JPS6328993A - Improved bleaching method and apparatus - Google Patents
Improved bleaching method and apparatusInfo
- Publication number
- JPS6328993A JPS6328993A JP62130081A JP13008187A JPS6328993A JP S6328993 A JPS6328993 A JP S6328993A JP 62130081 A JP62130081 A JP 62130081A JP 13008187 A JP13008187 A JP 13008187A JP S6328993 A JPS6328993 A JP S6328993A
- Authority
- JP
- Japan
- Prior art keywords
- pulp
- extraction
- chlorination
- effluent
- washing
- 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.)
- Granted
Links
- 238000004061 bleaching Methods 0.000 title claims description 13
- 238000000034 method Methods 0.000 title claims description 12
- 238000000605 extraction Methods 0.000 claims description 64
- 238000005406 washing Methods 0.000 claims description 42
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 33
- 238000005660 chlorination reaction Methods 0.000 claims description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 238000004140 cleaning Methods 0.000 claims description 8
- 238000004064 recycling Methods 0.000 claims 2
- 238000002474 experimental method Methods 0.000 description 9
- 239000000523 sample Substances 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 6
- OSVXSBDYLRYLIG-UHFFFAOYSA-N dioxidochlorine(.) Chemical compound O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 239000002023 wood Substances 0.000 description 5
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 4
- 235000019398 chlorine dioxide Nutrition 0.000 description 4
- 239000002655 kraft paper Substances 0.000 description 4
- 239000004155 Chlorine dioxide Substances 0.000 description 3
- 241000218657 Picea Species 0.000 description 3
- 239000003513 alkali Substances 0.000 description 3
- 210000000988 bone and bone Anatomy 0.000 description 3
- 239000000460 chlorine Substances 0.000 description 3
- 229910052801 chlorine Inorganic materials 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- 240000009002 Picea mariana Species 0.000 description 2
- 235000017997 Picea mariana var. mariana Nutrition 0.000 description 2
- 235000018000 Picea mariana var. semiprostrata Nutrition 0.000 description 2
- 229920001131 Pulp (paper) Polymers 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 239000012670 alkaline solution Substances 0.000 description 2
- 239000007844 bleaching agent Substances 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical compound Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000013068 control sample Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 125000000621 oxo-lambda(3)-chloranyloxy group Chemical group *OCl=O 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000000123 paper Substances 0.000 description 1
- 150000002978 peroxides Chemical class 0.000 description 1
- 238000004076 pulp bleaching Methods 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 1
- 229910001948 sodium oxide Inorganic materials 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- SFKTYEXKZXBQRQ-UHFFFAOYSA-J thorium(4+);tetrahydroxide Chemical compound [OH-].[OH-].[OH-].[OH-].[Th+4] SFKTYEXKZXBQRQ-UHFFFAOYSA-J 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Wood Science & Technology (AREA)
- Paper (AREA)
Abstract
(57)【要約】本公報は電子出願前の出願データであるた
め要約のデータは記録されません。(57) [Abstract] This bulletin contains application data before electronic filing, so abstract data is not recorded.
Description
【発明の詳細な説明】
本発明は、漂白の方法および装置の改良に関し、特に漂
白抽出工程において必要な化学薬品の装入車を減少する
改良された方法および装置に関する。DETAILED DESCRIPTION OF THE INVENTION This invention relates to improvements in bleaching methods and equipment, and more particularly to improved methods and equipment that reduce the number of chemical loads required in the bleach extraction process.
化学パルプの漂白中に抽出流出液のいくらかを再循環す
ることは熱を保ちかつ酸性の塩素化液を置換するための
慣行である。再循環された抽出段階液は、塩素化された
パルプが洗浄機シャワーを軽で塩素化段階洗浄機を去る
時に塩素化されたパルプに加えられ、そしてこの再循環
された液はパルプと共に抽出段階に戻される［１ｌｉｓ
ｔｅｄ、 Ｊ、 Ａ。It is common practice to recirculate some of the extraction effluent during bleaching of chemical pulps to conserve heat and displace the acidic chlorinating liquor. Recirculated extraction stage liquor is added to the chlorinated pulp as it leaves the chlorination stage washer in the washer shower, and this recycled liquor passes through the extraction stage with the pulp. [1lis
ted, J.A.
およびＮｅ１ＳＯｎ、 Ｊｒｌ、Ｇ、 Ｇ、、Ｔｈｅ
Ｂｌｃａｃｈｉｎｇｏｒｐｕｌｐ、 Ｒ，Ｐ、 Ｓｉｎ
ｇｈ １ｉｉｉ集、第３版、ＴＡＰＰＩ Ｐｒｅｓｓ、
＾ｔｒａｎｔａ 、 １９７９、第３９３頁； ｔ（ｉ
ｎｓｔｅｄ、 Ｊ。and Ne1SOn, Jrl, G, G,,The
Blcachingorpulp, R.P., Sin
gh 1iii collection, 3rd edition, TAPPI Press,
^tranta, 1979, p. 393; t(i
nsted, J.
＾、および旧ｃｏｌｌｅ、 Ｆ、 Ｈ，Ａ、 、Ｐｕ１
ｐ ＰａＤ（！ｒ Ｍａｒｃａｎ、、７４ （５）Ｔ１
７１ （１９７４）；）１ａｒｔｉＯＶａａｒａ、 １
． 、Ｐａｐｅｒｉ ｊａ Ｐｕｕ 、 ６２ （５）
３１９（１９８０）およびＷａｒｔｉｏｖａａｒａ、
１．、Ｐｕ１ｐ Ｐａｐｅｒ Ｃａｎ、 、８１ （７
） Ｔ１６７ （１９８０）］。^, and old colle, F, H, A, , Pu1
p PaD(!r Marcan,, 74 (5) T1
71 (1974);)1 artiOVaara, 1
．． , Paperi ja Puu, 62 (5)
319 (1980) and Wartiovaara,
1. , Pu1p Paper Can, , 81 (7
) T167 (1980)].
また先行技術［ＢＬｌｒｋａｒｔ、 Ｌ、Ｆ、 、Ｐａ
ｐｅｒ ＴｒａｄｅＪ、１５６（２＞３３ （１９７２
）および八ｚａｄ、 Ａ。Also, prior art [BLlrkart, L, F, , Pa
per TradeJ, 156 (2>33 (1972
) and Yazad, A.
ＨｌおよびＢＩＪｒｋａｒｔ、 Ｌ、 Ｆ、、ＴａＤｐ
ｉ 、 ５９ （４＞ １４０（１９７６）］において
、第１抽出段階用抽出液として水酸化ナトリウムをもっ
て補強された再循環流出液を用いることも知られている
。このことで抽出段階に必要な水酸化ナトリウムの巳を
約１６％減少させることが判っている。Hl and B.I.Jrkart, L.F., TaDp.
I, 59 (4>140 (1976)), it is also known to use a recycled effluent enriched with sodium hydroxide as extractant for the first extraction stage. This reduces the water requirement for the extraction stage. It has been found to reduce the amount of sodium oxide by about 16%.
本ｊ！！発明の目的は、化学パルプ漂白系列の抽出段階
に必要な化学薬品の量を減少させる改良された方法およ
び装はを提供することである。Book j! ! It is an object of the invention to provide an improved method and equipment that reduces the amount of chemicals required for the extraction stage of a chemical pulp bleaching series.
本発明においては、抽出工程が開始される前に追加洗浄
工程がある。In the present invention, there is an additional washing step before the extraction step is started.
更に詳細には、パルプを逐次塩素化、塩素化洗浄工程、
アルカリ性溶液（通常、水酸化すトリウムおよび水蒸気
〉との混合工程、抽出工程、次いで抽出段階洗浄工程か
ける、漂白方法において、パルプを塩素化洗浄工程と混
合工程との間で追加洗浄工程にかける工程を含む改良さ
れた漂白方法である。抽出段階洗浄工程からの流出液は
、塩素化洗浄工程直後のパルプに再循環される。追加洗
浄工程からの流出液は再循環され、塩素化洗浄工程に用
いられる。More specifically, the pulp is sequentially chlorinated, the chlorination washing process,
In a bleaching process, the pulp is subjected to an additional washing step between the chlorination washing step and the mixing step, in which the pulp is subjected to a mixing step with an alkaline solution (usually thorium hydroxide and water vapor), an extraction step, and then an extraction step washing step. The effluent from the extraction stage washing step is recycled to the pulp immediately following the chlorination washing step.The effluent from the additional washing step is recycled to the chlorination washing step. used.
また、塩素化洗浄機と、パルプが抽出塔に入る前に水蒸
気およびアルカリ性Ｗ３液と混合されるミキサーどの闇
に、追加洗浄機を含む改良された漂白装置である。追加
洗浄機からの流出液を塩素化洗浄様に導く手段、および
抽出洗浄機からの流出液を塩素化洗浄機と追加流１９ｉ
ｖＡの間の位置でパルプに導く手段である。There is also an improved bleaching equipment that includes an additional washer in addition to the chlorination washer and the mixer where the pulp is mixed with steam and alkaline W3 liquor before entering the extraction column. Means for directing the effluent from the additional washer to the chlorinating washer, and means for directing the effluent from the extracting washer to the chlorinating washer and the additional stream 19i
It is a means for leading to pulp at a position between vA.
以上本願発明を一般的に説明したが、本発明の実施態様
を図示する添付図面を参照とすることにする。Having thus generally described the present invention, reference will now be made to the accompanying drawings that illustrate embodiments of the invention.
ここに記載された塩素化には、塩素のいくらか又はすべ
てを二酸化塩素に代えるなどの塩素化工程の種々の変形
が含まれる。塩素および二酸化塩素は、抽出段階＾ａに
使用できる酸化性化学薬品の例である。酸化工程が先立
つどのような抽出段階でも、本願発明の適用によって改
良できる。The chlorination described herein includes various variations of the chlorination process, such as replacing some or all of the chlorine with chlorine dioxide. Chlorine and chlorine dioxide are examples of oxidizing chemicals that can be used in the extraction step ^a. Any extraction step that is preceded by an oxidation step can be improved by application of the present invention.
更に詳細には、第１図に示すように、再循環工程を有す
る従来の塩素化漂白系には、塩素他塔１０Ｓ塩素化洗浄
機１４に至る配管１２、アルカリ性溶液および水蒸気を
パルプと混合するミキサー１８に至る配管１６、更に抽
出塔２２への輸送管２０および抽出段階洗浄機２６に導
く輸送管２４が含まれる。抽出段階洗浄機２６からの流
出液を塩素化洗浄機１４に戻す手段２８が設けられてい
る。More specifically, as shown in FIG. 1, a conventional chlorination bleaching system with a recirculation step includes a chlorine column 10S piping 12 leading to a chlorination washer 14, which mixes the alkaline solution and steam with the pulp. Contains piping 16 leading to a mixer 18, as well as a transport pipe 20 to an extraction column 22 and a transport pipe 24 leading to an extraction stage washer 26. Means 28 are provided for returning the effluent from the extraction stage washer 26 to the chlorination washer 14.
第２図に図示する本願発明においては同様の参照数字が
同様の構成に用いられる。黙しながら、塩素化洗浄機１
４とミキサー１８の間に追加洗浄機３０が設けられてい
ることが判るであろう。この例では、抽出洗浄機２６か
らの流出液を、ライン２８を経て、洗浄機１４と３０の
間の位置のパルプに再循環する。この位置における乱流
源は、適切な混合の確保に有益である。追加洗浄ｌ１３
０からの流出液は、ライン３２を経て塩素化洗浄機１４
に再循環される。Like reference numerals are used for like structures in the invention illustrated in FIG. In silence, chlorination cleaning machine 1
It will be seen that an additional washer 30 is provided between 4 and mixer 18. In this example, the effluent from extraction washer 26 is recycled via line 28 to the pulp at a location between washers 14 and 30. A source of turbulence at this location is beneficial to ensure proper mixing. Additional cleaning l13
The effluent from 0 passes through line 32 to chlorination washer 14.
is recirculated to
追加洗浄１ｆ１３０におけるシャワーに用いられる液体
は、ライン３４を経て導入され、これは抽出流出液また
は水ａ（図示せず）からもたらされる。The liquid used for the shower in the additional wash 1f 130 is introduced via line 34, which comes from the extraction effluent or water a (not shown).
洗浄工程は、重要である。なぜならば、この洗浄工程は
、塩素化されたパルプと抽出流出液との反応において＜
ＮａＣｌと共（ｄ）形成されたＮａＨＣＯおよびＣｏ２
を除去するからである。The washing step is important. This is because this washing step involves a reaction between the chlorinated pulp and extraction effluent.
NaHCO and Co2 formed (d) with NaCl
This is because it removes.
ＮａＨＣＯおよびＣｏ２がパルプと共に存在する場合は
、これらは油出段階における化学薬品の装入量の大部を
無駄に消費する。If NaHCO and Co2 are present with the pulp, they waste a large portion of the chemical charge in the extraction stage.
好ましい実施態様の実施を具体的に説明する例を示す。Examples are provided to illustrate implementation of the preferred embodiments.
例１は、抽出流出液で処理されたパルプの洗浄によって
可能となる水酸化ナトリウムの節約を説明するものであ
る。Example 1 illustrates the sodium hydroxide savings made possible by washing pulp treated with extraction effluent.
トウヒ材りラフトパルプ（カッパー１［ｉ２７．５＞を
塩素化し十分に洗浄し、次いで濃度２０％にプレスした
。次いで、このパルプを、第１抽出段階からの流出液を
もって濃度１０％に希釈した。これで、絶対乾燥パルプ
各１９についての再循環された流出液は５ｍｌとなる。Spruce wood raft pulp (copper 1 [i27.5>) was chlorinated, thoroughly washed and then pressed to a consistency of 20%. The pulp was then diluted to a consistency of 10% with the effluent from the first extraction stage. This results in 5 ml of recycled effluent for each 19 absolutely dry pulps.
しかしながら、この５ ｍ Ｌ ａ−’の液は、パルプ
と組み合さった液を置換するかまたは単に更に低い濃度
へと希釈することによって添加できたものである。６０
℃の抽出流出液を、パルプと５分間接触させた。パルプ
を水洗し、次いで水性アルカリをもって抽出した。However, this 5 m L a-' of liquid could be added by displacing the liquid associated with the pulp or simply diluting it to an even lower concentration. 60
The extraction effluent at °C was contacted with the pulp for 5 minutes. The pulp was washed with water and then extracted with aqueous alkali.
第２の試料を塩素化し、十分に洗浄し、次いで濃度１０
％にプレスした。次に、この試料を、第１抽出段階から
の抽出流出液をもって濃度１０％に希釈した。６０℃の
抽出流出液を、５分間パルプと接触させ、次いでアルカ
リをこれに加えて、抽出を完了させた。洗浄、塩素化さ
れたパルプの対照試料を、何ら前処理なしに抽出した。A second sample was chlorinated, thoroughly washed and then concentrated at 10
Pressed to %. This sample was then diluted to a concentration of 10% with the extraction effluent from the first extraction stage. The extraction effluent at 60°C was contacted with the pulp for 5 minutes and then alkali was added thereto to complete the extraction. A control sample of washed, chlorinated pulp was extracted without any pretreatment.
次いで、全３種のパルプをさらにＤＥＣ部分系列を用い
て漂白した。All three pulps were then further bleached using the DEC subseries.
第１表に示すように、本願発明によって流出液の再循環
および洗浄を行った場合、Ｅ１段階における化学薬品消
費ｍが１／３減少しても最終白色度８９％が容易に得ら
れた。再循環された流出液を、パルプから洗い流してい
ない従来の型の再循環は、ＧＥカッパー価またはＮａＯ
Ｈ使用最について利点を与えなかった。As shown in Table 1, when the effluent was recirculated and washed according to the present invention, a final brightness of 89% was easily obtained even though the chemical consumption m in the E1 stage was reduced by 1/3. Conventional types of recirculation, in which the recycled effluent is not washed away from the pulp, have a GE kappa number or NaO
The use of H gave no advantage.
１１羞
抽出段階
における
ａＯＨ
装入量、
絶対乾燥 ＣＥ
再循環なし ３．０ ５．４ ８１．０ ８９
．５２．０ ６．１ ７Ｇ、７ −１．０
９．０ ５６．５ ８４．６従来の再循ＥＭ ３
．０ ５．５ ８１，４ ８９．６（洗浄なし＞
２．０ ５．８ ７６．６ ８７．９１．
０ ８．４ ６０．７ ８５．５再循環後
３．０ ５．１ ８２．２ ８９．９洗浄
２．０ ５．３ ’８１．７ ８９．６１．
０ ５．８ ７９．６ ８８．７未晒パルプ：ク
ロトウヒ材クラフトパルプ；カッパー価２７゜５
Ｃ−段階： 絶対乾燥パルプ当たりＣＩ２５．５％；２
５℃において４５分：
濁度３．５％
Ｅ−段階： ７０℃において９０分：ｌ！度１０％
Ｄｌ−段階：絶対乾燥パルス当たりＣｌ０２１％および
ＮａＯＨ０，５５％＝
６０℃において３時間；濃度
１０％
Ｅ２−段階：絶対乾燥パルプ当たりＮａＯＨ１％＝６０
℃において１時間；
１度１０％
Ｄ２−段階：絶対乾燥パルプ当たりＮａＯＨ０，５％二
６０℃において３時間；
濃度１０％
再循環に用いた抽出流出液は、同じ塩素化されたパルプ
を、絶対乾燥パルプ当たりＮａＯＨ３％をもって抽出す
ることによって製造されたものである。11 aOH charge in extraction stage, absolutely dry CE without recirculation 3.0 5.4 81.0 89
．． 52.0 6.1 7G, 7 -1.0
9.0 56.5 84.6 Conventional recirculating EM 3
．． 0 5.5 81.4 89.6 (no cleaning>
2.0 5.8 76.6 87.91.
0 8.4 60.7 85.5 After recirculation
3.0 5.1 82.2 89.9 Washing
2.0 5.3 '81.7 89.61.
0 5.8 79.6 88.7 Unbleached pulp: Black spruce wood kraft pulp; Kappa number 27°5 C-stage: CI 25.5% per absolute dry pulp; 2
45 minutes at 5°C: turbidity 3.5% E-stage: 90 minutes at 70°C: l! degree 10% Dl-stage: Cl021% and NaOH 0,55% per absolute dry pulse = 3 hours at 60 °C; concentration 10% E2-stage: NaOH 1% per absolute dry pulp = 60
1 hour at 60 °C; once 10% D2-stage: NaOH 0,5% per absolutely dry pulp for 3 hours at 60 °C; concentration 10% It was produced by extraction with 3% NaOH per dry pulp.
匠ユ
第２表は、例１において可能であることが判つたアルカ
リの節約は、再循環系が定常状態に近付いた場合に保た
れることを示している。Table 2 shows that the alkali savings found possible in Example 1 are maintained when the recirculation system approaches steady state.
実験１において、トウヒ材クラフトパルプ（カッパー価
２７．５）を塩素化し、十分洗浄し、次いで何ら前処理
せずに（絶対乾燥パルプ当たりＮａＯ８３，０％）抽出
した。実１２においては、同じパルプの第２の試料を塩
素化し１、十分洗浄し、次いでａ度２０％にプレスした
。次いでこの試料を実験１の抽出段階からの抽出流出液
をもって希釈した。６０℃における抽出流出液をパルプ
と５分間接触させた。パルプを水洗し、次いで絶対乾燥
パルプ当たりＮａ’ＯＨ２％のみをもって抽出した。実
験３においては、パルプの第３の試料を塩素化し、十分
洗浄し、次いでａ度２０％にプレスした。次いでこの試
料を実験２からの抽出流出液をもって希釈した。パルプ
を、再び水洗し、次いで給体乾燥パルプ当たりＮａＯ８
２％のみをもって抽出した。先行実験からの流出液を用
いるこの操作を繰り返した。第２表は、Ｎ ａ ＯＨ装
入量が実３１１２．３および４における絶対乾燥パルプ
当たり３．０％から２．０％に減少したとしても、ＣＥ
カッパー価は維持されることを示している。In experiment 1, spruce wood kraft pulp (kappa number 27.5) was chlorinated, thoroughly washed and then extracted without any pretreatment (83.0% NaO per absolute dry pulp). In Example 12, a second sample of the same pulp was chlorinated 1, thoroughly washed, and then pressed to 20% a degree. This sample was then diluted with the extraction effluent from the extraction step of Experiment 1. The extraction effluent at 60°C was contacted with the pulp for 5 minutes. The pulp was washed with water and then extracted with only 2% Na'OH per absolute dry pulp. In Experiment 3, a third sample of pulp was chlorinated, thoroughly washed, and then pressed to 20% a degree. This sample was then diluted with the extraction effluent from Experiment 2. The pulp was washed again with water and then fed with NaO8 per dry pulp.
Only 2% was extracted. This operation was repeated using the effluent from the previous experiment. Table 2 shows that even if the N a OH charge was reduced from 3.0% to 2.0% per absolute dry pulp in Examples 3112.3 and 4, the CE
This shows that the kappa number is maintained.
実１５においては、パルプの試料を塩素化し、十分に洗
浄し、次いで絶対乾燥パルプ当たりＮａＯＨ２％のみを
もって抽出した。ＧＥカッパー価は、本願発明による流
出液の再循環および洗浄を用いた場合に１９られた値よ
り高い価であった。In Example 15, a sample of pulp was chlorinated, thoroughly washed, and then extracted with only 2% NaOH per bone dry pulp. The GE kappa number was 19 higher than that obtained using effluent recirculation and washing according to the present invention.
本願発明によって用いられた絶対乾燥パルプ当たりＮａ
ＯＨ２％の装入槽は、明らかに従来の様式で用いられた
ＮａＯＨ３％に等しい。Na per absolute dry pulp used according to the present invention
A charge of 2% OH is clearly equivalent to 3% NaOH used in the conventional manner.
第２表
当たり％
従 来 １ 再循環なし ３．０ ４．３再循
環／洗浄 ２ 実験１ ２．０ ４Ｊ再循環／洗
浄 ３ 実験２ ２．０ ４．１再循環／洗浄
４ 実験３ ２．０ ４．０性ユ
この例は、塩素化されたパルプを再循環された抽出流出
液をもって処理する時間および温度の変化は、操作の結
果に影響しないことを示している。% per Table 2 Conventional 1 No recirculation 3.0 4.3 Recirculation/washing 2 Experiment 1 2.0 4J Recirculation/washing 3 Experiment 2 2.0 4.1 Recirculation/washing
4 Experiment 3 2.0 4.0 This example shows that changes in time and temperature in treating chlorinated pulp with recycled extraction effluent do not affect the results of the operation.
トウヒ材クラフトパルプ（カッパー１ａｉ２７．５＞を
塩素化し、十分洗浄し、次いで濃度２０％にプレスした
。次いで、このパルプを、第１抽出段階からの流出液を
もって濃度１０％に稀釈した。塩素化されたパルプと再
循環された抽出流出液の間のこの反応に向いている時間
と温度の組み合せを選択した。パルプを水洗し、次いで
絶対乾燥パルプ当たりＮａＯ８２，０％をもって抽出し
た。Spruce wood kraft pulp (copper 1ai 27.5>) was chlorinated, thoroughly washed and then pressed to a consistency of 20%. This pulp was then diluted to a consistency of 10% with the effluent from the first extraction stage. Chlorination A time and temperature combination was chosen that favored this reaction between the recycled pulp and the recycled extraction effluent.The pulp was washed with water and then extracted with 82.0% NaO per bone dry pulp.
この実験を、塩素化されたパルプと再循環された抽出流
出液の間の反応について異なった時間と温度の組み合せ
をもって繰り返した。This experiment was repeated with different time and temperature combinations for the reaction between the chlorinated pulp and the recycled extraction effluent.
第３表は、塩素化されたパルプと再循環された抽出流出
液の間の有用な反応は、温度２５℃およびそれ以上にお
いては３０秒間以内に起こることを示している。この意
味は、反応を管路中において行うことができ、しかも特
別の反応容器が必要ないということである。Table 3 shows that useful reactions between chlorinated pulp and recycled extraction effluent occur within 30 seconds at temperatures of 25° C. and above. This means that the reaction can be carried out in pipes and no special reaction vessels are required.
第３表
再循環された抽出流出液
温度 接触時間 ＣＥ
℃ 分 カッパー価
２５ ０．５ ３．９６０
０、５ ４．０６０ １．０
４．Ｏｐ−６０５，０４，１
６０１０，０３，９
Ｃ−段階およびＥ−段階条件：第１表の脚注の通り。Table 3 Recirculated extraction effluent temperature Contact time CE °C min Kappa number 25 0.5 3.960
0, 5 4.060 1.0
4. Op-605,04,1 6010,03,9 C-stage and E-stage conditions: As footnotes in Table 1.
例４
塩素化段階においてパルプに少量の二塩化基糸を添加す
ることは、塩素化の間のセルロースに対する′＃Ａ傷を
最小にするための慣行である。Example 4 Adding a small amount of dichloride base yarn to the pulp during the chlorination step is a practice to minimize '#A damage to cellulose during chlorination.
第４表は、従来法で処理されたパルプのＧＥカッパー価
が、ＣｌＯ２で１０％置換した場合に大きく影響されな
いことを示している。さらに、塩素化されたパルプを本
願発明によって処理することによって、Ｃ１ｏ２を用い
るか否かにかかわらず、Ｅ−段階のＮａＯＨを２．０％
またはそれ以下に減少できる。Table 4 shows that the GE kappa number of conventionally treated pulp is not significantly affected by 10% substitution with ClO2. Furthermore, by treating the chlorinated pulp according to the present invention, the E-stage NaOH can be reduced to 2.0% with or without C1o2.
or can be reduced to less.
従来 ０ ３．８ ４．３再
循環／洗浄 ０ ２．０ ４．２再循環
／洗浄 ０ １．５ ４．２再循環／洗
浄 ０ １．０ ４．１従来
１０ ３．０ ４゜１再循ｍ／洗浄
１０ ２．８ ４．０再循環／洗浄 １
０ １．５ ４．３再循環／洗浄 １０
１．０ ４．４未晒パルプ： クロトウ
ヒ材クラフトパルプ：カッパー価２７．５
Ｃ−段階： 絶対乾燥パルプ当たりＣｊ！２５．５％
；２５℃において４５分；
濃度３．５％
Ｃ−段階： 絶対乾燥パルプ当たりＣ１２５，０％およ
びＣ１０２０，２％：
２５℃において４５分：濃度
３．５％
Ｅ−段階： ７０℃において９０分；温度１０％
再循環に用いた抽出流出液は、同じ塩素化されたパルプ
を絶対乾燥パルプ当たりＮａＯ８３％をもって抽出する
ことによって生成された。Conventional 0 3.8 4.3 Recirculation/Cleaning 0 2.0 4.2 Recirculation/Cleaning 0 1.5 4.2 Recirculation/Cleaning 0 1.0 4.1 Conventional
10 3.0 4゜1 recirculation m/washing
10 2.8 4.0 Recirculation/Washing 1
0 1.5 4.3 Recirculation/Washing 10
1.0 4.4 Unbleached pulp: Black spruce wood kraft pulp: Kappa number 27.5 C-stage: Cj per absolute dry pulp! 25.5%
; 45 minutes at 25°C; concentration 3.5% C-stage: C125.0% and C1020.2% per absolute dry pulp: 45 minutes at 25°C: concentration 3.5% E-stage: 90 minutes at 70°C temperature 10% The extraction effluent used for recirculation was produced by extracting the same chlorinated pulp with 83% NaO per bone dry pulp.
前記の実施態様は、具体的説明のためのみであって、当
業者に明かな変形およびμ正をなし得ることは理解され
よう。It will be understood that the embodiments described above are for illustrative purposes only, and modifications and variations obvious to those skilled in the art may be made.
また置換漂白系を用いて、本願発明の工程を実施できる
ことも明らかである。It is also clear that displacement bleaching systems can be used to carry out the process of the present invention.
前記の抽出流出液を用いる概念は、抽出段階への化学薬
品の添加によって影響されるものでない。The concept of using the extraction effluent described above is not affected by the addition of chemicals to the extraction stage.
抽出段階への酸素、過酸化物または次亜塩ｇ酸塩の添加
は、再循環後で抽出段階前の洗浄によって水酸化ナトリ
ウム装入量を減少する原理を変更させるものでない。The addition of oxygen, peroxide or hypochlorite to the extraction stage does not change the principle of reducing the sodium hydroxide charge by washing after recirculation and before the extraction stage.
第１図は、塩素化段階に次いで抽出段階を有する従来の
漂白プラントにおける再循ｌ】系の簡単な流れ図である
。
第２図は、本願発明の改良された系を説明する第１図と
同様の流れ図である。
１０：塩素他塔
１２：配管
１４：塩素化洗浄機
１６：配管
１８：ミキサー
２０コ輸送管
２２：抽出塔
２４：輸送管
２６：抽出段階洗浄機
２８：流出液を戻す手段
３ｏ：追加洗浄機
３２ニライン
３４ニラインFIG. 1 is a simple flow diagram of a recirculation system in a conventional bleach plant having a chlorination stage followed by an extraction stage. FIG. 2 is a flowchart similar to FIG. 1 illustrating the improved system of the present invention. 10: Chlorine and other columns 12: Piping 14: Chlorination cleaning machine 16: Piping 18: Mixer 20 transport pipe 22: Extraction tower 24: Transport pipe 26: Extraction stage washer 28: Means for returning effluent 3o: Additional washing machine 32 ni line 34 ni line
Claims (7)
け、アルカリ性抽出溶液と混合し、抽出工程にかけ、次
いで抽出段階洗浄工程にかける漂白方法において、前記
塩素化洗浄工程と、前記アルカリ性抽出溶液と混合の間
で、前記パルプを追加洗浄工程にかける工程、および抽
出段階洗浄工程からの流出液を塩素化洗浄工程直後のパ
ルプに再循環するというさらに付け加えられた工程を含
む改良された漂白方法。(1) A bleaching method in which chlorinated pulp is sequentially subjected to a chlorination washing step, mixed with an alkaline extraction solution, subjected to an extraction step, and then subjected to an extraction stage washing step, wherein the chlorination washing step and the alkaline extraction solution and the further step of subjecting said pulp to an additional washing step between and mixing, and recycling the effluent from the extraction stage washing step to the pulp immediately after the chlorination washing step. .
行われる、特許請求の範囲第１項の改良された漂白方法
。(2) The improved bleaching method of claim 1, wherein said additional washing step is performed using water or extraction effluent.
おいて用いられて、塩素化洗浄機においてパルプに添加
される、特許請求の範囲第１項の改良された漂白方法。(3) The improved bleaching method of claim 1, wherein the effluent from the additional washing step is used in a chlorination washing step and added to the pulp in a chlorination washing machine.
よび水蒸気を含む、特許請求の範囲第１項、第２項また
は第３項の改良された漂白方法。(4) The improved bleaching method of claim 1, 2 or 3, wherein the alkaline extraction solution contains sodium hydroxide and water vapor.
出液の添加位置において適切な混合を確保する乱流を与
える工程を含む、特許請求の範囲第１項、第２項または
第３項の改良された方法。(5) Claims 1, 2, or 3, wherein the step of recycling the effluent from the extraction stage washing step comprises providing turbulence to ensure proper mixing at the point of addition of the effluent. Improved method of terms.
塩素化洗浄工程にかけ； （ｂ）前記パルプを追加洗浄機に輸送し； （ｃ）前記追加洗浄機中で、前記パルプを洗浄し； （ｄ）アルカリ性抽出溶液を、前記追加洗浄後のパルプ
と混合し； （ｅ）パルプを抽出工程にかけ； （ｆ）抽出されたパルプを抽出段階洗浄工程において洗
浄し； （ｇ）前記抽出段階洗浄工程からの流出液を工程（ｂ）
のパルプ中に再循環し；および （ｈ）工程（ｃ）における追加洗浄ユニットからの流出
液を工程（ａ）の塩素化洗浄機に輸送すること、 を改良された工程として含む漂白方法。(6) (a) subjecting the chlorinated pulp to a chlorination washing step in a chlorination washer; (b) transporting said pulp to an additional washer; (c) in said additional washer, said pulp (d) mixing an alkaline extraction solution with the pulp after said additional washing; (e) subjecting the pulp to an extraction step; (f) washing the extracted pulp in an extraction stage washing step; (g) The effluent from the extraction stage washing step is processed in step (b).
and (h) transporting the effluent from the additional washing unit in step (c) to the chlorination washer of step (a).
性抽出溶液をパルプと混合する系、抽出塔および抽出洗
浄機を含む漂白装置において、前記塩素化洗浄機および
混合系との間に追加洗浄機、前記追加洗浄機からの流出
液を前記塩素化洗浄機へ輸送する手段、および前記抽出
洗浄機からの流出液を前記第１塩素化洗浄機および前記
追加洗浄機の間のパルプへ輸送する手段を含む、改良さ
れた漂白装置。(7) In a bleaching equipment including a chlorination tower, a chlorination washing machine, a system for mixing steam and alkaline extraction solution with pulp, an extraction tower and an extraction washing machine, additional cleaning is performed between the chlorination washing machine and the mixing system. a machine, means for transporting effluent from said additional washer to said chlorination washer, and means for transporting effluent from said extraction washer to a pulp between said first chlorination washer and said additional washer; Improved bleaching equipment, including means.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA510446 | 1986-05-30 | ||
| CA000510446A CA1294396C (en) | 1986-05-30 | 1986-05-30 | Process for decreasing the charge of chemical required in a bleaching extraction stage |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6328993A true JPS6328993A (en) | 1988-02-06 |
| JPH0415313B2 JPH0415313B2 (en) | 1992-03-17 |
Family
ID=4133252
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62130081A Granted JPS6328993A (en) | 1986-05-30 | 1987-05-28 | Improved bleaching method and apparatus |
Country Status (4)
| Country | Link |
|---|---|
| JP (1) | JPS6328993A (en) |
| CA (1) | CA1294396C (en) |
| FI (1) | FI91289C (en) |
| SE (1) | SE500585C2 (en) |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS56159384A (en) * | 1980-04-10 | 1981-12-08 | Sca Development Ab | Production of mechanical cellulose pulp |
-
1986
- 1986-05-30 CA CA000510446A patent/CA1294396C/en not_active Expired - Lifetime
-
1987
- 1987-05-22 SE SE8702141A patent/SE500585C2/en not_active IP Right Cessation
- 1987-05-28 JP JP62130081A patent/JPS6328993A/en active Granted
- 1987-05-28 FI FI872391A patent/FI91289C/en not_active IP Right Cessation
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS56159384A (en) * | 1980-04-10 | 1981-12-08 | Sca Development Ab | Production of mechanical cellulose pulp |
Also Published As
| Publication number | Publication date |
|---|---|
| FI91289B (en) | 1994-02-28 |
| FI872391A (en) | 1987-12-01 |
| FI872391A0 (en) | 1987-05-28 |
| CA1294396C (en) | 1992-01-21 |
| SE8702141L (en) | 1987-12-01 |
| SE500585C2 (en) | 1994-07-18 |
| FI91289C (en) | 1994-06-10 |
| JPH0415313B2 (en) | 1992-03-17 |
| SE8702141D0 (en) | 1987-05-22 |
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