pressure prevailing therein such as a pressure of 3 superatmospheric atmospheres.
  • a conduit 29 water having a temperature of about 100 C. is supplied immediately before the refiner 26, so as to cause the concentration of the pulp in the suspension to be reduced to 20 percent, for example. Further the temperature of the pulp is lowered to about l-l40 C.
  • the pulp is blown under utilization of the superatmospheric pressure through a throttle or a reducing valve 30 through a conduit 32 into a second refiner driven by an electric motor 42.
  • the pressure in the refiner 40 may be reduced to 2 superatmospheric atomspheres.
  • water is supplied through a pipe 44, said water having a temperature lower than 100 C., such as C.
  • the pipe 44 debouches ahead of the refiner 40 so as to give to the pulp suspension a consistency of a still lower concentration, which may be about 8 percent, for example, at a temperature of about C.
  • the finally treated pulp escapes through a sluice 46 into an escape opening 48 and is collected in a pulp bin 50. From there the pulp is conveyed through a conduit 52 and a pump 54 to a following station of treatment.
  • refiners or rafiinators 26 and 40 a further separation of the individual fibers of the pulp from one another is elfected together with the disintegration of the individual fibers.
  • These refiners or raffinators may be of principally the same kind as the defibrator 18 and differ therefrom mainly by the grinding members thereof, such as grinding discs, being adapted to accomplish an increased decomposition of the fiber bundles and the fibers into their constituents.
  • bleaching chemicals and/or hydrating agents may be added in one or several of the refining steps and they are then suitably added immediately ahead of the grinding discs.
  • the kind of these chemicals depends on the treatment of the chips or the type of the pulp to be produced. If, for example, the pre-treatment consists in a partial decomposition by means of a solution of sulfite, there may be used sulfite, S0 and hydrosulfite. If, on the contrary, the defibration is conducted in the presence of alkaline solutions hydrogen peroxide or sodium peroxide maybe used. Due to the fact that the bleaching is effected under pressure at high temperature and/or concentration, an effect bleaching may be conducted directly in the refining system.
  • the chips are decomposed with larger quantities of cooking chemicals, which for some reason or another must be recovered or made non-dangerous, the dilution of the pulp during the refining operation may be to advantage be effected by means of recovered waste liquid.
  • a method of continuously producing chemo-mechanical and semichemical pulp from lignocellulosic material which comprises, in combination:

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  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Mechanical Engineering (AREA)
  • Paper (AREA)
US702483A 1963-04-03 1968-02-01 Method of producing pulps from lignocellulose containing materials Expired - Lifetime US3446699A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
SE368263 1963-04-03

Publications (1)

Publication Number Publication Date
US3446699A true US3446699A (en) 1969-05-27

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ID=20262649

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Application Number Title Priority Date Filing Date
US702483A Expired - Lifetime US3446699A (en) 1963-04-03 1968-02-01 Method of producing pulps from lignocellulose containing materials

Country Status (8)

Country Link
US (1) US3446699A (de)
AT (1) AT260008B (de)
BE (1) BE646028A (de)
CH (1) CH423451A (de)
DE (1) DE1253031B (de)
FI (1) FI42161C (de)
GB (1) GB1057232A (de)
NL (1) NL6403555A (de)

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3652387A (en) * 1969-06-05 1972-03-28 Ethyl Corp Process for the manufacture of dissolving-grade pulp
US3919041A (en) * 1969-02-06 1975-11-11 Ethyl Corp Multi-stage chlorine dioxide delignification of wood pulp
US3929558A (en) * 1974-03-11 1975-12-30 Ontario Paper Co Ltd Method of adding a soluble aluminum salt to chemically softened wood chips followed by mechanical refining
US4002528A (en) * 1972-02-18 1977-01-11 Kamyr, Inc. Apparatus for processing pulp
US4037792A (en) * 1972-10-23 1977-07-26 Sca Development Aktiebolag Continuously refining raw fibrous material to produce mechanical refiner pulp
US4116758A (en) * 1976-05-14 1978-09-26 Canadian International Paper Co. Method of producing high yield chemimechanical pulps
US4152197A (en) * 1974-09-23 1979-05-01 Mo Och Domsjo Ab Process for preparing high-yield cellulose pulps by vapor phase pulping an unpulped portion of lignocellulosic material and a partially chemically pulped portion
US4217169A (en) * 1975-12-12 1980-08-12 Aizenberg Sergei A Method of manufacturing fibrous sheet material
US4294653A (en) * 1974-09-23 1981-10-13 Mo Och Domsjo Aktiebolag Process for manufacturing chemimechanical cellulose pulp in a high yield within the range from 65 to 95%
US4298425A (en) * 1978-05-03 1981-11-03 Defibrator Aktiebolag Method and apparatus for refining lignocellulose-containing material to produce fiber pulp
US4357208A (en) * 1978-02-17 1982-11-02 Sca Development Aktiebolag Method of making pulp
FR2544757A1 (fr) * 1983-04-20 1984-10-26 Process Evaluation Devel Procede et appareil de digestion pour la production de pulpe de haute qualite
FR2546545A1 (fr) * 1983-05-23 1984-11-30 Process Evaluation Devel Procede de digestion thermomecanique utilisant des blanchissants
US4689117A (en) * 1980-11-24 1987-08-25 Process Evaluation And Development Corporation Thermomechanical digestion process for enhancing the brightness of cellulose pulp using bleachants
US4699691A (en) * 1980-11-24 1987-10-13 W. R. Grace & Co. Thermomechanical digestion process
US4789429A (en) * 1985-11-06 1988-12-06 Sunds Defibrator Aktiebolag Method of making mechanical pulp
US6165317A (en) * 1995-06-12 2000-12-26 Andritz Sprout-Bauer, Inc. Control of refined pulp quality by adjusting high temperature pre-heat residence time
US20010050151A1 (en) * 1997-08-08 2001-12-13 Marc J. Sabourin Method of pretreating lignocellulose fiber-containing material for the pulp making process
US20050029373A1 (en) * 2003-05-21 2005-02-10 Vaders Dennis Henry Refiner steam separation system for reduction of dryer emissions
AT518800A1 (de) * 2016-06-17 2018-01-15 Andritz Ag Maschf Verfahren zur herstellung von faserstoff

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT330562B (de) * 1972-10-23 1976-07-12 Sca Project Ab Verfahren zur herstellung von mechanisch verfeinertem faserstoff hoher dichte
CN109208364B (zh) * 2018-08-24 2020-08-18 武汉迪因生物科技有限公司 蒸汽爆破装置

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2641164A (en) * 1946-07-08 1953-06-09 Hill Harold Sanford Method for processing fibrous pulp
US2697661A (en) * 1946-07-31 1954-12-21 Alton Box Board Co Digestion of pulp

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE886839C (de) * 1953-07-02 Phrix Werke Ag Verfahren und Vorrichtung zur kontinuierlichen Behandlung von cellulosehaltigen Ausgangsstoffen mit Kochfluessigkeiten

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2641164A (en) * 1946-07-08 1953-06-09 Hill Harold Sanford Method for processing fibrous pulp
US2697661A (en) * 1946-07-31 1954-12-21 Alton Box Board Co Digestion of pulp

Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3919041A (en) * 1969-02-06 1975-11-11 Ethyl Corp Multi-stage chlorine dioxide delignification of wood pulp
US3652387A (en) * 1969-06-05 1972-03-28 Ethyl Corp Process for the manufacture of dissolving-grade pulp
US4002528A (en) * 1972-02-18 1977-01-11 Kamyr, Inc. Apparatus for processing pulp
US4037792A (en) * 1972-10-23 1977-07-26 Sca Development Aktiebolag Continuously refining raw fibrous material to produce mechanical refiner pulp
US3929558A (en) * 1974-03-11 1975-12-30 Ontario Paper Co Ltd Method of adding a soluble aluminum salt to chemically softened wood chips followed by mechanical refining
US4152197A (en) * 1974-09-23 1979-05-01 Mo Och Domsjo Ab Process for preparing high-yield cellulose pulps by vapor phase pulping an unpulped portion of lignocellulosic material and a partially chemically pulped portion
US4294653A (en) * 1974-09-23 1981-10-13 Mo Och Domsjo Aktiebolag Process for manufacturing chemimechanical cellulose pulp in a high yield within the range from 65 to 95%
US4217169A (en) * 1975-12-12 1980-08-12 Aizenberg Sergei A Method of manufacturing fibrous sheet material
US4116758A (en) * 1976-05-14 1978-09-26 Canadian International Paper Co. Method of producing high yield chemimechanical pulps
US4357208A (en) * 1978-02-17 1982-11-02 Sca Development Aktiebolag Method of making pulp
US4298425A (en) * 1978-05-03 1981-11-03 Defibrator Aktiebolag Method and apparatus for refining lignocellulose-containing material to produce fiber pulp
US4689117A (en) * 1980-11-24 1987-08-25 Process Evaluation And Development Corporation Thermomechanical digestion process for enhancing the brightness of cellulose pulp using bleachants
US4699691A (en) * 1980-11-24 1987-10-13 W. R. Grace & Co. Thermomechanical digestion process
FR2544757A1 (fr) * 1983-04-20 1984-10-26 Process Evaluation Devel Procede et appareil de digestion pour la production de pulpe de haute qualite
FR2546545A1 (fr) * 1983-05-23 1984-11-30 Process Evaluation Devel Procede de digestion thermomecanique utilisant des blanchissants
US4789429A (en) * 1985-11-06 1988-12-06 Sunds Defibrator Aktiebolag Method of making mechanical pulp
US6165317A (en) * 1995-06-12 2000-12-26 Andritz Sprout-Bauer, Inc. Control of refined pulp quality by adjusting high temperature pre-heat residence time
US20010050151A1 (en) * 1997-08-08 2001-12-13 Marc J. Sabourin Method of pretreating lignocellulose fiber-containing material for the pulp making process
US6899791B2 (en) 1997-08-08 2005-05-31 Andritz Inc. Method of pretreating lignocellulose fiber-containing material in a pulp refining process
US20050029373A1 (en) * 2003-05-21 2005-02-10 Vaders Dennis Henry Refiner steam separation system for reduction of dryer emissions
US7368037B2 (en) 2003-05-21 2008-05-06 Masonite Corporation Refiner steam separation system for reduction of dryer emissions
AT518800A1 (de) * 2016-06-17 2018-01-15 Andritz Ag Maschf Verfahren zur herstellung von faserstoff
AT518800B1 (de) * 2016-06-17 2019-09-15 Andritz Ag Maschf Verfahren zur herstellung von faserstoff

Also Published As

Publication number Publication date
FI42161B (de) 1970-02-02
FI42161C (fi) 1970-05-11
AT260008B (de) 1968-02-12
CH423451A (de) 1966-10-31
DE1253031B (de) 1967-10-26
BE646028A (de) 1964-07-31
GB1057232A (en) 1967-02-01
NL6403555A (de) 1964-10-05

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