EP0207062A1 - Pressurized pulp chlorination, and chlorine introduction in minute bubbles - Google Patents
Pressurized pulp chlorination, and chlorine introduction in minute bubbles Download PDFInfo
- Publication number
- EP0207062A1 EP0207062A1 EP86890168A EP86890168A EP0207062A1 EP 0207062 A1 EP0207062 A1 EP 0207062A1 EP 86890168 A EP86890168 A EP 86890168A EP 86890168 A EP86890168 A EP 86890168A EP 0207062 A1 EP0207062 A1 EP 0207062A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- mixer
- chlorine gas
- slurry
- pressure
- retention vessel
- Prior art date
- Legal status (The legal status 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 status listed.)
- Granted
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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
- 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
Definitions
- chlorine is injected through nozzles into a mixer, and then is passed to a retention vessel which is at approximately atmospheric pressure. During the residence of the pulp in the mixer and the retention vessel the chlorine reacts with impurities and encrustants (such as lignin and bark) in the pulp slurry, to effect desired bleaching or delignification.
- impurities and encrustants such as lignin and bark
- a method and apparatus are provided for significantly enhancing the efficiency and efficacy of the treatment of comminuted cellulosic fibrous material slurries with chlorine gas, particularly for the bleaching or delignification of chemical pulps.
- the pressure within the mixer and/or the retention vessel is increased, such as to the range of about 15-150 psig, the solubility of the chlorine gas increases.
- the chlorine gas has a tendency to take the form of minute bubbles thus increasing the overall reactivity area, and the network of interlocked fibers at this pressure inhibits the coalescence of gas bubbles.
- the chlorine gas is introduced into the mixer through porous material discs, such as porous ceramic discs or porous sintered metal discs having a pore size of about 5-175 microns, so that from the time of introduction the chlorine is in the form of minute bubbles.
- porous material discs such as porous ceramic discs or porous sintered metal discs having a pore size of about 5-175 microns
- the improvements in solubility of the chlorine gas in the pulp slurry that are achieved according to the present invention result in a number of beneficial effects, including decreased overall chemical consumption, use of more chlorine relative to chlorine dioxide (which is also added during treatment, and which is more costly than chlorine gas), decreased volume of slurry in the retention vessel, treatment to lower Kappa numbers, less chemical wastage, and decreased consumption of bleaching agents in subsequent stages.
- the present invention it is preferred to intimately mix the chlorine gas with the pulp slurry in a fluidizing mixer, the pulp having a consistency of about 2.5-16%, and preferably about 7-12%, and then pass the slurry through a discharge line into a retention vessel.
- a throttling valve is utilized to throttle the discharge and thereby increase the pressure within the mixer and maintain it at the range of about 15-150 psig (1 to 10 bar above atmospheric pressure).
- a similar throttling valve is placed at the discharge of the retention vessel to also maintain the pressure therewithin within the range of 15-150 psig (1 to 10 bar above atmospheric pressure).
- the chlorine gas when introduced into the mixer is introduced through porous material discs so as to be in the form of minute bubbles.
- the invention is applicable to a wide variety of procedures for the treatment of comminuted cellulosic fibrous material slurries with chlorine gas.
- the invention is useful as the first stage of a multistate bleach feed in the bleaching of deciduous wood chemical pulps, coniferous wood chemical pulps, mixtures of chemical pulps, and non-wood fibrous chemical pulps; as the first stage of a delignification procedure as a stage subsequent to an initial delignification using oxygen; and in like bleaching, delignification, and related procedures.
- Chemical pulp is provided in a conventional bleach feed storage tank 10, the pulp being introduced therein through an inlet 11, and being pumped from the bottom of the tank 10 utilizing a conventional fluidizing centrifugal pump 12, such as the type shown in U.S. Patent 4,435,193.
- the pulp has a consistency of about 2.5-16%, preferable 3.5-13%, and most preferably about 7-12%.
- the temperature of the pulp slurry typically will be from 50°F-160°F (10 to 71 °C), more preferably 80-150°F (27 to 66°C).
- the pulp is pumped in line 13 to conventional fluidizing centrifugal mixer 14.
- the mixer 14 preferably is capable of fluidizing pulp even if it has a consistency up to about 16%, to effectively intimately mix the pulp with chemicals that are added to it within the mixer.
- a form such a mixer 16 might take is shown in Canadian Patent 1102604, and such a mixer also is commercially available from Kamyr, Inc. of Glens Falls, New York and sold under the trademark "MC".
- Chlorine gas from source 15 passes through barometric loop 16' in line 16 and is added to the mixer 14, as is chlorine dioxide from source 17 through line 18.
- the chlorine'gas will have a temperature of about 75°F-140°F (24 to 60°C), and more commonly in the range of about 90°F-125°F (32 to 52°C).
- the pressure at source 15 and in line 16 typically will be in the range of about 60-125 psig (4,1 to 8,6 bar above atmospheric pressure) conventional safety devices, valves, and interlocks will be used with the chlorine gas system.
- Chlorine dioxide from source 17 will typically have a temperature of 35°F-100°F(1,6 to 38°C), more commonly 40°F-55°F (4,4 to 13°C).
- the chlorine dioxide will be added in liquid form, with concentrations ranging from 4-14 gpl, preferably 6-10 gpl.
- Total retention time in the pressurized zone - is about 0.01-60 minutes, preferably about 0.1-20 minutes.
- the invention is particularly applicable to the bleaching of deciduous wood chemical pulps with Kappa numbers in the range of 10-25 (more commonly 15-20), bleaching of coniferous wood chemical pulps with Kappa numbers in the range of 25-150 (more commonly 28-38), bleaching of mixtures of chemical pulps, and bleaching of non-wood fibrous chemical pulps with Kappa numbers in the range of 14-150.
- the pulp is passed to retention vessel 20 and flows upwardly therein with dilution liquid added through introduction structure 21.
- the pulp is discharged by a scraper into the discharge line 23 at the top of the retention vessel, and then passes into a stock line and from that preferably into a pressure diffuser or like vessel at the same pressure, for further retention or washing under pressure.
- the solubility of chlorine in the pulp is significantly increased thus causing more efficient reaction with the impurities in encrustants (such as lignin and bark) on, with, and in the pulp fibers.
- encrustants such as lignin and bark
- the application of pressure favors the production of minute bubbles of chlorine gas, and the network of interlocked fibers coupled with the increased pressure inhibits the coalescence of gas bubbles.
- the end result is decreased overall chemical consumption, decreased degree of substitution of chlorine dioxide for chlorine (chlorine dioxide being more expensive), a decreased volume of slurry in the vessel 20, lower extracted Kappa numbers for the pulp, less chemical wastage, and decreased consumption of bleaching agents in subsequent stages.
- Pressurization of the mixer 14 and vessel 20 is preferably effected utilizing a valve 30 at the discharge from the mixer 14, and a valve 31 at the discharge 23 from the tank 20.
- the valves 30, 31 may be selected from a wide variety of available throttling valves, such as valves having all wetted parts of materials resistant to the corrosive-aggressive conditions that are present.
- the valve 30 may comprise a four inch (100 mm) diameter ball valve
- the valve 31 may comprise an eight inch (200 mm) diameter ball valve.
- Typical throttling ball valves that can be utilized in this regard are available from WKM of Houston, Texas, and are sold under the tradename DynaSeal 350.
- valves 30, 31 are operated, either manually or automatically, to control the pressure within the mixer 14 and/or the tank 20 so that it is within the range of about 15-150 psig (1 to 10 bar above atmospheric pressure) (preferably about 30-120 psig) (2 to 8,3 bar above atmospheric pressure).
- FIGURE 2 shows the chlorine source 15 connected through line 16 to the mixer 14.
- the particular interconnection structures illustrated in FIGURE 2 include the branched connection 40 which has branch conduits 41,42 extending therefrom.
- branch conduit In each branch conduit is disposed a filter 44 and one or more valves 45, and each branch conduit terminates in a chlorine gas injecting nozzle 47.
- Two such structures are utilized in case one malfunctions (in which case it can be closed off and the other utilized until repair is effected), and also to evenly introduce the chlorine gas into the mixer.
- the injection nozzles 47 (any reasonable number of nozzles may be provided) in the embodiment illustrated in FIGURE 2 are connected to the mixer 14 at opposite sides of the circular cross-section pulp inlet portion 50 of the mixer.
- a typical filter 44 is illustrated in FIGURE 3, and includes the solid annular metal body 52 which mounts a circular disc 53 of porous material.
- Typical porous material for the disc 53 include porous ceramics and sintered metals.
- a typical chlorine gas injection nozzle 47 is illustrated in FIGURES 4 and 5 and includes a metal housing including annular flange 55 and annular body 56, with a conical surface 57 formed at the innermost end of the body 56 (the end closest to, or extending into, the mixer 14). Disposed within the body 56 and having a conical surface abutting the conical surface 57 is disc 58.
- the disc 58 comprises means for introducing the chlorine gas in the form of minute bubbles, and comprises a porous material having pore sizes ranging from about 5-175 microns.
- Typical porous materials utilizable for the formation of the disc 50 are conventionally available porous ceramics and porous sintered metals.
- the disc 58 is held in place against the conical surface 57 by the gasket 59, locking ring 60, and locking clip 61.
- the locking ring 60 can be screw- threaded into engagement with the body portion 56 (which has internal threads therein), with the clip 61 engaging the body 56 and the ring 60 to hold them in the position illustrated in FIGURE 4 wherein the ring 60 presses against the gasket 59 and the disc 58.
Abstract
Description
- In typical medium consistency chlorination facilities, such as in the bleaching or delignification of chemical pulps, chlorine is injected through nozzles into a mixer, and then is passed to a retention vessel which is at approximately atmospheric pressure. During the residence of the pulp in the mixer and the retention vessel the chlorine reacts with impurities and encrustants (such as lignin and bark) in the pulp slurry, to effect desired bleaching or delignification.
- According to the present invention, a method and apparatus are provided for significantly enhancing the efficiency and efficacy of the treatment of comminuted cellulosic fibrous material slurries with chlorine gas, particularly for the bleaching or delignification of chemical pulps. According to the present invention it has been found that if the pressure within the mixer and/or the retention vessel is increased, such as to the range of about 15-150 psig, the solubility of the chlorine gas increases. Also at increased pressure the chlorine gas has a tendency to take the form of minute bubbles thus increasing the overall reactivity area, and the network of interlocked fibers at this pressure inhibits the coalescence of gas bubbles. Also, according to the present invention, the chlorine gas is introduced into the mixer through porous material discs, such as porous ceramic discs or porous sintered metal discs having a pore size of about 5-175 microns, so that from the time of introduction the chlorine is in the form of minute bubbles.
- The improvements in solubility of the chlorine gas in the pulp slurry that are achieved according to the present invention result in a number of beneficial effects, including decreased overall chemical consumption, use of more chlorine relative to chlorine dioxide (which is also added during treatment, and which is more costly than chlorine gas), decreased volume of slurry in the retention vessel, treatment to lower Kappa numbers, less chemical wastage, and decreased consumption of bleaching agents in subsequent stages.
- According to the present invention it is preferred to intimately mix the chlorine gas with the pulp slurry in a fluidizing mixer, the pulp having a consistency of about 2.5-16%, and preferably about 7-12%, and then pass the slurry through a discharge line into a retention vessel. At the discharge line from the mixer a throttling valve is utilized to throttle the discharge and thereby increase the pressure within the mixer and maintain it at the range of about 15-150 psig (1 to 10 bar above atmospheric pressure). A similar throttling valve is placed at the discharge of the retention vessel to also maintain the pressure therewithin within the range of 15-150 psig (1 to 10 bar above atmospheric pressure). The chlorine gas when introduced into the mixer is introduced through porous material discs so as to be in the form of minute bubbles.
- It is the primary object of the present invention to provide for the more efficient treatment of comminuted cellulosic fibrous material slurries with chlorine gas. This and other objects of the invention will become clear from an inspection of the
-
- FIGURE 1 is a schematic view of exemplary apparatus according to the present invention, for the bleaching of chemical pulp according to the present invention;
- FIGURE 2 is a detail end view of the front of the mixer of the apparatus of FIGURE 1, showing the interconnection thereof to chlorine gas and chlorine dioxide liquid sources;
- FIGURE 3 is a side cross-sectional view of the
structure 44 of FIGURE 2; - FIGURE 4 is a side cross-sectional view of an
introduction nozzle 47 of FIGURE 2; and - FIGURE 5 is an end view of the nozzle of FIGURE 4.
- The invention is applicable to a wide variety of procedures for the treatment of comminuted cellulosic fibrous material slurries with chlorine gas. In particular the invention is useful as the first stage of a multistate bleach feed in the bleaching of deciduous wood chemical pulps, coniferous wood chemical pulps, mixtures of chemical pulps, and non-wood fibrous chemical pulps; as the first stage of a delignification procedure as a stage subsequent to an initial delignification using oxygen; and in like bleaching, delignification, and related procedures.
- For the purposes of description, the method according to the invention will be described with respect to the chlorine bleaching, along with chlorine dioxide, of chemical pulp, but it is to be understood that the invention has wider appiicabii- ity.
- Chemical pulp is provided in a conventional bleach
feed storage tank 10, the pulp being introduced therein through an inlet 11, and being pumped from the bottom of thetank 10 utilizing a conventional fluidizingcentrifugal pump 12, such as the type shown in U.S. Patent 4,435,193. The pulp has a consistency of about 2.5-16%, preferable 3.5-13%, and most preferably about 7-12%. - The temperature of the pulp slurry typically will be from 50°F-160°F (10 to 71 °C), more preferably 80-150°F (27 to 66°C). The pulp is pumped in
line 13 to conventional fluidizingcentrifugal mixer 14. Themixer 14 preferably is capable of fluidizing pulp even if it has a consistency up to about 16%, to effectively intimately mix the pulp with chemicals that are added to it within the mixer. A form such amixer 16 might take is shown in Canadian Patent 1102604, and such a mixer also is commercially available from Kamyr, Inc. of Glens Falls, New York and sold under the trademark "MC". - Chlorine gas from
source 15 passes through barometric loop 16' inline 16 and is added to themixer 14, as is chlorine dioxide fromsource 17 throughline 18. Typically the chlorine'gas will have a temperature of about 75°F-140°F (24 to 60°C), and more commonly in the range of about 90°F-125°F (32 to 52°C). The pressure atsource 15 and inline 16 typically will be in the range of about 60-125 psig (4,1 to 8,6 bar above atmospheric pressure) conventional safety devices, valves, and interlocks will be used with the chlorine gas system. - Chlorine dioxide from
source 17 will typically have a temperature of 35°F-100°F(1,6 to 38°C), more commonly 40°F-55°F (4,4 to 13°C). The chlorine dioxide will be added in liquid form, with concentrations ranging from 4-14 gpl, preferably 6-10 gpl. - Total retention time in the pressurized zone - (
mixer 14 and/or vessel 20) is about 0.01-60 minutes, preferably about 0.1-20 minutes. - The invention is particularly applicable to the bleaching of deciduous wood chemical pulps with Kappa numbers in the range of 10-25 (more commonly 15-20), bleaching of coniferous wood chemical pulps with Kappa numbers in the range of 25-150 (more commonly 28-38), bleaching of mixtures of chemical pulps, and bleaching of non-wood fibrous chemical pulps with Kappa numbers in the range of 14-150.
- From
mixer 14 the pulp is passed toretention vessel 20 and flows upwardly therein with dilution liquid added throughintroduction structure 21. The pulp is discharged by a scraper into thedischarge line 23 at the top of the retention vessel, and then passes into a stock line and from that preferably into a pressure diffuser or like vessel at the same pressure, for further retention or washing under pressure. - According to the present invention it has been found that by pressurizing the
mixure 14 and/or thevessel 20 the solubility of chlorine in the pulp is significantly increased thus causing more efficient reaction with the impurities in encrustants (such as lignin and bark) on, with, and in the pulp fibers. Also the application of pressure favors the production of minute bubbles of chlorine gas, and the network of interlocked fibers coupled with the increased pressure inhibits the coalescence of gas bubbles. The end result is decreased overall chemical consumption, decreased degree of substitution of chlorine dioxide for chlorine (chlorine dioxide being more expensive), a decreased volume of slurry in thevessel 20, lower extracted Kappa numbers for the pulp, less chemical wastage, and decreased consumption of bleaching agents in subsequent stages. - Pressurization of the
mixer 14 andvessel 20 is preferably effected utilizing avalve 30 at the discharge from themixer 14, and avalve 31 at thedischarge 23 from thetank 20. Thevalves valve 30 may comprise a four inch (100 mm) diameter ball valve, and thevalve 31 may comprise an eight inch (200 mm) diameter ball valve. Typical throttling ball valves that can be utilized in this regard are available from WKM of Houston, Texas, and are sold under the tradename DynaSeal 350. Of course a wide variety of other throttling valves that are commercially available may be utilized. Thevalves mixer 14 and/or thetank 20 so that it is within the range of about 15-150 psig (1 to 10 bar above atmospheric pressure) (preferably about 30-120 psig) (2 to 8,3 bar above atmospheric pressure). - In order to ensure that the chlorine gas, from the time of its introduction, is in the form of minute bubbles, the structures illustrated in FIGURES 2 through 5 preferably are utilized. FIGURE 2 shows the
chlorine source 15 connected throughline 16 to themixer 14. The particular interconnection structures illustrated in FIGURE 2 include thebranched connection 40 which hasbranch conduits filter 44 and one ormore valves 45, and each branch conduit terminates in a chlorinegas injecting nozzle 47. Two such structures are utilized in case one malfunctions (in which case it can be closed off and the other utilized until repair is effected), and also to evenly introduce the chlorine gas into the mixer. The injection nozzles 47 (any reasonable number of nozzles may be provided) in the embodiment illustrated in FIGURE 2 are connected to themixer 14 at opposite sides of the circular cross-sectionpulp inlet portion 50 of the mixer. - A
typical filter 44 is illustrated in FIGURE 3, and includes the solidannular metal body 52 which mounts acircular disc 53 of porous material. Typical porous material for thedisc 53 include porous ceramics and sintered metals. - A typical chlorine
gas injection nozzle 47 is illustrated in FIGURES 4 and 5 and includes a metal housing includingannular flange 55 andannular body 56, with aconical surface 57 formed at the innermost end of the body 56 (the end closest to, or extending into, the mixer 14). Disposed within thebody 56 and having a conical surface abutting theconical surface 57 isdisc 58. Thedisc 58 comprises means for introducing the chlorine gas in the form of minute bubbles, and comprises a porous material having pore sizes ranging from about 5-175 microns. Typical porous materials utilizable for the formation of thedisc 50 are conventionally available porous ceramics and porous sintered metals. - The
disc 58 is held in place against theconical surface 57 by thegasket 59,locking ring 60, andlocking clip 61. Thelocking ring 60 can be screw- threaded into engagement with the body portion 56 (which has internal threads therein), with theclip 61 engaging thebody 56 and thering 60 to hold them in the position illustrated in FIGURE 4 wherein thering 60 presses against thegasket 59 and thedisc 58. - It will thus be seen that according to the present invention a method and apparatus are provided for increasing the efficiency and efficacy of the treatment of comminuted cellulosic fibrous material slurries with chlorine gas. While the invention has been herein shown and described in what is presently conceived to be the most practical and preferred embodiment thereof, it will be apparent to those of ordinary skill in the art that many modifications may be made thereof within the scope of the invention, which scope is to be accorded the broadest interpretation of the appended claims so as to emcompass all equivalent methods and apparatus.
Claims (10)
(c) maintaining the pressure in the retention vessel between about 15 psig -150 psig (1 to 10 bar above atmospheric pressure) to enhance the solubility of chlorine gas in the slurry and thereby enhance the efficiency and/or efficacy of the chlorine treatment.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AT86890168T ATE48452T1 (en) | 1985-06-14 | 1986-06-06 | CHLORINATION OF PULP UNDER PRESSURE AND INTRODUCTION OF CHLORINE IN BUBBLES. |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US74467885A | 1985-06-14 | 1985-06-14 | |
US744678 | 1985-06-14 |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0207062A1 true EP0207062A1 (en) | 1986-12-30 |
EP0207062B1 EP0207062B1 (en) | 1989-12-06 |
Family
ID=24993592
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP86890168A Expired EP0207062B1 (en) | 1985-06-14 | 1986-06-06 | Pressurized pulp chlorination, and chlorine introduction in minute bubbles |
Country Status (9)
Country | Link |
---|---|
EP (1) | EP0207062B1 (en) |
JP (1) | JPS61289192A (en) |
AT (1) | ATE48452T1 (en) |
BR (1) | BR8602738A (en) |
CA (1) | CA1276408C (en) |
DE (1) | DE3667310D1 (en) |
FI (1) | FI85728C (en) |
NO (1) | NO168123C (en) |
SE (1) | SE466459B (en) |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US56833A (en) * | 1866-07-31 | Improvement in bleaching paper-stock | ||
US1971241A (en) * | 1933-04-01 | 1934-08-21 | Pennsylvania Salt Mfg Co | Method of chlorination |
DE1621684A1 (en) * | 1967-10-04 | 1971-07-08 | Bellmer Geb Kg Maschf | Machine combination for the line section in pulp processing plants |
FR2227388A1 (en) * | 1973-04-27 | 1974-11-22 | Mo Och Domsjoe Ab | Bleach tower for wood cellulose slurry - having a device to maintain a pressure difference between the bleach inlet and outlet |
-
1985
- 1985-10-25 CA CA000493830A patent/CA1276408C/en not_active Expired - Fee Related
-
1986
- 1986-05-19 FI FI862082A patent/FI85728C/en not_active IP Right Cessation
- 1986-05-28 NO NO862116A patent/NO168123C/en unknown
- 1986-06-04 JP JP61128270A patent/JPS61289192A/en active Pending
- 1986-06-06 DE DE8686890168T patent/DE3667310D1/en not_active Expired - Fee Related
- 1986-06-06 EP EP86890168A patent/EP0207062B1/en not_active Expired
- 1986-06-06 AT AT86890168T patent/ATE48452T1/en not_active IP Right Cessation
- 1986-06-10 SE SE8602592A patent/SE466459B/en not_active IP Right Cessation
- 1986-06-11 BR BR8602738A patent/BR8602738A/en not_active IP Right Cessation
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US56833A (en) * | 1866-07-31 | Improvement in bleaching paper-stock | ||
US1971241A (en) * | 1933-04-01 | 1934-08-21 | Pennsylvania Salt Mfg Co | Method of chlorination |
DE1621684A1 (en) * | 1967-10-04 | 1971-07-08 | Bellmer Geb Kg Maschf | Machine combination for the line section in pulp processing plants |
FR2227388A1 (en) * | 1973-04-27 | 1974-11-22 | Mo Och Domsjoe Ab | Bleach tower for wood cellulose slurry - having a device to maintain a pressure difference between the bleach inlet and outlet |
Non-Patent Citations (7)
Title |
---|
ABSTRACT BULLETIN OF THE INSTITUTE OF PAPER CHEMISTRY, vol. 53, no. 2, August 1982, pages 173,174, abstract no. 1392, Appleton, Wisconsin, US; PULP & PAPER: "Ball valves give reliable service in digester blowline application", & PULP PAPER 55, no. 13: 87-88 (Dec. 1981) * |
ABSTRACT BULLETIN OF THE INSTITUTE OF PAPER CHEMISTRY, vol. 55, no. 4, October 1984, page 461, abstract no. 4340, Appleton, Wisconsin, US; G.W. PATTYSON: "Kamyr MC (Medium-Consistency) mixer for chlorine dioxide mixing at Great Lakes forest products, Thunder Bay, Ontario", & CPPA ANN. MTG. (MONTREAL) PREPRINTS 70A: 63-68 (Jan. 31-Feb. 1, 1984) * |
ABSTRACT BULLETIN OF THE INSTITUTE OF PAPER CHEMISTRY, vol. 56, no. 3, September 1985, page 366, abstract no. 3205, Appleton, Wisconsin, US; D.W. REEVE et al.: "Chlorine gas dispersion optimizes chlorination and reduces corrosion", & PULP PAPER 59, no. 3: 172-175 (March 1985) * |
F.A. HENGLEIN: "Grundriss der chemischen Technik", 11th edition, 1963, pages 43,44,126-128, Verlag Chemie GmbH, Weinheim, DE * |
TAPPI JOURNAL, vol. 67, no. 5, May 1984, pages 114-117, Atlanta, Georgia, US; A.H.J. PATERSON et al.: "Fundamentals of mixing in pulp suspensions: diffusion of reacting chlorine" * |
TAPPI, vol. 59, no. 11, November 1976, pages 106-109, Atlanta, Georgia, US; J. GULLICHSEN: "Medium-consistency chlorination" * |
TAPPI, vol. 64, no. 9, September 1981, pages 113-116, Atlanta, Georgia, US; J. GULLICHSEN et al.: "Medium-consistency technology. II. Storage dischargers and centrifugal pumps" * |
Also Published As
Publication number | Publication date |
---|---|
NO168123B (en) | 1991-10-07 |
JPS61289192A (en) | 1986-12-19 |
SE8602592D0 (en) | 1986-06-10 |
EP0207062B1 (en) | 1989-12-06 |
NO168123C (en) | 1992-01-15 |
FI862082A (en) | 1986-12-15 |
SE466459B (en) | 1992-02-17 |
FI862082A0 (en) | 1986-05-19 |
FI85728C (en) | 1992-05-25 |
SE8602592L (en) | 1986-12-15 |
FI85728B (en) | 1992-02-14 |
NO862116L (en) | 1986-12-15 |
CA1276408C (en) | 1990-11-20 |
ATE48452T1 (en) | 1989-12-15 |
BR8602738A (en) | 1987-02-10 |
DE3667310D1 (en) | 1990-01-11 |
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