EP1790771A1 - Méthode pour blanchir de la pâte - Google Patents

Méthode pour blanchir de la pâte Download PDF

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Publication number
EP1790771A1
EP1790771A1 EP05748560A EP05748560A EP1790771A1 EP 1790771 A1 EP1790771 A1 EP 1790771A1 EP 05748560 A EP05748560 A EP 05748560A EP 05748560 A EP05748560 A EP 05748560A EP 1790771 A1 EP1790771 A1 EP 1790771A1
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EP
European Patent Office
Prior art keywords
pulp
bleaching
light
treatment
brightness
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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EP05748560A
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German (de)
English (en)
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EP1790771A4 (fr
Inventor
Shoichi Miyawaki
Kazuhiro Kurosu
Takashi Ochi
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Nippon Paper Industries Co Ltd
Jujo Paper Co Ltd
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Nippon Paper Industries Co Ltd
Jujo Paper Co Ltd
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Priority claimed from JP2004169367A external-priority patent/JP4603298B2/ja
Priority claimed from JP2004289267A external-priority patent/JP2006104587A/ja
Priority claimed from JP2005102615A external-priority patent/JP2006283213A/ja
Priority claimed from JP2005102558A external-priority patent/JP2006283211A/ja
Application filed by Nippon Paper Industries Co Ltd, Jujo Paper Co Ltd filed Critical Nippon Paper Industries Co Ltd
Publication of EP1790771A1 publication Critical patent/EP1790771A1/fr
Publication of EP1790771A4 publication Critical patent/EP1790771A4/fr
Withdrawn legal-status Critical Current

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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
    • D21C9/1005—Pretreatment of the pulp, e.g. degassing the pulp
    • 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
    • D21C9/1084—Bleaching ; Apparatus therefor with reducing compounds
    • 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
    • D21C9/16—Bleaching ; Apparatus therefor with per compounds

Definitions

  • the present invention relates to a bleaching process for pulp characterized in that a pulp washed after an acid treatment is irradiated with UV light and/or visible light under alkaline conditions; a bleaching process characterized in that a pulp washed after an acid treatment is treated by a combination of irradiation with UV light and/or visible light and ozone feeding, thereby promoting pulp bleaching; and a bleaching process for chemical pulp by which a high brightness chemical pulp can be obtained (herein collectively referred to as the first invention); as well as a high brightness chemical pulp with greatly improved discoloration and a paper containing it, more specifically a novel high brightness chemical pulp with greatly improved discoloration obtained by further treating a bleached chemical pulp with UV light and a paper containing it (herein collectively referred to as the second invention).
  • Such acid treatment techniques previously disclosed include a process for delignifying a pulp prepared from a lignocellulose material by oxygen bleaching, comprising first adding a nitrite and an acid to the pulp to pretreat the pulp, followed by oxygen bleaching, or a bleaching process comprising subjecting a cooked chemical pulp to an acid treatment followed by delignification with a peroxide and pressurized oxygen in an alkaline medium (e.g., patent document 1, patent document 2).
  • Another bleaching process comprising subjecting a cooked chemical pulp to an oxygen bleaching treatment at high temperature and high pressure and then an acid treatment or a chelator treatment followed by delignification/bleaching with a peroxide or hydrogen peroxide and oxygen in an alkaline medium (e.g., patent document 3).
  • a technique was disclosed wherein a suspension of a cellulose pulp prepared by the sulfate process or alkaline process is heated and treated at about 85 to 150°C and a pH of about 2 to 5 to remove at least about 50% of hexenuronic acid in the cellulose pulp, thereby decreasing the Kappa number of the pulp by 2 to 9 units (see patent document 4).
  • Bleaching techniques using irradiation were also disclosed, such as techniques involving UV irradiation in hydrogen peroxide bleaching of unbleached kraft pulps (e.g., see non-patent document 1, or patent document 5), or UV irradiation in oxygen bleaching of unbleached kraft pulps (e.g., see non-patent document 2).
  • UV irradiation in the presence of a peroxide as a pretreatment for promoting normal alkaline hydrogen peroxide bleaching was also disclosed (e.g., see patent document 6).
  • Paper products mainly made from chemical pulp, especially communication papers such as inkjet papers and thermal transfer papers or photographic base papers are required to have high brightness.
  • materials responsible for coloration such as lignin or polysaccharides remaining in the unbleached pulp are removed by multistage bleaching with chemicals such as chlorine, hypochlorites, chlorine dioxide, oxygen, hydrogen peroxide, ozone, etc.
  • the ISO brightness of pulp obtained by chlorine bleaching with chlorine gas or more environmentally friendly ECF bleaching with reduced production of organic chlorine compounds using chlorine dioxide is normally 82 - 86%.
  • High brightness pulp bleached to a higher brightness level than normal is typically prepared by applying harsher cooking and/or bleaching conditions or by using easy-to-cook and bleach wood species having low contents of phenolic extract components.
  • a process for preparing a high brightness pulp was disclosed, for example, characterized in that a pulp bleached in a sequence including at least one chlorine bleaching stage is treated with xylanase and further bleached in a bleaching sequence including a hypochlorite stage and a chlorine dioxide stage (see patent document 10).
  • Another process for preparing a high brightness pulp comprising further bleaching a bleached pulp derived from a lignocellulose material via a continuous sequence of a hypochlorite bleaching stage under high temperature and highly alkaline conditions and a chlorine dioxide bleaching stage, characterized in that the chlorine dioxide bleaching stage is performed at a chlorine dioxide concentration of 1-3% by weight (on the basis of the bone dry weight of the pulp) at a high temperature of 91°C or more and less than 100°C (see patent document 11).
  • a photographic base paper was also disclosed, characterized in that it uses a chemical pulp bleached in a bleaching sequence of oxygen bleaching - ozone bleaching - alkali extraction - hydrogen peroxide bleaching - chlorine dioxide bleaching - hydrogen peroxide bleaching - chlorine dioxide bleaching and that the chemical pulp is bleached with 0.1 - 1.0% by weight of ozone on the basis of the bone dry weight of the pulp during the ozone bleaching stage (see patent document 12).
  • a process for preparing a high brightness pulp with improved discoloration for use in photosensitive materials was also disclosed, characterized in that an unbleached kraft pulp having a kappa number of 23 or less is bleached with oxygen at a delignification degree of 40% or more and then bleached with ozone at a pulp consistency of 25% or more and then adjusted to a PN number of 2.8 or less followed by multistage bleaching including hydrogen peroxide bleaching and chlorine dioxide bleaching (see patent document 13).
  • it was difficult to avoid brightness loss with time or so-called discoloration phenomenon in high brightness pulps obtained by the conventional processes because very small amounts of potential coloring matters liable to be darkened by heat or UV light remain in them.
  • the first invention aims to further advance the acid treatment or irradiation technology for pulp as described above to develop a bleaching process using less chlorine chemicals with higher efficiency as compared with conventional bleaching processes, and to develop a TCF bleaching process capable of achieving a final ISO brightness of 84% or more while greatly shortening the irradiation period at the light bleaching stage by inserting an acid treatment and a bleaching stage used in normal TCF bleaching before the light bleaching stage and an alkaline hydrogen peroxide bleaching stage after the light bleaching stage.
  • the second invention aims to overcome the drawbacks of the conventional technology and to provide a high brightness pulp having a low environmental impact and no discoloration as well as a paper containing it.
  • TCF totally chlorine-free
  • the second invention relates to a high brightness chemical pulp having an ISO brightness of 88% or more and a brightness loss of 1.0% or less in the following fading test:
  • the first and second aspects of the first invention are applied to pulps washed after an acid treatment. Especially, they are applied to kraft pulps (KPs) and are well suitable for not only unbleached KPs but also oxygen-delignified KPs, ozone-bleached KPs, etc.
  • the bleaching process according to the third aspect of the first invention is applied to kraft-cooked and oxygen-delignified chemical pulps.
  • the pulp materials used in the first invention and the second invention (chemical pulp) are not specifically limited and include hardwood and softwood as well as other plants such as kenaf, flax, rice, bagasse, bamboo, etc.
  • the oxygen-delignified pulp is acid-treated and then bleached by a bleaching process used in normal TCF bleaching, and the resulting pulp is further subjected to an irradiation treatment with UV light and/or visible light at a wavelength of 100 - 400 nm under alkaline conditions, followed by alkaline hydrogen peroxide bleaching.
  • the type of the acid used in the acid treatment of the present invention may be inorganic or organic.
  • Inorganic acids that can be used include mineral acids such as sulfuric acid, hydrochloric acid, nitric acid, sulfurous acid, nitrous acid, phosphoric acid, and residual acids in chlorine dioxide generators. Sulfuric acid is preferred.
  • Organic acids that can be used include acetic acid, lactic acid, oxalic acid, citric acid, formic acid, etc.
  • the pH during the acid treatment is in the range of 1.0 - 6.0, preferably1.0 - 5.0, more preferably 2.0 - 5.0, most preferably 2.5 - 3.5.
  • the acid treatment can be performed at an atmospheric pressure or under pressure and at a temperature of 80°C - 180°C, preferably 80°C - 130°C. Temperatures of 30 °C or higher and lower than 80°C are effective for removing metals but not effective for removing hexenuronic acid or the like. Temperatures lower than 100°C are advantageous in terms of equipment costs because no pressure-tight reaction chamber is required.
  • the pulp consistency during the acid treatment is in the range of 0.1 - 50% by weight, preferably1.0 - 30% by weight, more preferably 2.0 - 20% by weight.
  • reaction period is determined as appropriate depending on the other two conditions, but typically the reaction period is 1.5 - 6 hours at a reaction temperature of 90°C, the reaction period is 50 minutes - 5 hours at a reaction temperature of 95°C, the reaction period is 30 minutes - 4.5 hours at a reaction temperature of 100°C, and the reaction period is 5 - 50 minutes at a reaction temperature of 120 - 130°C.
  • Ozone bleaching under acidic conditions is also a form of the acid treatment contemplated by the present invention, and normal acidic ozone bleaching conditions can be applied.
  • typical acidic ozone bleaching conditions regarded as suitable include using ozone gas at an ozone concentration of 1 - 20% by weight at pH 1.0 - 8.0 (the first and third aspects of the first invention) or pH 1 - 7(the second aspect of the first invention) at a pulp consistency of 0.1 - 50% by weight and a temperature of 25 - 95°C.
  • the pressure here is not specifically limited from a negative pressure state to a pressurized state.
  • a further greater bleaching reaction promoting effect is obtained in the irradiation treatment by using chelating agents such as EDTA, DPTA in combination with the acid treatment.
  • the pulp can be dehydrated and/or washed by using a known dehydrator and/or washing after the acid treatment including ozone bleaching. Washing can be performed by using not only fresh water but also wastewater generated from bleaching processes after the acid treatment or wastewater generated from papermaking processes.
  • the acid-treated pulp is irradiated with UV light and/or visible light at a wavelength of 100 - 400 nm under alkaline conditions, preferably at pH 10 - 13.
  • hardwood pulps are preferably treated at pH 10 - 12, and softwood pulps are treated at pH 11 - 13.
  • the acid-treated pulp is irradiated with UV light and/or visible light at a wavelength of 100 - 400 nm under alkaline conditions or acidic conditions.
  • the alkaline conditions are in a pH range of 10 - 13 and the acidic conditions are in a pH range of 2 - 4.
  • the alkalis used for this pH adjustment can be normal alkaline chemicals, but especially preferred are sodium hydroxide, potassium hydroxide, sodium silicate and sodium carbonate because of easy handling.
  • the pulp consistency during the irradiation treatment according to the present invention is preferably 0.1 - 12% by weight. Consistencies lower than 0.1% by weight are not preferred because energy efficiency decreases though bleaching reaction efficiency increases. Consistencies higher than 12% by weight are not preferred because the rheology of pulp slurry in the irradiator decreases so that bleaching reaction efficiency decreases.
  • the temperature of pulp slurry during this irradiation treatment is preferably 20 - 95°C, and temperatures lower than 20 °C are not preferred because bleaching reaction efficiency is low while temperatures exceeding 95°C are not preferred, either, because pulp quality may deteriorate or the pressure in the reactor may exceed atmospheric pressure so that the reactor must be designed to resist pressure.
  • the wavelength of the light emitted in the irradiator of the present invention is preferably 100 - 400 nm, especially 200 - 360 nm (180 - 360 nm in the second aspect of the first invention). Wavelengths shorter than 100 nm are not preferred because photodegradation of cellulose is promoted so that pulp strength is greatly lowered, while wavelengths exceeding 400 nm are not preferred, either, because photosensitive coloring matters are insufficiently photoexcited so that light bleaching performance is greatly lowered.
  • Irradiation sources that can be used include those emitting light in a wavelength range of 100 - 400 nm, specifically xenon short arc lamps, ultra high pressure mercury lamps, high pressure mercury lamps, low pressure mercury lamps, deuterium lamps, metal halide lamps, etc., [see Kinoshita: “UV irradiators", Adhesion (2002, vol. 46, No. 7) pp. 20 - 27 ; or Sugimori Akira: "Photochemistry, Chapter 8 Experimental methods of photochemistry I” (Shokabo Publishing Co., Ltd. 1998) pp. 126-136 ], which can be used alone or by combining two or more methods.
  • the degree of irradiation to which pulp is exposed in the irradiation reactor can be adjusted at will by controlling the retention time of pulp in the irradiation reactor or controlling the power of the irradiation source.
  • the retention time of pulp in the irradiation reactor can be controlled by diluting the pulp consistency in the irradiation reactor with water or by blowing air or an inert gas such as nitrogen into pulp slurry to control the pulp consistency. These conditions can be selected as appropriate depending on the pulp quality goals (brightness, etc.) after the irradiation reaction.
  • the second aspect of the first invention is characterized in that the irradiation treatment with UV light and/or visible light at a wavelength of 100 - 400 nm is performed in the presence of ozone.
  • ozone is normally generated due to the presence of air in the gas layer around the light source.
  • air is continuously supplied to the surroundings of the light source while continuously extracting the generated ozone and injecting it into the irradiation target material, whereby the ozone can be used as a reaction promoter without supplying ozone from any external source.
  • a larger amount of ozone can be obtained by supplying air to the gas layer around the light source.
  • the generated ozone can be used not only as a promoter during the irradiation reaction but also for regular ozone bleaching.
  • another great advantage of the present invention is that the ozone by-produced in the irradiation reactor can be used.
  • Ozone can also be generated by supplying such air or oxygen to the pulp to be treated but not to the surroundings of the light source.
  • ozone obtained from an external source by a method not relying on such effect of UV light can also be used as a reaction promoter.
  • the concentration of the ozone by-produced in the irradiation reactor is 0.5 - 100 ppm, depending on the manner of supplying air or oxygen or the concentration of oxygen.
  • a major feature of the second aspect of the first invention is that a high bleaching efficiency can be obtained with even such low-concentration ozone by combination with the irradiation treatment.
  • This concept can be further expanded to select and use multiple light sources having a characteristic wavelength range within 100 - 400 nm and different characteristic wavelengths as light sources in the irradiation reactor.
  • a light source having a narrow wavelength characteristic of 135 - 242 nm providing a high ozone-generating efficiency and a light source having an evenly distributed wavelength range of 100 - 400 nm suitable for irradiation reaction can be combined, for example, whereby a further higher bleaching efficiency can be obtained.
  • the irradiation reaction efficiency can be increased by using a combination of additives such as reducing agents (e.g., NaBH 4 , hydrazine, hydrogen), oxidizing agents (e.g., oxygen, ozone), peroxides (e.g., hydrogen peroxide, peracetic acid, Na percarbonate, Na perborate), hydrogen-donating organic compounds (e.g., alcohols; linear amines such as ethyl amine, diethylamine; cyclic amines such as tetramethyl piperidine), acetyl-containing organic compounds (e.g., a-acetyl- ⁇ -butyrolactone, acetol, acetone).
  • additives such as reducing agents (e.g., NaBH 4 , hydrazine, hydrogen), oxidizing agents (e.g., oxygen, ozone), peroxides (e.g., hydrogen peroxide, peracetic acid, Na percarbonate, Na perborate),
  • ozone bleaching, hydrogen peroxide bleaching and the like can be used alone or in combination as TCF bleaching for attaining an ISO brightness of 70 - 75% before the light bleaching stage.
  • ozone bleaching can be performed under normal ozone bleaching conditions. That is, ozone bleaching conditions may include using ozone gas at an ozone concentration of 1 - 20% by weight at pH 1 - 8, a pulp consistency of 0.1 - 50% by weight, and a temperature of 25 - 95°C.
  • the pressure during ozone bleaching is not specifically limited from a negative pressure state to a pressurized state.
  • hydrogen peroxide bleaching can be performed under normal alkaline hydrogen peroxide bleaching. That is, alkaline hydrogen peroxide bleaching can be performed with hydrogen peroxide at a concentration of 0.1 - 2.0% by weight based on the pulp, pH 11 - 13, a pulp consistency of 0.1 - 50% by weight, and a temperature of 50 - 95°C.
  • the ISO brightness has been improved to 70 - 75% in advance by normal TCF bleaching after the acid treatment, whereby the treatment period for light bleaching can be greatly shortened, and as a result, electric power costs required for light bleaching can be greatly reduced.
  • the ISO brightness is improved by 5% or more to reach 75 - 80% by light bleaching followed by hydrogen peroxide bleaching at the final bleaching stage, whereby the hydrogen peroxide bleaching reaction is promoted so that a pulp having an ISO brightness of 84% or more can be efficiently obtained.
  • the brightness is preferably improved by hydrogen peroxide bleaching rather than light bleaching in terms of bleaching costs. If the brightness after TCF bleaching is lower than 70%, large amounts of coloring components are contained in the pulp so that a long period is required for the light bleaching treatment to achieve a final brightness of 84% or more, which invites an increase in electric power costs. If the brightness after light bleaching is lower than 75%, it is difficult to achieve a final brightness of 84% or more by hydrogen peroxide bleaching alone because of relatively large amounts of hard-to-bleach coloring components remaining in the pulp.
  • An acid-treated pulp is received in an irradiation target material conditioning tank (10), where it is conditioned to a temperature, pH and pulp consistency suitable for irradiation reaction while stirring.
  • the conditioned irradiation target material 1 is sent to an irradiation reactor (12) via an irradiation reactor feeding pump (11). Before that, an additive such as a reducing agent in the irradiation reaction is added as a chemical solution, if desired.
  • the additive can be added at the site indicated in Figure 1 or the irradiation target material conditioning tank (10) or both at will depending on the properties of the additive or irradiation reaction conditions, but fast-reacting additives or highly decomposable additives are preferably added immediately before the entry into the irradiation reactor (12), i.e. the site indicated in Figure 1.
  • a gas can be supplied before the entry into the irradiation reactor (12). This allows the pulp consistency in the irradiation reactor (12) to be controlled (in terms of% by volume here because of the low gas density), whereby the retention time of the pulp in the irradiation reactor (12) or the irradiation reaction period can be controlled at will.
  • the type of the gas used here is preferably air or an inert gas such as nitrogen, and such gas is used as fine bubbles dispersed in a pulp slurry.
  • a gas such as hydrogen, oxygen or ozone is used among photoreaction promoters, it can also be supplied to a site indicated in the figure in the same manner.
  • the pulp having reached quality goals and leaving the irradiation reactor (12) after the irradiation reaction exits the irradiation reaction and is sent to the subsequent step (C1: pulp after irradiation reaction 1).
  • the pulp falling short of pulp quality goals is recycled to repeat the irradiation reaction (C2: pulp after irradiation reaction 2).
  • the ratio of C1 to C2 can be determined at will in response to pulp quality goals.
  • the irradiation reactor basically consists of an irradiation source section and a pulp slurry container section, and the present invention is not specifically limited to either the internal irradiation type in which the irradiation source section exists inside the pulp slurry container section or the external irradiation type in which the irradiation source section exists outside the pulp slurry container section [see Sugimori Akira: "Photochemistry, Chapter 8 Experimental methods of photochemistry I" (Shokabo Publishing Co., Ltd. 1998) pp. 126 - 136 ]. It is necessary to provide a barrier against gases such as air normally existing around the light source section from which light is emitted to a pulp slurry. In this regard, the choice of the barrier material is important in order that light energy may permeate through the barrier without being attenuated.
  • a hard glass barrier can be used in combination with light at a wavelength longer than e.g., 300 nm, while a quartz glass barrier is used in combination with light at a wavelength shorter than 254 nm.
  • the materials of parts of the pulp slurry container not involved in light transmission reaction can be selected from suitable materials less sensitive to the light wavelength used.
  • An example of an irradiation reactor is shown in Figure 2.
  • An acid-treated pulp is conditioned to a temperature, pH and pulp consistency suitable for irradiation reaction and optionally combined with additives such as reducing agents if desired, and then injected as slurry (a1) into a reaction chamber (20) via (25).
  • the injected pulp slurry undergoes irradiation reaction with light generated from an irradiation source (22) and having passed through the barrier (21: quartz glass tube) while it flows within the reactor (20), after which it is discharged from an outlet (26) of the reactor.
  • a gas can be supplied via a diffuser (24) fitted to the irradiation reactor (20).
  • the type of the gas used here is preferably air or an inert gas such as nitrogen, and such gas is used as fine bubbles dispersed in a pulp slurry.
  • ozone exists in the gas discharged from the irradiation section.
  • This discharged gas containing ozone can be injected into a pulp slurry in the irradiation reactor (20) via diffuser (24), whereby the ozone can be used as a reaction promoter without supplying ozone from any external source.
  • the generated ozone can be used not only as an irradiation reaction promoter but also for normal ozone bleaching. It can also be used in combination with a gas effective as an irradiation reaction promoter such as hydrogen, oxygen or ozone injected from an external source. The use of these gases can be selected at will by providing a three-way valve (23a, 23b).
  • the irradiation reactor can be fitted at will with accessory equipments such as temperature/pH controller, gas concentration detector, etc., if desired.
  • the irradiation treatment of the present invention can be repeated one or more times in any manner that can be selected as appropriate depending on a situation such as bleaching efficiency, pulp quality goals (brightness), or the relationship with other bleaching processes used in combination.
  • Examples of manners of repeating the irradiation treatment one or more times are as follows. (1) Two or more irradiators shown in Figure 1 can be provided. In this case, they can be arranged in a series or in parallel. (2) Multiple irradiation sources (which may have identical or different characteristics) can be placed in the irradiator shown in Figure 1. (3) Pulp can be recycled in the system shown in Figure 1.
  • the bleaching process of the present invention can be combined with any other known chlorine or chlorine-free bleaching process.
  • another bleaching process can be followed by the bleaching process of the present invention, or the bleaching process of the present invention can be followed by another bleaching process.
  • bleaching of the present invention is preferably followed by a hydrogen peroxide treatment.
  • These sequences can be repeated multiple times, and a washing stage can be inserted between different bleaching processes.
  • the bleaching sequence incorporating an irradiation system can also be repeated multiple times. When the irradiation treatment is performed multiple times, the irradiation treatment is preferably followed by washing.
  • Embodiments of the second invention are explained below.
  • the present invention relates to a high brightness chemical pulp having an ISO brightness of 88% or more and a brightness loss of 1.0% or less in the fading test described below. That is, our studies revealed that the discoloration of paper evaluated by the fading test using UV light as described below shows a good correlation with the actual discoloration, rather than the conventional thermal fading test.
  • a hand-made paper is prepared according to JIS P 8222 and irradiated with a xenon lamp at an intensity of 67 W/m 2 for 30 minutes in an atmosphere at 30°C according to fading test method B of J. TAPPI No.21 Paper and Paperboard (using a xenon arc lamp light fastness tester) and then the ISO brightness is measured and a loss from the ISO brightness before treatment is determined.
  • the chemical pulp used in the present invention can be obtained by using known cooking processes such as kraft cooking, polysulfide cooking, sodium hydroxide cooking or alkaline sulfite cooking, among which kraft cooking is preferred in terms of pulp quality and energy efficiency.
  • Kraft cooking processes include known modified cooking processes such as MCC, EMCC, ITC, and Lo-solids processes, any of which can be applied to the present invention without limitation.
  • Wood can be kraft-cooked under known conditions, for e.g., under conditions described below.
  • the sulfidity of the cooking liquor is 7 - 75%, preferably 15 - 45%
  • the effective alkali content is 5 - 30% by weight, preferably 10 - 25% by weight on the basis of the bone dry weight of wood
  • the cooking temperature is 140 - 170°C.
  • the cooking process may be in a continuous mode or a batch mode, and the type of cooker is not specifically limited.
  • the chemical pulp used in the present invention is obtained by washing an unbleached chemical pulp obtained by a known cooking process, passing it through coarse screening and fine screening steps and then subjecting it to an oxygen delignification treatment.
  • the oxygen delignification can be performed under known conditions. In the case of hardwood chemical pulps, the kappa number after oxygen delignification is typically in the range of 5 - 15, preferably 7 - 15, more preferably 8 - 12.
  • This oxygen delignification treatment is performed by a known, medium consistency process or high consistency process.
  • typical reaction conditions for the medium consistency process include a pulp consistency of 10 - 18% by weight, a temperature of 100 - 110°C, a reaction period of 60 - 120 minutes, and a pressure in the reactor of 3 - 6 kg/m 2 , and the sodium hydroxide content and the oxygen content are adjusted depending on the target kappa number.
  • a pulp having undergone oxygen delignification followed by an acid treatment it is preferable to use a pulp having undergone oxygen delignification followed by an acid treatment.
  • the type of the acid used in the acid treatment of the pulp may be inorganic or organic.
  • Inorganic acids that can be used include mineral acids such as sulfuric acid, hydrochloric acid, nitric acid, sulfurous acid, nitrous acid, phosphoric acid, and residual acids in chlorine dioxide generators. Sulfuric acid is preferred.
  • Organic acids that can be used include acetic acid, lactic acid, oxalic acid, citric acid, formic acid, etc.
  • Hardwood pulps are desirably acid-treated in a pH range of 1.5 - 6.0, preferably 1.0 - 5.0, more preferably 2.0 - 5.0, most preferably 2.5 - 3.5. If the pH is less than 1.0, hexenuronic acid and metal ions are sufficiently removed, but the pulp viscosity greatly decreases because of excessive acidity. If the pH exceeds 6.0, however, the acid concentration is so low that hexenuronic acid and metal ions are insufficiently removed. Hardwood chemical pulps can be acid-treated at lower temperatures in a pH range of 2.5 - 3.5, which leads to the advantage that the acid treatment cost can be reduced.
  • the acid treatment can be performed at an atmospheric pressure or under pressure.
  • the reaction temperature during the acid treatment at an atmospheric pressure is in the range of 80°C or higher and lower than 100°C. Preferably, it is 80 - 95°C, more preferably 80 - 90°C. Temperatures of 30°C or higher and lower than 80°C are effective for removing metals but not effective for removing hexenuronic acid.
  • the pulp is continuously bleached by a multistage bleaching process.
  • Chemicals used include those consisting of known bleaching agents such as atomic chlorine (C), sodium hydroxide (E), hypochlorites (H), chlorine dioxide (D), oxygen (O), hydrogen peroxide (P), ozone (Z), sulfuric acid (A), and organic peracids in combination with bleaching additives, and any combination appropriately selected from the above list is used as bleaching chemicals.
  • the bleaching sequence is not specifically limited, and examples that can be used include sequences including atomic chlorine and chlorine bleaching chemicals such as C/D-E/O-H-D; ECF bleaching sequences free from atomic chlorine such as D-E-D, Z-E/O-D; and TCF bleaching sequences totally free from chlorine chemicals such as Z-E-P, A-Z-E/O-P.
  • the high brightness chemical pulp of the present invention is preferably prepared by a process further comprising irradiating the bleached chemical pulp obtained by the process described above with UV light and/or visible light.
  • the bleached chemical pulp before light treatment preferably has been bleached to an ISO brightness of 80% or more, preferably. 86% or more.
  • ISO brightness 80% or more, preferably. 86% or more.
  • very high brightness pulp can be easily obtained by introducing a peroxide bleaching stage after the light treatment stage.
  • the irradiation treatment with UV light and/or visible light is preferably performed under alkaline conditions.
  • the alkaline conditions are preferably in a pH range of 10 - 13.
  • the alkalis that can be used for this pH adjustment include normal alkaline chemicals, among which sodium hydroxide is preferred.
  • the acids that can be used for the pH adjustment include normal acidic chemicals, among which sulfuric acid is preferred.
  • the pulp consistency during the irradiation treatment with UV light and/or visible light is preferably 0.1 - 12% by weight. Consistencies lower than 0.1% by weight are not preferred because energy efficiency decreases though bleaching reaction efficiency increases. Consistencies higher than 12% by weight are not preferred because the rheology of pulp slurry in the bleacher decreases so that bleaching reaction efficiency decreases.
  • the temperature during the irradiation treatment with UV light and/or visible light is not specifically limited, either, but preferably 20 - 95°C. Temperatures lower than 20°C are not preferred because bleaching reaction efficiency is low while temperatures exceeding 95°C are not preferred, either, because pulp quality may deteriorate or the pressure in the reactor may exceed atmospheric pressure so that the reactor must be designed to resist pressure.
  • the irradiation period of UV light and/or visible light can be determined as appropriate by taking into account the structures or concentrations of potential coloring matters contained in the material pulp.
  • UV light and/or visible light used in the present invention is not specifically limited, but it is desirable to use UV light and/or visible light at a wavelength of about 100 - 400 nm, preferably 200 - 360 nm. UV light at a wavelength shorter than 100 nm is not preferred because photodegradation of cellulose is promoted so that pulp strength and brightness are greatly lowered, while UV light at a wavelength exceeding 400 nm is not preferred, either, because coloring matters are insufficiently photoexcited so that light bleaching performance is greatly lowered.
  • Irradiation sources that can be used include conventional light sources such as low-pressure mercury lamps, highpressure mercury lamps, and xenon lamps as well as various excimer lamps and various lasers, but when a large amount of pulp is to be treated, it is desirable to use a high power ozone-generating low-pressure mercury lamp.
  • Ozone-generating UV lamps mainly emit UV light at a wavelength of 254 nm and also include UV light at a wavelength of 185 nm and visible light.
  • the irradiation intensity of UV light at a wavelength of 185 nm is not influenced by temperature, but the intensity of UV light at a wavelength of 254 nm is temperature-dependent and reaches its maximum at 20 - 40°C.
  • high power ozone-generating lamps having a high surface temperature are cooled with air, and at the same time, ozone gas is generated from oxygen in the air by UV light at a wavelength of 185 nm.
  • this ozone gas decomposes by UV light at a wavelength of 254 nm to produce a highly active oxygen species which remarkably promotes decomposition of coloring components.
  • reducing agents include, for example, hydrosulfite and borohydride compounds, etc.
  • oxidizing agents include hydrogen peroxide; sodium percarbonate, peracetic acid, etc.
  • hydrogen-donating organic compounds include primary alcohols such as ethanol.
  • Additives in the present invention may be used alone without using solvents, but should desirably be used as dispersions or solutions in solvents transparent to UV/visible light. Different additives can also be used as mixtures.
  • solvents include water, alcohols, linear or cyclic alkanes, ethers, etc. as single solvents or mixed solvents thereof, preferably water.
  • the amount of each additive to be used is not specifically limited so far as it is at or below the saturated concentration of the additive in the solvent, but a suitable amount is preferably 0.01 - 40% by weight, more preferably 0.1 - 20% by weight in the solvent.
  • Papers containing the high brightness chemical pulp of the present invention can be used as not only book papers but also offset printing papers, relief printing papers, gravure printing papers, newsprint papers, electrophotographic papers, or base papers for coated papers, inkjet recording papers, thermosensitive recording papers, pressure sensitive recording papers or the like.
  • papers containing the high brightness chemical pulp of the present invention may use other raw pulps such as chemical pulps, mechanical pulps and deinked pulps alone or in admixture at any ratio.
  • the pH during the papermaking process may be acidic or neutral or alkaline.
  • Papers containing the high brightness pulp of the present invention can contain paper strength enhancers.
  • paper strength enhancers include starches, modified starches, polyacrylamide, polyvinyl alcohol, polyamide-polyamine resins, urea-formalin resins, melamine-formalin resins, polyethylene imines, etc.
  • the paper strength enhancers are preferably contained in an amount of 0.1% by weight or more and 2% by weight or less on the basis of the bone dry weight of the pulp.
  • Papers containing the high brightness pulp of the present invention can contain fillers.
  • Fillers that can be used include known fillers such as white carbon, talc, kaolin, clay, ground calcium carbonate, precipitated calcium carbonate, titanium oxide, synthetic resin fillers, etc.
  • Papers containing the high brightness pulp of the present invention can further contain aluminum sulfate, sizing agents, yield improvers, freeness improvers, colorants, dyes, antifoaming agents, bulking agents, fluorescent whitening agents or the like, if desired.
  • Papers containing the high brightness pulp of the present invention may not be coated or may be coated with a pigment-free finishing agent.
  • Non-coated papers are desirably coated with a finishing agent based on a water-soluble polymer for the purpose of improving surface strength or sizing performance.
  • Suitable water-soluble polymers include commonly used finishing agents such as starches, modified starches, polyacrylamide, polyvinyl alcohol, etc. alone or as mixtures thereof.
  • the finishing agents can also contain paper strength enhancers designed to improve water resistance or surface strength and external sizing additives designed to provide sizing performance.
  • the finishing agents can be applied with coaters such as two-roll size press coaters, gate roll coaters, blade metering coaters, rod metering coaters, etc.
  • the finishing agents are preferably applied in an amount of 0.1 g/m 2 or more and 3 g/m 2 or less per side.
  • Pulp was defibrated and then formed into a sheet having a basis weight of 60 g/m 2 according to Tappi test method T205os-71 (JIS P 8222), and measured for pulp brightness according to JIS P 8148.
  • An irradiation reaction chamber (1) consists of a 3L glass cylinder (100 mm f x 620 mm H). This irradiation reaction chamber (1) is equipped with a temperature controller and a pH meter in addition to a stirrer (4) and a diffuser tube (5) shown in the figure.
  • An irradiation source (16W low-pressure mercury lamp, AY-1 from Photoscience Japan Corporation) is placed in a quartz glass tube (45 mm f x 470 mm H, thickness 2 mm) in such a manner that air can be injected around the irradiation source.
  • Acid treatment conditions pulp consistency 10% by weight, pH 3.0 (adjusted with sulfuric acid), temperature 95°C, treatment period 180 minutes. After the treatment was completed, the pulp was washed with water.
  • a 5 g (bone dry weight) portion of the acid-treated pulp thus obtained was collected and diluted to a pulp consistency of 0.25% by weight and then prepared into pulp slurries at pHs over an acidic to alkaline range using NaOH and H 2 SO 4 .
  • These slurries were injected into the experimental apparatus shown in Figure 3, and subjected to an irradiation reaction while stirring under conditions of a temperature of 25°C for a treatment period of 120 minutes using a low-pressure UV lamp having a dominant wavelength at 254 nm. After the reaction was completed, the pulps were washed and then formed into sheets and measured for brightness. The results are shown in Figure 4 and Table 1.
  • Example 2 The same oxygen-delignified hardwood kraft pulp as used in Example 1 was treated with ozone under the following conditions to give a pulp having a kappa number of 3.0 and a brightness of 56.6%.
  • Ozone treatment conditions pulp consistency 10%, ozone feed 7 kg/ADTP, temperature 50°C, treatment period 30 seconds, pH 2.5 (adjusted with sulfuric acid).
  • a 5 g (bone dry weight) portion of the ozone-treated pulp thus obtained- was collected and prepared into pulp slurries at pHs over an acidic to alkaline range and subjected to an irradiation reaction under similar conditions to those of Example 1, and the resulting pulps were measured for brightness.
  • the results are shown in Figure 4 and Table 1.
  • Example 1 A 5 g (bone dry weight) portion of the same oxygen-delignified hardwood kraft pulp as used in Example 1 was collected and prepared into pulp slurries at pHs over an acidic to alkaline range and subjected to an irradiation reaction under similar conditions to those of Example 1, and the resulting pulps were measured for brightness. The results are shown in Figure 4 and Table 1.
  • a 5 g (bone dry weight) portion of the same acid-treated pulp as used in Example 1 was collected and diluted to a pulp consistency of 0.25% by weight and then prepared into a pulp slurry at pH 11.5 (adjusted with NaOH and H 2 SO 4 ).
  • This slurry was injected into the experimental apparatus shown in Figure 3, and subjected to an irradiation reaction while stirring under conditions of a temperature of 25°C for varying treatment periods using a low-pressure UV lamp having a dominant wavelength at 254 nm. After the reaction was completed, the pulps were washed and then formed into sheets and measured for brightness. The results are shown in Figure 5 and Table 2.
  • Example 2 A 5 g (bone dry weight) portion of the same ozone-treated pulp as used in Example 2 was collected and subjected to an irradiation reaction under similar conditions to those of Example 3 for varying treatment periods and measured for brightness. The results are shown in Figure 5 and Table 2.
  • Acid treatment conditions pulp consistency 10% by weight, pH 3.0 (adjusted with sulfuric acid), temperature 95°C, treatment period 180 minutes. After the treatment was completed, the pulp was washed with water.
  • a 5 g (bone dry weight) portion of the acid-treated pulp thus obtained was collected and diluted to a pulp consistency of 0.25% by weight and then prepared into pulp slurries at pHs over an acidic to alkaline range using NaOH and H 2 SO 4 .
  • These slurries were injected into the experimental apparatus shown in Figure 3, and subjected to an irradiation reaction while stirring under conditions of a temperature of 25°C for a treatment period of 120 minutes using a low-pressure UV lamp having a dominant wavelength at 254 nm. After the reaction was completed, the pulps were washed and then formed into sheets and measured for brightness. The results are shown in Figure 5 and Table 3.
  • Example 5 A 5 g (bone dry weight) portion of the same oxygen-delignified softwood kraft pulp as used in Example 5 was collected and prepared into pulp slurries at pHs over an acidic to alkaline range and subjected to an irradiation reaction under similar conditions to those of Example 5, and the resulting pulps were measured for brightness. The results are shown in Figure 6 and Table 3.
  • Acid treatment conditions pulp consistency 10% by weight, pH 3 (adjusted with sulfuric acid), temperature 85°C, treatment period 180 minutes. After the treatment was completed, the pulp was washed with water.
  • a 5 g (bone dry weight) portion of the acid-treated pulp thus obtained was collected and diluted to a pulp consistency of 0.5% by weight and then prepared into a pulp slurry at pH 11.5 with NaOH.
  • This slurry was injected into the experimental apparatus shown in Figure 3, and subjected to an irradiation reaction while stirring under conditions of a temperature of 25°C for a treatment period of 120 minutes using a low-pressure UV lamp having a dominant wavelength at 254 nm. After the reaction was completed, the pulp was washed and then formed into a sheet and measured for brightness. The results are shown in Table 4.
  • a 15 g (bone dry weight) portion of the same acid-treated pulp as used in Example 6 was collected and diluted to a pulp consistency of 0.5% by weight and then injected into the experimental apparatus shown in Figure 3, and subjected to an ozone treatment while stirring at a temperature of 25°C, pH 11.5 for 120 minutes (without using an irradiation source).
  • the accumulated ozone feed to the pulp during the time was 0.7% by weight.
  • Table 4 The results are shown in Table 4.
  • a 15 g (bone dry weight) portion of the same acid-treated pulp as used in Example 6 was collected and diluted to a pulp consistency of 0.5% by weight and then injected into the experimental apparatus shown in Figure 3, and subjected simultaneously to an ozone treatment and an irradiation reaction while stirring at a temperature of 25°C, pH 11.5 for 120 minutes using a low-pressure UV lamp having a dominant wavelength at 254 nm.
  • the accumulated ozone feed to the pulp during the time was 0.7% by weight.
  • Table 4 The results are shown in Table 4.
  • Example 2 The same oxygen-delignified hardwood kraft pulp as used in Example 1 (kappa number 11.6, ISO brightness 45.6%) was treated with ozone under the following conditions to give a pulp having a kappa number of 3.0 and a brightness of 56.6%.
  • Ozone treatment conditions pulp consistency 10%, ozone feed 7 kg/ADTP, temperature 55°C, treatment period 30 seconds, pH 2.5.
  • a 15g (bone dry weight) portion of the ozone-treated pulp thus obtained was collected and diluted to a pulp consistency of 0.5% by weight and then injected into the experimental apparatus shown in Figure 3, and subjected to an irradiation reaction while stirring at a temperature of 25°C, pH 11.5 for 120 minutes using a low-pressure UV lamp having a dominant wavelength at 254 nm.
  • the results are shown in Table 4.
  • An irradiation reaction chamber (20) consists of a 4L glass cylinder (100 mm f x 620 mm H). This irradiation reaction chamber (20) is equipped with a temperature controller and a pH meter in addition to a stirrer (27) and a diffuser tube (24) shown in the figure.
  • An irradiation source (16W low-pressure mercury lamp, AY-1 from Photoscience Japan Corporation) is placed in a quartz glass tube (25 mm f x 470 mm H, thickness 2 mm) in such a manner that air can be injected around the irradiation source. In the examples below, two such irradiation sources were used.
  • An oxygen-delignified hardwood kraft pulp available from Nippon Paper Group, Inc. (kappa number 11.6, ISO brightness 45.6%) was acid-treated at a pulp consistency of 10% by weight, pH 3.0 (adjusted with sulfuric acid), at a temperature of 95°C for a treatment period of 180 minutes. After the acid treatment was completed, the pulp was washed with water to give a pulp having a kappa number of 5.5 and a brightness of 47.5%.
  • a 15 g (bone dry weight) portion of the acid-treated pulp was collected and prepared into a pulp slurry having a consistency of 0.5% by weight with water, and then the pulp slurry was adjusted to pH 11.5 with NaOH.
  • This pulp slurry was injected into the experimental apparatus shown in Figure 3, and subjected to an irradiation reaction while stirring under conditions of a temperature of 25°C for a treatment period of 120 minutes using a low-pressure UV lamp having a dominant wavelength at 254 nm. Simultaneously, the air injected into the quartz glass tube shown in Figure 3 to cool the light source was discharged via the diffuser and ozone was fed. After the treatment was completed, the pulp was washed and then formed into a sheet and measured for brightness. The results are summarized in Table 5.
  • Irradiation treatment was performed under similar conditions to those of Example 9 except that ozone feeding was omitted (i.e., air was not injected into the quartz glass tube shown in Figure 3 but directly introduced into the diffuser to feed the pulp slurry), after which the resulting pulp was measured for brightness.
  • ozone feeding was omitted (i.e., air was not injected into the quartz glass tube shown in Figure 3 but directly introduced into the diffuser to feed the pulp slurry), after which the resulting pulp was measured for brightness.
  • Table 5 The results are summarized in Table 5.
  • Reaction was performed under similar conditions to those of Example 9 except that irradiation treatment was omitted (i.e., the light source was not turned on) and the ozone (concentration 50 ppm) generated from an ozone generator (ozone spray, NS-3 available from Kankyo Kogaku Co., Ltd.) was fed via the diffuser shown in Figure 3, after which the resulting pulp was measured for brightness.
  • irradiation treatment was omitted (i.e., the light source was not turned on) and the ozone (concentration 50 ppm) generated from an ozone generator (ozone spray, NS-3 available from Kankyo Kogaku Co., Ltd.) was fed via the diffuser shown in Figure 3, after which the resulting pulp was measured for brightness.
  • ozone concentration 50 ppm
  • pulps with higher brightness can be prepared in Examples 9 - 11 involving irradiation with UV light or visible light or both in the presence of ozone.
  • brightness was somewhat lower in Example 11 wherein irradiation was not performed under acidic conditions of pH 2 - 4 or under alkaline conditions of pH 10 - 13.
  • An oxygen-delignified hardwood kraft pulp (ISO brightness 45.6%, available from Nippon Paper Group, Inc.) was further subjected to acid treatment - ozone bleaching under the following conditions and the resulting pulp was used in the examples and comparative examples below.
  • the ozone-bleached pulp was further bleached in a bleaching sequence of hydrogen peroxide bleaching 1 - light bleaching - hydrogen peroxide bleaching 2 under the following conditions.
  • Bleaching treatment was performed under the same conditions as those of Example 1 except that the treatment period of light bleaching was 30 minutes.
  • the ISO brightness after light bleaching was 80.0%.
  • the resulting light bleached pulp was treated under the conditions of hydrogen peroxide bleaching 2 above.
  • the final ISO brightness was 86.1%.
  • Example 2 Treatment was performed under the same conditions as those of Example 1 except that the treatment period of hydrogen peroxide bleaching 1 was 45 minutes.
  • the ISO brightness after hydrogen peroxide bleaching 1 was 71.0%.
  • the ISO brightness after light bleaching was 74.5%.
  • the resulting pulp was treated under the same conditions as those of hydrogen peroxide bleaching 2 above.
  • the final ISO brightness was 84.1%.
  • the ozone-bleached pulp was further bleached in a bleaching sequence of light bleaching - hydrogen peroxide bleaching.
  • Light bleaching was performed under the same conditions as those of Example 12 except that the treatment period was 60 minutes.
  • the brightness after light bleaching was 75.4%.
  • the resulting pulp was treated under the same conditions as those of hydrogen peroxide bleaching 2 of Example 12.
  • the final ISO brightness was 84.3%.
  • Example 4 Treatment was performed under the same conditions as those of Example 4 except that the treatment period of light bleaching was 120 minutes.
  • the ISO brightness after light bleaching was 81.8%.
  • the resulting pulp was treated under the same conditions as those of hydrogen peroxide bleaching 2 of Example 12.
  • the final ISO brightness was 85.2%.
  • Example 12 Treatment was performed under the same conditions as those of Example 12 except that the treatment period of hydrogen peroxide bleaching 1 was 30 minutes.
  • the ISO brightness after hydrogen peroxide bleaching 1 was 68.2%.
  • the ISO brightness after light bleaching was 72.3%.
  • the resulting pulp was treated under the same conditions as those of hydrogen peroxide bleaching 2 of Example 12.
  • the final ISO brightness was 81.7%.
  • the ozone-bleached pulp was further bleached in a bleaching sequence of hydrogen peroxide bleaching 1 - hydrogen peroxide bleaching 2.
  • Bleaching treatment was performed under the same conditions as those of Example 12 except that light bleaching was omitted.
  • the final ISO brightness was 79.3%.
  • the ozone-bleached pulp was further bleached in a bleaching sequence of hydrogen peroxide bleaching 1 - light bleaching.
  • Light bleaching was performed under the same conditions as those of Example 12 except that the treatment period was 60 minutes.
  • Hydrogen peroxide bleaching 1 was performed under the same conditions as those of Example 12.
  • the final ISO brightness was 83.3%.
  • the ozone-bleached pulp was further bleached in a bleaching sequence of hydrogen peroxide bleaching 1 - light bleaching - hydrogen peroxide bleaching 2.
  • Bleaching treatment was performed under the same conditions as those of Example 1 except that light bleaching was performed at pH 4.0 (adjusted with sulfuric acid).
  • the brightness after light bleaching was 75.9%.
  • the resulting pulp was treated under the same conditions as those of hydrogen peroxide bleaching 2 of Example 12.
  • the final ISO brightness was 82.6%.
  • This slurry was injected into the experimental apparatus shown in Figure 7, and subjected to a UV light bleaching treatment while stirring at a temperature of 25°C for a treatment period of 120 minutes.
  • the pulp was washed and then formed into a sheet and measured for brightness.
  • the sheet measured for brightness was then used in a fading test.
  • a sheet was prepared from the pulp after defibration and measured for breaking length. The methods for these evaluations are described below, and the results are shown in Table 1.
  • a 200 g (bone dry weight) portion of a bleached hardwood pulp (ISO brightness 84.9%) obtained by the ozone ECF bleaching process [acid treatment (oxygen-delignified pulp consistency 10% by weight, pH 3 (adjusted with sulfuric acid), temperature 85°C, treatment period 180 minutes); ozone treatment (pulp consistency 10% by weight, pH 2.5 (adjusted with sulfuric acid), ozone feed 7 kg/ 1t of air-dried pulp, temperature 55°C, treatment period 30 seconds)] of plant B of Nippon Paper Group, Inc. was collected and diluted to a pulp consistency of 1% and then adjusted to pH 11.5 with sodium hydroxide.
  • This slurry was injected into the experimental apparatus shown in Figure 7, and subjected to a UV light bleaching treatment while stirring at a temperature of 25°C for a treatment period of 120 minutes.
  • the pulp was washed and then formed into a sheet and measured for brightness.
  • the sheet measured for brightness was then used in the fading test.
  • a sheet was prepared from the pulp after defibration and measured for breaking length. The results are shown in Table 7.
  • a bleached hardwood pulp (ISO brightness 89.3%) obtained by a commercially available chlorine dioxide ECF bleaching process was used to form a sheet and measured for brightness. The sheet measured for brightness was then used in the fading test. A sheet was prepared from the pulp after defibration and measured for breaking length. The results are shown in Table 7.

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JP2004169367A JP4603298B2 (ja) 2004-06-08 2004-06-08 パルプの漂白方法
JP2004289267A JP2006104587A (ja) 2004-09-30 2004-09-30 高白色度化学パルプ及びその製造方法
JP2005102615A JP2006283213A (ja) 2005-03-31 2005-03-31 パルプの漂白方法及び漂白装置
JP2005102558A JP2006283211A (ja) 2005-03-31 2005-03-31 化学パルプの漂白方法
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