JPH0127798B2 - - Google Patents
Info
- Publication number
- JPH0127798B2 JPH0127798B2 JP22622982A JP22622982A JPH0127798B2 JP H0127798 B2 JPH0127798 B2 JP H0127798B2 JP 22622982 A JP22622982 A JP 22622982A JP 22622982 A JP22622982 A JP 22622982A JP H0127798 B2 JPH0127798 B2 JP H0127798B2
- Authority
- JP
- Japan
- Prior art keywords
- energy
- heavy oil
- terms
- liquid
- concentrated
- 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
Links
- 239000007788 liquid Substances 0.000 claims description 37
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 20
- 240000004808 Saccharomyces cerevisiae Species 0.000 claims description 13
- 238000000034 method Methods 0.000 claims description 13
- 238000000855 fermentation Methods 0.000 claims description 8
- 230000004151 fermentation Effects 0.000 claims description 8
- 238000000108 ultra-filtration Methods 0.000 claims description 8
- 239000002699 waste material Substances 0.000 claims description 8
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 claims description 6
- 239000012466 permeate Substances 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 5
- 238000005406 washing Methods 0.000 claims description 5
- 238000010411 cooking Methods 0.000 claims description 3
- 239000012528 membrane Substances 0.000 claims description 3
- 239000002351 wastewater Substances 0.000 claims 2
- 239000000295 fuel oil Substances 0.000 description 22
- 239000007787 solid Substances 0.000 description 18
- 235000000346 sugar Nutrition 0.000 description 14
- 239000012141 concentrate Substances 0.000 description 11
- 238000007796 conventional method Methods 0.000 description 11
- 238000011084 recovery Methods 0.000 description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 239000000047 product Substances 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 4
- RWSXRVCMGQZWBV-WDSKDSINSA-N glutathione Chemical compound OC(=O)[C@@H](N)CCC(=O)N[C@@H](CS)C(=O)NCC(O)=O RWSXRVCMGQZWBV-WDSKDSINSA-N 0.000 description 4
- 235000015097 nutrients Nutrition 0.000 description 4
- 241000222120 Candida <Saccharomycetales> Species 0.000 description 3
- 241000235646 Cyberlindnera jadinii Species 0.000 description 3
- 108010024636 Glutathione Proteins 0.000 description 2
- 229960003180 glutathione Drugs 0.000 description 2
- 229920002477 rna polymer Polymers 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004278 EU approved seasoning Substances 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 235000011194 food seasoning agent Nutrition 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 239000000825 pharmaceutical preparation Substances 0.000 description 1
- 229940127557 pharmaceutical product Drugs 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 150000008163 sugars Chemical class 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Landscapes
- Paper (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Treatment Of Sludge (AREA)
Description
【発明の詳細な説明】
本発明は亜硫酸パルプ排液（以下、SP排液と
称す）の濃縮、回収を効率良く行なう方法に係る
ものであり、特にSP排液中の糖分を炭素源とし
て酵母を生産する場合、通常の真空蒸発缶による
濃縮・回収ボイラーでの燃焼において排液の限外
過による濃縮をすることと、限外過透過液に
よつて酵母の生産により排出される排液（以下、
発酵軽液と称す）のメタン発酵処理とを組み合わ
せることによつて、エネルギー源としてのパルプ
廃液中の有機物を極めて有効に回収利用するため
に要する回収エネルギー費を大幅に低減する方法
に関するものである。Detailed Description of the Invention The present invention relates to a method for efficiently concentrating and recovering sulfite pulp effluent (hereinafter referred to as SP effluent). When producing yeast, it is necessary to concentrate the waste liquid by ultrafiltration during combustion in a concentration/recovery boiler using a normal vacuum evaporator, and to concentrate the waste liquid discharged from yeast production ( below,
This invention relates to a method for significantly reducing the energy recovery costs required for extremely effective recovery and utilization of organic matter in pulp waste liquid as an energy source by combining the process with methane fermentation treatment of fermented light liquid (referred to as fermented light liquid). .
現在、SP排液を用いて酵母を生産する場合に
は通常、発酵軽液を真空蒸発缶により濃縮した
後、回収ポイラーで燃焼している。またSP排液
を限外過して得られる透過液を利用する場合の
発酵軽液についても同様である。 Currently, when producing yeast using SP waste liquid, the fermented light liquid is usually concentrated in a vacuum evaporator and then combusted in a recovery boiler. The same applies to the fermentation light liquid when the permeate obtained by ultrafiltration of the SP effluent is used.
SP排液中の糖分を炭素源として酵母を生産し
得られた酵母より調味料の原料であるリボ核酸
を、また医薬品であるグルタチオンを抽出するこ
とは工業的規模において行なわれている。しかし
発酵軽液の真空蒸発缶による濃縮に要する蒸気費
の割合はリボ核酸またはグルタチオンの製造にお
いて極めて大きく、エネルギーコストが上昇して
いる今日、上記蒸気費を大幅に削減することは極
めて大きな意味を持つている。 Extracting ribonucleic acid, which is a raw material for seasonings, and glutathione, which is a pharmaceutical product, from the yeast produced by producing yeast using the sugar content in SP drainage fluid as a carbon source is carried out on an industrial scale. However, the steam cost required for concentrating fermented light liquid using a vacuum evaporator is extremely large in the production of ribonucleic acid or glutathione, and in today's world where energy costs are rising, significantly reducing the above steam cost is extremely significant. I have it.
本発明者等は嫌気的消化、所謂メタン発酵が天
然系有機廃棄物に利用出来ることに着目し鋭意検
討した結果、蒸解排液及び／または洗浄工程より
の希釈排液を限外過などの膜処理によつて濃縮
し、該濃縮液を真空蒸発缶によつて更に濃縮した
後、回収ボイラーで燃焼し、他方、限外過した
際の透過液を用いて酵母の生産を行ない、発酵軽
液をメタン発酵処理しエネルギーとして回収する
ことにより発酵軽液の濃縮蒸気費を大幅に削減し
得ることを確認し本発明法を開発したものであ
り、この点に特徴を有するものである。 The present inventors focused on the fact that anaerobic digestion, or so-called methane fermentation, can be used for natural organic waste, and as a result of intensive study, they discovered that the cooking waste and/or the diluted waste from the washing process can be processed through ultrafiltration or other membranes. After the concentrated liquid is further concentrated in a vacuum evaporator, it is burned in a recovery boiler, and the permeated liquid after ultrafiltration is used to produce yeast, and fermented light liquid is produced. The method of the present invention was developed after confirming that the cost of concentrating and steaming the fermented light liquid could be significantly reduced by subjecting it to methane fermentation treatment and recovering it as energy, and is unique in this respect.
以下、本発明方法を実施例によつて更に具体的
に説明する。 Hereinafter, the method of the present invention will be explained in more detail with reference to Examples.
実施例 １
(1) 従来法
Caベース亜硫酸パルプ製造工程より排出さ
れる固形分14％（以下、総べてＷ／Ｖ％を示
す）、還元糖５％を含む亜硫酸パルプ排液（以
下、Ca−SSLと称す）1000を培地としてカ
ンデイダ・ウテイリス（Candida utilis
IFO0626）を培養した。培養は培地に通常の栄
養剤を加え2000フアーメンターを用い通気撹
拌しながら行ない、残糖が２％となつた時点で
ストップした。培養液は遠心離機で酵母を分離
後、水800で洗浄し再び分離した。酵母を分
離した液は洗液と合わせて（以下、発酵軽液と
称す）1650であり、その固形分は6.7％であ
つた。Example 1 (1) Conventional method A sulfite pulp effluent (hereinafter referred to as Ca - Candida utilis (referred to as SSL) 1000 as a medium.
IFO0626) was cultured. Culture was carried out by adding ordinary nutrients to the medium and using a 2000 fermenter with aeration and stirring, and was stopped when the residual sugar content reached 2%. The yeast was separated from the culture solution using a centrifuge, washed with 800 g of water, and separated again. The liquid from which the yeast was separated, together with the washing liquid (hereinafter referred to as fermentation light liquid), weighed 1,650 ml, and its solid content was 6.7%.
従来法ではボイラーで燃焼するため発酵軽液
を総べて真空蒸発缶で固形分が53％になるまで
濃縮するので下記発酵軽液は1440の水を蒸気
する必要があつた。発酵軽液の濃縮に要するエ
ネルギーは重油換算で26であり、濃縮液を燃
焼して得られる回収エネルギーは重油換算で36
であつた。即ち回収エネルギーから濃縮エネ
ルギーを差引いた差引回収エネルギーは重油換
算で10であつた。 In the conventional method, the entire fermented light liquid is concentrated in a vacuum evaporator until the solid content reaches 53% in order to burn it in a boiler, so it was necessary to steam 1440 ml of water to produce the fermented light liquid below. The energy required to concentrate fermented light liquid is 26 in terms of heavy oil, and the energy recovered by burning the concentrated liquid is 36 in terms of heavy oil.
It was hot. In other words, the subtractive recovery energy obtained by subtracting the concentration energy from the recovery energy was 10 in terms of heavy oil.
(2) 本発明法
(1)の従来法と全く同じ組成のCa−SSL1000
を用いた。先ずCa−SSL1000をPCI社製の
T6／Ｂ膜を用いた限外過法により1/2液量に
なるまで濃縮した。濃縮液（500）は固形分
18.5％で、このものを濃縮53％にまで濃縮し燃
焼するため真空蒸発缶で325の水を蒸発させ
た。この際使用した濃縮エネルギーは重油換算
で5.9、回収エネルギーは28.4で差引回収
エネルギーは22.5であつた。(2) Method of the present invention Ca-SSL1000 with exactly the same composition as the conventional method (1)
was used. First, use Ca-SSL1000 manufactured by PCI.
It was concentrated to 1/2 liquid volume by ultrafiltration using a T6/B membrane. Concentrate (500) is solid content
At 18.5%, 325 water was evaporated in a vacuum evaporator in order to concentrate this product to 53% and burn it. The concentration energy used at this time was 5.9 in terms of heavy oil, the recovery energy was 28.4, and the subtraction recovery energy was 22.5.
一方、透過液（500）は固形分8.8％、還元
糖4.7％で(1)の従来法と同様の方法でカンデイ
ダ・ウテイリスを残糖が1.7％になる迄培養し
た。透過液はCa−SSLに比べて清澄であるた
め酵母の洗浄水は少なくて済み発酵軽液は525
（固形分５％）であつた。発酵軽液は100
のメタン発酵槽で連続的に処理されメタンガス
1.7Nm3を得た。このものの燃焼エネルギーは
重油換算で1.5であつた。 On the other hand, the permeate (500) had a solid content of 8.8% and reducing sugars of 4.7%, and Candida uteilis was cultured in the same manner as the conventional method in (1) until the residual sugar was 1.7%. The permeate is clearer than Ca-SSL, so less water is needed for washing the yeast, and the fermentation light liquid is 525 ml.
(solid content 5%). Fermented light liquid is 100
Methane gas is continuously processed in a methane fermentation tank.
1.7 Nm 3 was obtained. The combustion energy of this product was 1.5 in terms of heavy oil.
本発明法による差引回収エネルギーは合わせ
て重油換算で24.0であつた。 The total net recovery energy by the method of the present invention was 24.0 in terms of heavy oil.
以下の結果から従来法に比べて本発明法は
Ca−SSL1000当り重油換算で14も余計に
エネルギーを回収出来た。なお消費電力量は従
来法より若干増加するが、差引き全体では回収
エネルギーには殆んど影響を与えなかつた。 The following results show that the method of the present invention is better than the conventional method.
An additional 14 times more energy was recovered in terms of heavy oil per 1000 Ca-SSLs. Note that although the amount of power consumed increased slightly compared to the conventional method, the overall subtraction had almost no effect on the recovered energy.
実施例 ２
Mg−ベース亜硫酸パルプ排液（以下、Mg−
SSLと称す）を用いた。使用したMg−SSLは固
形分13.3％、還元糖5.3％であつた。Example 2 Mg-based sulfite pulp effluent (hereinafter referred to as Mg-
(referred to as SSL). The Mg-SSL used had a solid content of 13.3% and a reducing sugar content of 5.3%.
従来法では通常の栄養剤を加えたMg−
SSL1000を用い実施例１における従来法(1)と同
様に残糖が２％になる迄カンデイダ・ウテイリス
（Candida utilis IFO0626）を培養し発酵軽液
1600を得た。発酵軽液の固形分は6.2％で、固
形分53％にまで濃縮するのに1413の水を蒸発さ
せねばならず、このために必要な濃縮エネルギー
は重油換算で25.5であつた。一方、回収エネル
ギーは重油換算で32.2であつたので差引回収エ
ネルギーは6.7であつた。 In the conventional method, Mg-
Candida utilis IFO0626 was cultured using SSL1000 in the same manner as the conventional method (1) in Example 1 until the residual sugar reached 2%, and the fermented light liquid was
Got 1600. The solid content of the fermented light liquid was 6.2%, and 1413 parts of water had to be evaporated to concentrate it to 53% solid content, and the concentration energy required for this was 25.5 parts in terms of heavy oil. On the other hand, the recovered energy was 32.2 in terms of heavy oil, so the subtracted recovered energy was 6.7.
本発明法ではMg−SSL1000を先ず限外過
法（PCI社 T6／Ｂ使用）で液量を1/2.5にまで
濃縮した。濃縮液（400）は固形分20.7％で、
このものを濃縮53％にまで濃縮するには244の
水を蒸発させねばならず、このために必要な濃縮
エネルギーは重油換算で4.4であつた。回収エ
ネルギーは重油換算で26.9で差引き回収エネル
ギーは重油換算で22.5であつた。 In the method of the present invention, Mg-SSL1000 was first concentrated to 1/2.5 of its liquid volume by ultrafiltration (using PCI T6/B). Concentrate (400) has a solid content of 20.7%,
To concentrate this product to 53% concentration, 244 liters of water had to be evaporated, and the concentration energy required for this was 4.4 in terms of heavy oil. The recovered energy was 26.9 in terms of heavy oil, and the subtraction recovered energy was 22.5 in terms of heavy oil.
一方、透過液（600）は固形分8.4％、還元糖
５％であつた。之に通常の栄養剤を加え還元糖が
２％になる迄カンデイダ・ウテイリスを培養し発
酵軽液650を得た。発酵軽液を100のメタン発
酵槽で連続的に処理し1.9Nm3のメタンガスが得
られた。このものの燃焼エネルギーは重油換算で
1.7であつた。 On the other hand, the permeate (600) had a solid content of 8.4% and a reducing sugar content of 5%. A normal nutrient was added to this and Candida uteilis was cultured until the reducing sugar content was 2% to obtain fermented light liquid 650. The fermented light liquid was continuously treated in 100 methane fermenters and 1.9Nm 3 of methane gas was obtained. The combustion energy of this product is converted into heavy oil.
It was 1.7.
本発明法の差引回収エネルギーは重油換算で
24.2であり、従来法に比べて重油換算でMg−
SSL1000当り17.5の節約が出来た。 The energy recovered by the method of the present invention is calculated in terms of heavy oil.
24.2, which reduces Mg− in terms of heavy oil compared to the conventional method.
We were able to save 17.5 points per SSL1000.
実施例 ３
Caベース亜硫酸パルプ製造工程より排出され
る蒸解排液（固形分17.6％、還元糖6.4％）を洗
浄希釈排液（固形分1.5％、還元糖0.5％）で希釈
し、固形分15％、還元糖5.3％に調製した。培養
酵母はカンデイダ・ウテイリス（Candida utilis
IAM4220）を用いた。Example 3 Cooking effluent discharged from the Ca-based sulfite pulp manufacturing process (solid content 17.6%, reducing sugar 6.4%) was diluted with washing diluted effluent (solid content 1.5%, reducing sugar 0.5%) to reduce the solid content to 15%. %, and the reducing sugar content was adjusted to 5.3%. The cultured yeast is Candida utilis.
IAM4220) was used.
従来法ではCa−SSL1000に通常の栄養剤を
加え残糖が1.5％になる迄酵母を培養し実施例１
と同様に処理して発酵軽液1600を得た。発酵軽
液の固形分は6.7％で固形分53％にまで濃縮する
のに1400の水を蒸発させねばならない。このた
めに必要な濃縮エネルギーは重油換算で25.3で
あつた。また濃縮液を燃焼して得られる回収エネ
ルギーは重油換算で34.7であることから差引回
収エネルギーは9.4であつた。 In the conventional method, ordinary nutrients were added to Ca-SSL1000 and yeast was cultured until the residual sugar became 1.5%.
Fermented light liquid 1600 was obtained by processing in the same manner as above. The solids content of the fermented light liquid is 6.7%, and 1400 ml of water must be evaporated to concentrate it to 53% solids. The concentration energy required for this was 25.3 in terms of heavy oil. Furthermore, since the recovered energy obtained by burning the concentrate was 34.7 in terms of heavy oil, the subtracted recovered energy was 9.4.
本発明法では先ずCa−SSL（1000）を限外
過によつて液量を1/3にまで濃縮した。濃縮液
（333）は固形分26.7％で之を濃縮53％にまで濃
縮するのに必要な蒸発水量は165であつた。こ
のために必要な濃縮エネルギーは重油換算で3.0
であつた。また回収エネルギーは重油換算28.9
であつたので差引回収エネルギーは25.9であ
つた。 In the method of the present invention, first, Ca-SSL (1000) was concentrated to 1/3 of its liquid volume by ultrafiltration. The concentrated liquid (333) had a solid content of 26.7%, and the amount of evaporated water required to concentrate it to 53% was 165. The concentration energy required for this is 3.0 in terms of heavy oil.
It was hot. Also, the recovered energy is 28.9 in terms of heavy oil.
Therefore, the net recovery energy was 25.9.
一方、透過液（667）は固形分9.1％、還元糖
6.1％であつた。このものに通常の栄養剤を加え
還元糖が３％になるまでカンデイダ・ウテイリス
を培養し発酵軽液800（固形分4.5％）を得た。
発酵軽液を100容メタン発酵槽で連続的に処理
しメタンガス2.1Nm3を得た。このものの燃焼エ
ネルギーは重油換算で1.9であつた。 On the other hand, the permeate (667) has a solid content of 9.1% and reducing sugar.
It was 6.1%. A normal nutrient was added to this and Candida uteilis was cultured until the reducing sugar content was 3% to obtain fermented light liquid 800 (solid content 4.5%).
The fermented light liquid was continuously treated in a 100 volume methane fermenter to obtain methane gas of 2.1Nm3 . The combustion energy of this product was 1.9 in terms of heavy oil.
本発明法の差引回収エネルギーは重油換算で
27.8であり、従来法に比べて重油換算で18.4
の節約が出来た。 The energy recovered by the method of the present invention is calculated in terms of heavy oil.
27.8, which is 18.4 in terms of heavy oil compared to the conventional method.
I was able to save money.
Claims (1)
液及び／または洗浄工程よりの希釈排液を限外
過その他の膜処理により濃縮し、該濃縮液を更に
真空蒸発缶によつて濃縮した後、回収ボイラーで
燃焼し他方、限外過の透過液を用いて酵母の生
産を行ない、酵母生産を終えた排液をメタン発酵
処理してエネルギーとして回収することを特徴と
する亜硫酸パルプ排液の処理方法。1 The cooking waste liquid discharged from the sulfite pulp manufacturing process and/or the diluted waste liquid from the washing process is concentrated by ultrafiltration or other membrane treatment, and the concentrated liquid is further concentrated by a vacuum evaporator, and then recovered. A method for treating sulfite pulp wastewater, which is characterized by burning it in a boiler, producing yeast using the ultrafiltered permeate, and treating the wastewater after yeast production with methane fermentation to recover it as energy. .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57226229A JPS59115795A (en) | 1982-12-24 | 1982-12-24 | Treatment of waste liquid of pulp digester |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57226229A JPS59115795A (en) | 1982-12-24 | 1982-12-24 | Treatment of waste liquid of pulp digester |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS59115795A JPS59115795A (en) | 1984-07-04 |
| JPH0127798B2 true JPH0127798B2 (en) | 1989-05-30 |
Family
ID=16841914
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP57226229A Granted JPS59115795A (en) | 1982-12-24 | 1982-12-24 | Treatment of waste liquid of pulp digester |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS59115795A (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6250000A (en) * | 1985-08-26 | 1987-03-04 | Shimizu Constr Co Ltd | Methane fermentation treatment of evaporation condensate of waste water of pulp paper making |
| JPS62239983A (en) * | 1986-04-10 | 1987-10-20 | Nishihara Environ Sanit Res Corp | Cultivation of yeast with waste water |
| DE19600967C2 (en) * | 1996-01-12 | 1998-06-04 | Schweizer Electronic Ag | Process for the separation of organic process solutions originating from the production of printed circuit boards |
| AT408544B (en) * | 1996-02-12 | 2001-12-27 | Oebs Gmbh | METHOD FOR TREATING POLLUTED ALKALINE AQUEOUS CLEANING SOLUTIONS |
-
1982
- 1982-12-24 JP JP57226229A patent/JPS59115795A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS59115795A (en) | 1984-07-04 |
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