Source: http://www.google.com/patents/US5409570?dq=6978253
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Patent US5409570 - Process for ozone bleaching of oxygen delignified pulp while conveying the ... - Google Patents
A process for delignifying and bleaching a lignocellulosic pulp without the use of elemental chlorine or chlorine-containing compounds by oxygen delignifying the pulp to a K No. of about 14 or less and a viscosity of greater than about 10 cps and thereafter further delignifying the partially delignified...http://www.google.com/patents/US5409570?utm_source=gb-gplus-sharePatent US5409570 - Process for ozone bleaching of oxygen delignified pulp while conveying the pulp through a reaction zone
Publication number US5409570 A
Application number US 07/981,467
Publication number 07981467, 981467, US 5409570 A, US 5409570A, US-A-5409570, US5409570 A, US5409570A
Inventors Bruce F. Griggs, Thomas P. Gandek, Michael A. Pikulin, Allen Rosen, Stuart T. Terrett, Spencer W. Eachus, David E. White, William H. Friend, Omar F. Ali
Patent Citations (101), Non-Patent Citations (196), Referenced by (15), Classifications (25), Legal Events (7)
Process for ozone bleaching of oxygen delignified pulp while conveying the pulp through a reaction zone
US 5409570 A
1. A process for the manufacture of a bleached pulp having a certain GE brightness and a certain strength as indicated by a certain viscosity which comprises:
chemically digesting a lignocelluloeic material to initially form a pulp;
oxygen delignifying the pulp to remove a substantial portion of the lignin therefrom, with the combination of the digesting and oxygen delignifying steps being conducted to form an intermediate pulp. having a specified amount of lignin and a specified viscosity; and
ozone delignifying the intermediate pulp with a gaseous mixture that contains ozone by adjusting the consistency of the pulp to a high consistency of above about 20%, adjusting the pH of the pulp to below about 4, and treating the pulp with an amount of the ozone containing gaseous mixture sufficient to remove a substantial portion, but not all, of the remaining lignin by intimately contacting and turbulently mixing the pulp particles with the gaseous mixture in a dynamic reaction zone by introducing the high consistency pulp into the reaction zone to fill the zone to at least about 10% by volume, dispersing the pulp substantially completely throughout the reaction zone while simultaneously conveying the pulp through the reaction zone in a plug flow-like manner at a dispersion index of about 7 or less thus exposing substantially all of the pulp to the ozone for reaction therewith for a sufficient time and at a temperature sufficient to allow access of the ozone to substantially all of the pulp for reaction therewith while the pulp advances through substantially all of the reaction zone, thus obtaining substantially uniform delignification of a significant portion of the pulp and forming a delignified pulp having a reduced amount of lignin and the certain strength, viscosity and GE brightness;
wherein the specified amount of lignin of the intermediate pulp is such that, after ozone delignification, the delignified pulp attains the certain GE brightness, and wherein the specified viscosity of the intermediate pulp is sufficiently high to permit the delignified pulp, after ozone delignification, to attain the certain strength as evidenced by the certain viscosity.
2. The process of claim 1 wherein the reaction zone is a horizontal chamber.
3. The process of claim 1 wherein the ozone delignification of the intermediate pulp is carried out by:
intimately contacting and mixing the pulp with the ozone by lifting, displacing and tossing the pulp in a radial direction to disperse the pulp and expose substantially all of the pulp to the gaseous bleaching agent while advancing the dispersed pulp axially through the reactor in a plug-flow like manner and at said dispersion index for a predetermined time to obtain substantially uniform bleaching of the pulp and to form a bleached pulp having the certain GE brightness, certain strength and certain viscosity.
4. The process of claim 1 wherein the ozone delignifying step comprises:
increasing the consistency of said intermediate pulp to at least about 28%;
uniformly contacting said comminuted pulp particles and said ozone containing gaseous mixture during said turbulent mixing while the pulp is advanced through the reaction zone for a sufficient time to obtain substantially uniform delignification of a majority of the pulp particles.
5. The process of claim 1 which further comprises:
comminuting the pulp into pulp particles having a relatively low bulk density prior to introducing said pulp particles into the reaction zone; and
maintaining a substantially constant and predetermined fill level of said pulp particles in the reaction zone by initially advancing said relatively low bulk density pulp particles at a first rate thus increasing the low bulk density, and advancing said increased bulk density particles at a second rate less than said first rate.
6. The process of claim 1 wherein the oxygen delignification step comprises forming a low to medium consistency pulp; treating the low to medium consistency pulp with an aqueous solution of an alkaline material for a predetermined time and at a predetermined temperature relative to the quantity of the alkaline material to substantially uniformly distribute the alkaline material throughout the low to medium consistency pulp; raising the consistency of the pulp to a high consistency; and subjecting the resulting high consistency pulp to high consistency oxygen delignification to obtain the intermediate pulp.
8. The process which further comprises:
oxygen delignifying the pulp by:
applying a first amount of alkaline material to brownstock pulp having a low consistency of less than about 5% by weight by combining the low consistency pulp with a sufficient quantity of alkaline material with uninterrupted mixing in a manner to ensure that all pulp fibers are exposed to the alkaline material to obtain a substantially uniform distribution of alkaline material throughout the pulp and then increasing the consistency of the alkaline material containing pulp to at least about 18% by weight to obtain high consistency pulp and to remove liquid while retaining the first amount of alkaline material substantially uniformly distributed throughout the high consistency pulp, said pulp fibers containing the alkaline material being directly passed from the combining step to the consistency increasing step;
applying a second amount of alkaline material onto the high consistency pulp to obtain a total amount of alkaline material on the pulp of at least about 0.8 to 7 percent by weight based on the oven dry weight of the pulp, wherein at least about 55% of the total amount of alkaline material is applied to the pulp during the alkaline material combining step; and
9. The process of claim 8 wherein the total amount of alkaline material is applied upon the low consistency pulp.
It has been conventional for many years to delignify and bleach wood pulp by using elemental chlorine. Exemplifying the bleaching of lignocellulosic pulps are the processes disclosed in, for example, U.S. Pat. No. 1,957,937 to Campbell et al., U.S. Pat. No. 2,975,169 to Cranford et al. and, U.S. Pat. No. 3,462,344 to Kindron et al.; and Handbook For Pulp and Paper Technologists--Chapter 11: Bleaching (§11.3) (TAPPI, USA).
Moreover, the preferred alkaline treatment of pulp according to the present invention may be carried out over a wide range of temperature conditions. According to a preferred practice, the treatment step is carried out at a temperature of from about room temperature to about 150° F., with temperatures ranging from about 90° to 150° F. being even more preferred. Atmospheric pressure or elevated pressure may be employed. The treatment step is completed when the aqueous alkaline solution is substantially uniformly distributed throughout the low consistency pulp. The amount of aqueous alkaline solution present in the treatment step can vary greatly according to the particular process parameters of the delignification reaction. The amount of the alkaline solution effective for the purpose of the present invention will depend primarily upon the extent of delignification desired in the oxygen bleaching step and the strength of the particular solution being used.
Thereafter, oxygen delignification is conducted on the high consistency pulp. Methods are available and well known in the art for dissolving gaseous oxygen into the liquid phase of high consistency pulp to affect delignification thereof. It is contemplated that any of these well known methods are adaptable for use according to the present invention. It is preferred, however, that oxygen delignification according to the present invention comprise introducing gaseous oxygen at about 80 to about 100 psig into the liquid phase of the high consistency pulp while maintaining the temperature of the pulp between about 90° and 130° C. The average contact time between the high consistency pulp and the gaseous oxygen is preferably from about 20 to 60 minutes.
The alkaline treated pulp 38 is then forwarded to the oxygen delignification reactor 40 where it is contacted with gaseous oxygen 42. Suitable conditions for oxygen delignification according to either the O, Om or Os processes comprise introducing gaseous oxygen at about 80 to about 100 psig to the high consistency pulp while maintaining the temperature of the pulp between about 90° and 130° C. The average contact time between the high consistency pulp and the gaseous oxygen ranges from about 15 to 60 minutes.
The reaction temperature at which the ozone bleaching is conducted is likewise an important factor in the process of the present invention. The maximum temperature of the pulp at which the reaction should be conducted should not exceed the temperature at which excessive degradation of the cellulose occurs, which with southern U.S. softwood is a maximum of about 120° F.-150° F.
Pulp fiber flocs 102, after treatment, are directed into tank 104 by spray from water nozzles which create a water shower that soaks the pulp and quenches the ozone bleaching reaction on the pulp particles. It is desirable that the quenching occur as uniformly and as quickly as possible in order to preserve the bleaching uniformity achieved in the reactor apparatus. Thus, these nozzles are arranged to provide an even, soaking shower of water while also being angled downward at an angle of at least 30° with respect to the horizontal and preferably at about 45°, in order to force the pulp down into the tank and avoid the formation of a water curtain which would inhibit the free fall of the pulp. The pulp is collected in this tank 104 and transported to the a subsequent bleaching treatment stage described below.
The pulp was then subjected to oxygen delignification at a pressure of about 80 psig oxygen at 110° C. for about 30-40 minutes. The resulting intermediate pulp had a lignin content evidenced by a K No. of less than about 14, and a strength evidenced by a viscosity of greater than about 9 cps.
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172 * Secrist et al., Studies on the Ozonation of Chemical Pulps, p. 215.
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174 * Seifert et al., Engineering Considerations in the Design of Oxygen Reactors, p. 309.
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U.S. Classification 162/40, 162/56, 162/65, 162/57, 162/90
International Classification D21C9/147, B01F7/00, D21C9/153, D21C9/16, D21C9/10, B01F15/00
Cooperative Classification D21C9/1057, D21C9/1005, D21C9/147, D21C9/163, D21C9/10, B01F7/00141, D21C9/153
European Classification D21C9/147, D21C9/16B, D21C9/10, D21C9/10G, D21C9/10B, D21C9/153, B01F7/00B12B4
Owner name: UNION CAMP PATENT HOLDING, INC. A DELAWARE CORPOR
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST.;ASSIGNORS:GRIGGS, BRUCE F.;GANDEK, THOMAS P.;PIKULIN, MICHAEL A.;AND OTHERS;REEL/FRAME:006406/0649;SIGNING DATES FROM 19921201 TO 19930122