WO1995035410A1 - Procede de lavage du gaz resultant de la gazeification de la liqueur noire - Google Patents

Procede de lavage du gaz resultant de la gazeification de la liqueur noire Download PDF

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Publication number
WO1995035410A1
WO1995035410A1 PCT/SE1995/000586 SE9500586W WO9535410A1 WO 1995035410 A1 WO1995035410 A1 WO 1995035410A1 SE 9500586 W SE9500586 W SE 9500586W WO 9535410 A1 WO9535410 A1 WO 9535410A1
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WO
WIPO (PCT)
Prior art keywords
gas
stage
liquid bath
liquid
process according
Prior art date
Application number
PCT/SE1995/000586
Other languages
English (en)
Inventor
Bengt Nilsson
Original Assignee
Kvaerner Pulping Ab
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Kvaerner Pulping Ab filed Critical Kvaerner Pulping Ab
Priority to AU28112/95A priority Critical patent/AU2811295A/en
Priority to CA002193516A priority patent/CA2193516C/fr
Priority to BR9508080A priority patent/BR9508080A/pt
Priority to JP8502006A priority patent/JPH10504607A/ja
Publication of WO1995035410A1 publication Critical patent/WO1995035410A1/fr
Priority to US08/764,603 priority patent/US6113739A/en
Priority to FI965088A priority patent/FI118899B/fi
Priority to US09/096,506 priority patent/US6062547A/en

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Classifications

    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters
    • D21C11/12—Combustion of pulp liquors
    • D21C11/125—Decomposition of the pulp liquors in reducing atmosphere or in the absence of oxidants, i.e. gasification or pyrolysis
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters
    • D21C11/0064—Aspects concerning the production and the treatment of green and white liquors, e.g. causticizing green liquor
    • D21C11/0071—Treatment of green or white liquors with gases, e.g. with carbon dioxide for carbonation; Expulsion of gaseous compounds, e.g. hydrogen sulfide, from these liquors by this treatment (stripping); Optional separation of solid compounds formed in the liquors by this treatment
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters
    • D21C11/06—Treatment of pulp gases; Recovery of the heat content of the gases; Treatment of gases arising from various sources in pulp and paper mills; Regeneration of gaseous SO2, e.g. arising from liquors containing sulfur compounds
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Definitions

  • the present invention relates to a process for recovering of chemicals and energy from black liquor which is obtained during paper pulp production by means of chemical digestion of fibre raw material.
  • a spent liquor generally termed black liquor
  • black liquor which contains organic material and the residual chemicals which have been obtained when cooking the fibre raw material.
  • this black liquor is evaporated and conveyed to a separate process for recovering of the energy content of the organic material and recovering the cooking chemicals as so-called green liquor.
  • Tomlinson process has been the com ⁇ flashally dominant method used for this recovery of energy and chemicals.
  • a disadvantage of this process which is now very old, is that it requires very large combustion ovens which are complicated both from the technical point of view and as regards their operation.
  • Swedish patent SE 448,173 describes a more recent process which, besides requiring process equip ⁇ ment which is appreciably simplified, achieves an improved recovering of both energy and chemicals.
  • This process is based on a pyrolysis reaction in which the black liquor is gasified in a reactor, resulting in the formation of an energy-rich gas, principally comprising carbon monoxide, carbon dioxide, methane, hydrogen and hydrogen sulphide, and of inorganic chemicals in the form of small drops of smelt, principally comprising sodium carbonate, sodium hydroxide and sodium sulphide.
  • the resulting mixture of gas and smelt drops is rapidly cooled, in a first stage, by means of direct contact with a cooling liquid consisting of water and green liquor, which is formed when the smelt chemicals and hydrogen sulphide dissolve in the cooling liquid.
  • the gas is subsequently washed, in a second stage, in a gas-washing apparatus of the scrubber type.
  • the gas is then used as a fuel for generating steam and/or electric power.
  • the physical calorific value of the gas can also be utilized when the gas is cooled down from the gasification temperature to the saturation temperature for aqueous steam at the selected pressure. At a saturation temperature of 200°C, corresponding to 40 bar, for example, steam having a pressure of 3-8 bar can be generated when the green liquor is cooled and when the gas is cooled and its water content is condensed downstream of the gas-washing tower.
  • the present invention is a further development of the concept of SE 448,173 and effectively eliminates the disadvantages associated with this known technique.
  • the concept behind the method which has been devised is to bring about the possibility of producing green liquor without unwanted hydrogen carbonate being formed in this liquor, and to bring about the possi- bility of optimally utilizing the content of thermal energy and the steam-formation heat in the gas, at the same time as the content of small particles, so-called fumes or microsolids, in the gas is efficiently separated off.
  • the principle is that the gas/smelt mixture which leaves the reactor is cooled, in a first stage, by means of direct contact with a cooling liquid which principally consists of water in the form of condensate.
  • the gas washing in the second stage is configured so that the maximum degree of thorough contact is achieved between the gas and the washing liquid, which principally consists of water in the form of condensate.
  • this object is achieved by means of quenching in two stages, with the gas in the first quenching stage not being permitted to bubble through the liquid bath of green liquor which has collected in the bottom of the vessel.
  • the gas is washed by being allowed to bubble through a second liquid bath which principally consists of water in the form of condensate. In this way, the hot gas is efficiently purified and saturated with moisture.
  • Energy in the form of condensation heat and thermal energy is then preferably recovered from the hot, moisture-saturated gas by using a countercurrent indirect condenser.
  • a countercurrent falling-film condenser for example, it is possible efficiently to generate high- quality steam, preheat feed water and produce warm water in a single unit.
  • the small particles, microsolids principally consisting of sodium carbonate, which are contained in the gas function as condensation nuclei in the condenser and are therefore efficiently separated out of the gas, and collected and dissolved in the condensate.
  • Figure 1 shows a preferred embodiment of the concept according to the invention.
  • Figure 2 shows a preferred embodiment for recovering energy from combustion gas by means of indirect countercurrent cooling.
  • FIG 3 shows an embodiment of the invention where the two quenching stages are accommodated in the same vessel.
  • Detail number 1 in Figure 1 indicates a pressure vessel which contains a ceramically lined gasification reactor 2.
  • the reactor is provided with an inlet 3 for black liquor and an inlet 4 for oxygen or oxygen-containing gas, and a burner (not shown) .
  • the opening at the bottom of the reactor chamber is in the form of a chute 5, which opens out directly above the surface of the liquid in a green liquor liquid chamber 6 which is situated below.
  • a number of nozzles 7 for cooling liquid open out into the chute.
  • Green liquor which is produced is transported from the chamber 6 through a conduit 8, via a pump 9 and a heat exchanger 10, to subsequent process stages for generating white liquor, or to another process stage in which green liquor is employed.
  • the combustion gas from the first vessel is conveyed through a conduit 11 to a second pressure vessel 12 for gas treatment and energy recovering.
  • This conduit 11 opens out in the pressure vessel 12 under the surface of the liquid in a washing liquid chamber 13 at the bottom of the vessel.
  • An indirect condenser of the countercurrent falling-film condenser type 16 is located above the chamber 13.
  • An outlet 17 for cooled combustion gas is located at the top of the second pressure vessel 12.
  • the liquid in the washing liquid chamber of the second vessel can be conveyed, through a conduit 14 via a pump 15, to the first vessel in order to serve as diluting liquid or as cooling liquid which is provided via the spray nozzles 7.
  • Feed water for generating steam is supplied to the condenser 16 via a conduit 18, and steam which is produced exits via a conduit 19. (The recovery of energy is shown in more detail in Figure 2.)
  • Cold water is supplied to the upper part of the condenser via a conduit 20, and warm water which is produced exits via conduit 21. Water which is added to maintain liquid balance is supplied to the system via a conduit 22.
  • the product resulting from flash pyrolysis carried out in the presence of an understoichiometrie quantity of oxygen principally consists of a mixture of gaseous hydrogen, carbon monoxide, carbon dioxide, aqueous steam and hydrogen sulphide, and also smelt drops of sodium carbonate, sodium hydroxide and sodium sulphide, at a temperature of approximately 950°C and at an absolute pressure of 26 bar.
  • the velocity of the gas is high, and this helps to transfer the smelt drops, some of which form a film on the reactor walls, to the green liquor liquid chamber 6, which is arranged below the gasification reactor 2.
  • the outlet from the reactor consists of a chute 5 into which cooling liquid is sprayed through a number of nozzles 7 in order to achieve maximum contact with the smelt/gas mixture.
  • the cooling liquid principally consists of water, some of which water will be evaporated when it makes contact with the hot gas and the smelt at the reactor temperature.
  • the smelt drops and the smelt film along the reactor walls dissolve in the remaining part of the cooling liquid and thereby form green liquor, which falls down into the liquid chamber 6.
  • the smelt drops fall down directly into the liquid chamber 6 and only then dissolve in the green liquor which is already present in this location.
  • the smelt drops are then cooled by the evaporation of water in the green liquor bath.
  • the chute 5 opens out directly above the level of the liquid in the liquid chamber 6. This is very important in order to avoid a high degree of contact between the gas and the green liquor which is formed. If the chute had opened out below the surface of the liquid, the gas would have been forced to bubble through the green liquor, as a consequence of which hydrogen carbonate would have been formed by means of reaction between carbon dioxide present in the gas and sodium hydroxide and sodium carbonate present in the green liquor.
  • the temperature after cooling is controlled by the operating pressure which has been selected and is related to the temperature of the saturated steam at this pressure. Thus, at an operating pressure of 26 bar, the green liquor and the gas can be expected to have an equilibrium temperature of 200°C in the cooling stage if the steam partial pressure is 60%.
  • the green liquor leaves the first pressure vessel 1 through a conduit 8, and is pumped, using a pump 9, through a heat exchanger 10, in which heat energy is recovered from the green liquor by cooling the latter.
  • a minor part of the green liquor is employed for wetting the inside of the chute 5 by means of being returned to the chute and being permitted to form a thin film on the inside of the chute.
  • Stage 2 Gas washing.
  • the cooled gas which is partially saturated with moisture, leaves the first vessel 1 via a conduit 11, which opens out in the second vessel 12.
  • the conduit 11 opens out in the form of a liquid seal, consisting of a chute and an ascending pipe, under the surface of the liquid in the washing liquid chamber 13, which is located at the very bottom of the vessel.
  • the temperature of the washing liquid bath 13, and of the gas which leaves the bath is, in the main, the same as the temperature in the green liquor liquid chamber 6 in the first vessel 1. This makes it possible to achieve a high partial pressure of steam in the combustion gas.
  • the washing liquid in the liquid chamber 13 is returned to the first vessel 1 through a conduit 14 in order to provide diluting liquid for the green liquor in the liquid chamber 6, or in order to provide the cooling liquid which is sprayed into the chute 5 via the nozzles 7.
  • the gas leaves the system in a flow 17. Any sulphur-containing compounds which may remain are subsequently washed out of the gas using an alkaline washing liquid, for example sodium carbonate.
  • Stage 3 - Energy recovery shows the concept for recovering energy, in accordance with the invention, in a preferred embodiment at a system pressure of 26 bar.
  • the principle is based on using a countercurrent falling-film condenser 16, which is installed above the washing liquid bath 13 in the second pressure vessel 12.
  • the moisture-saturated gas, at a temperature of 200°C, which leaves the washing liquid bath 13 is caused to condense as a result of indirect heat transfer to pre-heated feed water 23 at a temperature of approximately 180°C.
  • This causes the feed water to volatilize, and the resulting steam, at approximately 10 bar of excess pressure and approximately 184°C, can leave the system, via a steam dome 24, in a flow 25 so that it can be used elsewhere in the mill.
  • the feed water reaches a temperature of approximately 180°C and can be used, after having passed though the steam dome 24, for generating steam as described above.
  • the temperature of the gas is approximately 80°C, and the remaining calorific value down to approximately 30°C can be utilized in the same condenser unit for generating warm water.
  • cold water enters the condenser, through a conduit 20, at approximately 15°C and leaves the condenser, through a conduit 21, at approximately 70°C.
  • Water which is added in order to balance the loss of liquid from the system, inter alia in the form of green liquor 8 which is removed, is supplied, in a quantity of approximately 2.1 m 3 per ton of pulp, to the upper part of the condenser in a flow 22. This water is heated to 200°C by the countercurrent procedure before it joins the condensate in the washing liquid chamber 13.
  • the heat of evaporation from the cooling stage in the first vessel is fully utilized as condensation heat in the second vessel.
  • a countercurrent condensor gives higher condensate temperature, greater flow and consequently larger steam production, when compared to a concurrent condensor.
  • a high thermal level, which makes it possible to generate high-quality steam, is based on the principle that the gas is washed, in the second stage, in its "own" hot condensate. Returning this condensate to the cooling stage also allows 90-100% of the cooling requirement for smelt/gas from the reactor to consist of evaporation heat.
  • Moisture-saturated combustion gas contains approximately four times more aqueous steam than gas when the comparison is made on the basis of specific volume. This means, as a result of the countercurrent procedure, that while the steam/gas mixture has a velocity of approximately 10 m/s, for example, on entry into the condenser, the velocity of the gas decreases as the moisture condenses out, so that the velocity on leaving the condenser is approximately 4-5 m/s. This makes it easier for drops which are being carried along by the gas to separate out.
  • the 0.01-1.0 ⁇ -sized small particles, so-called microsolids or fumes, which still remain within the gas and which are otherwise extremely difficult to separate out, are utilized as condensation nuclei, thereby rendering it possible to separate out these particles.
  • the low gas velocity, which is required in accordance with the countercurrent principle, provides these virtually hydrophobic particles with a longer dwell time for wetting than is usually the case when cooling is carried out in accordance with the concurrent principle.
  • a further advantage of the countercurrent procedure is that the susceptible lower cooling surfaces in the condenser, which are inclined to become smeared, are kept free from any coating by being flushed at high temperature with the whole of the condensate flow.
  • a compact, multifunctional gas treatment tower having a single location for collecting condensate constitutes, as regards apparatus construction and control and regulation of the process, a substantial simplification as compared with the conventional concept.
  • the gasification temperature in the reactor can be 500-1,600°C, preferably 700-1,300°C and more preferably 800-1,000°C
  • the system pressure can be up to 150 bar absolute pressure, preferably 21- 50 bar
  • atmospheric pressure is also conceivable even if it is then not possible to generate high-quality steam.
  • the level of the temperature of the condensate and the green liquor should be as high as possible, this level is limited by the saturation temperature at each given system pressure.
  • the temperature can, for example, be approximately 170- 260°C if the system pressure is 21-50 bar and the partial pressure of steam in the cooling stage in the first vessel is approximately 35-90%. At, for example, a partial pressure of steam of 83%, and 26 bar absolute pressure, the temperature is 216°C.
  • water for maintaining the liquid balance can also be supplied directly to the condensate, for example to the conduit 14.
  • the condenser 16 does not need to be accom ⁇ modated in the same vessel as the washing liquid bath 13, even if this is advantageous, and, instead, cooling and condensation of the moisture-saturated gas can be carried out in a separate condenser, with the condensate from this condenser being returned to the vessel which contains the washing liquid bath 13.
  • this separate condenser can consist of a conventional condenser, which is not a countercurrent falling-film condenser, which naturally results in the advantages accruing from using the latter condenser not being achieved.
  • the design of the two quenchers/rapid cooling baths, with chute and liquid bath can be configured in different ways as regards apparatus construction.
  • dry separation can be effected in the first vessel 1 by means of the smelt drops being allowed to fall down into the cooling bath 6 without cooling liquid being sprayed into the stream of smelt drops.
  • the gas is then conducted away from the stream of smelt drops, and the cooling liquid is instead sprayed directly into this gas stream, with any drops of smelt which have been carried along being dissolved and falling down into the cooling bath.
  • the quench can be designed to achieve an unlimited mammoth pump effect, that is to say with a possibility for the gas to lift the liquid, thereby achieving a good circulation and washing effect.
  • a so-called Venturi quench can be utilized in one or both quenching stages, where appropriate with a diverter screen.
  • an extra gas treatment step could for example consist of a Venturi scrubber with wash liquid being supplied from the second liquid bath 13. Utilization of such a Venturi scrubber enhances the separation of microsolids or fumes in the gas stream.
  • the two liquid baths 6 and 13 can also be accommodated in one and the same vessel, where they are separated, for example, by means of an intermediate wall.
  • One possibility is to use a horisontal pressure vessel with an intermediate wall for the two liquid baths 6 and 13. The vertical pressure vessel 1, containing the reactor 2, would then be joined to the horisontal vessel at one end and the vertical pressure vessel 12, containing the condensor 16, at the other end.
  • FIG. 3 Another possibility of accommodating the two liquid baths 6 and 13 in one and the same vessel is shown in Figure 3.
  • the green liquor liquid bath 6 is located around the centre of the vertical axis of the upright vessel containing the reactor 1.
  • the gas is forced to pass through the liquid in the washing liquid bath 13, which is located around the periphery of the vessel.
  • the two liquid baths are completely separated from each other by an intermediate wall and a number of extra, concentrically arranged walls 26, which extend down into the washing liquid bath 13, serve, together with a diverter screen 27, as a ulti stage mammoth pump for forcing of the gas through the liquid.
  • the washing liquid bath 13 principally consists of water in the form of condensate
  • the liquid bath 13 could consist of a green liquor of a different type than the green liquor in the first liquid bath 6.
  • This different type of green liquor would in that case, due to the intense contact with the gas, contain greater amounts of sodium hydrogen carbonate and sodium hydrogen sulfide, which means that it, for example, can be used for subsequent extracting of H 2 S and CO 2 •
  • the concept of the invention can also be applied in relation to the recovery of chemicals in processes involving completely different types of spent liquors and recovered chemicals, for example bleaching plant spent liquors, spent liquors from the production of semi-chemical pulp, for example CTMP, or spent liquors from a pulp process which is founded on using potassium as the base in place of sodium.
  • the concept of the invention can also be applied when utilizing increased partial pressure of H 2 S in the reactor with moved equlibrium (see SE 468 600) and Na 2 S-production as a result.

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  • Paper (AREA)
  • Treating Waste Gases (AREA)
  • Polysaccharides And Polysaccharide Derivatives (AREA)

Abstract

Procédé de récupération de produits chimiques et d'énergie contenus dans de la liqueur noire consistant à la gazéifier en CO, CO2, CH4, H2, et H2S, sous forme gazeuse et en Na2CO3, NaOH et Na2S sous forme de gouttelettes fondues. Le mélange de gaz et de gouttelettes est ensuite refroidi dans une première étape par contact direct avec un liquide de refroidissement lequel est ensuite partiellement volatilisé tandis que les gouttelettes sont séparées et dissoutes dans le reliquat du liquide de refroidissement de façon à former un bain liquide (6) de liqueur verte. Dans une seconde étape, le gaz est lavé puis saturé en humidité par contact direct avec le bain liquide de lavage (13). Après quoi l'énergie thermique et la chaleur de condensation du gaz sont récupérées dans un condenseur indirect (16). Le contact entre le gaz et le bain liquide (6) de liqueur verte de la première étape est sensiblement moindre que celui entre le gaz et le bain liquide (13) de lavage de la deuxième étape car dans la première étape, le gaz ne peut pas bouillonner dans le bain liquide (6) de liqueur verte, tandis qu'il le peut dans le bain liquide (13) de lavage pendant la deuxième étape.
PCT/SE1995/000586 1994-06-22 1995-06-15 Procede de lavage du gaz resultant de la gazeification de la liqueur noire WO1995035410A1 (fr)

Priority Applications (7)

Application Number Priority Date Filing Date Title
AU28112/95A AU2811295A (en) 1994-06-22 1995-06-15 Process for washing gas formed by gasifying black liquor
CA002193516A CA2193516C (fr) 1994-06-22 1995-06-15 Procede de lavage du gaz resultant de la gazeification de la liqueur noire
BR9508080A BR9508080A (pt) 1994-06-22 1995-06-15 Processo para a recuperação de produtos quimicos e de energia do licor negro
JP8502006A JPH10504607A (ja) 1994-06-22 1995-06-15 黒液をガス化させることによって形成されたガスの洗浄法
US08/764,603 US6113739A (en) 1995-06-15 1996-12-11 Process for washing gas formed by gasifying black liquor
FI965088A FI118899B (fi) 1994-06-22 1996-12-18 Menetelmä mustalipeää kaasuttamalla muodostetun kaasun pesemiseksi
US09/096,506 US6062547A (en) 1994-06-22 1998-06-12 Quench vessel for recovering chemicals and energy from spent liquors

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SE9402197-9 1994-06-22
SE9402197A SE502038C2 (sv) 1994-06-22 1994-06-22 Förfarande för tvättning och kylning av gaser vid förgasning av svartlut

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US08/764,603 Continuation US6113739A (en) 1994-06-22 1996-12-11 Process for washing gas formed by gasifying black liquor

Publications (1)

Publication Number Publication Date
WO1995035410A1 true WO1995035410A1 (fr) 1995-12-28

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ID=20394481

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Application Number Title Priority Date Filing Date
PCT/SE1995/000586 WO1995035410A1 (fr) 1994-06-22 1995-06-15 Procede de lavage du gaz resultant de la gazeification de la liqueur noire

Country Status (7)

Country Link
JP (1) JPH10504607A (fr)
AU (1) AU2811295A (fr)
BR (1) BR9508080A (fr)
CA (1) CA2193516C (fr)
FI (1) FI118899B (fr)
SE (1) SE502038C2 (fr)
WO (1) WO1995035410A1 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1998048102A1 (fr) * 1997-04-24 1998-10-29 Kvaerner Pulping Ab Separation des metaux alcalins d'une liqueur noire gazeifiee
US6062547A (en) * 1994-06-22 2000-05-16 Kvaerner Pulping Ab Quench vessel for recovering chemicals and energy from spent liquors
WO2000060161A1 (fr) * 1999-04-01 2000-10-12 Chemrec Aktiebolag Procede de refroidissement d'un materiau solide et gazeux pendant la gazeification de la liqueur epuisee
WO2000060163A1 (fr) * 1999-04-01 2000-10-12 Chemrec Aktiebolag Appareil permettant de gazeifier une liqueur épuisée
WO2000075421A1 (fr) * 1999-06-07 2000-12-14 Chemrec Aktiebolag Dispositif de gazeification d'une liqueur epuisee
CN103306154A (zh) * 2012-03-15 2013-09-18 秦才东 制浆黑液的处理及利用方法

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6030493A (en) 1994-11-04 2000-02-29 Kvaerner Pulping, Ab Process for recovering chemicals and energy from cellulose spent liquor using multiple gasifiers
SE535117C2 (sv) * 2010-03-30 2012-04-17 Chemrec Ab Förgasning av sulfittjocklut

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4808264A (en) * 1985-06-03 1989-02-28 Kignell Jean Erik Process for chemicals and energy recovery from waste liquors
WO1994020677A1 (fr) * 1993-03-11 1994-09-15 Kvaerner Pulping Technologies Ab Procede de separation de composes de soufre

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4808264A (en) * 1985-06-03 1989-02-28 Kignell Jean Erik Process for chemicals and energy recovery from waste liquors
WO1994020677A1 (fr) * 1993-03-11 1994-09-15 Kvaerner Pulping Technologies Ab Procede de separation de composes de soufre

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6062547A (en) * 1994-06-22 2000-05-16 Kvaerner Pulping Ab Quench vessel for recovering chemicals and energy from spent liquors
WO1998048102A1 (fr) * 1997-04-24 1998-10-29 Kvaerner Pulping Ab Separation des metaux alcalins d'une liqueur noire gazeifiee
WO2000060161A1 (fr) * 1999-04-01 2000-10-12 Chemrec Aktiebolag Procede de refroidissement d'un materiau solide et gazeux pendant la gazeification de la liqueur epuisee
WO2000060163A1 (fr) * 1999-04-01 2000-10-12 Chemrec Aktiebolag Appareil permettant de gazeifier une liqueur épuisée
US6790246B1 (en) 1999-04-01 2004-09-14 Chemrec Aktiebolag Apparatus for gasification of spent liquor
US7217302B1 (en) 1999-04-01 2007-05-15 Chemrec Aktiebolag Process for cooling solid and gaseous material during gasification of spent liquor
WO2000075421A1 (fr) * 1999-06-07 2000-12-14 Chemrec Aktiebolag Dispositif de gazeification d'une liqueur epuisee
US6780211B1 (en) 1999-06-07 2004-08-24 Chemrec Aktiebolag Device for gasification of spent liquor
CN103306154A (zh) * 2012-03-15 2013-09-18 秦才东 制浆黑液的处理及利用方法

Also Published As

Publication number Publication date
CA2193516C (fr) 2005-02-08
BR9508080A (pt) 1997-09-02
FI118899B (fi) 2008-04-30
SE9402197D0 (sv) 1994-06-22
FI965088A0 (fi) 1996-12-18
AU2811295A (en) 1996-01-15
CA2193516A1 (fr) 1995-12-28
FI965088A (fi) 1996-12-18
SE9402197L (sv) 1995-07-24
SE502038C2 (sv) 1995-07-24
JPH10504607A (ja) 1998-05-06

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