EP0502852B1 - Heizung mit verschiebung in kontinuierlichen zellstoffkochern - Google Patents

Heizung mit verschiebung in kontinuierlichen zellstoffkochern Download PDF

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Publication number
EP0502852B1
EP0502852B1 EP90914988A EP90914988A EP0502852B1 EP 0502852 B1 EP0502852 B1 EP 0502852B1 EP 90914988 A EP90914988 A EP 90914988A EP 90914988 A EP90914988 A EP 90914988A EP 0502852 B1 EP0502852 B1 EP 0502852B1
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EP
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Prior art keywords
liquor
chips
chamber
temperature
digester
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Expired - Lifetime
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EP90914988A
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English (en)
French (fr)
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EP0502852A1 (de
Inventor
Bertil K. E. Fagerlund
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Beloit Technologies Inc
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Beloit Technologies Inc
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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
    • D21C7/14—Means for circulating the lye
    • 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

Definitions

  • the present invention relates to improvements in apparatus and methods for the fiber liberating digestion of continuously fed comminuted cellulosic fiber material by cooking liquor and subsequent washing of the liberated fiber material. More particularly, the invention relates to an improved apparatus and process utilizing spent black liquor for heating the chips to effect savings in thermal energy, and for accomplishing high sulfidity cooking without changes to the overall sulfide balance of the system to accomplish a pulp having improved mechanical characteristics, to improve pulp yield, and to achieve extended delignification.
  • the first is batch cooking in which the chips are placed in a digester, liquor is added, the temperature and pressure are raised and the "batch" is maintained at the elevated temperature and pressure to reach the desired stage of delignification.
  • the digester is then emptied, and a subsequent fill is started for another batch.
  • a chip column continuously moves through the digester with hot liquor circulating therethrough. Process conditions are controlled such that the desired stage of delignification has occurred when the chips flow out of the digester.
  • the spent liquor is allowed to flash and steam is generated.
  • the steam is normally utilized to pre-steam the chips and to generate hot water.
  • the heat and cooking chemicals could be utilized more efficiently if the spent liquors were used to preheat and precondition the chips and to preheat the cooking chemicals such as white liquor in kraft processes which enters the process.
  • a further object of the invention is to provide a continuous digestion process wherein the used black cooking liquors and the white liquors are utilized in a unique manner in the process so as to obtain a saving in thermal energy, and to effect an improvement in the resultant qualities of the pulp which is produced.
  • Yet another object of the present invention is to provide a process for achieving high sulfidity cooking without significant changes to the overall sulfide balance of the cooking system, and for achieving extended delignification in a continuous digesting system while improving pulp yield over existing continuous digesting systems.
  • a feature of the invention is the provision of a continuous digestion process wherein a plurality of containers are used in sequence, with the first container receiving preconditioned chips and the chips being preimpregnated and heated in the first container with a low temperature black liquor. Further heating of the chips is accomplished with higher temperature liquors in the second and subsequent containers, and after the chips are brought up to the desired elevated temperature, a white liquor is circulated through the chips at the digestion temperature and pressure.
  • the chips are continuously fed from the last of the preimpregnation containers to the digester for cooking.
  • the cooked delignified chips are removed as pulp from the bottom of the digester and circulated to final washing.
  • the wash liquor from the washer is utilized in two or more stages to displace from the digester the free liquor and liquor within the chips.
  • the hot spent liquor is utilized to heat the incoming materials for the continuous digester.
  • the spent liquor having been extracted from the digester, is accumulated in pressure vessels substantially at digester temperature. Lower temperature liquors from final displacement stages are also accumulated.
  • the incoming chips are first exposed to the lower temperature liquors and then the higher temperature liquors.
  • the white liquor is preheated in a heat exchanger, utilizing a portion of hot spent liquor.
  • the white liquor can be stored in a hot white liquor accumulator whereas the hot spent liquor, after having given energy to the white liquor, goes to the low temperature accumulator.
  • the process can be accomplished wherein a first initial chamber or vessel is utilized, being fed by a screw conveyor feeder to press the chips downwardly.
  • the vessel may be employed with an extraction screen at the top and with a recirculation screen further down the vessel, with the recycled liquor flowing through a central pipe ending at the screen level.
  • Low temperature liquor is fed from a low temperature tank to a circulation pump, and the liquor is evenly spread over the vessel area.
  • the amount of liquor extracted from the top screen is an amount that generally corresponds to the white liquor charge, wood moisture and the dilution factor.
  • the extracted liquor goes to the evaporators.
  • the remaining part of the liquor goes with the chips downwardly in the chamber.
  • the treatment with hot spent liquor takes place in a vessel at principally digester pressure.
  • this high pressure vessel is located underneath the first vessel, and the transfer of material takes place in utilizing a high pressure feeder.
  • the arrangement for heat exchange is, in principal, essentially the same as in the first lower temperature vessel.
  • the hot spent liquor is introduced in a recirculation circuit, and a portion of the liquor flows countercurrent to the chips, being extracted from a top screen.
  • the low temperature liquor is being displaced and substituted by a hot spent liquor.
  • the low temperature liquor which leaves the top screen is conveyed back to the low temperature tank.
  • a portion of the hot spent liquor is utilized to preheat the white liquor that is introduced in the bottom of the high pressure vessel.
  • white liquor should be added after that mechanical device to avoid pulp deterioration. This can be done by utilizing a vessel which forms part of the continuous digester and is integrated into the digester apparatus itself.
  • Figure 1 is a schematic drawing of a process for operating in accordance with the principles of the present invention.
  • Figure 2 is a schematic drawing of a modification of the process shown in Figure 1, wherein the high pressure preimpregnation vessel forms a part of the continuous digester.
  • wood chips are delivered to a first chamber or container 10 through a screw delivery mechanism 11.
  • the chips may be preconditioned, such as by being heated by steam, in a supply container 12.
  • the preheating occurs by a supply of low temperature black liquor supplied from a low temperature black liquor tank 13 through a supply line 14.
  • the black liquor is circulated through the chips through a recirculating mechanism including a recirculating line 15 and a recirculating pump 16.
  • preheated wood chips are forcibly conveyed downwardly to a second container 21, which is a hot liquor preimpregnator in which the wood chips are subjected to liquor for a predetermined time at a higher temperature and high pressure than in the first container.
  • a mechanism such as a rotary delivery valve 20 is employed.
  • Such valves are well-known to those skilled in the art and will not be described further herein.
  • hot black liquor is delivered to the second container by line 23, which receives hot black liquor from a hot black liquor tank 22 delivered by a pressure pump 22a.
  • the hot black liquor is recirculated through the moving chips by recirculation line 24, with the liquor being circulated by a pump 24a.
  • a portion of the liquor is removed through a line 24b, controlled by a valve 24c, to be delivered back to the low temperature black liquor tank 13, preferably upstream of a delivery pump 13a which pumps the low temperature black liquor to the first container 10.
  • screens 21a, 21b, and 21c Arranged in the second container 21 are screens 21a, 21b, and 21c, which allow for the removal of the liquor, with the screen 21a facilitating the removal of the excess black liquor through the line 24b, and the screens 21b and 21c facilitating the recirculation of the high temperature black liquor in two recirculation paths.
  • white liquor is delivered to the second container 21 through a line 25.
  • the white liquor can be supplied through a line 25a, shown by dotted line in Figure 1, as the chips leave the second container.
  • the white liquor is obtained from a high temperature white liquor tank 27, being delivered therefrom by a pump 27a.
  • the white liquor is preheated before delivery to the second container 21 in a heat exchanger 28, with the white liquor being supplied to the heat exchanger from a supply source not shown and a supply line 29.
  • the heat exchanger is heated by hot black liquor supplied through a line 30 leading from the high temperature black liquor tank 22, and, after passing through the heat exchanger, the black liquor flows through a line 31 to the low temperature black liquor tank 13.
  • Cooking liquor is recirculated at the top of the digester through a circuit 34 having a recirculation pump 34a and extraction screen 34b therein. Temperature adjustment of the cooking liquor may be achieved with a trim heat exchanger 34c heated by steam from a steam source 34d.
  • a portion of the cooking liquor is removed from the digester through a line 38 by a pump 38a, and is delivered through a line 39 to the location where the chips exit the second container. This recirculated cooking liquor further dilutes the chips and liquor exiting the second container to facilitate transport of the chips to the digester.
  • the chips move continuously downward, and are cooked to the desired level of delignification.
  • Recirculation takes place through an extraction line 35, an extraction screen 35a, a recirculation line 36, and a pump 36a.
  • a portion of the recirculated liquor is directed to the hot liquor tank 22, controlled by a valve 36b.
  • washer filtrate from a line 50 is recirculated through a circuit 52 by a pump 54, to eliminate temperature and spent liquor concentration gradients.
  • the filtrate is added between an extraction screen 56 and the pump 54, so that the extracted liquor volume is less than the flow into the digester through circuit 52, causing an upward flow of filtrate in the bottom of the digester.
  • a second recirculation circuit 60 including a pump 62, is provided to extract a portion of the upward flowing filtrate at an extraction screen 64, together with remaining hot spent black liquor.
  • a portion of the extracted filtrate and liquor is directed to the low temperature tank 13, through line 66 controlled by a valve 68.
  • a blow line 80 is provided for removing pulp from the digester to a washer.
  • the manner in which the pulp is moved from the digester, including any secondary dilution, is well-known in the art of continuous digesters and will not be described further herein.
  • preconditioned pulp is delivered via a screw conveyor 11 into a first chip preheating container 10 where it is heated by low temperature black liquor obtained from a low temperature black liquor tank 13.
  • the preheated chips pass downwardly through a rotary delivery valve 20 to a second chamber 21, where the chips are further preheated by high temperature black liquor received from a high temperature black liquor tank 22.
  • the high temperature and low temperature black liquors are obtained from the pulp washer with the high temperature liquor also being utilized for heating the white liquor through the heat exchanger 28.
  • White liquor delivered through the screen 21c from a white liquor supply line 25, is added to the chips before the chips enter digester 33.
  • the region of the countercurrent flow between screen 64 and screen 35a should be sufficiently long that the filtrate is heated by the chips substantially to cooking temperature, and the liquor and filtrate removed through line 35a are at or near cooking temperature.
  • Figure 2 illustrates, in schematic format, a process in which the second chamber 21 is continguous with the digester. Corresponding parts of the process depicted in Figure 2 have been numbered similarly to Figure 1.
  • the various extraction screens, recirculation circuits, pumps, and the like for both the high pressure preimpregnation process and the final digestion process are contained in the combined preimpregnation and digester vessel.

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  • Paper (AREA)
  • Chemical And Physical Treatments For Wood And The Like (AREA)

Claims (12)

  1. Aufschließvorrichtung für das Freisetzen von Cellulosefasermaterial für Papierzellstoff unter Verwendung von Kochlauge bei einem hohen Druck und einer hohen Temperatur in einem kontinuierlichen Prozeß, beinhaltend in Kombination:
    eine erste Kammer (10);
    eine Fördereinrichtung (11) zum Fördern von Celluloseholzschnitzeln in die erste Kammer (10);
    einen Niedertemperaturlaugentank (13), der mit der ersten Kammer (10) verbunden ist, zum Hindurchleiten von Niedertemperaturschwarzlauge durch die Schnitzel in der ersten Kammer (10) für den Austausch von Wärmeenergie zum Erhöhen der Temperatur der Schnitzel und zum Übertragen von restlichen Chemikalien auf die Schnitzel;
    eine zweite Kammer (21), die so angeschlossen ist, daß sie durch die Niedertemperaturlauge vorgewärmte Schnitzel aus der ersten Kammer (10) empfängt;
    eine Fördervorrichtung (20), die zwischen den Kammern (10, 21) angeschlossen ist, zum Fördern der Schnitzel in die zweite Kammer (21);
    einen Hochtemperaturlaugentank (22), der an die zweite Kammer (21) angeschlossen ist, zum Hindurchleiten von Hochtemperaturschwarzlauge durch die Schnitzel für den Austausch von Wärmeenergie, um die Temperatur der Schnitzel in die Nähe der Aufschließtemperatur zu bringen und restliche Chemikalien auf die Schnitzel zu übertragen;
    eine Auslaßeinrichtung (32), die aus der zweiten Kammer (21) führt, zum kontinuierlichen Fördern von vorgewärmten Schnitzeln zu einem Aufschließer (33);
    eine Einrichtung (25, 25a, 27, 27a) zum Fördern von Weißlauge zu den in der zweiten Kammer vorgewärmten Schnitzeln zur weiteren Entlignifizierung der Schnitzel in dem Aufschließer;
    eine Rezirkulationseinrichtung (35, 35a, 36, 36a) in dem oberen Teil des Aufschließers zur Rezirkulation von heißer Lauge in dem Aufschließer; und mit einer Ableiteinrichtung (36b) zum Leiten eines Teils der rezirkulierenden heißen Lauge in den Hochtemperaturlaugentank (22);
    eine erste Rezirkulationseinrichtung (52, 54, 56) in dem unteren Teil des Aufschließers zum Rezirkulieren von Lauge in dem unteren Teil, mit einer Einrichtung (50) zum Zusetzen von Wascherfiltrat zu der rezirkulierenden Lauge; und
    eine zweite Rezirkulationseinrichtung (60, 62, 64) in dem unteren Teil des Aufschließers, die eine Extrahiereinrichtung (66, 68) aufweist zum Leiten von Lauge in den Niedertemperaturlaugentank; und eine Verbindung (80) von dem Aufschließer zu einem Zellstoffwascher zum Übertragen des entlignifizierten Zellstoffes.
  2. Aufschließvorrichtung für das Freisetzen von Cellulosefasermaterial für Papierzellstoff unter Verwendung von Kochlauge bei einem hohen Druck und einer hohen Temperatur in einem kontinuierlichen Prozeß, der gemäß Anspruch 1 ausgebildet ist:
    mit einer Rezirkulationseinrichtung (14, 15, 16) für die erste Kammer zum Empfangen von Niedertemperaturlauge aus dem Niedertemperaturtank (13) und zum Rezirkulieren der Lauge durch die Schnitzel in der ersten Kammer (10) im Gegenstrom zu der kontinuierlichen Bewegung der Schnitzel durch die erste Kammer (10).
  3. Aufschließvorrichtung für das Freisetzen von Cellulosefasermaterial für Papierzellstoff unter Verwendung von Kochlauge bei einem hohen Druck und einer hohen Temperatur in einem kontinuierlichen Prozeß, der gemäß Anspruch 1 ausgebildet ist:
    mit einer Rezirkulationseinrichtung (23, 24, 24a) für die zweite Kammer (21), die so angeschlossen ist, daß sie Lauge aus dem Hochtemperaturtank (22) empfängt, zur Rezirkulation der Hochtemperaturlauge durch den zweiten Tank (21) im Gegenstrom zu der kontinuierlichen Hindurchbewegung der Schnitzel, um die Temperatur der Schnitzel darin zu erhöhen.
  4. Aufschließvorrichtung für das Freisetzen von Cellulosefasermaterial für Papierzellstoff unter Verwendung von Kochlauge bei einem hohen Druck und einer hohen Temperatur in einem kontinuierlichen Prozeß, der gemäß Anspruch 1 ausgebildet ist:
    mit einer Weißlaugenrezirkulationseinrichtung (34, 34a, 34b, 38, 38a, 39), die mit dem Aufschließer (33) verbunden ist, zum Rezirkulieren der Weißlauge im Gegenstrom zu der Schnitzelbewegung während des Aufschließprozesses.
  5. Aufschließvorrichtung für das Freisetzen von Cellulosefasermaterial für Papierzellstoff unter Verwendung von Kochlauge bei einem hohen Druck und einer hohen Temperatur in einem kontinuierlichen Prozeß, der gemäß Anspruch 1 ausgebildet ist:
    mit einem Wärmetauscher (28), der mit dem Hochtemperaturlaugentank (22) und mit dem Weißlaugenbehälter (27) verbunden ist, um die Temperatur der Weißlauge unter Verwendung der thermischen Energie in der Lauge in dem Hochtemperaturlaugentank (22) zu erhöhen.
  6. Aufschließvorrichtung für das Freisetzen von Cellulosefasermaterial für Papierzellstoff unter Verwendung von Kochlauge bei einem hohen Druck und einer hohen Temperatur in einem kontinuierlichen Prozeß, der gemäß Anspruch 1 ausgebildet ist:
    mit einer Laugenabfuhrleitung (17), die mit der ersten Kammer (10) verbunden ist, zur Abfuhr der Niedertemperaturlauge.
  7. Kontinuierlicher Aufschließprozeß zum Behandeln von zerschnitzeltem Holz, beinhaltend die Schritte:
    Fördern von Holzschnitzeln in eine erste Kammer (10);
    kontinuierliches Hindurchbewegen der Schnitzel durch diese Kammer (10);
    Hindurchleiten einer Schwarzlauge mit mäßigen Temperaturen in der ersten Kammer (10), um die Schnitzel zu erwärmen und restliche Chemikalien zu recyceln;
    kontinuierliches Fördern der vorgewärmten und chemisch vorkonditionierten Schnitzel und der Lauge mäßiger Temperatur in eine zweite Kammer (21) mit einer höheren Temperatur und höherem Druck;
    Verdrängen der Schwarzlauge mäßiger Temperatur mit heißer Schwarzlauge;
    Hindurchleiten der heißen Schwarzlauge durch die Schnitzel in der zweiten Kammer (21), um die Temperatur der Schnitzel weiterzusteigern und restliche Chemikalien weiter zu recyceln;
    Fördern von Weißlauge zu den heißen Schnitzeln, um die heiße Schwarzlauge zu verdrängen;
    Transportieren der Schnitzel in einem kontinuierlichen Strom zu einem Aufschließer (33);
    Hindurchbewegen der Schnitzel durch den Aufschließer (33) mit einer Geschwindigkeit, einer Temperatur und einem Druck zum Erreichen der gewünschten Entlignifizierung, während die Schnitzel in dem Aufschließer (33) sind;
    Rezirkulieren von heißer Schwarzlauge in dem Aufschließer und Ableiten eines Teils derselben zur weiteren Verwendung in der zweiten Kammer (21);
    Verdrängen von Lauge aus dem aufgeschlossen Zellstoff unter Verwendung einer Lauge niedrigerer Temperatur und Fördern der Lauge in die erste Kammer (10);
    separates Sammeln von Lauge mäßiger Temperatur und von Lauge hoher Temperatur, die in dem Prozeß verdrängt und während der Laugenumwälzschritte abgeleitet worden sind; und
    Entfernen von aufgeschlossenem Zellstoff aus dem Aufschließer (33), nachdem er der Einwirkung der Weißlauge für eine vorbestimmte Zeit ausgesetzt gewesen ist.
  8. Verfahren zum Behandeln von Celluloseholzschnitzeln in einem kontinuierlichen Aufschließprozeß bei hohem Druck und hoher Temperatur für die Freisetzung von Zellstoff gemäß den Schritten nach Anspruch 7:
    beinhaltend das Fördern des aufgeschlossenen Zellstoffes in einen Wascher und Verwenden der Waschlauge als die Flüssigkeit niedriger Temperatur.
  9. Verfahren zum Behandeln von Celluloseholzschnitzeln in einem kontinuierlichen Aufschließprozeß bei hohem Druck und hoher Temperatur für die Freisetzung von Zellstoff gemäß den Schritten nach Anspruch 7:
    beinhaltend das Rezirkulieren der Schwarzlauge in der ersten Kammer (10) über einer vorbestimmten Zeit, um die Schnitzel vorzuwärmen und chemisch vorzukonditionieren.
  10. Verfahren zum Behandeln von Celluloseholzschnitzeln in einem kontinuierlichen Aufschließprozeß bei hohem Druck und hoher Temperatur für die Freisetzung von Zellstoff gemäß den Schritten nach Anspruch 7:
    beinhaltend das Verwenden der heißen Schwarzlauge zum Vorwärmen der Weißlauge.
  11. Verfahren zum Behandeln von Celluloseholzschnitzeln in einem kontinuierlichen Aufschließprozeß bei hohem Druck und hoher Temperatur für die Freisetzung von Zellstoff gemäß den Schritten nach Anspruch 7:
    beinhaltend das Entfernen der Schwarzlauge aus der ersten Kammer (10) zum Nachbearbeiten der Lauge.
  12. Verfahren zum Behandeln von Celluloseholzschnitzeln in einem kontinuierlichen Aufschließprozeß bei hoem Druck und hoher Temperatur für die Freisetzung von Zellstoff gemäß den Schritten nach Anspruch 7:
    beinhaltend das Umwälzen der heißen Schwarzlauge in der zweiten Kammer (21).
EP90914988A 1989-09-28 1990-09-25 Heizung mit verschiebung in kontinuierlichen zellstoffkochern Expired - Lifetime EP0502852B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US41392089A 1989-09-28 1989-09-28
US413920 1989-09-28

Publications (2)

Publication Number Publication Date
EP0502852A1 EP0502852A1 (de) 1992-09-16
EP0502852B1 true EP0502852B1 (de) 1993-11-03

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EP (1) EP0502852B1 (de)
JP (1) JPH0674557B2 (de)
KR (1) KR0171423B1 (de)
CN (1) CN1021980C (de)
CA (1) CA2066181C (de)
DE (1) DE69004438T2 (de)
ES (1) ES2045948T3 (de)
FI (1) FI921373A7 (de)
NO (1) NO179016C (de)
WO (1) WO1991005103A2 (de)

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CN103080417A (zh) * 2010-07-07 2013-05-01 斯托拉恩索公司 由黑液制造沉淀木质素的方法和通过这种方法制造的沉淀木质素
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CN102154398A (zh) * 2010-12-28 2011-08-17 国润金华（北京）国际能源投资有限公司佛山高明分公司 一种高温高压纤维素转糖工艺
CN103597139B (zh) * 2011-03-25 2016-03-30 S·L·凯斯瓦尼 用于自横管式连续蒸煮器提取黑液的方法和系统
CN102154874B (zh) * 2011-04-29 2012-11-21 白福安 一种置换蒸煮制浆方法
CN102797189A (zh) * 2012-08-11 2012-11-28 李肥生 两段式自加热螺旋结构蒸煮分离器
US9644317B2 (en) * 2014-11-26 2017-05-09 International Paper Company Continuous digester and feeding system
FR3039567A1 (fr) 2015-07-31 2017-02-03 Commissariat Energie Atomique Dispositif et procede de traitement de la liqueur noire provenant de la preparation de pate a papier par liquefaction hydrothermale
CN108867131A (zh) * 2016-12-20 2018-11-23 常州爱上学教育科技有限公司 用于制浆造纸的木、竹原料节能环保置换蒸煮工艺
KR102295018B1 (ko) 2019-09-11 2021-08-30 한병엽 포장용기 자동 주문발주 장치
KR102490233B1 (ko) 2020-11-24 2023-01-18 한병엽 포스 장치, 포스 장치의 주문 정보 처리방법, 기록매체

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JPS6059189A (ja) * 1983-08-24 1985-04-05 ベロイト　コ−ポレ−ション 多段式木材チツプ蒸解法
FI71176C (fi) * 1983-11-30 1991-12-03 Ekono Oy Foerfarande foer framstaellning av cellulosa med satsvis kokning.
JP6347836B2 (ja) 2014-07-10 2018-06-27 国立大学法人大阪大学 脚相移行タイミング判定方法、脚相移行タイミング判定装置、歩行支援制御方法及び歩行支援装置

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EP0502852A1 (de) 1992-09-16
FI921373A0 (fi) 1992-03-27
CN1050579A (zh) 1991-04-10
JPH0674557B2 (ja) 1994-09-21
NO920630L (no) 1992-02-18
CN1021980C (zh) 1993-09-01
NO179016C (no) 1996-07-17
CA2066181C (en) 1995-09-26
FI921373A7 (fi) 1992-03-27
CA2066181A1 (en) 1991-03-29
WO1991005103A3 (en) 1991-05-16
JPH05503739A (ja) 1993-06-17
DE69004438D1 (de) 1993-12-09
KR0171423B1 (ko) 1999-05-01
ES2045948T3 (es) 1994-01-16
NO920630D0 (no) 1992-02-18
NO179016B (no) 1996-04-09
KR920703920A (ko) 1992-12-18
WO1991005103A2 (en) 1991-04-18
DE69004438T2 (de) 1994-05-11

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