JPH0672386B2 - Oxygen delignification and bleaching method for cellulose pulp - Google Patents
Oxygen delignification and bleaching method for cellulose pulpInfo
- Publication number
- JPH0672386B2 JPH0672386B2 JP63101465A JP10146588A JPH0672386B2 JP H0672386 B2 JPH0672386 B2 JP H0672386B2 JP 63101465 A JP63101465 A JP 63101465A JP 10146588 A JP10146588 A JP 10146588A JP H0672386 B2 JPH0672386 B2 JP H0672386B2
- Authority
- JP
- Japan
- Prior art keywords
- oxygen
- delignification
- concentration
- cellulose pulp
- pulp
- 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.)
- Expired - Fee Related
Links
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims description 57
- 239000001301 oxygen Substances 0.000 title claims description 57
- 229910052760 oxygen Inorganic materials 0.000 title claims description 57
- 238000000034 method Methods 0.000 title claims description 36
- 229920002678 cellulose Polymers 0.000 title claims description 27
- 239000001913 cellulose Substances 0.000 title claims description 27
- 238000004061 bleaching Methods 0.000 title claims description 16
- 239000003513 alkali Substances 0.000 claims description 18
- 239000013055 pulp slurry Substances 0.000 claims description 16
- 239000002994 raw material Substances 0.000 claims description 14
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 27
- 238000010586 diagram Methods 0.000 description 5
- 239000007864 aqueous solution Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 239000004155 Chlorine dioxide Substances 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- OSVXSBDYLRYLIG-UHFFFAOYSA-N chlorine dioxide Inorganic materials O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 description 1
- 235000019398 chlorine dioxide Nutrition 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 239000011122 softwood Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Landscapes
- Paper (AREA)
Description
【発明の詳細な説明】 （産業上の利用分野） 本発明はセルロースパルプの脱リグニン、漂白方法に関
し、更に詳細には中濃度のセルロースパルプスラリーを
アルカリ及び酸素により脱リグニン、漂白する方法に関
する。TECHNICAL FIELD The present invention relates to a method for delignifying and bleaching cellulose pulp, and more particularly to a method for delignifying and bleaching a medium-concentration cellulose pulp slurry with alkali and oxygen.
（従来の技術） セルロースパルプを脱リグニン、漂白する方法として従
来工業的に実施された種々の塩素系薬品による方法、例
えばＣ（塩素）−Ｅ（アルカリ）−Ｄ（二酸化塩素）−
Ｅ−Ｄの５段漂白法に代り、アルカリ及び酸素を用いて
セルロースパルプを脱リグニン、漂白する方法が以前か
ら提案されている。そして最近では廃水処理負荷の軽
減、漂白工程薬品費の減少を目的として高濃度酸素脱リ
グニン法（処理セルロースパルプ濃度20〜35％）、中濃
度酸素脱リグニン法（処理セルロースパルプ濃度８〜15
％）と一般に称される酸素脱リグニン法が商業的に実施
されている。中濃度酸素脱リグニン法は高濃度酸素脱リ
グニン法に比較して、設備費及びセルロースパルプの品
質劣化が若干小さいため、最近は中濃度酸素脱リグニン
法が採用されることが多い。中濃度酸素脱リグニン法は
特公昭57−47798号公報に記載されているようにパルプ
スラリーの濃度は２〜６重量％である場合がある。この
方法の改良方法としてより高度の脱リグニンを達成する
方法として含酸素アルカリ性水溶液をまず調整し、その
一部（第一部分）をセルロースパルプスラリーと混合し
て加圧容器中で約73〜149℃の温度および21kg/cm2まで
の圧力で予備処理にかけ、この加圧スラリーを含酸素ア
ルカリ性水溶液の残部（第２部分）と混合して漂白塔に
連続的に導入する方法（特公昭58−57558号）がある。(Prior Art) As a method for delignifying and bleaching a cellulose pulp, a method using various chlorine-based chemicals that has been conventionally industrially implemented, for example, C (chlorine) -E (alkali) -D (chlorine dioxide)-
In place of the 5-stage bleaching method of ED, a method of delignifying and bleaching cellulose pulp using alkali and oxygen has been proposed. Recently, high concentration oxygen delignification method (treated cellulose pulp concentration 20-35%), medium concentration oxygen delignification method (treated cellulose pulp concentration 8-15
%) Is commonly practiced commercially. Compared with the high-concentration oxygen delignification method, the medium-concentration oxygen delignification method has a slightly smaller equipment cost and deterioration of the quality of the cellulose pulp. Therefore, recently, the middle-concentration oxygen delignification method is often adopted. In the medium-concentration oxygen delignification method, the concentration of the pulp slurry may be 2 to 6% by weight as described in JP-B-57-47798. As an improved method of this method, an oxygen-containing alkaline aqueous solution is first prepared as a method for achieving a higher delignification, and a part (first part) thereof is mixed with a cellulose pulp slurry to about 73 to 149 ° C in a pressure vessel. At a temperature of up to 21 kg / cm 2 and the pressure slurry is mixed with the rest of the oxygen-containing alkaline aqueous solution (second part) and continuously introduced into the bleaching tower (Japanese Patent Publication No. 58-57558). No.)
前記の中濃度酸素脱リグニン法は幾分パルプ濃度の低い
範囲の脱リグニン法を対象とするが基本的には第４図の
装置系列図に示す個々の装置を使用する方法であり、図
中１は中濃度ポンプ又は高濃度ポンプ、２は含酸素アル
カリ性水溶液と混合したセルロースパルプに高速度で高
剪断力を与えるいわゆる高剪断混合機（この混合機を直
列して２段に設けることがある。）、３は酸素脱リグニ
ン塔、４は脱気器である。図示のようにアルカリ、具体
的には水酸化ナトリウム水溶液又は酸化白液はポンプ１
の前、後の位置及び／又は混合機２に、そして酸素は混
合機２の前の位置又混合機２に供給される。未晒原料チ
エスト（図示されてない）からのセルロースパルプスラ
リーはポンプ１を通り、混合機２でアルカリ、酸素及び
必要に応じて蒸気と混合され、脱リグニン塔３に供給さ
れ、脱リグニン、漂白されたセルロースパルプスラリー
は脱気器４に供給され、セルロースパルプスラリーに含
有されたガラスは脱気され、セルロースパルプスラリー
は通常は洗浄機（図示されてない）に送られる。The above-mentioned medium-concentration oxygen delignification method is intended for the delignification method in a range where the pulp concentration is somewhat low, but basically it is a method using individual devices shown in the device sequence diagram of FIG. 1 is a medium-concentration pump or high-concentration pump, 2 is a so-called high-shear mixer that gives high shearing force at high speed to cellulose pulp mixed with an oxygen-containing alkaline aqueous solution (this mixer may be installed in two stages in series ) 3 is an oxygen delignification tower, 4 is a deaerator. As shown in the figure, pump 1 is used for alkali, specifically sodium hydroxide aqueous solution or white oxide liquor.
Before and / or before and / or to the mixer 2, and oxygen is supplied to the position before and / or to the mixer 2. Cellulose pulp slurry from unbleached raw material Tiesto (not shown) passes through pump 1, is mixed with alkali, oxygen and steam as necessary in mixer 2, and is supplied to delignification tower 3 for delignification and bleaching. The cellulose pulp slurry thus prepared is supplied to the deaerator 4, the glass contained in the cellulose pulp slurry is degassed, and the cellulose pulp slurry is normally sent to a washing machine (not shown).
一般に実機による中濃度酸素脱リグニン法では脱リグニ
ン塔３へ供給されるセルロースパルプスラリーのパルプ
濃度は８〜15％、スラリー温度は70〜140℃、酸素脱リ
グニン塔の塔内圧力（塔頂）は大気圧〜7kg/cm2パルプ
の塔内滞留時間は10〜90分間であり、酸素添加量は0.7
〜1.5kg/カツパー価減少量1/絶乾パルプｔ、NaOH添加量
は1.0〜1.7kg/カツパー価減少量1/絶乾パルプｔであ
る。Generally, in the medium-concentration oxygen delignification method using an actual machine, the pulp concentration of the cellulose pulp slurry supplied to the delignification tower 3 is 8 to 15%, the slurry temperature is 70 to 140 ° C., the pressure inside the oxygen delignification tower (the top of the tower) Is atmospheric pressure ~ 7kg / cm 2 pulp residence time in the tower is 10 ~ 90 minutes, the oxygen addition amount is 0.7
-1.5 kg / Kupper number decrease amount 1 / excess dry pulp t, NaOH addition amount is 1.0 to 1.7 kg / Kupper value decrease amount 1 / excess dry pulp t.
前記した中濃度酸素脱リグニン法は、一般的に使用され
ている前記の第４図に示す基本的な装置系列及び条件下
では酸素、アルカリを過剰に供給してもセルロースパル
プを多量に脱リグニンさせて低カツパー価のセルロース
パルプを得ることができないという問題があつた。The above-mentioned medium-concentration oxygen delignification method is a method of delignifying a large amount of cellulose pulp even if oxygen and alkali are excessively supplied under the basic apparatus series and conditions shown in FIG. 4 which are generally used. However, there is a problem in that it is impossible to obtain a cellulose pulp having a low Kupper number.
本発明者の一人は中濃度酸素脱リグニン法における前記
問題を解決するために中濃度のセルロースパルプスラリ
ーをアルカリ及び酸素により脱リグニン、漂白するに当
り、高剪断混合機と酸素脱リグニン装置との組合せ単位
を直列して複数段設けた装置により脱リグニン、漂白を
行う方法（特願昭61−241518号明細書（特開昭63−9938
9号公報）参照）を提案した。この方法の基本的な装置
系列を第３図に示す。この装置は第４図に示す高剪断混
合機２及び酸素脱リグニン装置３の１段の組合せに高剪
断混合機２′及び酸素脱リグニン装置３′との組合せ単
位を更に直列して複数段設けたものである。第３図中1,
2,3,4は第４図の1,2,3,4に対応し、５は未晒原料チエス
ト（第４図では図示されてない。）を示す。この方法に
より従来法に比して低カツパー価のセルロースパルプを
取得する目的は達成されたが、よりアルカリを効率的に
使用し、しかも低カツパー価の酸素漂白パルプを取得す
るには充分満足な方法ではないという問題があつた。One of the inventors of the present invention is a high-shear mixer and an oxygen delignification apparatus for delignifying and bleaching a medium-density cellulose pulp slurry with alkali and oxygen in order to solve the above problems in the medium-density oxygen delignification method. A method of delignification and bleaching with a device having a plurality of combination units connected in series (Japanese Patent Application No. 61-241518 (Japanese Patent Application Laid-Open No. 63-9938).
9))). The basic equipment sequence of this method is shown in FIG. In this apparatus, a combination of the high-shear mixer 2 and the oxygen delignification apparatus 3 shown in FIG. It is a thing. 1, in FIG.
2,3,4 correspond to 1,2,3,4 in FIG. 4, and 5 denotes an unbleached raw material cheest (not shown in FIG. 4). By this method, the purpose of obtaining a cellulose pulp having a lower Kappa number as compared with the conventional method was achieved, but it was sufficiently satisfactory to use an alkali more efficiently and to obtain an oxygen bleached pulp having a low Kappa number. There was a problem that it was not a method.
（発明が解決しようとする問題点） 本発明は中濃度酸素脱リグニン法における前記問題を解
決するためになされたもので、その目的は低カツパー価
のセルロースパルプを取得することのでき、アルカリの
使用が効率的な中濃度酸素脱リグニン法を提供すること
にある。(Problems to be Solved by the Invention) The present invention has been made to solve the above problems in the medium-concentration oxygen delignification method, and the purpose thereof is to obtain a cellulose pulp having a low Kupper number, The purpose is to provide an efficient medium oxygen delignification method.
（問題点を解決するための手段） 前記目的を達成する本発明の中濃度酸素脱リグニン法は
高剪断混合機と塔状加圧型の酸素脱リグニン装置との組
合せ単位を直列して複数段設けた装置を使用して中濃度
のセルロースパルプスラリーをアルカリ及び酸素により
脱リグニン、漂白するに当り、未晒原料チエストと第一
の高剪断混合機の前に設けたポンプとの間の部位におい
てアルカリの全量を添加し、一方酸素は複数段の高剪断
混合機に添加することを特徴とする。(Means for Solving the Problems) In the medium-concentration oxygen delignification method of the present invention that achieves the above object, a combination unit of a high-shear mixer and a tower-type pressure-type oxygen delignification apparatus is provided in multiple stages in series. When delignifying and bleaching a medium-concentration cellulosic pulp slurry with alkali and oxygen using the equipment described above, the alkali at the site between the unbleached raw material est and the pump installed before the first high-shear mixer is used. Of oxygen, while oxygen is added to the multi-shelf high shear mixer.
すなわち本発明は特願昭61−241518号（特開昭63−9938
9号）発明の改良法に関するもので、未晒原料チエスト
と第一の高剪断混合機の前に設けたポンプとの間の部位
においてアルカリの全量を添加することにより同一量の
アルカリ使用量であるにも拘らず、意外にもより低カツ
パー価の酸素漂白パルプを取得することが認められた。That is, the present invention is disclosed in Japanese Patent Application No. 61-241518 (JP-A-63-9938).
No. 9) relates to an improved method of the invention, in which the same amount of alkali is used by adding the total amount of alkali at the site between the unbleached raw material cheest and the pump provided in front of the first high shear mixer. Despite this, it was surprisingly found that oxygen bleached pulp with a lower Kupper number was obtained.
本発明における前記組合せ単位を複数段結合する装置の
実施態様を、前記発明の明細書及び図面の記載と同様に
その装置系列図である第１図及び第２図で説明すると、
第１図において５は未晒原料チエスト、１は中濃度又は
高濃度ポンプ、2,2′は高剪断混合機、3,3′は塔状加圧
型の酸素脱リグニン装置、４は脱気器であつて組合せ単
位を２段とする装置を示し、第２図において５は未晒原
料チエスト、１は中濃度又は高濃度ポンプ、2,2′,2″
は高剪断混合機、3,3′,3″は塔状加圧型の酸素脱リグ
ニン装置であり、４は脱気器であつて組合せ単位を３段
とする装置を示す。塔状加圧型の酸素脱リグニン装置と
しては通常の塔状加圧型酸素脱リグニン塔が使用され、
以下単に脱リグニン塔という。An embodiment of a device for combining the combination units in a plurality of stages in the present invention will be described with reference to FIGS. 1 and 2 which are device sequence diagrams of the same as the description of the specification and the drawings of the present invention.
In FIG. 1, 5 is an unbleached raw material thest, 1 is a medium- or high-concentration pump, 2, 2'is a high shear mixer, 3, 3'is a tower pressure type oxygen delignification device, and 4 is a deaerator. Here, an apparatus having two stages of combination units is shown. In FIG. 2, 5 is an unbleached raw material cheest, 1 is a medium or high concentration pump, and 2, 2 ', 2 "
Is a high-shear mixer, 3,3 ', 3 "is a tower-type pressure type oxygen delignification apparatus, and 4 is a deaerator which has a combination unit of three stages. As the oxygen delignification equipment, a conventional tower-type pressure-type oxygen delignification tower is used,
Hereinafter referred to simply as the delignification tower.
高剪断混合機としては特公昭61−15728号公報に示され
るカミヤ（Kamyr）社のエム、シー（M.C）ミキサー、ス
ンズ（Sunds）社のエス・エム（S.M）ミキサー、イムプ
コ（Impco）社のハイシエアーミキサー、ウエアハウザ
ー社が開発し、ラウマ・レポラ（Rauma−Repola）社が
改良したスミトモ ラウマ ケミカル（Sumitomo Rauma
Chemical）ミキサー等が好適に使用される。As the high shear mixer, the Kam, M, M mixer, Sunds, SM mixer, and Impco, which are disclosed in Japanese Patent Publication No. 61-15728, are used. High shear air mixer developed by Weirhauser and improved by Rauma-Repola Sumitomo Rauma Chemical
Chemical) mixer is preferably used.
セルロースパルプスラリーは未晒原料チエスト５（パル
プ濃度８〜15％）からポンプ１により給送され、高剪断
混合機と脱リグニン塔の組合せ単位（２−３）及び
（２′−３′）更には（２″−３″）を順次に経由して
脱気器４より排出される。Cellulose pulp slurry was fed from unbleached raw material 5 (pulp concentration 8 to 15%) by pump 1, and combined units (2-3) and (2'-3 ') of high shear mixer and delignification tower were added. Is discharged from the deaerator 4 via (2 ″ -3 ″) in sequence.
アルカリは未晒原料チエスト５と中濃度又は高濃度ポン
プ１と間の部位、望ましくはチエスト５の出口において
全量添加される。アルカリとしては一般には水酸化ナト
リウム又は酸化白液が使用される。The entire amount of alkali is added at a site between the unbleached raw material cheest 5 and the medium-concentration or high-concentration pump 1, preferably at the outlet of the cheest 5. Sodium hydroxide or oxidized white liquor is generally used as the alkali.
未晒原料チエスト５に保持されるパルプはカツパー価
（Ka）50〜25程度が好ましい。該チエスト５の出口にお
いて全量添加されるアルカリはNaOH換算で1.0〜13.5kg/
BDT（絶乾パルプｔ）/Kaである。The pulp retained in the unbleached raw material cheest 5 preferably has a Kupper number (Ka) of about 50 to 25. The total amount of alkali added at the outlet of the chiest 5 is 1.0 to 13.5 kg / in terms of NaOH.
It is BDT (extremely dry pulp t) / Ka.
酸素は純酸素又は酸素富化空気（酸素含有量80％以上）
の形態で高剪断混合機2,2′,2″の前の部位又は該混合
機に直接供給される。セルロースパルプスラリーの昇温
を必要とする場合一般の中濃度脱リグニン法と同様に蒸
気は高剪断混合機2,2′,2″の前の位置又は該混合機2,
2′,2″に直接供給される。酸素添加量は0.7〜3.0kg/BD
T/Ka程度であり、この添加量は各段で分割添加されても
よい。Oxygen is pure oxygen or oxygen-enriched air (oxygen content 80% or more)
In the form of a high-shear mixer 2,2 ', 2 "or directly to the mixer. When it is necessary to raise the temperature of the cellulose pulp slurry, steam is used as in the general medium-concentration delignification method. Is located in front of the high shear mixer 2, 2 ', 2 "or the mixer 2,
Directly supplied to 2 ', 2 ". Oxygen added amount is 0.7 ~ 3.0kg / BD
It is about T / Ka, and this addition amount may be divided and added at each stage.
組合せ単位の各段の脱リグニン塔3,3′更には３″にお
ける各段の脱リグニン条件はセルロースパルプスラリー
のパルプ濃度は８〜15％、スラリー温度は70〜140℃、
塔圧力（塔頂）１〜7kg/cm2（ゲージ圧）、パルプの滞
留時間は５〜90分間である。塔圧力を維持するために３
と３′の間又は３′と３″との間に中濃度又は高濃度ポ
ンプを介在させてもよい。The delignification conditions of each stage in the delignification towers 3, 3'and 3 "of each stage of the combination unit are as follows: the pulp concentration of the cellulose pulp slurry is 8 to 15%, the slurry temperature is 70 to 140 ° C,
The column pressure (column top) is 1 to 7 kg / cm 2 (gauge pressure), and the pulp residence time is 5 to 90 minutes. 3 to maintain tower pressure
A medium-concentration pump or a high-concentration pump may be interposed between the 3'and 3'or between the 3'and 3 ".
次に本発明を実施例及び比較例について説明するが、本
発明はこれによりなんら限定されるものではない。Next, the present invention will be described with reference to Examples and Comparative Examples, but the present invention is not limited thereto.
比較例１ 第３図に示す装置系列の実機を用い、酸素30kg/BDTを混
合機2,2′に2:1の割合で供給し、NaOH 30kg/BDTを混合
機2,2′に1:1の割合で供給し、脱リグニン塔３′の塔内
圧力（塔頂）を4kg/cm2（ゲージ圧）、３に供給するパ
ルプスラリーの温度を100℃、パルプ濃度を11.5％とし
て針葉樹（北米産ダクラスフアー）セルロースパルプ
（カツパー価30）を中濃度酸素脱リグニン処理し、酸素
脱リグニン装置３′の出口パルプのカツパー価減少量を
測定し、その結果を第１表に示す。Comparative Example 1 Using an actual machine of the apparatus series shown in FIG. 3, oxygen 30 kg / BDT was supplied to the mixers 2,2 ′ at a ratio of 2: 1 and NaOH 30 kg / BDT was supplied to the mixers 2,2 ′ at 1: 2. The pulp pressure is 100% and the pulp concentration is 11.5% when the delignification column 3 ′ is supplied with the internal pressure (column top) of the delignification column 3 ′ at 4 kg / cm 2 (gauge pressure), and the pulp concentration is 11.5%. A North American Dacrashua) cellulose pulp (Kupper number 30) was subjected to a medium-concentration oxygen delignification treatment, and the amount of reduction in the Kuppar number of the outlet pulp of the oxygen delignification apparatus 3'was measured. The results are shown in Table 1.
比較例２ 第３図に示す装置系列の実機を用い酸素30kg/BDTを混合
機2,2′に2:1の割合で供給し、NaOH 30kg/BDTを混合機
２に全量供給し脱リグニン塔３′の塔内圧力（塔頂）を
4kg/cm2（ゲージ圧）、３に供給するパルプスラリーの
温度を100℃、パルプ濃度を11.5％として針葉樹（北米
産ダクラスフアー）セルロースパルプ（カツパー価30）
を中濃度酸素脱リグニン処理し脱リグニン塔３′の出口
パルプのカツパー価減少量を測定しその結果を第２表に
示す。 Comparative Example 2 Using an actual machine of the equipment series shown in FIG. 3, oxygen 30 kg / BDT was supplied to the mixers 2,2 ′ at a ratio of 2: 1 and NaOH 30 kg / BDT was supplied to the mixer 2 in the total amount to carry out the delignification tower. 3'inside pressure (top)
4kg / cm 2 (gauge pressure), the temperature of the pulp slurry supplied to 3 is 100 ° C, the pulp concentration is 11.5%, and the softwood (Duclas fur from North America) cellulose pulp (Kupper number 30)
Was subjected to a medium-concentration oxygen delignification treatment to measure the amount of reduction in the Kupper number of the outlet pulp of the delignification tower 3 ', and the results are shown in Table 2.
実施例１ 第１図に示す装置系列の実機を用い酸素30kg/BDTを混合
機2,2′に2:1の割合で供給し、NaOH 30kg/BDTを未晒原
料チエストの出口において全量供給し脱リグニン塔３′
の塔内圧力（塔頂）を4kg/cm2（ゲージ圧）３に供給す
るパルプスラリー温度を100℃、パルプ濃度を11.5％と
して針葉樹（北米産ダグラスフアー）セルロースパルプ
（カツパー価30）を中濃度、酸素脱リグニン処理し脱リ
グニン塔３′の出口パルプカツパー価減少量を測定しそ
の結果を第３表に示す。 Example 1 Using an actual machine of the equipment series shown in FIG. 1, oxygen 30 kg / BDT was supplied to the mixers 2, 2 ′ at a ratio of 2: 1 and NaOH 30 kg / BDT was entirely supplied at the outlet of the unbleached raw material cheest. Delignification tower 3 '
The inside pressure of the tower (top) is 4 kg / cm 2 (gauge pressure) 3, the pulp slurry temperature is 100 ° C, and the pulp concentration is 11.5%. The concentration and oxygen delignification treatment and the amount of decrease in the pulp pulp number at the outlet of the delignification tower 3'are measured, and the results are shown in Table 3.
第１表及び第２表と第３表との対比からも明らかなよう
に、NaOHの供給を未晒原料チエストの出口において行な
うことによりNaOH同一添加量において本発明の目的を達
成することができる。 As is clear from the comparison between Tables 1 and 2 and Table 3, by supplying NaOH at the outlet of the unbleached raw material cheest, the object of the present invention can be achieved at the same NaOH addition amount. .
（発明の効果） 以上の説明から明らかなように本発明は未晒原料チエス
トと第一の高剪断混合機の前に設けたポンプとの間の部
位においてアルカリの全量を添加することにより、高剪
断混合機と脱リグニン塔との組合せ単位を直列して複数
段設けた装置を使用する酸素による脱リグニン、漂白方
法（特願昭61−241518号発明）に比してより低カツパー
価のパルプが得られ、その結果として廃水負荷の低減及
び次工程の漂白薬品量及び漂白段数を減らすことができ
るという利点がある。(Effects of the Invention) As is clear from the above description, the present invention improves the efficiency by adding the total amount of alkali at the site between the unbleached raw material cheest and the pump provided in front of the first high shear mixer. Pulp of lower cuter number than oxygen delignification and bleaching method (invention of Japanese Patent Application No. 61-241518) using a device in which a combination of a shear mixer and a delignification tower is connected in series and provided in plural stages. As a result, there is an advantage that the load of waste water can be reduced and the amount of bleaching chemicals and the number of bleaching stages in the next step can be reduced.
第１図及び第２図は本発明の実施態様である装置の系列
図を示し、第３図は特願昭61−241518号（特開昭63−99
389号）発明の中濃度酸素脱リグニン法に使用される装
置の系列図を示し、第４図は従来法の中濃度酸素脱リグ
ニン法に使用される装置の系列図を示す。 １……ポンプ、2,2′,2″……高剪断混合機、3,3′,3″
……塔状加圧型の酸素脱リグニン装置、４……脱気器、
５……未晒原料チエストFIG. 1 and FIG. 2 show a sequence diagram of an apparatus which is an embodiment of the present invention, and FIG. 3 shows a Japanese Patent Application No. 61-241518 (Japanese Patent Laid-Open No. 63-99).
No. 389) A sequence diagram of an apparatus used for the medium-concentration oxygen delignification method of the invention is shown, and FIG. 4 is a sequence diagram of an apparatus used for the conventional medium-concentration oxygen delignification method. 1 …… Pump, 2,2 ′, 2 ″ …… High shear mixer, 3,3 ′, 3 ″
...... Tower pressure type oxygen delignification device, 4 …… Deaerator,
5: Unbleached raw material cheest
───────────────────────────────────────────────────── フロントページの続き (72)発明者 松村 修 北海道苫小牧市王子町２丁目１番１号 王 子製紙株式会社苫小牧工場内 (56)参考文献 特開 昭56−91094（ＪＰ，Ａ) 特開 昭56−4791（ＪＰ，Ａ) 特開 昭63−99389（ＪＰ，Ａ) 特表 昭58−501383（ＪＰ，Ａ) ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Osamu Matsumura 2-1-1 Ojimachi, Tomakomai, Hokkaido Oji Paper Co., Ltd., Tomakomai Mill (56) Reference JP-A-56-91094 (JP, A) Kai Sho 56-4791 (JP, A) JP 63-99389 (JP, A) Special Table Sho 58-501383 (JP, A)
Claims (1)
ン装置との組合せ単位を直列して複数段設けた装置を使
用して中濃度のセルロースパルプスラリーをアルカリ及
び酸素により脱リグニン、漂白するに当り、未晒原料チ
エストと第一の高剪断混合機の前に設けたポンプとの間
の部位においてアルカリの全量を添加し、一方酸素は複
数段の高剪断混合機に添加することを特徴とするセルロ
ースパルプの酸素による脱リグニン、漂白方法。1. A medium-concentration cellulose pulp slurry is delignified with alkali and oxygen using a device in which a combination of a high-shear mixer and a tower-type pressure-type oxygen delignification device is provided in multiple stages in series. Upon bleaching, add the total amount of alkali at the site between the unbleached raw material cheest and the pump in front of the first high shear mixer, while adding oxygen to the multistage high shear mixer. Oxygen delignification and bleaching method of cellulose pulp characterized by:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63101465A JPH0672386B2 (en) | 1988-04-26 | 1988-04-26 | Oxygen delignification and bleaching method for cellulose pulp |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63101465A JPH0672386B2 (en) | 1988-04-26 | 1988-04-26 | Oxygen delignification and bleaching method for cellulose pulp |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH01272890A JPH01272890A (en) | 1989-10-31 |
| JPH0672386B2 true JPH0672386B2 (en) | 1994-09-14 |
Family
ID=14301462
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63101465A Expired - Fee Related JPH0672386B2 (en) | 1988-04-26 | 1988-04-26 | Oxygen delignification and bleaching method for cellulose pulp |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0672386B2 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SE510740C2 (en) * | 1996-11-26 | 1999-06-21 | Sunds Defibrator Ind Ab | Oxygen delignification control |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS564791A (en) * | 1979-06-18 | 1981-01-19 | Kogyo Gijutsuin | Bleaching of mechanical pulp |
| US4363697A (en) * | 1979-12-03 | 1982-12-14 | The Black Clawson Company | Method for medium consistency oxygen delignification of pulp |
-
1988
- 1988-04-26 JP JP63101465A patent/JPH0672386B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH01272890A (en) | 1989-10-31 |
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