JPH0768675B2 - Oxygen delignification and bleaching method for cellulose pulp - Google Patents
Oxygen delignification and bleaching method for cellulose pulpInfo
- Publication number
- JPH0768675B2 JPH0768675B2 JP61241518A JP24151886A JPH0768675B2 JP H0768675 B2 JPH0768675 B2 JP H0768675B2 JP 61241518 A JP61241518 A JP 61241518A JP 24151886 A JP24151886 A JP 24151886A JP H0768675 B2 JPH0768675 B2 JP H0768675B2
- Authority
- JP
- Japan
- Prior art keywords
- pulp
- delignification
- oxygen
- concentration
- cellulose 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 - Lifetime
Links
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
- D21C9/10—Bleaching ; Apparatus therefor
- D21C9/147—Bleaching ; Apparatus therefor with oxygen or its allotropic modifications
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Wood Science & Technology (AREA)
- 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 pressure of up to 21 kg / cm 2 and the pressure slurry is mixed with the rest of the oxygen-containing alkaline aqueous solution (the 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３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
剪断力を付えるいわゆる高剪断混合機（以下混合機とい
う。この混合機を直列して２段に設けることがあ
る。）、３は塔状加圧型の酸素脱リグニン装置（以下酸
素脱リグニン装置又は脱リグニン塔という。）、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。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 (hereinafter referred to as a mixer, which can apply a high-shear force to cellulose pulp mixed with an oxygen-containing alkaline aqueous solution at high speed. 3 is a column-type pressure-type oxygen delignification apparatus (hereinafter referred to as an oxygen delignification apparatus or delignification tower), and 4 is a deaerator. As shown, alkali, specifically aqueous sodium hydroxide or white oxidizer, is placed in front of and / or behind pump 1 and / or in mixer 2 and oxygen is placed in front of mixer 2 and / or in mixer 2. Supplied. The cellulose pulp slurry passes through the pump 1, is mixed with alkali, oxygen and steam as required in the mixer 2, and is supplied to the delignification tower 3. The delignified and bleached cellulose pulp slurry is supplied to the deaerator 4. The gas contained in the cellulose pulp slurry is degassed, and the cellulose pulp slurry is normally sent to a washing machine (not shown).
前記高剪断混合機は中濃度ミキサーとも呼ばれ、その構
造はメーカーによって差があるが、固定部と回転部の間
で高剪断力を発生させ、そこをパルプが通過する際に剪
断力を受けパルプ懸濁液があたかも水のような流体とな
るように工夫してある（昭和61年１月20日株式会社テッ
クタイムス発行 紙パルプ技術タイムス臨時増刊号第５
頁中欄参照）。そしてその１例は昭和59年12月１日 紙
パルプ技術協会発行「紙パ技協誌」第38巻第12号第10頁
右欄「7.1.1」Kamyr中濃度漂白法の項中に示すMCミキサ
ーについて、その第11頁図21MCミキサー断面図として紹
介されている。The high-shear mixer is also called a medium-concentration mixer, and its structure varies depending on the manufacturer, but it generates high shear force between the fixed part and the rotating part, and receives the shear force when the pulp passes through it. The pulp suspension is devised so that it becomes a fluid like water (January 20, 1986, issued by Tech Times Co., Ltd. Paper Pulp Technology Times Extra Number 5)
See the middle column of the page). And one example is shown in the section "7.1.1" Kamyr Medium Concentration Bleaching Method on December 10, 1984, "Paper and Paper Cooperative Magazine," Vol. 38, No. 12, page 10, right column, published by Japan Pulp and Paper Technology Association. The MC mixer is introduced on page 11 as a cross section of Figure 21 MC mixer.
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
ている前記の基本的な装置系列及び条件下では後記の実
験（比較例１）に示すように酸素、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
いう問題があった。The above-mentioned medium-concentration oxygen delignification method, even if oxygen and alkali are excessively supplied as shown in the experiment (Comparative Example 1) described later, under the above-mentioned basic apparatus series and conditions that are generally used. There has been a problem that a large amount of cellulose pulp cannot be delignified to obtain a low Kupper number cellulose pulp.
（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る中濃度酸素脱リ
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-mentioned problems in the medium-concentration oxygen delignification method, and its purpose is to obtain medium-concentration oxygen deoxidation capable of obtaining a cellulose pulp having a low Kupper number. To provide a lignin 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
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により脱リグニン、漂白を行うこと
を特徴とするものである。(Means for Solving Problems) The medium-concentration oxygen delignification method of the present invention for achieving the above-mentioned object is a high-shear mixer and a tower for delignifying and bleaching a medium-concentration cellulose pulp slurry with alkali and oxygen. It is characterized in that delignification and bleaching are carried out by an apparatus in which a plurality of units are provided in series in combination with a combined pressurization type oxygen delignification apparatus.
本発明の構成は、一般には従来法として前記した第３図
に示す中濃度酸素脱リグニン、漂白法の装置では中濃度
のセルロースパルプが高剪断混合機において酸素及びア
ルカリと混合され、次に酸素脱リグニン装置で脱リグニ
ン、漂白されるという高剪断混合機と酸素脱リグニン装
置の組み合せが一段である代りに高剪断混合機と酸素脱
リニン装置との組合せ単位を直列して複数段、例えば２
段結合して脱リグニン、漂白を行う方法である。In the constitution of the present invention, generally, in the apparatus of the medium concentration oxygen delignification and bleaching method shown in FIG. 3 described above as the conventional method, medium concentration cellulose pulp is mixed with oxygen and alkali in a high shear mixer, and then oxygen is mixed. Instead of a combination of a high shear mixer and an oxygen delignification apparatus that is delignified and bleached in a delignification apparatus, a combination unit of a high shear mixer and an oxygen delignification apparatus is connected in series to a plurality of stages, for example, 2 units.
This is a method of delignification and bleaching by connecting in stages.
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、先行技術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。酸素脱リグニン装置として
は塔状加圧型の装置が適用される。An embodiment of an apparatus for combining the combination units in a plurality of stages according to the present invention will be described with reference to FIGS. 1 and 2 which are apparatus sequence diagrams of the same as in the prior art. In FIG. 1, 1 is medium concentration or high concentration. Pump, 2,2 'is a high shear mixer, 3,3' is an oxygen delignification device, 4 is a deaerator, and the combination unit is 2
In FIG. 2, 1 is a medium- or high-concentration pump, 2,2 ′, 2 ″ is a high shear mixer, 3,3 ′, 3 ″ is an oxygen delignification device, and 4 is a device. A deaerator having a combination unit of three stages is shown. As the oxygen delignification apparatus, a tower pressure type apparatus is applied.
セルロースパルプスラリーはポンプ１から供給され、高
剪断混合機と酸素脱リグニン装置の組合せ単位（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。The cellulose pulp slurry is supplied from the pump 1, and the combination unit (2-shear mixer and oxygen delignification unit) (2-
3) and (2'-3 ') and then (2 "-3") are sequentially discharged from the deaerator 4.
アルカリは一般の中濃度酸素脱リグニン法と同様にポン
プ１の前後の位置又は混合機２に供給され酸素も同様に
混合機２の前の位置又は混合機２に供給される。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混合機２の前の位置又は
混合機２に供給される。前記のように必要量のアルカリ
及び酸素を１段目に全量供給する場合でも、脱リグニン
塔３と３′と３″の間、同じく３′と３″の間に混合機
を設置しないと後記の実験（比較例２）に示すように本
発明の目的は達成できない。Alkali is supplied to a position before and after the pump 1 or to the mixer 2 similarly to the general medium concentration oxygen delignification method, and oxygen is also supplied to a position before the mixer 2 or to the mixer 2. When it is necessary to raise the temperature of the cellulose pulp slurry, the steam is supplied to the position in front of the mixer 2 or to the mixer 2 as in the general medium concentration delignification method. As described above, even if the required amount of alkali and oxygen are all supplied to the first stage, a mixer is not installed between the delignification towers 3 and 3'and 3 ", and also between 3'and 3". The object of the present invention cannot be achieved as shown in the experiment (Comparative Example 2).
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。必要量のアルカリ、酸素、蒸
気は前記のように全量１段目に供給すれば良いが第1,第
２図に示したように分割添加しても本発明の目的を達成
することができる。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
And 3'or 3'and 3 "may be provided with a medium or high concentration pump. The necessary amounts of alkali, oxygen and steam may be supplied to the first stage as described above. However, the object of the present invention can be achieved even when dividedly added as shown in FIGS.
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35kg/絶乾パ
ルプｔ、NaOH35kg/絶乾パルプｔを混合機２に供給し、
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28）を中濃度酸素脱
リグニン処理した。Comparative Example 1 Using an actual machine of the device series shown in FIG. 3, oxygen 35 kg / absolute dry pulp t and NaOH 35 kg / absolute dry pulp t were supplied to the mixer 2.
The pressure in the tower (top) of the delignification tower 3 is 4 kg / cm 2 (gauge pressure), the temperature of the pulp slurry supplied to 3 is 100 ° C., and the pulp concentration is 11.5%. Valency 28) was subjected to a medium concentration oxygen delignification treatment.
この脱リグニン塔の側面にはセルロースパルプを塔内よ
り採取するためのサンプリング口を設置した。このサン
プリング口よりセルロース、パルプを採取し、塔内滞留
時間と脱リグニン量と関係を調査し、その結果を示すグ
ラフを第４図に示す。A sampling port for collecting cellulose pulp from the inside of the tower was installed on the side surface of the delignification tower. Cellulose and pulp were collected from this sampling port, the relationship between the residence time in the tower and the amount of delignification was investigated, and a graph showing the result is shown in FIG.
第４図に示すように、一般の中濃度酸素脱リグニン装置
を使用する酸素脱リグニン法ではカツパー価28程度の針
葉樹セルロースパルプに、過剰にアルカリ、及び酸素を
供給しても、カツパー価減少量は12程度であり、また塔
内のセルロースパルプの滞留時間を20分間以上にして
も、カツパー価減少量は、あまり増加しない。As shown in Fig. 4, in the oxygen delignification method using a general medium-concentration oxygen delignification apparatus, even if excessive alkali and oxygen are supplied to a softwood cellulose pulp with a Kupper value of about 28, the reduction amount of the Kuppar value is reduced. Is about 12, and even if the residence time of the cellulose pulp in the tower is 20 minutes or more, the reduction amount of Kupper number does not increase so much.
実施例１ 第２図に示す装置系列の３段中濃度酸素脱リグニン装置
のテストプラントを用い、NaOH35kg/絶乾パルプｔ、酸
素35kg/絶乾パルプｔ、及び蒸気を混合機２に供給し、
又脱リグニン塔3,3′,3″の塔内圧力（塔頂）を３は約6
kg/cm2、３′は約4kg/cm2、３″は約2kg/cm2、パルプス
ラリー温度を100℃、3,3′,3″の滞留時間を各80分間と
なるようにして比較例１と同一の針葉樹セルロースパル
プを酸素脱リグニン処理した。その結果を第１表に示
す。Example 1 Using a test plant of a three-stage medium-concentration oxygen delignification apparatus of the apparatus series shown in FIG. 2, NaOH 35 kg / absolute dry pulp t, oxygen 35 kg / absolute dry pulp t, and steam were supplied to the mixer 2,
In addition, the internal pressure (top) of the delignification towers 3, 3 ', 3 "is about 6
kg / cm 2 , 3 ′ is about 4 kg / cm 2 , 3 ″ is about 2 kg / cm 2 , the pulp slurry temperature is 100 ° C., and the residence time of 3,3 ′, 3 ″ is 80 minutes each for comparison. The same softwood cellulose pulp as in Example 1 was oxygen delignified. The results are shown in Table 1.
第１表 カツパー価 カツパー価減少量 供給パルプ（１出） 28.0 １段処理後（３出） 17.3 10.7 ２段処理後（３′出） 11.2 6.1 ３段処理後（３″出） 8.2 3.0 実施例１と比較例との対比から同一の酸素量及びアルカ
リ量においては本発明は低カツパー価が得られることは
明らかである。Table 1 Kupper number Reduction of Kupper number Supply pulp (1 out) 28.0 After 1-stage treatment (3 out) 17.3 10.7 After 2 stage treatment (3 'out) 11.2 6.1 After 3 stage treatment (3 out) 8.2 3.0 Example From the comparison between No. 1 and Comparative Example, it is clear that the present invention provides a low Kuppa number at the same oxygen amount and alkali amount.
実施例２ 脱リグニン塔のセルロースパルプスラリー滞留時間を各
々20分間にした第２図に示す装置系列の３段中濃度酸素
脱リグニン装置のテストプラントを用い、実施例１と同
一条件で比較例１と同一の針葉樹セルロースパルプを酸
素脱リグニン処理した。その結果を第２表に示す。Example 2 Comparative Example 1 under the same conditions as in Example 1 using a test plant of a three-stage medium concentration oxygen delignification apparatus of the apparatus series shown in FIG. 2 in which the residence time of the cellulose pulp slurry in the delignification tower was set to 20 minutes each. The same softwood cellulosic pulp was treated with oxygen delignification. The results are shown in Table 2.
第２表 カツパー価 カツパー価減少量 供給パルプ（１出） 27.1 １段処理後（３出） 17.8 9.3 ２段処理後（３′出） 11.5 6.3 ３段処理後（３″出） 8.5 3.0 第２表から明らかなように脱リグニン塔の滞留時間を20
分間にしても実施例１と同様に低カツパー価のパルプが
得られた。Table 2 Kupper Number Reduction of Kupper Number Supply pulp (1 out) 27.1 After 1-stage treatment (3 out) 17.8 9.3 After 2 stage treatment (3 'out) 11.5 6.3 3 stage after treatment (3 out) 8.5 3.0 Second As is clear from the table, the residence time in the delignification tower was 20
A pulp with a low Kupper number was obtained in the same manner as in Example 1 even in the case of minutes.
実施例1,2と同様の中濃度脱リグニン処理（Mg塩のよう
なプロテクターは使用しない。）をした時の供給パル
プ、１段処理後パルプ、２段処理後パルプ、３段処理後
パルプのカツパー価と粘度の関係を示したグラフを第５
図に示す。Of the feed pulp, the pulp after one-stage treatment, the pulp after two-stage treatment, the pulp after three-stage treatment, and the pulp after the medium-density delignification treatment (a protector such as Mg salt is not used) similar to those in Examples 1 and 2 The graph showing the relationship between the cut number and the viscosity is
Shown in the figure.
第５図に示すようにカツパー価とパルプ粘度との関係
は、直線関係にあり、カツパー価30程度の針葉樹セルロ
ースパルプを３段中濃度酸素脱リグニン処理して、カツ
パー価８程度までにしても急激にパルプ粘度が低下する
ことはなかつた。As shown in FIG. 5, there is a linear relationship between the Kappa number and the pulp viscosity, and softwood cellulose pulp having a Kappa number of about 30 is subjected to a three-stage medium-concentration oxygen delignification treatment to a Kappa number of about 8 or less. The pulp viscosity never dropped sharply.
実施例３ 第１図に示す装置系列の２段中濃度酸素脱リグニン装置
の実機を用いて酸化白液25kgNaOHとして／絶乾パルプ
ｔ、酸素25kg/絶乾パルプｔ、蒸気を混合機２に供給
し、又、脱リグニン塔3,3′の塔内圧力（塔頂）３は約6
kg/cm2、３′は約3kg/cm2、３に供給するパルプスラリ
ー温度を100℃、パルプ濃度を12.0％、３の滞留時間を1
0分間、３′の滞留時間を60分間にして比較例１と同一
の針葉樹セルロースパルプを酸素脱リグニン処理した。
その結果を第３表に示す。Example 3 Using a real machine of a two-stage medium-concentration oxygen delignification apparatus of the apparatus series shown in FIG. 1, 25 kg of oxidized white liquor as NaOH / boiled pulp t, oxygen 25 kg / boiled pulp t, and steam were supplied to the mixer 2. In addition, the internal pressure (top) 3 of the delignification towers 3, 3'is about 6
kg / cm 2 , 3 ′ is about 3 kg / cm 2 , and the pulp slurry temperature to be supplied to 3 is 100 ° C., the pulp concentration is 12.0%, and the residence time of 3 is 1
The same softwood cellulose pulp as in Comparative Example 1 was subjected to oxygen delignification treatment with a retention time of 0 minutes and 3 ′ of 60 minutes.
The results are shown in Table 3.
第３表 カツパー価 カツパー価減少量 供給パルプ（１出） 29.5 １段処理後（３出） 16.5 13.0 ２段処理後（３′出） 12.1 4.4 実施例４ 実施例３と同一設備を用いて混合機２に酸化白液17kgNa
OHとして／絶乾パルプｔ、酸素17kg/絶乾パルプｔ、混
合機２′に酸化白液8kgNaOHとして／絶乾パルプｔ、酸
素8kg/絶乾パルプｔを分割供給した。他の条件は実施例
３と同一の条件で比較例１と同一の針葉樹セルロースパ
ルプを酸素脱リグニン処理した。その結果を第４表に示
す。Table 3 Kupper number Reduction amount of Kupper number Supply pulp (1 out) 29.5 After 1-stage treatment (3 out) 16.5 13.0 After 2 stage treatment (3 'out) 12.1 4.4 Example 4 Mixing using the same equipment as in Example 3 Oxidized white liquor 17kgNa in machine 2
As OH / absolute dry pulp t, oxygen 17 kg / absolute dry pulp t, 8 kg of oxidized white liquor NaOH / absolute dry pulp t, oxygen 8 kg / absolute dry pulp t were separately supplied to the mixer 2 '. Other conditions were the same as in Example 3, and the same softwood cellulose pulp as in Comparative Example 1 was subjected to oxygen delignification treatment. The results are shown in Table 4.
第４表 カツパー価 カツパー価減少量 供給パルプ（１出） 27.3 １段処理後（３出） 16.9 10.4 ２段処理後（３′出） 11.8 5.1 酸化白液と酸素を分割供給しても実施例３と同様の結果
が得られた。Table 4 Kupper number Reduction of Kupper number Supply pulp (1 out) 27.3 After 1-stage treatment (3 out) 16.9 10.4 After 2 stage treatment (3 'out) 11.8 5.1 Example even if oxygen white liquor and oxygen are supplied separately Results similar to those of No. 3 were obtained.
比較例２ 実施例３と同一設備を用いて酸化白液25kgNaOHとして／
絶乾パルプｔ、酸素25kg/絶乾パルプｔ、蒸気を混合機
２に供給し、脱リグニン塔3,3′の塔内圧力（塔頂）３
は約6kg/cm2、３′は約3kg/cm2、３に供給するパルプス
ラリー温度を100℃、パルプ濃度を12.0％、３の滞留時
間を10分間、３′の滞留時間を60分間にして、比較例１
と同一の針葉樹セルロースパルプを酸素脱リグニン処理
した。ただし混合機２′は使用せずバイパスして処理し
た。その結果を第５表に示す。Comparative Example 2 Using the same equipment as in Example 3 as 25 kg of oxidized white liquor /
The dry pulp t, oxygen 25 kg / dry pulp t, and steam are supplied to the mixer 2, and the internal pressure of the delignification towers 3, 3 '(top) 3
Is about 6 kg / cm 2 , 3'is about 3 kg / cm 2 , the pulp slurry temperature to be supplied to 3 is 100 ℃, the pulp concentration is 12.0%, the residence time of 3 is 10 minutes, the residence time of 3'is 60 minutes Comparative Example 1
The same softwood cellulosic pulp was treated with oxygen delignification. However, the mixer 2'was not used and bypassed. The results are shown in Table 5.
第５表 カツパー価 カツパー価減少量 供給パルプ（１出） 28.3 １段処理後（３出） 16.8 11.5 ２段処理後（３′出） 16.0 0.8 第５表より明らかなように、脱リグニン塔３と３′の間
に設置された混合機２′をバイパスして中濃度酸素脱リ
グニン処理すると、２基の脱リグニン塔で処理したにも
かかわらず、本発明の目的を達成することができない。Table 5 Kupper number Reduction of Kupper number Supply pulp (1 out) 28.3 After 1-stage treatment (3 out) 16.8 11.5 After 2 stage treatment (3 'out) 16.0 0.8 As can be seen from Table 5, delignification tower 3 If the intermediate concentration oxygen delignification treatment is performed by bypassing the mixer 2'installed between No. 3 and 3 ', the object of the present invention cannot be achieved despite treatment with two delignification towers.
なお前記実施例では針葉樹セルロースパルプについて説
明したが、広葉樹セルロースパルプについても同様な結
果を得ることができる。In addition, although the softwood cellulose pulp was described in the said Example, the same result can be obtained also about a hardwood cellulose pulp.
（発明の効果） 以上の説明から明らかなように、本発明の高剪断混合機
と酸素脱リグニン装置との組合せ単位を複数段直列した
装置を使用してセルロースパルプを脱リグニン、漂白す
ることにより従来の中濃度酸素脱リグニン法に比して低
カツパー価のパルプが得られ、又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。(Effect of the invention) As is clear from the above description, by delignifying and bleaching cellulose pulp using a device in which a combination unit of the high shear mixer and the oxygen delignification device of the present invention is connected in multiple stages in series, As compared with the conventional medium-concentration oxygen delignification method, a pulp having a lower Kupper number can be obtained, and as a result, the wastewater load 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図は従来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図は従来法を示す比
較例１における酸素脱リグニン装置の滞留時間と脱リグ
ニン量の関係を示すグラフであり、第５図は中濃度酸素
脱リグニン法におけるパルプ粘度とカツパー価との関係
を示すグラフである。 １……ポンプ、2,2′,2″……高剪断混合機、3,3′,3″
……酸素脱リグニン装置、４……脱気器1 and 2 show a series diagram of an apparatus which is an embodiment of the present invention, FIG. 3 shows a series diagram of an apparatus used for a conventional medium concentration oxygen delignification method, and FIG. 4 shows a conventional apparatus. FIG. 5 is a graph showing the relationship between the residence time of the oxygen delignification apparatus and the amount of delignification in Comparative Example 1 showing the method, and FIG. 5 is a graph showing the relationship between pulp viscosity and Kuppa number in the medium-concentration oxygen delignification method. . 1 …… Pump, 2,2 ′, 2 ″ …… High shear mixer, 3,3 ′, 3 ″
...... Oxygen delignification equipment, 4 …… Deaerator
───────────────────────────────────────────────────── 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 (72)発明者 上田 正 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 (72)発明者 近藤 晋一郎 東京都中央区銀座４丁目７番５号 王子製 紙株式会社内 (56)参考文献 特開 昭56−91094（ＪＰ，Ａ) 特公 昭53−9286（ＪＰ，Ｂ２) ─────────────────────────────────────────────────── ─── Continuation of front page (72) Inventor Osamu Matsumura 2-1-1 Ojimachi, Tomakomai, Hokkaido Oji Paper Co., Ltd. Tomakomai Mill (72) Inventor Tadashi Ueda 2-1-1 Omachi, Tomakomai, Hokkaido No. Oji Paper Co., Ltd. Tomakomai Mill (72) Inventor Shinichiro Kondo 4-7-5 Ginza, Chuo-ku, Tokyo Oji Paper Co., Ltd. (56) Reference JP-A-56-91094 (JP, A) Public Sho 53-9286 (JP, B2)
Claims (1)
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により脱リグニン、漂
白を行う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. When a medium-concentration cellulose pulp slurry is delignified and bleached with alkali and oxygen, a combination of a high shear mixer and a tower pressure type oxygen delignification apparatus is provided in multiple stages in series. A method for delignification and bleaching with oxygen of cellulose pulp, characterized in that delignification and bleaching are performed by an apparatus.
Priority Applications (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61241518A JPH0768675B2 (en) | 1986-10-13 | 1986-10-13 | Oxygen delignification and bleaching method for cellulose pulp |
| SE8703929A SE8703929L (en) | 1986-10-13 | 1987-10-12 | PROCEDURE FOR DELIGNIFICATION AND WHEATING OF A LIGNOCELLULOSALLY MASS MATERIAL WITH ACID AND ALKALI |
| FI874478A FI874478A (en) | 1986-10-13 | 1987-10-12 | FOERFARANDE FOER DELIGNIFIERING OCH BLEKNING AV LIGNOCELLUMASSAMATERIAL MED SYRE OCH ALKALI. |
| NO874276A NO874276L (en) | 1986-10-13 | 1987-10-13 | PROCEDURE FOR DELIGNIFICATION AND WHITING OF A LIGNOCELLULOS MASS WITH OXYGEN AND ALKALI. |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61241518A JPH0768675B2 (en) | 1986-10-13 | 1986-10-13 | Oxygen delignification and bleaching method for cellulose pulp |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP18164896A Division JPH08325970A (en) | 1996-06-24 | 1996-06-24 | Delignification and bleaching of cellulose pulp by oxygen |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6399389A JPS6399389A (en) | 1988-04-30 |
| JPH0768675B2 true JPH0768675B2 (en) | 1995-07-26 |
Family
ID=17075535
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61241518A Expired - Lifetime JPH0768675B2 (en) | 1986-10-13 | 1986-10-13 | Oxygen delignification and bleaching method for cellulose pulp |
Country Status (4)
| Country | Link |
|---|---|
| JP (1) | JPH0768675B2 (en) |
| FI (1) | FI874478A (en) |
| NO (1) | NO874276L (en) |
| SE (1) | SE8703929L (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5011572A (en) * | 1989-05-19 | 1991-04-30 | Fmc Corporation | Two stage process for the oxygen delignification of lignocellulosic fibers with peroxide reinforcement in the first stage |
| AT404740B (en) | 1989-10-30 | 1999-02-25 | Chemiefaser Lenzing Ag | Process for the chlorine-free bleaching of pulps |
| SE522593C2 (en) * | 1999-07-06 | 2004-02-24 | Kvaerner Pulping Tech | Oxygen gas delignification system and method of pulp of lignocellulosic material |
| EP1813345A1 (en) * | 2006-01-30 | 2007-08-01 | Sulzer Pumpen Ag | Method and apparatus for controlling the efficiency of mixing |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS539286A (en) * | 1976-07-13 | 1978-01-27 | Matsushita Electric Ind Co Ltd | Production of catalyst body |
| US4363697A (en) * | 1979-12-03 | 1982-12-14 | The Black Clawson Company | Method for medium consistency oxygen delignification of pulp |
-
1986
- 1986-10-13 JP JP61241518A patent/JPH0768675B2/en not_active Expired - Lifetime
-
1987
- 1987-10-12 SE SE8703929A patent/SE8703929L/en unknown
- 1987-10-12 FI FI874478A patent/FI874478A/en not_active Application Discontinuation
- 1987-10-13 NO NO874276A patent/NO874276L/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6399389A (en) | 1988-04-30 |
| SE8703929D0 (en) | 1987-10-12 |
| SE8703929L (en) | 1988-04-14 |
| NO874276D0 (en) | 1987-10-13 |
| NO874276L (en) | 1988-04-14 |
| FI874478A0 (en) | 1987-10-12 |
| FI874478A (en) | 1988-04-14 |
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