WO1991018145A1 - Environmentally improved process for bleaching lignocellulosic materials - Google Patents
Environmentally improved process for bleaching lignocellulosic materials Download PDFInfo
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- WO1991018145A1 WO1991018145A1 PCT/US1990/002823 US9002823W WO9118145A1 WO 1991018145 A1 WO1991018145 A1 WO 1991018145A1 US 9002823 W US9002823 W US 9002823W WO 9118145 A1 WO9118145 A1 WO 9118145A1
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- pulp
- ozone
- viscosity
- lignin
- delignification
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Classifications
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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
- 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
- D21C9/1057—Multistage, with compounds cited in more than one sub-group D21C9/10, D21C9/12, D21C9/16
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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
- 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
- D21C9/147—Bleaching ; Apparatus therefor with oxygen or its allotropic modifications
-
- 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
- D21C9/147—Bleaching ; Apparatus therefor with oxygen or its allotropic modifications
- D21C9/153—Bleaching ; Apparatus therefor with oxygen or its allotropic modifications with ozone
Definitions
- This invention relates to a novel, environmentally acceptable process for delignifying and bleaching ligno ⁇ ellulosic pulp which does not require the use of elemental chlorine and which produces a pulp of acceptable strength. Use of this process also reduces the amount of environmental pollutants.
- Wood is comprised of two main components - a fibrou carbohydrate, i.e., cellulosic portion, and a non-fibrous component.
- the polymeric chains forming the fibrous cellulos portion of the wood are aligned with one another and form strong associated bonds with adjacent chains.
- the non-fibrou portion of the wood comprises a three-dimensional polymeric material formed primarily of phenylpropane units, known as lignin. Part of the lignin is between the cellulosic fibers, bonding them into a solid mass, although a substantial portio of the lignin is also distributed within the fibers themselve For use in paper-making processes, wood must first reduced to pulp.
- Pulp may be defined as wood fibers capable being slurried or suspended and then deposited upon a screen form a sheet, i.e., of paper.
- the methods employed to accomplish the pulping step usually involve either physical o chemical treatment of the wood, or a combination of these two treatments, to alter the wood's chemical form and to impart desired properties to the resultant product.
- pulping techniques There are thus two main types of pulping techniques, i. :-, mechanical pulpin and chemical pulping.
- mechanical pulping the wood is physically separated into individual fibers.
- chemical pulping the wood chips are digested with chemical solutions solubilize a portion of the lignin and thus permit its removal.
- the commonly utilized chemical pulping processes are broadly classified as: (1) the soda process, (2) the sulfite process, and (3) the Kraft process, with the latter process being most commonly used and being capable of a variety of well-known modifications as described below.
- the soda process is well known in the art. It employs sodium hydroxide (NaOH) as the active reagent to break down the lignin and to assist in its removal.
- NaOH sodium hydroxide
- the sulfite process is also well known in the art (see, e.g., Handbook for Pulp & Paper Technologists - Chapter 6: Sulfite Pulping (TAPPI U.S.A.) .
- Kraft Pulping involves digesting the wood chips in an aqueous solution of sodium hydroxide (NaOH) and sodium sulfide (Na_S) .
- NaOH sodium hydroxide
- Na_S sodium sulfide
- This process is highly effective in the pulping of even difficult woods such as southern softwoods, as well as the other more readily pulped species of wood such as northern hardwoods and softwoods.
- the Kraft process likewise generally produces a relatively high-strength pulp since its use results in a diminished attack on the cellulose component of the wood.
- the modified Kraft techniques can result in even les degradation in the polymeric structure of the cellulosic fiber during pulping and therefore the strength loss in the resultan paper product is diminished as compared to that occurring with the standard Kraft process.
- One modified Kraft pulping proces is known as "extended delignification", which is a broad term used in the art to encompass a variety of modified Kraft techniques, such as adding the pulping chemicals in a specific defined sequence, or at different locations within the digeste apparatus, or at different time periods, or with a removal and reinjection of cooling liquors in a prescribed sequence, so a to more effectively remove a greater amount of lignin while reducing the severity of the pulping liquor's chemical attack on the cellulosic fibers.
- Another modification of the Kraft process is the Kraft-AQ process, wherein a small amount of anthraquinone is added to the Kraft pulping liquor to accelerate delignification while limiting the attack upon the cellulosic fibers which comprise the wood.
- the digested material Prior to bleaching the pulp, however, the digested material is conventionally transferred to a separate blow tan after the chemical treatments involved in the pulping process are completed.
- the pressure developed during the initial chemical treatment of the lignocellulosic material is relieved and the pulp material is separated into a fibrous mass.
- the resulting fibrous mass is then subjected to a series of washing steps to remove the combination of any residual chemicals and the soluble materials (such as the lignin) which were separated from the fibrous materials in the pulping process.
- the pulp also undergoes one or more screening steps designed to separate out the larger portions of undefibered wood for special processing (recooking mechanical grinding, etc.).
- black liquor The residue obtained from the washing process, commonly referred to as black liquor, is collected, concentrated, and then incinerated in an environmentally safe manner in a recovery boiler.
- the technique for the collection concentration and burning of the black liquor is conventional and is well known in the art.
- the delignification and bleaching processes are conducted on the washed fibrous mass in a series of steps, using selected combinations of chemical reactants.
- various combinations of chemical treatments have been suggested.
- individual treatment steps have been rearranged in an almost limitless number of combinations and permutations. Therefore, in order to simplify the explanation of the various bleaching processes and systems, th use of letter codes is conventionally employed in combination to describe the particular chemical reactants employed and the sequence of the steps of the process.
- O Oxygen Reaction with elemental oxygen in alkaline medium.
- O Modified Uniform alkali treatment of low Oxygen to medium consistency pulp followed b reaction of high consistency pulp wit oxygen.
- H - Hypochlorite - Reaction with hypochlorite in an alkaline solution.
- O and Z are modified processes according to the present invention and are described further in the Detailed Description of the Invention.
- ozone may initially appear to be an ideal material f bleaching lignocellulosic materials
- the exceptional oxidativ properties of ozone and its relative high cost have heretofor limited the development of satisfactory ozone bleaching processes for lignocellulosic materials, especially southern softwoods.
- Ozone will readily react with lignin to effective reduce the K No., but it will also, under most conditions, aggressively attack the carbohydrate which comprises the cellulosic fibers and substantially reduce the strength of th resulting pulp.
- Ozone likewise, is extremely sensitive to process conditions such as pH with respect to its oxidative a chemical stability, and such changes can significantly alter the reactivity of ozone with respect to the lignocellulosic materials.
- U.S. Pat. No. 4,196,043 to Singh discloses a multi-stage bleaching process which also attempts to eliminate the use of chlorine compounds, and includes examples specifically directed to hardwoods. It is well known to those skilled in the art that hardwoods are easier to bleach than most softwoods.
- This process is characterized by from one to three ozone bleaching stages and a final treatment with alkaline hydrogen peroxide, each stage being separated by an alkaline extraction.
- One such sequence may be described in t common shorthand nomenclature of the paper industry as ZEZEP.
- the effluent from each treatment stage may be collected and recycled for use in bleaching operations, preferably at an earlier stage than tha from which it was obtained.
- This patent also provides a so- called countercurrent effluent flow.
- the present invention provides novel combinations o pulping and bleaching steps which overcome the problems encountered in the prior art as discussed herein and which essentially eliminate the discharge of chlorinated organics a minimizes color and BOD releases to produce a high grade bleached pulp in a commercially feasible manner.
- the process of the present invention is composed of three or more steps with a number of possible variations with and between the steps. These steps can be described as follows:
- a first step involves delignification of wood chips into a lignocellulosic pulp, using any one of several chemica pulping processes, followed by a washing removal of most of t dissolved organics and cooking chemicals for recycle and recovery. Usually included is a screening of the pulp to remove bundles of fibers that have not been separated in pulping.
- This delignification step is conducted so that, for southern U.S. softwood, for example, pulp with a K No. in the range of about 20-24 (target of 21) , a cupriethylenediamine (“CED”) viscosity in the range of about 21-28, and a GE brightness in the range of about 15-25 is typically obtained.
- CED cupriethylenediamine
- the effective embodiments of this first step are: a. Kraft pulping using either a continuous or batc digestion stage; b. Continuous digestion kraft pulping with extende delignification using staged alkali addition an countercurrent final cooking; c. Batch digestion kraft pulping with extended delignification using rapid liquor displacement and cold blowing techniques; or d. Kraft-AQ pulping to achieve extended delignification using either a continuous or batch digestion stage.
- the extended delignification techniques discussed in (b) and (c) above may include, for example, the Kamyr MCC, th Beloit RDH and Sunds Cold Blow Cooking techniques described in the background portion of this specification.
- the soda and sulfit processes mentioned above may be used.
- second step of the process includes an oxygen delignification treatment to further remove lignin without an accompanying significant loss in cellulosic fiber strength. This would include a washing removal of the dissolved organics and alkali for recycle and recovery. Pulp screening is also performed at times after oxygen delignification.
- the K No. of the increased consistency pulp is decreased by at least about
- the ratio of K No. to viscosity of the pulp is typically decreased by at least 25%.
- a K No. of about 7 to 10 and a viscosity of above about 13 is _. mm
- the possible embodiment to this step are: a. Conventional oxygen delignification, comprised an alkaline oxygen treatment of the pulp at either low, medium, or high pulp consistency ( or b.
- GEB often referred to as semi-bleached pulp
- a third step of the process includes an acidic, gaseous ozone bleaching treatment (Z or Z ) under defined process parameters to provide a highly selective removal and bleaching of lignin with minimal degradation of cellulose.
- process parameters include chelating agents for metal i control, pH control, pulp particle size control, pulp consistency, ozone concentration and gas/pulp contact control
- the chelating agent for examp oxalic acid, diethylenetriamine pentaacetic acid (“DTPA”) or ethylene diaminetetraacetic acid (“EDTA”) may be added to the pulp to substantially bind with metal ions contained therein.
- the pH of the pulp is preferably adjusted to a range of between about 1-4 prior to the third step.
- the consistency of the pulp is increased to between about 35-45% by weight and the partic size of the fiber floes are comminuted to a size of about 5 mm or less prior to the ozone delignification step. Included is dissolved organic washing stage for recycle and recovery.
- the pulp is preferably maintained at ambient temperature or at least at a pulp temperature of less than about 120 ⁇ F.
- the ozone may be provided by an ozone-containing gas which may comprise, for example, oxygen or air.
- the ozone concentration is preferably between about 1 and 8 percent by volume, whereas for ozone/air mixtures, an ozone concentration of between about 1 and 4 percent by volume is acceptable.
- the substantiall delignified pulp is advanced in a manner which subjects substantially all of the pulp particles to the ozone in a uniform fashion.
- pulps with K Nos. greater tha about 10 after the second step are not suitable for this third step, because of the substantial amounts of ozone required to reduce the K No. to the desired level, which typically results in the properties of the pulp being adversely and deleteriousl affected by excessive ozone degradation of the cellulose fiber of the pulp.
- a lesser concentration of ozone is used, with only a minimal amount of cellulose degradation occurring.
- the produc from this ozonation step for either the starting southern U.S. softwood or hardwood described above is a pulp having a K No. of less than about 5 and generally in the range of about 3 to (target of 3.5), a viscosity of above about 10, and a GE brightness of at least 50% (typically about 54% or higher for softwood and 63% or higher for hardwood) .
- the effective embodiments for this step are: a. Treatment of the acidified pulp by countercurrent contact of ozone in an oxygen or air carrier gas; or b. Treatment of the acidified pulp by cocurrent contact of ozone in an oxygen or air carrier gas.
- An additional bleaching step may then be used to bring the pulp to a desired fully bleached state, i.e., one having GE brightness levels of about 70 to 95% using any numb of possible, well recognized bleaching and extraction processes.
- the effective embodiments are: a. A conventional extraction stage with washing followed by a peroxide stage with washing; (i.e., EP) ; b.
- the extraction stage may comprise, in a further embodiment, combining the substantially delignified pulp with an effective amount of an alkaline material in an aqueous alkaline solution for a predetermined time and at a predetermined temperature correlated to the quantity of alkaline material to solubilize a substantial portion of any lignin which remains in the pulp. Thereafter, a portion of t aqueous alkaline solution may be extracted to remove substantially all of the solubilized lignin therefrom.
- the substantially delignified pulp may be treated in the additional bleaching step to raise the GE brightness of the resultant pulp to at least about 70%.
- Preferred brightening agents include chlorin dioxide or a peroxide.
- the (Eo)D, (Eo )D or EDED embodiments will achieve the highest brightness levels.
- the chlorine dioxide stage filtrate cannot, without treatment, be recycled for chemical recovery because of the presence of the inorganic chlorides. Since this is the only required sewered filtrate from the process, however, dramatic reductions in effluent volume, color, COD, BOD, and chlorinated organics ar achieved. Color of less than 2 pounds per ton, B0D 5 of less than 2 pounds per ton and total organic chloride (TOCl) of les than 2 and preferably less than 0.8 can be achieved. It is also possible to treat the chlorine dioxide stage filtrate wi a membrane filtration process which will allow essentially complete recycle. In the EP embodiment, no chlorinated materials are formed in the bleaching process and virtually a the liquid filtrates can be recycled and recovered, producing an almost effluent-free process.
- FIG. 1 is a block flow diagram of the preferred methods of this invention wherein a solid line represents pul flow and a broken line represents effluent flow;
- FIG. 2 is a schematic representation of a preferred method of the invention
- FIG. 3 is a cross-sectional drawing of a portion of an ozonation apparatus shown in Fig. 2, taken along line 3—3
- FIG. 3A is a cross-sectional drawing of a portion o a preferred ozonation apparatus shown in Fig. 2, taken along line 3—3;
- FIG. 4 is a comparison of the recycle and waste streams for a variety of pulp treatment processes. Detailed Description of the Invention
- the present invention relates to novel methods for delignifying and bleaching pulp while minimizing the degree o attack upon the cellulosic portion of the wood, thus forming product having acceptable strength properties for the manufacture of paper and various paper products.
- Consistency is defined as the amount of pulp fibe in a slurry, expressed as a percentage of the total weight of the oven dry fiber and water. It is sometimes also referred as pulp concentration. The consistency of a pulp will depend upon operation of and the type of dewatering equipment used. The following definitions are based on those found in Rydholm Pulping Processes, Interscience Publishers, 1965, pages 862-8 and TAPPI Monograph No. 27, The Bleaching of Pulp, Rapson, Ed The Technical Association of Pulp and Paper Industry, 1963, pages 186-187.
- Low consistency includes ranges up to 6%, usually between 3 and 5%. It is a suspension that is pumpable by an ordinary centrifugal pump and is obtainable using deckers and filters without press rolls.
- Medium consistency is between about 6 and 20%. Fifteen percent is a dividing point within the medium- consistency range. Below 15% the consistency can be obtained by filters. This is the consistency of the pulp mat leaving vacuum drum filter in the brownstock washing system and the bleaching system. The consistency of a slurry from a washer, either a brownstock washer or a bleaching stage washer, is 9- 15%. Above about 15%, press rolls are needed for dewatering. Rydholm states that the usual range for medium consistency is
- Rapson states it is 9-15%.
- the slurry is pumpable by special machinery even though it is still a coherent liquid phase at higher temperatures and under some compression.
- Pulping is used in its conventional sense to refer to a digestion of lignocellulosic material to form brownstock. Pulping would include, for example, Kraft, the Kraft-AQ process and forms of extended delignification.
- modified Kraft process is used herein to include extended delignification and all other modified Kraft processes with the exception of the Kraft-AQ process, since this process has achieved a special status and acceptance in the art and is separately known by that name. Also, the oxyge
- delignification step following completion of pulping will not be considered as an extended delignification; rather, we have chosen to call it a first step of a delignification process fo bleaching or brightening the pulp.
- the brightness factor is normally us in connection with the bleaching process because it tends to more precise when the pulp is lightly colored and its reflectivity is high.
- the normal permanganate test provides a permanganate o "K No.” which is the number of cubic centimeters of tenth normal potassium permanganate solution consumed by one gram o oven dried pulp under specified conditions. It is determined by TAPPI Standard Test T-214.
- pul brightness is usually a measure of reflectivity and its value is expressed as a percent of some scale.
- a standard method is GE brightness which is expressed as a percentage of a maximum GE brightness as determined by TAPPI Standard Method TPD-103.
- K No. viscosity and GE brightnes obtained by use of the present pulping, delignification and bleaching process, as set forth below, demonstrate the abilit of this process to enhance the degree of lignin removal from the pulp while minimizing the resultant degradation of the cellulose.
- the pulp After the oxygen delignification step, and prior brightening, the pulp has been partially delignified to a K N of about 5 to 10, preferably between about 7 to 10 for U.S. softwoods and about 5 to 7 for U.S. hardwoods.
- This partiall delignified pulp has a viscosity of above about 10, generally more than 13 and preferably, at least 14 (for softwood pulp) 15 (for hardwood pulp) .
- This partially delignified material thus has good strength and suitable viscosity so that it can withstand the effects of ozone.
- the partially delignified pul is subjected to ozone to further delignify the pulp, thus reducing the K No. of the pulp to about 3 to 4 for both softwoods and hardwoods while increasing the GE brightness of the pulp to at least about 50-70%.
- a GE brightness of about 54% or higher is typically achieved, while for hardwood pulp, values of about 63% or more are attained.
- the brightness of the pulp is further increased by an alkali extraction and an additional bleaching step using chlorine dioxide or peroxide.
- Fig. 1 sets forth, in schematic form, the various stages utilized in pulping, delignifying and brightening a pulp according to the invention.
- the invention comprises a multi-stage process including the steps of:
- step (d) washing the partially delignified pulp obtaine in step (c) above to remove dissolved organics from the oxygen treatment; optionally, screeni may be done at this point, while also recyclin at least a portion of the effluent from this step to a previous step; (e) chelation and acidification of the pulp to bin metal ions and to adjust the pH to a preferred level;
- the first stage in the method of the present invention wherein procedures can be utilized which improve the amount of lignin removed from the lignocellulosic material while minimizing the amount of degradation of the cellulose, i in the pulping step.
- the particular pulping process used in the method of the invention is, to a large extent, dependent o the type of lignocellulosic materials and, more particularly, the type of wood which is used as a starting material.
- the pulping liquor used in chemical pulping techniques may be recovered and reused in a manner well-known in the art. This step is typically followed by washing to remove most of the dissolved organics and cookin chemicals for recycle and recovery, as well as a screening stage in which the pulp is passed through a screening apparatu to remove bundles of fibers that have not been separated in pulping.
- the Kraft process is generally acceptable for use with all woods as compared to the other noted processes, as th final pulps obtained from the Kraft process have acceptable physical properties, although the brownstock pulp is also darker in color.
- the results obtained with conventional Kraft processes may be enhanced by the use of extended delignification techniques or the Kraft-AQ process. Moreover, these techniques are preferre for obtaining the greatest degree of reduction in K No. of the pulp without deleteriously affecting the strength and viscosit properties of the pulp.
- the amount of anthraquinone in the cooking liquor should be an amount of at least about 0.01% by weight, based on the oven dried weight of the wood to be pulped, with amounts of from about 0.02 to abou 0.1% generally being preferred.
- the inclusion of anthraquinon in the Kraft pulping process contributes significantly to the removal of the lignin without adversely affecting the desired strength characteristics of the remaining cellulose.
- th additional cost for the anthraquinone is partially offset by the savings in cost of chemicals in the subsequent Z , E and D or P steps.
- AQ is the use of techniques for extended delignification such as the Kamyr MCC, Beloit RDH and Sunds Cold Blow Methods for batch digesters. These techniques also offer the ability to _ _
- the next step in the method of the present inventio concerns the portion of the bleaching process which primarily involves removal of the residual lignin from the brownstock pulp being processed.
- this stage comprises an oxygen delignification step.
- the solid materials removed in this stage are oxygenated materials whic can, like the black liquor, be collected, concentrated, and then incinerated in an environmentally safe manner in a conventional recovery boiler. At least a portion of the liqu phase is recycled as illustrated in Fig. 1.
- the oxygen delignification step can be conducted in the manner which allows for the removal of increased percentages of the remaining lignin in t brownstock pulp without causing an unacceptable corresponding decrease in the viscosity of the pulp.
- the process which has been identified is practiced by treating the brownstock pulp from the pulping process at low to medium consistency, as described below, with the required amount of alkali necessary for the oxygen delignification step so as to ensure uniform application of the alkali, and thereafter raising the consistency and delignifying at high consistencie
- high consistency delignification is preferred, low o medium consistency oxygen delignification techniques may be utilized in place of high consistency delignification.
- the high consistency oxygen delignification step is preferably carried out in the presence of an aqueous alkaline solution at a pulp consistency of from about 25% to about 35%, and even more preferably, at about 27%. This improved proces
- the treatment step of the modified oxygen process (0 ) comprises substantially uniformly combining wood pulp, preferably Kraft brownstock pulp, with an aqueous alkaline solution while maintaining the consistency of the pulp at less than about 10% and preferably less than about 5% by weight.
- the aqueous alkaline solution is preferably present in an amount sufficient to provide from about 0.5% to about 4% activ alkali by weight after thickening based upon the oven dry pulp weight of the brownstock pulp, and even more preferably about 2.5% active alkali by weight after thickening based upon the oven dry weight of the brownstock pulp.
- This step uniformly distributes the aqueous alkaline solution throughout the low consistency brownstock and ensures that substantially all the brownstock fibers are exposed to a uniform application of alkaline solution.
- the brownstock pulp treated in this manner is not substantially delignified in the treatment step, but it is more effectively delignified in the subsequent high consistency oxygen delignification step than brownstock that is treated with alkaline solutions at high consistency according to the metho conventionally employed.
- the localized inhomogeneities in th distribution of alkali in conventional high consistency pulp are avoided, thus eliminating attendant non-uniform oxygen delignification.
- This homogeneous distribution step thus preferably comprises uniformly combining the pulp with an aqueous alkaline solution for at least about 1 minute and preferably no more than about 15 minutes. It is believed that treatment times of less than about 1 minute will not generally provide sufficient time to attain substantially uniform distribution whereas treatment times in excess of about 15 minutes are no expected to produce substantial further benefit.
- the preferred alkaline treatment of pulp according to the present invention may be carried out over a wide range of temperature conditions.
- the treatment step is carried out at a temperature of from about room temperature to about 150°F, with temperatures ranging from about 90°F to about 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 uniforml distributed throughout the low consistency pulp.
- the amount aqueous alkaline solution present in the treatment step can vary greatly according to the particular process parameters 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.
- the aqueous alkaline soluti preferably used comprise a sodium hydroxide solution having concentration of from about 20 to about 120 g/1.
- This solut is mixed with the low consistency pulp, so that the overall mixture has a concentration of alkaline material of between about 6.5 and 13.5 g/1, and preferably around 9 g/1.
- an aqueous sodium hydroxide solution is added to t low consistency pulp in an amount sufficient to provide from about 15% to about 30% by weight of sodium hydroxide based on dry pulp weight.
- Other alkaline sources having an equivalent sodium hydroxide content such as oxidized white liquor from the conventional Kraft recovery and regeneration cycle, may also be employed.
- the consistency of the treated pulp is increased to greater than about 20%, preferably from about 25% to about 35%.
- Several methods are available and well known in the art for increasing the consistency of the pulp, such as pressing the wood pulp to remove liquid therefrom.
- 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 ⁇ C and 130°C.
- the average contact time between the high consistency pulp and the gaseous oxygen is preferably from about 20 minutes to about 60 minutes.
- the present preferred process unexpectedly provides an increase of at least 20% in delignification compared to prior art delignification processes: i.e., from 50% to at least about 60% reduction of the K No. for the incoming pulp. Reductions of 70% and more can even be achieved with minimal cellulose degradation. The avoidance of deterioration of the cellulose component of the pulp is evident by the minimal change in viscosity of pulp which is treated in accordance with the present invention.
- pulp K Nos. for the particular pulp range from about 10-26 depending upon the type of wood (e.g., for Kraft pulping, about 10-14, target 12.5 for hardwood and about 20-24, target 21, for softwood) , while after oxygen delignifi ⁇ cation, the K No. is generally in the range of about 5-10.
- FIG. 2 A processing scheme for carrying out the method of the present invention is depicted in schematic form in Fig. 2.
- the steps depicted therein represent a preferred operating system that tends to maximize certain benefits of the present invention.
- Wood chips 2 are introduced into a digester 4 where they are cooked in a liquor such as a liquor of sodium hydroxide and sodium sulfide.
- the cooking unit 4 produces a Kraft brownstock 8 and a black liquor 6 containing the reaction products of lignin solubilization.
- the brownstock is treated in washing units comprising, preferably, blow tank 10 and washer 12 where residual liquor contained in the pulp is removed.
- washing units comprising, preferably, blow tank 10 and washer 12 where residual liquor contained in the pulp is removed.
- Many methods are available and well known in the art for washing brownstock, such as diffusion washing, rotary pressure washing, horizontal belt filtering, and dilution/extraction.
- the washed brownstock is introduced into a treatment unit 14 where it is treated with an alkaline solution and maintained at a consistency of less than about 10% and preferably less than about 5%.
- the process of the present invention preferably includes means for introducing make-up caustic 16 into the treatment stage to maintain the desired caustic application level.
- the treated pulp 18 is forwarded to a thickening unit 20 where the consistency of the pulp is increased, by pressing for example, to at least about 20% by weight and preferably to about 25% to about 35%.
- the liquid 22 removed from the thickening unit 20 is preferably returned to washing unit 12 for further use.
- the high consistency "pressed" brownstock 24 produced in the thickening unit 20 is forwarded to the oxygen delignification reactor vessel 26 where it is contacted with gaseous oxygen 28.
- the delignified brownstock 30 is preferably forwarded through blow tank 32 and then to a second washing unit 34 wherein the pulp is washed with water to remove any dissolved organics and to produce high quality, low color pulp 36.
- At least a portion of the effluent 38 from this washing step is preferably returned to washing unit 12 for use therein.
- the effluent 13 from washing unit 12 may be recycled alone or optionally with all or a portion of effluent 38, to either the blow tank 10 or ultimately black liquor line 6.
- the partially delignified pulp obtained after oxygen delignification may be screened to remove fiber bundles from the pulp that have not separated for further treatment such as mechanical grinding. From here, pulp 36 could be sent to subsequent bleaching stages to produce a fully bleached product.
- Kraft pulping of the wood may be carried out, followed by the modified low-consistency alkali treatment/hig consistency oxygen delignification procedure (0 ) described above.
- this combination resul in a pulp with a K No. of about 8 to 10, preferably 9, and a viscosity of greater than about 13 to 14.
- the ozone consumption may be reduced by using a number of alternate routes, such as standard kraft cooking followed by a modified oxygen delignification step (0 ) , or modified kraft pulping with extended delignification (such as Kamyr MCC, Beloit RDH Sunds Cold Blow) followed by a conventional oxygen delignification step (O) , or by Kraft AQ cooking followed by conventional oxygen delignification step (O) as discussed above.
- alternate routes such as standard kraft cooking followed by a modified oxygen delignification step (0 ) , or modified kraft pulping with extended delignification (such as Kamyr MCC, Beloit RDH Sunds Cold Blow) followed by a conventional oxygen delignification step (O) , or by Kraft AQ cooking followed by conventional oxygen delignification step (O) as discussed above.
- the next step in the method of this invention is ozone delignification and bleaching of the oxygen-delignified brownstock pulp.
- This ozonation takes place in an ozone reactor which is described below in detail and illustrated in Figs. 2, 3 and 3A.
- the pulp Prior to treatment of the pulp with the ozone, the pulp is conditioned so as to ensure the most effective selective delignification of the pulp and to minimiz the chemical attack of the ozone on the cellulose.
- the incoming pulp 36 is directed into a mixing chest 40, where it is diluted to a low consistency.
- An acid 42 such as sulfuric acid, formic acid, acetic acid or the like, is added to the l consistency pulp to decrease the pH of the pulp in mixing che 40 to the range of about 1 to 4 and preferably between 2 and 5
- the pH is adjusted as described above since it is known that the relative effectiveness of ozone bleaching of pulps is dependent upon the pH of the pulp mixture. Lower pH values d not appear to have any beneficial effect on the further processing of the pulp, whereas increasing the pH to above in about 4 to 5 causes a decrease in viscosity and an increase i ozone consumption.
- the acidified pulp is treated with chelating agent to complex any metals or metal salts which may be present in the pulp. This chelating step is used to render such metals
- Chelating agents are known per se and include, for 0 example, polycarboxylate and polycarb ⁇ xylate derivatives such as the di-, tri-, and tetra-carboxylates, amides, and the lik Preferred chelating agents for this ozone treatment, for reasons of cost and efficiency, include DTPA, EDTA and oxalic acid. Amounts of these chelating agents ranging from about 5 0.1% to about 0.2% by weight of oven dry pulp are generally effective, although additional amounts may be needed when hig metal ion concentrations are present.
- the effectiveness of the ozone bleaching process is controlled by a number of inter-related process parameters, 0 including the pH level and the amount of metal salts in the pulp as discussed above- Another very important parameter is the consistency of the lp during the ozone bleaching proces
- the pulp which is to be bleached must contain sufficient wate so that the water exists as a continuous phase through the 5 individual fibers, that is, the fiber should be sufficiently saturated with water.
- the water in the fiber allows the transfer of the ozone from the gaseous ozone atmosphere to bot treat the outer surface of the fibers, and possibly more importantly, for the ozone to be transferred via the water phase to the less accessible interior portion of the individua fibers and thereby provide more complete removal of lignin fro the fibers.
- the consistency should not be so low that the ozone is diluted and tends to chemically break down rather than bleach the pulp.
- the preferred range of consistency especially for southern U.S. softwood, has been found to be between about 28% and about 50%, with the optimum results being obtained at between about 38% and about 45%. Within the above ranges, preferred results are obtained as indicated by the relative amount of delignification, the relatively low amount of degradation of the cellulose, and the noticeable increase in the brightness of the treated pulps.
- the reaction temperature at which the ozone bleachin is conducted is likewise an important controlling factor in th process of the present invention.
- the ozone step can be effectively conducted at temperatures up to a certain critical temperature, at which the reaction commences to cause excessiv degradation of the cellulose.
- This critical temperature will vary significantly depending upon the particular type of wood employed to form the pulp and the history of the prior treatment of the pulp.
- the maximum temperature of the pulp fiber 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.
- the ozone gas which is used in the bleaching process may be employed as a mixture of ozone with oxygen and/or an inert gas, or can be employed as a mixture of ozone with air.
- the amount of ozone which can satisfactorily be incorporated into the treatment gases is limited by the stability of the ozone in the gas mixture.
- Ozone gas mixtures which typically contain about 1-8% by weight of ozone in an ozone/oxygen mixture, or about 1-4% ozone in an ozone/air mixture, are suitable for use in this invention.
- the higher concentration of ozone in the ozone gas mixture allows for the use of relatively smaller size reactors and shorter reaction time to treat equivalent amounts of pulp, thereby lessening the capit cost required for the equipment.
- ozone gas mixtures containing lower amounts of ozone tend to be less expensive t produce and may reduce operating costs.
- a further controlling factor is the relative weight of the ozone used to bleach a given weight of the pulp. This amount is determined, at least in part, by the amount of lign which is to be removed during the ozone bleaching process, balanced against the relative amount of degradation of the cellulose which can be tolerated during ozone bleaching. In accordance with the preferred method of this invention, an amount of ozone is used which will react with about 50% to 70% of the lignin present in the pulp. The entire amount of ligni in the pulp is not removed in the ozone bleaching step as evidenced by the K No.
- the amount of ozone added typically is about from 0.2% to abou 1% to reach the lignin levels of a 3-4 K No. Higher amounts may be required if significant quantities of dissolved solids are present in the system.
- the time of the reaction used for the ozone bleachin step is determined by the desired rate of completion of the ozone bleaching reaction as indicated by complete or substantially complete consumption of the ozone which is utilized. This time will vary depending upon the concentratio of the ozone in the ozone gas mixture, with relatively more concentrated ozone mixtures reacting more quickly, and the relative amount of lignin which it is desired to remove. The time required is preferably less than two minutes, but the procedure may take substantially longer depending on other reaction parameters.
- the pulp is bleached uniformly. This feature is obtained in part, by comminution of the pulp into discrete floe particles of a size which is of a sufficiently small diameter and of a sufficiently low bulk density so that the ozone gas mixture will completely penetrate a majority of the fiber floes, i.e., which comprise agglomerations of fibers. During comminution i is not feasible to completely separate the pulp fibers into distinct fibers.
- the floe particles resulting fro comminution have a relatively compacted central core surrounde by a plurality of outwardly extending fibers.
- the floe particle size is determined by measuring what was determined to be the smallest diameter of this relatively unfluffed central core.
- Bleaching uniformity is to a large extent also dependent on certain of the other process parameters, but it has been found that if the floe particle size is limited to a maximum of 5mm, and preferably even less —for example, 3mm— that uniform treatment of a substantial majority of these particles can readily be achieved, as evidenced by observation of an insignificant number of darker underbleached floe centers. Where the floe particle size was greater than about 5mm, bleaching was non-uniform, as evidenced by a majority of darker unbleached floe centers. Therefore it is important to achieve sufficient comminution so that a majority of the floes measure below an average of about 5 mm for uniform ozone treatment thereof.
- a still further important process parameter is that during the ozone bleaching process the particles to be bleach should be exposed to the ozone bleaching mixture by mixing so as to allow access of the ozone gas mixture to all surfaces the floes and equal access of the ozone gas mixture to all floes.
- the mixing of the pulp in the ozone gas mixture give superior results with regard to uniformity as compared to th results obtained with a static bed of floes wherein some of floes are isolated from the ozone gas relative to other floe and thereby bleached less than other floes.
- the movement of the floes so as to expose them to ozone gas mixture causes uniform treatment of the floes with respect to each other.
- This treatment results in the desire amount of lignin being removed uniformly from the pulp witho excessive deterioration of the cellulose in the fibers which comprise the floes.
- the control of the ozone treatment in accordance with this invention by use of a controlled particl size and by turbulent movement during ozone treatment has bee found to result in a final pulp typically having less than about a 5% variation in GE brightness, K No. and viscosity.
- the present application designates such a non-uniform ozone treatment wit the letter "Z".
- Pulp exiting the ozone reactor has a GE brightness o about at least 50 percent and generally around 50 to 70 percent, with hardwoods usually being above about 55 percent.
- the pulp (for hardwoods or softwoods) also has a K No. of
- washed Q pulp 36 is directed to mixing chest 40 where it is treated wit an acid 42 and a chelating agent 44.
- the acidified, chelated low-consistency pulp 46 is introduced into thickening unit 48 for removing excess liquid 50 from the pulp, such as a twin roll press wherein the consistency of the pulp is raised to th 5 desired level. At least a portion of this excess liquid 50 ma be recycled to mixing chest 40, with a remaining portion being directed to blow tank 32.
- the resulting high consistency pulp 52 is then passed through screw feeder 54 which acts as a gas seal for the ozone gas and thereafter through a comminuting unit 56, such as a fluffer, where the pulp is comminuted to pulp fiber floes 60 of a pre-determined size which, as noted above, should measure about 5 mm or less in size.
- the comminuted particles are then introduced into a dynamic ozone reaction chamber 58 which, as illustrated, is a conveyor 62 5 powered by motor 64.
- Conveyor 62 is specifically designed fo mixing and transporting the pulp particles 60 so as to allow the entire surface of the particles to become exposed to the ozone gas mixture 66 during movement of the pulp.
- pulp fiber floes 60 after treatment are 0 allowed to fall into dilution tank 68.
- Fig. 3 is a cross-sectional view through ozone reactor 58 illustrating the arrangement of the pulp particles 60 as they are carried through the reactor by conveyor 62.
- Fig. 3A is a cross-sectional view of a preferred conveyor utilizing a paddle-like arrangement to move the comminuted particles through reaction chamber 58.
- Fig. 2 shows the pulp being treated with ozone cocurrently with the ozone-gas mixture.
- the portion of the pulp which has been bleached to the greatest extent may initially be contacted wi the newly introduced ozone mixture containing the maximum amount of ozone by passing the ozone-containing gas in a direction counter-current to the flow of pulp 60.
- the pulp entering the reactor has the highest lignin content and initially contacts the exiting, nearly exhausted ozone mixtur thereby providing the optimum chance to consume virtually all of the ozone. This is an efficient method for stripping ozon from the ozone/oxygen or ozone/air mixture.
- the remaining spent ozo gas 70 can be recovered from dilution tank 68.
- dilution water 72 which also serves as an ozone gas seal, is added to reduce the consistency of the pulp to a low level to facilitate movement of the bleached pulp 74 through the subsequent process steps.
- the spent ozone gas 70 from dilution tank 68 is directed to a carrier gas pretreatment stage 76 where a carri gas 78 of oxygen or air is added.
- This mixture 80 is directe to ozone generator 82 where the appropriate amount of ozone i generated to obtain the desired concentration.
- the proper ozone/air mixture 66 is then directed to ozone reactor 58 for delignification and bleaching of the pulp.
- the substantially delignified pulp 74 is again thoroughly washed washer 84 as shown in Fig. 2 and at least a portion of the water 86 which is recovered is recycled to washing unit 34 of the process, thereby producing major environmental benefits from the elimination of sewered liquid.
- the bleached low consistency pulp 74 after ozonatio will have a reduced amount of lignin, and therefore, a lower No. and an acceptable viscosity.
- the exact values for the K No. and the viscosity which are obtained are dependent upon t particular processing to which the pulp has been subjected.
- a southern U.S. softwood pulp which is pulped wi a conventional Kraft method, initially delignified by modifie high consistency oxygen delignification (0 ) , and subsequentl further delignified with ozone, preferably by a modified uniform ozone treatment (Z )
- ozone preferably by a modified uniform ozone treatment (Z )
- Southern U.S. softwoo pulp which is subjected to Kraft AQ pulping and then to modified high consistency oxygen bleaching (O ) and modified uniform ozone treatment (Z ) will typically have a K No. of about 2 and a viscosity of greater than about 12.
- the resulting pulp 74 will be noticeably brighter than the starting pulp.
- southern softwood, afte the pulping process has a GE brightness of about 15% to 25%; after the oxygen bleaching process, a GE brightness of about 25 % to 45%; and after the ozone bleaching process, a GE brightness of about 50% to 70%.
- the washed pulp 88 from the ozone stage is then combined with a sufficient amount of alkaline material 90 in • extraction vessel 92 to effect extraction.
- pulp 88 is subjected to an aqueous alkaline solution for a predetermined time and at a predetermined temperature correlated to the quantity of alkaline material to solubilize a substantial 0 portion of any lignin which remains in the pulp, in vessel 92
- This extraction process also increases the brightness of the pulp, typically by about 2 GE brightness points.
- the alkali treated pulp 94 is directed to washing unit 96, th aqueous alkaline solution is washed from the pulp so as to 5 remove substantially all of the solubilized lignin from the pulp, thus forming a substantially lignin-free pulp.
- This st is well known to those skilled in the art and no further comment is deemed necessary here.
- the examples illustrate th preferred extraction parameters for this step of the process. At least a portion of the alkaline solution 98 which is recovered is recycled to washing unit 84. Again, major environmental benefits are achieved from the elimination of sewering of this solution.
- the extraction step can be augment by incorporating an oxygen treatment within the caustic extraction step (E ) .
- This alternative also well known to those skilled in the art, requires no further comment here.
- a final brightness i the range of 50 to 65 is unsatisfactory. Accordingly, in ord to further raise the GE brightness to the more desirable rang of about 70 to 95%, the pulp is subjected to brightening bleaching, which is primarily intended to convert the chromophoric groups on the lignin remaining in the pulp into colorless state.
- the brightening bleaching of the ozone-bleached and extracted pul can be performed using a variety of materials.
- the washed pulp 100 is combined with the chosen bleaching agent 102 in bleaching vessel 104.
- the preferred bleaching agent is chlorine dioxide or peroxide.
- the pulp 106 is washed with water 114 in washing unit 108 and the effluent is either recycled 110 or sewered 112. When recycled, at least a portion of wash water stream 110 is directed to washing unit 96.
- the resultant bleached pulp 116 may then be collected and used in a variety of applications.
- chlorin dioxide D
- a appropriate amount of chlorine dioxide enables high-strength pulps having a GE brightness value greater than about 80% to b obtained. Since the pulps entering the chlorine dioxide stage are relatively low in lignin, the chlorine dioxide brightening bleaching can be carried out in the presence of only from abou 0.25% to about 1% of chlorine dioxide based on the oven dry weight of the pulp.
- the chlorine dioxide which is utilized in the brightening process should preferably be prepared by a process which is free from elemental chlorine.
- chlorine dioxide which does contain a minor amount of elemental chlorine can be used without any substantial increase in the relative amount of undesirable pollutants because of the relatively low amount of lignin present in the ozone-bleached pulp.
- the effluent from the final bleaching step of this invention when using chlorine dioxide is exceptionally low and can be discharged safely as shown in Fig. 2.
- the stream can, however, be further purified by being treated with a membrane filtration process such as reverse osmosis.
- a membrane filtration process such as reverse osmosis. This technique provides a clean filtrate that can be recycled back to previou bleaching stages for further use. This has the benefit of reducing fresh water usage.
- the concentrated chloride streams that result from the membrane filtration are relatively low in volume.
- the K No. of the pulp from either softwood or hardwood should be reduced to a level of about 6 prior to the ozonation step in order to obtain, as a final product following the peroxide bleaching stage, a pulp of acceptable brightness, i.e., a GE Brightness of greater than about 80%, since peroxide is not as effective at bleaching as is chlorine dioxide. Where a completely chlorine/chlorine dioxide-free process is desired, however, peroxide provides acceptable results.
- Typical peroxide brightening agents and their use i this step are conventional, and one skilled in the art would know the appropriate concentration, types and use of such peroxide agents. Hydrogen peroxide is preferred.
- the washed, further brightened pulp has a GE brightness of between about 70 and 95%, and preferably betwee about 80 and 95%. Also, the physical properties of this pulp are commensurate with those obtainable by pulp produced by conventional CEDED or OC/DED processes.
- this effluent may be treated by reverse osmosis to provide an even cleaner filtrat that may be recycled to previous bleaching stages as shown fo further use without the build-up of chlorides.
- steps may be taken to reduce the demand for chlorine dioxide.
- An E step may allow the pulp t achieve greater levels of brightness although additional expense is incurred by the use of additional sodium hydroxid and oxygen in this step.
- there are known industry procedures for preparing chlorine dioxide whereby residual chlorine levels are minimized e.g., the R8 process vs. the process) . These reduced chlorine level chemicals are prefer for use in the D stage to reduce the chloride levels of the wash water effluent.
- OmZmED instead of OmZmED, one may use the OmzmEP process the invention to obtain additional substantial advantages ov the prior art in that no chlorinated compounds whatsoever ar produced. This enables all of the effluent to be recycled without experiencing the problems of chloride build-up in th process wash water streams.
- the process of the present invention achieves substantial advantages with respect to reductions in effluent volume, color, COD, BOD and chlorinated organics. Moreover, since the effluent used in the washing steps contai significantly reduced chloride levels compared to prior art processes which utilize chlorine, the washing unit vents will not be carrying chlorinated organic compounds or gases which require treatment prior to discharge.
- Loblolly pine chips were lab batch cooked according to the conditions in Table I to produce a conventional kraft pulp.
- the resulting pulp had a K No. of 22.6 and a viscosity of 27.1 cps.
- the kraft pulp was then subjected to conventional oxygen treatment (Tables II and V) followed by bleaching to a final target brightness of 83 GEB using both a conventional OC/DED sequence (Table III) and an OZ ED bleaching sequence (Tables IV and V) .
- the ozone bleaching stage was run at 35% consistency with an ozone application of 0.61%.
- OZ ED bleaching und these conditions produced a pulp having acceptable strength properties compared to an 83% GE target brightness OC/DED baseline pulp.
- the OZ ED pulp had marginal viscosity of 9.7 cps.
- the strength properties were measured on an OZ ED pulp where the final D-stage applicatio was 2.5%.
- Target brightness was reached only with an excessive chlorine dioxide charge.
- the OZ E pulps response chlorine dioxide treatment shows that higher brightness can only be achieved by significantly increasing the ozone application, which then causes significant viscosity and strength loss of the pulp.
- a kraft/AQ brownstock was prepared in a laboratory batch digester from loblolly pine chips as described in Table VIII.
- the K No. of the resulting brownstock was 18.3 and the viscosity was 20.6 cps.
- the Kraft/AQ pulping conditions produced a pulp having a significantly lower lignin content than in Example 1 as evidenced by the K No. , without unacceptable deterioration of pulp strength as evidenced by the viscosity.
- the Kraft/AQ brownstock was then subjected to further bleaching using the conventional OC/DED sequence and the OZ ED sequence as shown in Tables II, III, IV and V to a target brightness of 83% GEB.
- Use of the Kraft AQ pulping technology achieved the goal of producing a starting pulp with a low K No. , having acceptable viscosity properties, for the ozone bleaching sequence.
- the ozone bleaching stage was run at 35% consistency with an ozone application of 0.35% and
- a pine Kraft brownstock having a K No. of about 24 was pressed to a consistency of about 30-36% by weight to produ a high consistency mat.
- the mat of brownstock was sprayed with a 10% sodium hydroxide solution in an amount sufficien to produce approximately 2.5 weight percent sodium hydroxide based on pulp dry weight.
- Dilution water was added in an amount sufficient to adjust the brownstock mat to about 27% consistency.
- the high consistency brownstock mat was then subjected to oxygen delignification using the following conditions: 110°C, 30 minutes, 80 psig 0 2 .
- Pine Kraft brownstock of Example 3 was introduced into treatment vessel along with a sufficient volume of 10% NaOH solution to effect a 30% NaOH addition based on oven-dried pulp. Sufficient dilution water was added to obtain a brownstock consistency of about 3% by weight in the treatmen vessel.
- the brownstock and the aqueous sodium hydroxide solution were uniformly mixed at room temperature by a ribbo mixer for about 15 minutes.
- the treated brownstock was then pressed to a consistency of about 27% by weight. After pressing, the sodium hydroxide on the fiber equaled about 2.5% as in Example 3.
- the treated brownstock was then delignified according to the oxygen delignification procedur described in Example 3. A comparison is shown in Table XI.
- EXAMPLE 5 Pulp produced from pine in accordance with the 0 process of Example 4 of the present invention is compared to that produced conventionally (0) (i.e., with no low consistency alkaline treatment step) .
- the average caustic dosage for high consistency oxygen delignification of brownstock pulp was found to be 45 pounds per oven dried ton (lb/t) or 2.3%. At that level, the average reduction in K No. across the oxygen delignification reactor was 10 units.
- an average K No. drop during delignification was found to be 13 units: a 30% improvement compared to the conventional process.
- Delignification selectivity can also be expressed as the change in viscosity versus the change in K No. between brownstock and the corresponding treated pulps.
- Oxygen delignification selectivity decreases rather rapidly when the change in K No. begins to exceed 10 K No. units. The decrease in selectivity is observed as a rapid increase in the change in viscosity for a given change in K No.
- the corresponding change in viscosity is expected to be 12 to 13 cps.
- the change in viscosity was found to be about 6 cps.
- the change in viscosity per change in K No. appears to be constant up to a 16 to 17 K No. unit change for pulps obtained using the preferred treatment process of the invention. The results are shown in Table XII.
- a southern pine pulp was produced in an operating 600 TPD fine paper mill using the modified oxygen delignification process (0 ) having the conditions of Table II in combination with the uniform alkali treatment as described in Examples 4 and 5 and the conditions as shown in Table XIII below.
- the O-stage pulp produced by this novel method had the properties needed to successfully complete the bleaching process using ozone, as described in the embodiment of this invention.
- the oxygen stage pulp had a K No. of 7.9 (compared to a typical conventional O-stage K No. of about 12) .
- Viscosity of the delignified pulp was 15 cps and was not significantly reduced by the high degree of delignification obtained by the use of the modified oxygen process.
- This pulp could then be further bleached with ozone, utilizing any of the numerous process embodiments described herein to produce a pulp having acceptable final strength and optical properties.
- the ozone bleaching stage was carried out in a pilot plant reactor as shown in Fig. 2. Conditions of operation of the pilot plant reactor are shown in Table XV.
- the ozone bleached pulp generated in the pilot plant reactor was then treated in extraction and chlorine dioxide stages in the laboratory, as described in Table V above, to produce a final bleached pulp product at target brightness.
- a final D stage charge of only 1.0 % C10_ was used on the fiber.
- the strength and optical properties of the ozone bleached pulp were acceptable compared to the conventional OC/DED baseline and the results of the comparison are shown in Tables XVI and XVII below.
- a southern hardwood fiber from mixed hardwood comprising predominantly gum and oak, was bleached with ozone in the pilot plant described in Example 6 above.
- a conventional oxygen stage pulp produced in the 600 TPD mill was treated with ozone in the pilot plant reactor.
- the oxygen stage pulp had a K No. of 5.7 and a viscosity of 14.1.
- the ozone reactor treatment conditions are shown in Table XIX.
- the pilot plant Z stage pulp was then final bleached by conventional E and D stages as shown in Table XX to a target brightness.
- a D-stage C10_ charge of only 0.35% was used on OD fiber.
- Strength and brightness properties were acceptable compared to the baseline as shown in Tables XXI and XXII. TABLE XIX
- Delignification selectivity can also be expressed in terms of the change in viscosity versus the change in K No. between brownstock and the corresponding modified oxygen treated pulps.
- the average change in viscosity was 4 cps for pulps produced by the conventional process.
- the change in K No. for the same change in viscosity for pulps produced by the modified oxygen method was 7 units.
- the OC/DED effluent is the C/D, E and D combined effluent and the OZ ED effluent is the D stage effluent, each representing the several effluent properties.
- Table XXVII the ozone bleaching sequence substantially reduces the environmental impact of the effluent from the bleaching process.
- EPA method 110.2 was used. From this data, it can be seen that the present invention provides a discharge effluent having a color of no greater than about 2 pounds per ton, a BOD., value of no greater than about 2 pounds per ton and an amount of total organic chloride of no greater than about 2 and preferably less than about 0.8 *
- Southern pine kraft pulp was bleached using three modifications of the basic OZED sequence.
- OZ ED the pulp was bleached as in Tables IV and with conventional oxygen, modified ozone, caustic extraction and chloride dioxide as produced in the R-3 sequence with a CIO /Cl 2 ratio of 6:1.
- the modified oxygen process (O ) was utilized and again the final stage used an R-3 type of chlorine dioxide.
- the modified oxygen process (O ) was used once again, and an R-8 chlorine dioxide solution was employed with 95:1 ratio in the final stage.
- Table XXVIII demonstrates the positive environmental impact offered with the use of the modified oxygen process (0 ) .
- the R-8 bleach liquor also had a positive effect.
- Southern loblolly pine pulps were prepared by the kraft and kraft/AQ pulping processes as described in Tables I and VIII above. These pulps were further subjected to conventional and modified oxygen delignification as described in Examples 4 and 5 to show the effect of combining these processes (for extending delignification with minimal impact on pulp strength) on the ozone bleaching sequence. As can readily be seen from Table XXIX, these processes produce an additive effect. Extremely ⁇ * low 0mzmE K Nos. can be reached with little impact on final viscosity. Conversely, the amoun of ozone needed to reach a targ 3 et 0mZmE K No. of about 3.5 for the previously described ozone bleaching process can be substantially reduced. In addition, the additive effect produces a southern pine pulp that can be fully bleached by a
- Wood based dirt was refined and added to the OZ ED starting brownstock a a level of 0.75% by weight to examine the ability of this sequence to remove dirt compared to CEDED and OC/DED bleachin Dirt properties of the three sequences, measured as Effective Black Area, bark and shives, were equivalent.
- Viscosity values after the 0 stage are interpolated values based on established data.
Abstract
Description
Claims
Priority Applications (16)
Application Number | Priority Date | Filing Date | Title |
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KR1019920700104A KR920703922A (en) | 1990-05-17 | 1990-05-17 | Bleaching method of lignocellulosic material with improved environmental pollution |
EP90908787A EP0483163B1 (en) | 1990-05-17 | 1990-05-17 | Environmentally improved process for bleaching lignocellulosic materials |
SU5011189A RU2102547C1 (en) | 1990-05-17 | 1990-05-17 | Method of preparing bleached pulp and a method for delignification and bleaching of lignocellulose material |
PCT/US1990/002823 WO1991018145A1 (en) | 1990-05-17 | 1990-05-17 | Environmentally improved process for bleaching lignocellulosic materials |
DE69019350T DE69019350T2 (en) | 1990-05-17 | 1990-05-17 | MORE ENVIRONMENTALLY FRIENDLY METHOD FOR BLEACHING LIGNOCELLULOSIC MATERIALS. |
BR909007533A BR9007533A (en) | 1990-05-17 | 1990-05-17 | PROCESS FOR THE MANUFACTURE OF TARGETED PULP AND TO DESIGNIFY AND TARGET A LIGNOSCELULOSIC MATERIAL |
AT90908787T ATE122421T1 (en) | 1990-05-17 | 1990-05-17 | MORE ENVIRONMENTALLY FRIENDLY PROCESS FOR BLEACHING LIGNOCELLULOSIC MATERIALS. |
CA002063591A CA2063591C (en) | 1990-05-17 | 1990-05-17 | Environmentally improved process for bleaching lignocellulosic materials |
AU56768/90A AU638017B2 (en) | 1990-05-17 | 1990-05-17 | Environmentally improved process for bleaching lignocellulosic materials |
JP2508269A JP2825346B2 (en) | 1990-05-17 | 1990-05-17 | Environmentally improved bleaching method for lignocellulosic materials |
ES90908787T ES2073027T3 (en) | 1990-05-17 | 1990-05-17 | ENVIRONMENTALLY IMPROVED PROCEDURE FOR WHITENING LIGNOCELLULOSIC MATERIALS. |
PT98487A PT98487B (en) | 1990-05-17 | 1991-07-29 | PROCESS OF PRODUCTION OF A WHITE PASTE AND DISLENCHIFICATION AND BLEACHING OF LENHOCELLULOSIC MATERIALS |
ZA915969A ZA915969B (en) | 1990-05-17 | 1991-07-30 | Process for bleaching lignocellulosic materials |
CN91108650A CN1043798C (en) | 1990-05-17 | 1991-08-07 | Environmentally improved process for bleaching lignocellnlosic materials |
SE9200107A SE9200107L (en) | 1990-05-17 | 1992-01-15 | Delignifying and bleaching lignocellulosic pulps - by digesting then treating in oxygen and ozone stages |
NO920217A NO300929B1 (en) | 1990-05-17 | 1992-01-16 | Process for bleaching lignocellulosic materials |
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PCT/US1990/002823 WO1991018145A1 (en) | 1990-05-17 | 1990-05-17 | Environmentally improved process for bleaching lignocellulosic materials |
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EP (1) | EP0483163B1 (en) |
JP (1) | JP2825346B2 (en) |
KR (1) | KR920703922A (en) |
CN (1) | CN1043798C (en) |
AT (1) | ATE122421T1 (en) |
AU (1) | AU638017B2 (en) |
BR (1) | BR9007533A (en) |
CA (1) | CA2063591C (en) |
DE (1) | DE69019350T2 (en) |
ES (1) | ES2073027T3 (en) |
NO (1) | NO300929B1 (en) |
PT (1) | PT98487B (en) |
RU (1) | RU2102547C1 (en) |
SE (1) | SE9200107L (en) |
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Cited By (23)
Publication number | Priority date | Publication date | Assignee | Title |
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WO1992012289A1 (en) * | 1991-01-03 | 1992-07-23 | Union Camp Patent Holding, Inc. | Chlorine-free process for bleaching lignocellulosic pulp |
EP0512590A1 (en) * | 1991-04-30 | 1992-11-11 | Eka Nobel Ab | Process for bleaching of lignocellulose-containing material |
EP0557112A1 (en) * | 1992-02-21 | 1993-08-25 | Kamyr, Inc. | Chlorine free bleaching and pulping process |
WO1993017178A1 (en) * | 1992-02-20 | 1993-09-02 | Macmillan Bloedel Limited | Nitric oxide treatment for ozone bleaching |
WO1993023607A1 (en) * | 1992-05-11 | 1993-11-25 | Kamyr Ab | A process for bleaching pulp without using chlorine-containing chemicals |
US5328564A (en) * | 1990-09-17 | 1994-07-12 | Kamyr, Inc. | Modified digestion of paper pulp followed by ozone bleaching |
EP0627029A1 (en) * | 1992-01-15 | 1994-12-07 | Union Camp Patent Holding, Inc. | Pulp bleaching apparatus and method |
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WO1995006773A1 (en) * | 1993-09-03 | 1995-03-09 | Union Camp Patent Holding, Inc. | Medium consistency ozone brightening of high consistency ozone bleached pulp |
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WO1995016818A1 (en) * | 1993-12-15 | 1995-06-22 | Mo Och Domsjö Aktiebolag | Method for the manufacture of bleached cellulose pulp |
EP0663030A1 (en) * | 1992-10-01 | 1995-07-19 | Union Camp Patent Holding, Inc. | Improved bleaching of high consistency lignocellulosic pulp |
US5441603A (en) * | 1990-05-17 | 1995-08-15 | Union Camp Patent Holding, Inc. | Method for chelation of pulp prior to ozone delignification |
EP0672210A1 (en) * | 1992-11-13 | 1995-09-20 | Union Camp Patent Holding, Inc. | Method for controlling an ozone bleaching process |
US5672247A (en) * | 1995-03-03 | 1997-09-30 | Union Camp Patent Holding, Inc. | Control scheme for rapid pulp delignification and bleaching |
EP0831170A2 (en) * | 1994-06-27 | 1998-03-25 | Champion International Corporation | Improved process for recycling bleach plant filtrate |
US5736004A (en) * | 1995-03-03 | 1998-04-07 | Union Camp Patent Holding, Inc. | Control scheme for rapid pulp delignification and bleaching |
US5810973A (en) * | 1993-09-21 | 1998-09-22 | Beloit Technologies, Inc. | Apparatus for producing small particles from high consistency wood pulp |
EP0905307A1 (en) * | 1997-08-25 | 1999-03-31 | Praxair Technology, Inc. | Method for applying ozone in ECF bleaching |
US5942088A (en) * | 1995-07-26 | 1999-08-24 | Beloit Technologies, Inc. | Apparatus for bleaching high consistency pulp with a gaseous bleaching reagent |
US5989388A (en) * | 1991-05-24 | 1999-11-23 | Union Camp Patent Holding, Inc. | Method for ozone bleaching of high consistency pulp in two stages |
US6077396A (en) * | 1997-05-16 | 2000-06-20 | Lariviere; Christopher J. | Apparatus for fluffing and contacting high consistancy wood pulp with a gaseous bleaching reagent |
CN103180345A (en) * | 2010-08-11 | 2013-06-26 | 佐治亚技术研究公司 | Chlorine dioxide treatment of biomass feedstock |
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CN1050642C (en) * | 1996-06-25 | 2000-03-22 | 华南理工大学 | Everyday production 30-150 ton high concentration paper pulp bleaching method by using hydrogen peroxide |
FR2910027B1 (en) * | 2006-12-13 | 2009-11-06 | Itt Mfg Enterprises Inc | PROCESS FOR WHITENING CHEMICAL STRIPPING PASTES BY FINAL OZONE TREATMENT AT HIGH TEMPERATURE |
FI119062B (en) * | 2006-12-28 | 2008-07-15 | Upm Kymmene Corp | Process for the manufacture of mechanical pulp |
JP4973284B2 (en) * | 2007-03-30 | 2012-07-11 | 栗田工業株式会社 | Pulp cleaning agent, pulp manufacturing method, and pulp cleaning method |
CN104313933A (en) * | 2014-09-23 | 2015-01-28 | 华南理工大学 | Green bleaching method of sulfate bagasse slurry |
CN115584653B (en) * | 2022-12-12 | 2023-03-10 | 河南禾力能源有限公司 | Method for extracting alpha-cellulose by furfural residues |
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- 1990-05-17 KR KR1019920700104A patent/KR920703922A/en active IP Right Grant
- 1990-05-17 WO PCT/US1990/002823 patent/WO1991018145A1/en active IP Right Grant
- 1990-05-17 RU SU5011189A patent/RU2102547C1/en active
- 1990-05-17 BR BR909007533A patent/BR9007533A/en not_active IP Right Cessation
- 1990-05-17 AU AU56768/90A patent/AU638017B2/en not_active Ceased
- 1990-05-17 DE DE69019350T patent/DE69019350T2/en not_active Expired - Fee Related
- 1990-05-17 ES ES90908787T patent/ES2073027T3/en not_active Expired - Lifetime
- 1990-05-17 JP JP2508269A patent/JP2825346B2/en not_active Expired - Lifetime
- 1990-05-17 AT AT90908787T patent/ATE122421T1/en not_active IP Right Cessation
-
1991
- 1991-07-29 PT PT98487A patent/PT98487B/en not_active IP Right Cessation
- 1991-07-30 ZA ZA915969A patent/ZA915969B/en unknown
- 1991-08-07 CN CN91108650A patent/CN1043798C/en not_active Expired - Lifetime
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1992
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- 1992-01-16 NO NO920217A patent/NO300929B1/en not_active IP Right Cessation
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US5441603A (en) * | 1990-05-17 | 1995-08-15 | Union Camp Patent Holding, Inc. | Method for chelation of pulp prior to ozone delignification |
US5328564A (en) * | 1990-09-17 | 1994-07-12 | Kamyr, Inc. | Modified digestion of paper pulp followed by ozone bleaching |
WO1992012289A1 (en) * | 1991-01-03 | 1992-07-23 | Union Camp Patent Holding, Inc. | Chlorine-free process for bleaching lignocellulosic pulp |
EP0512590A1 (en) * | 1991-04-30 | 1992-11-11 | Eka Nobel Ab | Process for bleaching of lignocellulose-containing material |
EP0554965A1 (en) * | 1991-04-30 | 1993-08-11 | Eka Nobel Ab | Process for bleaching of lignocellulose-containing material |
US5658429A (en) * | 1991-04-30 | 1997-08-19 | Eka Nobel Ab | Process for bleaching of lignocellulose-containing pulp using a chelating agent prior to a peroxide-ozone-peroxide sequence |
US5989388A (en) * | 1991-05-24 | 1999-11-23 | Union Camp Patent Holding, Inc. | Method for ozone bleaching of high consistency pulp in two stages |
EP0515303B2 (en) † | 1991-05-24 | 2001-07-04 | Union Camp Patent Holding, Inc. | Method for ozone bleaching |
EP0627029A1 (en) * | 1992-01-15 | 1994-12-07 | Union Camp Patent Holding, Inc. | Pulp bleaching apparatus and method |
EP0627029A4 (en) * | 1992-01-15 | 1995-12-06 | Union Camp Patent Holding | Pulp bleaching apparatus and method. |
US5364503A (en) * | 1992-02-20 | 1994-11-15 | Macmillan Bloedel Limited | Nitric oxide treatment for ozone bleaching |
WO1993017178A1 (en) * | 1992-02-20 | 1993-09-02 | Macmillan Bloedel Limited | Nitric oxide treatment for ozone bleaching |
EP0557112A1 (en) * | 1992-02-21 | 1993-08-25 | Kamyr, Inc. | Chlorine free bleaching and pulping process |
WO1993023607A1 (en) * | 1992-05-11 | 1993-11-25 | Kamyr Ab | A process for bleaching pulp without using chlorine-containing chemicals |
EP0663030A4 (en) * | 1992-10-01 | 1995-12-06 | Union Camp Patent Holding | Improved bleaching of high consistency lignocellulosic pulp. |
EP0663030A1 (en) * | 1992-10-01 | 1995-07-19 | Union Camp Patent Holding, Inc. | Improved bleaching of high consistency lignocellulosic pulp |
EP0672210A1 (en) * | 1992-11-13 | 1995-09-20 | Union Camp Patent Holding, Inc. | Method for controlling an ozone bleaching process |
EP0672210A4 (en) * | 1992-11-13 | 1995-11-29 | Union Camp Patent Holding | Method for controlling an ozone bleaching process. |
WO1995004188A1 (en) * | 1993-08-03 | 1995-02-09 | Kvaerner Pulping Technologies Ab | A method of integrating bleaching and recovery in the production of pulp |
WO1995006772A1 (en) * | 1993-09-02 | 1995-03-09 | Union Camp Patent Holding, Inc. | Improved method for bleaching lignocellulosic pulp |
WO1995006773A1 (en) * | 1993-09-03 | 1995-03-09 | Union Camp Patent Holding, Inc. | Medium consistency ozone brightening of high consistency ozone bleached pulp |
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US5810973A (en) * | 1993-09-21 | 1998-09-22 | Beloit Technologies, Inc. | Apparatus for producing small particles from high consistency wood pulp |
AU678333B2 (en) * | 1993-12-15 | 1997-05-22 | Mo Och Domsjo Aktiebolag | Method for the manufacture of bleached cellulose pulp |
WO1995016818A1 (en) * | 1993-12-15 | 1995-06-22 | Mo Och Domsjö Aktiebolag | Method for the manufacture of bleached cellulose pulp |
US6126782A (en) * | 1993-12-15 | 2000-10-03 | Mo Och Domsjo Aktiebolag | Method for non-chlorine bleaching of cellulose pulp with a totally closed counter-current liquid circuit |
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US5736004A (en) * | 1995-03-03 | 1998-04-07 | Union Camp Patent Holding, Inc. | Control scheme for rapid pulp delignification and bleaching |
US5672247A (en) * | 1995-03-03 | 1997-09-30 | Union Camp Patent Holding, Inc. | Control scheme for rapid pulp delignification and bleaching |
US5942088A (en) * | 1995-07-26 | 1999-08-24 | Beloit Technologies, Inc. | Apparatus for bleaching high consistency pulp with a gaseous bleaching reagent |
US5944952A (en) * | 1995-07-26 | 1999-08-31 | Beloit Technologies, Inc. | Method for bleaching high consistency pulp with a gaseous bleaching reagent |
US6077396A (en) * | 1997-05-16 | 2000-06-20 | Lariviere; Christopher J. | Apparatus for fluffing and contacting high consistancy wood pulp with a gaseous bleaching reagent |
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CN103180345A (en) * | 2010-08-11 | 2013-06-26 | 佐治亚技术研究公司 | Chlorine dioxide treatment of biomass feedstock |
Also Published As
Publication number | Publication date |
---|---|
ZA915969B (en) | 1992-04-29 |
NO300929B1 (en) | 1997-08-18 |
SE9200107L (en) | 1992-03-13 |
AU5676890A (en) | 1991-12-10 |
BR9007533A (en) | 1992-04-28 |
RU2102547C1 (en) | 1998-01-20 |
DE69019350D1 (en) | 1995-06-14 |
DE69019350T2 (en) | 1996-02-15 |
AU638017B2 (en) | 1993-06-17 |
CN1043798C (en) | 1999-06-23 |
ATE122421T1 (en) | 1995-05-15 |
SE9200107D0 (en) | 1992-01-15 |
JPH05500243A (en) | 1993-01-21 |
NO920217D0 (en) | 1992-01-16 |
EP0483163A4 (en) | 1992-08-05 |
PT98487A (en) | 1993-01-29 |
EP0483163B1 (en) | 1995-05-10 |
PT98487B (en) | 1998-06-30 |
CA2063591C (en) | 1998-02-03 |
EP0483163A1 (en) | 1992-05-06 |
ES2073027T3 (en) | 1995-08-01 |
CA2063591A1 (en) | 1991-11-18 |
KR920703922A (en) | 1992-12-18 |
CN1069304A (en) | 1993-02-24 |
JP2825346B2 (en) | 1998-11-18 |
NO920217L (en) | 1992-03-05 |
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