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
  • D21C9/08—Removal of fats, resins, pitch or waxes; Chemical or physical purification, i.e. refining, of crude cellulose by removing non-cellulosic contaminants, optionally combined with bleaching
  • D21C9/083—Removal of fats, resins, pitch or waxes; Chemical or physical purification, i.e. refining, of crude cellulose by removing non-cellulosic contaminants, optionally combined with bleaching with inorganic compounds

Definitions

• This invention relates to a process for producing dissolving pulps suitable for use in the manufacture of viscose rayon. More particularly, it relates to a new and improved refining and bleaching process for converting sulfite pulps into viscose grade dissolving pulps.
• a related object is to provide a process for producing bleached and refined dissolving pulps suitable from a physical and chemical standpoint as well as a commercial standpoint for use in preparing nonwovens and disposables.
• Another object is to provide a process for producing relatively low cost, viscose grade, dissolving pulps without forming highly toxic, hot caustic extraction efiiuents as a by-product during the bleaching and refining of the pulps.
• a further object is to provide a multi-stage bleaching and refining process for converting unbleached sulfite pulps into viscose grade dissolving pulps.
• a still further object is to provide a process for producing relatively high quality bleached and refined dissolving pulps which require a relatively low capital expenditure for processing and environmental protection plants.
• the process of our invention comprises a new and improved four stage bleaching and refining sequence for converting unbleached sulfite pulps into bleached and refined viscose grade dissolving pulps having the desired physical and chemical characteristics.
• the pulps produced by our process are particularly well suited for use in preparing viscose filaments and staple fibers for the manufacture of nonwoven and disposable fabrics.
• the bleached sulfite viscose pulps produced by our process are obtained in substantially increased yields as compared with prior art processes.
• our process does not require a hot caustic extraction stage during refining.
• the need for costly, high volume, high pressure, refining equipment which has been required heretofore is eliminated and the production of highly toxic, hot caustic extraction efiiuents with the attendant disposal problems also is eliminated.
• our process comprises subjecting a suitable unbleached sulfite pulp to a bleaching and refining sequence including the steps of (l) chlorination; (2) combined alkaline hypochlorite-high consistency, dilute caustic extraction; (3) low consistency extraction with concentrated caustic solution; and (4) alkaline hypochlorite treat.
• particularly desirable sulfite pulps for use in our process are the relatively inexpensive, high yield, easy bleaching, paper grade sulfite wood pulps.
• the soluble base cooking liquor used for the socalled acid sulfite" process has a total S0 content of about 6.0 to 8.5 percent and a relatively high combined S0 content of 0.8 to 1.2 percent, based on the weight of the liquor. Pulping is normally continued for about 5 to 7 hours at about to C. and at a pH of 1 to 2.
• the digested pulp is then blown out of the digester, washed and dewatered by conventional techniques.
• Another preferred raw material for use in our process is paper grade sulfite wood pulp prepared by the so-called bisulfite process in which the cooking liquor normally has a total S0 content of about 3.5 to 5.0 percent and a relatively high combined S0 content of about 1.75 to 2.5 percent. Pulping is continued for about 5 to 7 hours at a pH of about 3 to 6 and a temperature of about 150 to C. The pulp is then blown from the digester, washed and dewatered by conventional methods. Both of the foregoing techniques for producing preferred starting materials for our process provide minimum degradation and loss of cellulose and a maximum yield of easybleaching paper grade pulp.
• an unbleached sulfite pulp is initially treated in a chlorination stage at a consistency of about 3 percent on an oven dried pulp basis, with about 1-5 percent chlorine.
• This chlorination stage is performed at a pH not greater than about 4.0, preferably in a range of about pH 1.5 to 3.5, at a temperature of about 5-30 C., preferably about 3 20-30 C. for a period of time sufiicient to allow substantial completion of the reaction. This time period will vary depending on factors such as the particular pulp being treated and the processing conditions employed, but normally will not exceed about 60 minutes, preferably about 10-30 minutes.
• the pulp is washed with water and the aqueous pulp suspension then is subjected to a combination hypochlorite-mild caustic extraction stage wherein an alkaline hypochlorite treat is followed immediately without an intervening wash by a high consistency, mild caustic extraction.
• an alkaline hypochlorite for instance an alkali metal or alkaline earth metal hypochlorite, for example sodium or calcium hypochlorite, is added to the washed pulp suspension at a pulp consistency of about 9-17% on an oven dried pulp basis preferably about 12%.
• hypochlorite sufiicient to provide about 2-3 percent available chlorine based on the weight of the pulp with excess caustic soda being incrp0- rated to maintain the pH at about -11 when the hypochlorite is consumed. This treatment is continued until all the hypochlorite is consumed, preferably for a period of about 1-2 hours, at a temperature in the range of about 30-70 C., and preferably about 35 C.
• the pulp stock is subjected to a mild caustic extraction with suflicient sodium hydroxide to insure an excess of caustic at the end of treat,
• this mild caustic extraction is carried out at atmospheric pressure with the addition of less than about 4 percent sodium hydroxide (based on the weight of the pulp) and at a temperature of less than about 70 C. for a period of about l-4 hours depending upon the conditions used.
• the final pH of this mild caustic treat is again maintained at about 10-11.
• the suspension obtained in the combination hypochlorite-mild caustic extraction stage is then washed with water and dewatered.
• the pulp is then subjected to a cold caustic extraction stage with aqueous caustic soda solution at low pulp consistency to remove hemicelluloses and other carbohydrate impurities.
• the cold alkali extraction is conducted at a temperature in the range of about 50 0., preferably about l5-25 C., under atmospheric pressure with caustic concentration being about 4-11% (on a solution basis) and preferably about 7%, and a consistency of about 3% (based on the weight of the pulp), for about 3-20 minutes.
• an alkaline hypochlorite solution such as a sodium or calcium hypochlorite solution, having about 2% available chlorine (based on the weight of the pulp) is added to the pulp and a suflicient amount of sodium hydroxide is also added to maintain at all times a pH of at least 7, and preferably about 11.
• the temperature is kept between about 30 and 70 C., and preferably about 55 C., and the treatment is continued until the stock has the desired Cuene intrinsic viscosity (about 3-6 I.V.) and brightness (about 90-94 ELB). Normally, this takes about 45-120 minutes depending upon factors such as the pulp employed, the
• the resulting bleached and refined pulp is then dewatered, washed, treated with S0 and dried by conventional methods.
• the dissolving pulps produced by the process of the present invention have been found to be reactive and xanthate readily into easy filtering viscose solutions suitable for spinning into rayon filament that is particularly useful in preparing nonwoven and disposable fabrics. Additionally, the bleached and refined viscose grade dissolving pulps produced by our process are recovered in substantially higher yields and at lower cost than similar grade pulps produced by prior techniques.
• EXAMPLE I This example is set forth to demonstrate the advantages obtained when the process of the present invention is applied to an unbleached paper grade sulfite wood pulp as compared with a conventional prior art viscose-type bleaching and refining process applied to the same unbleached paper grade pulp.
• a batch of Western hemlock wood chips was prepared and cooked to a fairly raw sulfite paper grade pulp by conventional methods using a sodium base acid sulfite cooking liquor.
• the unbleached pulp which had a Cuene intrinsic viscosity (I.V.) of 11.1 and a permanganate No. (K No.) of 20 was obtained in a screened yield of 46.5 percent (on an oven dried pulp basis).
• Two samples of this pulp (3 kg. each) were bleached and refined by the following methods:
• Method (1) Normal bleaching and refining process previously employed in the production of viscose grade dissolving pulps First Stage. The unbleached pulp was chlorinated by conventional means for 20 minutes at 20 C. with 4 percent added chlorine. The pulp consistency was 3 percent on an OD. pulp basis. The pulp was then washed, dewatered and passed on to the next stage.
• Method (2) -Method of the present invention for bleachmg and refining pulps to produce viscous grade dissolving pulps
• Second stage The pulp from the preceding stage was treated with an alkaline sodium hypochlorite solution containing 2.2 percent available chlorine and 1.6 percent sodium hydroxide on an OD. pulp basis. The consistency was 14 percent and the treatment was continued for minutes at 35 C. Without washing and in the same vessel, l-3 percent NaOH was then added to the charge, the temperature was raised to 40 C. and the treatment con-- tinued for another 105 minutes. The pulp was then washed, dewatered and passed on to the next stage.
• pulp from the preceding stage was treated with an alkaline sodium hypochlorite solution containing 2.2 percent available chlorine and 0.9 percent sodium hydroxide on an O.D. pulp basis.
• the treatment was continued for 70 minutes at 55 C. and the consistency on an O.D. pulp basis was 15 percent.
• the bleached pulp was then washed, dewatered, treated with to a pH of 2.8 and dried by conventional methods.
• Viscosity b.f.s 47. 2 81- 2 Plugging value, g./cm. 1, 500 2, 200
• EXAMPLE Ii This example is set forth to demonstrate the very substantial increase in bleached yield obtained by applying the process of the present invention to a paper grade sulfite pulp as compared with a conventional prior art process applied to a conventional dissolving grade unbleached pulp.
• a batch of wood chips was prepared from Eucalyptus wood and divided into several portions. One portion was cooked to a rather raw paper grade pulp having a K No. of 18.8 and a Cuene I.V. of 12.4. The screened pulp yield was 53.9 percent. Another portion of the chips was cooked to a rather soft rayon grade pulp having a K No. 8.7 and a Cuene I.V. of 8.42 with a screened pulp yield of 6 48.4 percent. Both batches were cooked by the acid sulfite process using a soda base acid sulfite cooking liquor. The washed unbleached pulps were then bleached and refined by the processes of Example I under the conditions and with the results set forth in Table 2 wherein chemical additions are based on O.D. pulp except where noted.
• a process for producing dissolving pulps suitable for use in the manufacture of viscose rayon which comprises treating an unbleached sulfite pulp in a four-stage bleaching and refining process comprising in sequence (1) a chlorination stage wherein said sulfite pulp is treated with about 1-5 percent chlorine (ovendried pulp basis) for about 10-60 minutes, (2) a combined alkaline hypochlorite mild caustic extraction stage wherein at the conclusion of said hypochlorite treatment and without an intervening wash, said sulfite pulp is subjected to said caustic extraction at atmospheric pressure and at a temperature less than about 70 C. for a period of less than about 4 hours, (3) a cold caustic extraction stage at a temperature of about 15-50 C.
• an alkaline hypochlorite stage wherein an alkaline hypochlorite having about 2 percent available chlorine (based on the weight of the pulp) is added to the pulp and the pH is maintained at least about 7 and the temperature at about 30-70 C.
• paper grade sulfite pulp is prepared by a process comprising digesting wood chips in a soluble base cooking liquor having a total S content of about 6.0 to 8.5 percent and a combined 80;, content of 0.8 to 1.2 percent, based on the weight of the liquor, for about to 7 hours at about 130 to 150 C. and at apH of 1 to 2.
• said paper grade sulfitc pulp is prepared by a process comprising digesting wood chips in a cooking liquor having a total S0 content of about 3.5 to 5.0 percent and a combined S0 content of about 1.75 to 2.5 percent, based on the 'weight of the liquor, for about 5 to 7 hours at a pH of about 3 to 6 and a temperature of about 150 to 165 C.
• said combined alkaline hypochlorite-mild caustic extraction stage comprises treating said pulp with an alkaline hypochlorite at a pulp consistency of about 917% (oven dried pulp basis) in an amount sufiicient to provide about 2-3 percent available chlorine (based on the weight of pulp) with excess caustic soda being incorporated to maintain the pH at about -11 when the hypochlorite is consumed, continuing the hypochlorite treatment of said pulp for a period of about 1-2 hours, at a temperature in the range of about 3070 C., then without an intervening wash subjecting said pulp to a mild caustic extraction with an amount of sodium hydroxide sufiicient to provide a final pH of about 10-11 and less than about 4 percent sodium hydroxide (based on the weight of pulp), at a temperature of up to about 70 C., and for a period of about 1-4 hours.
• a process for bleaching and refining unbleached sulfite pulp which comprises treating said unbleached pulp in a chlorinatioin stage at a pulp consistency of about 3 percent (oven dried pulp basis) with about 1-5.
• hypochlorite treatment in said combination hypochlorite-mild caustic extraction stage is carried out for a period of about 1-2 hours.
• ROBERT L. LINDSAY 111.
• Primary Examiner A. L. CORBIN Assistant Examiner

Landscapes

• Life Sciences & Earth Sciences (AREA)
• Engineering & Computer Science (AREA)
• Wood Science & Technology (AREA)
• Paper (AREA)
• Polysaccharides And Polysaccharide Derivatives (AREA)

Priority Applications (5)

Applications Claiming Priority (1)

Publications (1)

Family

ID=23003954

Family Applications (1)

Country Status (5)

Cited By (4)

• 1972
  • 1972-06-19 US US00263954A patent/US3817825A/en not_active Expired - Lifetime
• 1973
  • 1973-05-31 FI FI1772/73A patent/FI60735C/fi active
  • 1973-06-15 SE SE7308428A patent/SE403151B/sv unknown
  • 1973-06-18 CA CA174,343A patent/CA988660A/en not_active Expired
  • 1973-06-19 ES ES416085A patent/ES416085A1/es not_active Expired

Also Published As

Similar Documents

Legal Events