JP2002361237A - Method and device for treating waste water containing cod component - Google Patents
Method and device for treating waste water containing cod componentInfo
- Publication number
- JP2002361237A JP2002361237A JP2001174215A JP2001174215A JP2002361237A JP 2002361237 A JP2002361237 A JP 2002361237A JP 2001174215 A JP2001174215 A JP 2001174215A JP 2001174215 A JP2001174215 A JP 2001174215A JP 2002361237 A JP2002361237 A JP 2002361237A
- Authority
- JP
- Japan
- Prior art keywords
- oxidation reaction
- chemical oxidation
- high silica
- cod
- suspension
- 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.)
- Pending
Links
- 239000002351 wastewater Substances 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title abstract description 25
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 102
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 64
- 238000005273 aeration Methods 0.000 claims abstract description 55
- 239000000126 substance Substances 0.000 claims abstract description 54
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 54
- 239000000377 silicon dioxide Substances 0.000 claims abstract description 50
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 47
- 239000003463 adsorbent Substances 0.000 claims abstract description 46
- 239000012528 membrane Substances 0.000 claims abstract description 29
- 239000000725 suspension Substances 0.000 claims abstract description 26
- 230000003647 oxidation Effects 0.000 claims abstract description 17
- 238000000926 separation method Methods 0.000 claims abstract description 17
- 239000010419 fine particle Substances 0.000 claims abstract description 13
- 239000007788 liquid Substances 0.000 claims abstract description 3
- 238000002347 injection Methods 0.000 claims description 7
- 239000007924 injection Substances 0.000 claims description 7
- 238000005192 partition Methods 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 4
- 238000004065 wastewater treatment Methods 0.000 claims description 4
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 12
- 239000007789 gas Substances 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- -1 hydroxyl radicals Chemical class 0.000 description 5
- 244000005700 microbiome Species 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 3
- 239000000460 chlorine Substances 0.000 description 3
- 230000006866 deterioration Effects 0.000 description 3
- 150000002013 dioxins Chemical class 0.000 description 3
- 239000005416 organic matter Substances 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 2
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 2
- 229910004298 SiO 2 Inorganic materials 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000006065 biodegradation reaction Methods 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 238000005345 coagulation Methods 0.000 description 2
- 230000015271 coagulation Effects 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000012510 hollow fiber Substances 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000011941 photocatalyst Substances 0.000 description 2
- 230000000644 propagated effect Effects 0.000 description 2
- 150000003254 radicals Chemical class 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 230000001954 sterilising effect Effects 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- PUKLDDOGISCFCP-JSQCKWNTSA-N 21-Deoxycortisone Chemical compound C1CC2=CC(=O)CC[C@]2(C)[C@@H]2[C@@H]1[C@@H]1CC[C@@](C(=O)C)(O)[C@@]1(C)CC2=O PUKLDDOGISCFCP-JSQCKWNTSA-N 0.000 description 1
- QJZYHAIUNVAGQP-UHFFFAOYSA-N 3-nitrobicyclo[2.2.1]hept-5-ene-2,3-dicarboxylic acid Chemical compound C1C2C=CC1C(C(=O)O)C2(C(O)=O)[N+]([O-])=O QJZYHAIUNVAGQP-UHFFFAOYSA-N 0.000 description 1
- 102100032566 Carbonic anhydrase-related protein 10 Human genes 0.000 description 1
- FCYKAQOGGFGCMD-UHFFFAOYSA-N Fulvic acid Natural products O1C2=CC(O)=C(O)C(C(O)=O)=C2C(=O)C2=C1CC(C)(O)OC2 FCYKAQOGGFGCMD-UHFFFAOYSA-N 0.000 description 1
- 241000276457 Gadidae Species 0.000 description 1
- 101000867836 Homo sapiens Carbonic anhydrase-related protein 10 Proteins 0.000 description 1
- BOTDANWDWHJENH-UHFFFAOYSA-N Tetraethyl orthosilicate Chemical compound CCO[Si](OCC)(OCC)OCC BOTDANWDWHJENH-UHFFFAOYSA-N 0.000 description 1
- 238000005276 aerator Methods 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012013 faujasite Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 239000002509 fulvic acid Substances 0.000 description 1
- 229940095100 fulvic acid Drugs 0.000 description 1
- 239000002638 heterogeneous catalyst Substances 0.000 description 1
- 239000005556 hormone Substances 0.000 description 1
- 229940088597 hormone Drugs 0.000 description 1
- 239000004021 humic acid Substances 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 230000001678 irradiating effect Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 150000004045 organic chlorine compounds Chemical class 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 150000004760 silicates Chemical class 0.000 description 1
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- 239000000979 synthetic dye Substances 0.000 description 1
- 239000004408 titanium dioxide Substances 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Water Treatment By Sorption (AREA)
- Biological Treatment Of Waste Water (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、各種難生物分解性
ＣＯＤ成分を含む各種排水の処理方法及び装置に関す
る。各種難生物分解性ＣＯＤ成分とは、通常の生物処理
単独では除去効果が少ない化学的に酸化し得る有機物を
意味する。難生物分解性ＣＯＤ成分としては、フミン
酸、フルボ酸などの水を黄色に着色させる有機物質、ダ
イオキシンなどの各種有機塩素化合物、農薬類、合成染
料、有機性環境ホルモン物質などをいう。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and an apparatus for treating various wastewater containing various biodegradable COD components. The various hardly biodegradable COD components mean organic substances that can be chemically oxidized and have little removal effect by ordinary biological treatment alone. Examples of the hardly biodegradable COD component include organic substances such as humic acid and fulvic acid, which color water in yellow, various organic chlorine compounds such as dioxin, pesticides, synthetic dyes, and organic environmental hormone substances.
【０００２】[0002]
【従来の技術】従来、難生物分解性ＣＯＤ成分を排水か
ら除去するための処理方法としては、凝集沈殿法、活性
炭吸着法、フェントン酸化法、促進酸化反応法が知られ
ている。なお、促進酸化反応法とは、オゾン、紫外線、
過酸化水素のうち少なくとも２種類以上を組み合わせ
て、ヒドロキシラジカルを発生させて有機化合物を酸化
分解する方法、及び光触媒を利用する光化学酸化法をい
う。2. Description of the Related Art Conventionally, a coagulation sedimentation method, an activated carbon adsorption method, a Fenton oxidation method, and an accelerated oxidation reaction method have been known as treatment methods for removing hardly biodegradable COD components from wastewater. In addition, the accelerated oxidation reaction method includes ozone, ultraviolet light,
It refers to a method in which at least two or more kinds of hydrogen peroxide are combined to generate hydroxyl radicals to oxidatively decompose an organic compound, and a photochemical oxidation method using a photocatalyst.
【０００３】[0003]
【発明が解決しようとする課題】上述したような、難生
物分解性ＣＯＤ含有排水の従来技術による処理では、次
の問題点がある。すなわち、凝集沈殿法、フェントン酸
化法は、大量の汚泥が発生し、汚泥中に有害物質が蓄積
される。活性炭吸着法は、活性炭の再生操作が非常に面
倒である。促進酸化反応法は、処理コストが非常に高
く、所要装置容積も大きい。光触媒を用いる光化学酸化
法は、紫外線照射コストが非常に高額になり、実用性が
少ない。本発明は、上述した問題点を解決し、難生物分
解性ＣＯＤ含有水について、難生物分解性ＣＯＤ成分を
効率よくかつ低コストで除去できる方法と、装置を提供
することを課題とする。The above-mentioned conventional treatment of the wastewater containing a hardly biodegradable COD as described above has the following problems. That is, in the coagulation sedimentation method and the Fenton oxidation method, a large amount of sludge is generated, and harmful substances are accumulated in the sludge. In the activated carbon adsorption method, the operation of regenerating activated carbon is very troublesome. The accelerated oxidation reaction method has a very high processing cost and requires a large equipment volume. The photochemical oxidation method using a photocatalyst has a very high ultraviolet irradiation cost and is less practical. An object of the present invention is to solve the above-mentioned problems and to provide a method and an apparatus capable of efficiently removing a biodegradable COD component from water containing a biodegradable COD efficiently and at low cost.
【０００４】[0004]
【課題を解決するための手段】本発明者等は、上記の課
題を解決すべく研究した結果、微粒子状高シリカ吸着剤
が懸濁流動している曝気域（以下「懸濁流動曝気域」、
あるいは単に「曝気域」という）で難生物分解性ＣＯＤ
成分を高シリカ吸着剤に吸着させ、次いでこれを化学酸
化反応域に供給し、高シリカ吸着剤にオゾンを吸着し、
必要に応じてこれに紫外線か過酸化水素を作用させる
と、難生物分解性ＣＯＤ成分が分解して低分子化し生分
解性が向上するので、これを再び曝気域に戻してやれ
ば、ＣＯＤ成分が効率的に生物分解を受け除去できるこ
とを見出し、この知見に基づき、本発明を完成するに至
った。The present inventors have studied to solve the above-mentioned problems, and as a result, have found that an aeration zone in which the particulate high silica adsorbent is in a suspended flow (hereinafter referred to as a “suspended-flow aeration zone”). ,
Or simply referred to as “aeration zone”) and difficult biodegradable COD
The components are adsorbed on a high silica adsorbent, which is then supplied to a chemical oxidation reaction zone, where ozone is adsorbed on the high silica adsorbent,
When ultraviolet rays or hydrogen peroxide is applied to this as required, the hardly biodegradable COD component is decomposed to lower molecular weight and biodegradability is improved. If this is returned to the aeration zone again, the COD component will be reduced. The present inventors have found that biodegradation can be efficiently received and removed, and based on this finding, have completed the present invention.
【０００５】すなわち、本発明は次の構成からなるもの
である。 （１）高シリカ吸着材微粒子の好気性懸濁流動部と膜分
離部を持つ懸濁流動曝気域内でＣＯＤ含有排水を生物処
理し、該生物処理された高シリカ吸着材微粒子の懸濁水
の一部を化学酸化反応域に供給し、該化学酸化反応域か
らの処理液を前記高シリカ吸着材微粒子の懸濁流動曝気
域に返送し、該膜分離部からの膜透過水を処理水として
得ることを特徴とするＣＯＤ含有排水処理方法。 （２）前記化学酸化反応域が、オゾン酸化又はオゾンを
併用する促進酸化処理を行う槽であることを特徴とする
前記（１）記載のＣＯＤ含有排水処理方法。That is, the present invention has the following configuration. (1) COD-containing wastewater is biologically treated in a suspension-flow aeration zone having an aerobic suspension-flow portion and a membrane separation portion of the high silica adsorbent fine particles, and one of the suspended water of the biotreated high silica adsorbent fine particles Is supplied to the chemical oxidation reaction zone, and the processing liquid from the chemical oxidation reaction zone is returned to the suspension flow aeration zone of the high silica adsorbent fine particles to obtain the permeated water from the membrane separation unit as the treated water. COD-containing wastewater treatment method characterized by the above-mentioned. (2) The COD-containing wastewater treatment method according to (1), wherein the chemical oxidation reaction zone is a tank for performing ozone oxidation or accelerated oxidation using ozone together.
【０００６】（３）膜分離部を浸漬した高シリカ吸着剤
微粒子の好気性懸濁流動曝気槽と化学酸化反応槽より構
成され、前記好気性流動曝気槽がＣＯＤ含有排水の導入
管、化学酸化反応槽への循環装置及び散気装置を槽底部
に有し、前記膜分離部がろ過水を系外へ排出する処理水
排出管を具備し、前記化学酸化反応槽が少なくともオゾ
ンガス注入手段を備えていることを特徴とするＣＯＤ含
有排水の処理装置。 （４）ＣＯＤ含有排水の導入管を具備した高シリカ吸着
剤微粒子の好気性懸濁流動曝気槽が仕切り板によって膜
分離部が浸漬された曝気部と化学酸化反応部とに区画さ
れ、かつ曝気部と化学酸化反応部とは仕切り板の上下で
連通しており、前記曝気部に散気装置を設け、化学酸化
反応部にオゾンガス注入管を設置し、前記膜分離部がろ
過水を系外へ排出する処理水排出管を具備したことを特
徴とするＣＯＤ含有排水の処理装置。(3) An aerobic suspension flow aeration tank of high silica adsorbent fine particles immersed in the membrane separation section and a chemical oxidation reaction tank, wherein the aerobic flow aeration tank is an introduction pipe for COD-containing wastewater, and a chemical oxidation reaction tank. A circulation device and a diffuser for the reaction tank are provided at the bottom of the tank, the membrane separation unit is provided with a treated water discharge pipe for discharging filtered water out of the system, and the chemical oxidation reaction tank is provided with at least an ozone gas injection means. An apparatus for treating COD-containing wastewater, comprising: (4) An aerobic suspension-flow aeration tank of high silica adsorbent fine particles having a COD-containing wastewater inlet pipe is partitioned by a partition plate into an aeration section in which a membrane separation section is immersed and a chemical oxidation reaction section, and aeration. The part and the chemical oxidation reaction part communicate with each other at the top and bottom of the partition plate, a diffuser is provided in the aeration part, an ozone gas injection pipe is installed in the chemical oxidation reaction part, and the membrane separation part filters the filtered water out of the system. An apparatus for treating COD-containing wastewater, comprising a treated water discharge pipe for discharging wastewater to a COD.
【０００７】[0007]
【発明の実施の形態】以下に、本発明の実施の形態を図
面に基づいて詳細に説明する。なお、本発明方法の具体
化においては、懸濁流動曝気域と化学酸化反応域とは別
の槽としてもよく、また一つの槽内に形成するようにし
てもよい。本発明の実施形態の一例を図１に示す。図１
は懸濁流動曝気域と化学酸化反応域とを別の槽に形成し
た場合の例である。難生物分解性ＣＯＤ含有排水（原
水）１を、粉末ないし微粒子状の高シリカ吸着材が懸濁
流動している懸濁流動曝気槽２に供給し、難生物分解性
ＣＯＤ成分を高シリカ吸着材に吸着させる。懸濁流動曝
気槽２には酸素含有ガス、例えば空気３を曝気ブロワ４
から供給し散気装置５から散気して好気性状態にし、好
気性微生物を増殖させる。懸濁流動曝気槽２には中空
糸、平膜などの分離膜からなるろ過体６が浸漬されてい
る。Embodiments of the present invention will be described below in detail with reference to the drawings. In the embodiment of the method of the present invention, the suspension flow aeration zone and the chemical oxidation reaction zone may be provided in separate tanks or may be formed in one tank. FIG. 1 shows an example of an embodiment of the present invention. FIG.
Is an example in which a suspension flow aeration zone and a chemical oxidation reaction zone are formed in separate tanks. The wastewater (raw water) 1 containing the hardly biodegradable COD is supplied to a suspended fluidized aeration tank 2 in which a powdery or finely particulate high silica adsorbent is suspended and fluidized, and the hardly biodegradable COD component is supplied to the high silica adsorbent. To be absorbed. The suspension-flow aeration tank 2 is supplied with an oxygen-containing gas, for example, air 3 by an aeration blower 4.
From the air diffuser 5 to make the aerobic state, and aerobic microorganisms are proliferated. A filter 6 made of a separation membrane such as a hollow fiber or a flat membrane is immersed in the suspension fluidized aeration tank 2.
【０００８】次に、懸濁流動曝気槽２から高シリカ吸着
材懸濁水７をポンプ８で引抜いて、オゾン９単独又はオ
ゾン９を併用する化学酸化反応槽１０に供給し、高シリ
カ吸着材共存下で化学酸化処理する。さらに、化学酸化
反応槽１０から化学酸化処理水（高シリカ吸着材が共存
している）１１を再び懸濁流動曝気槽２に戻す。曝気槽
２には好気性微生物が存在しているので、化学酸化処理
によって低分子化し、生物分解性が向上したＣＯＤ成分
が生物分解を受け除去される。懸濁流動曝気槽２におけ
る高シリカ吸着材の濃度は、１０００〜１００００ｍｇ
／リットル程度が好ましい。Next, the high silica adsorbent suspension water 7 is withdrawn from the suspension fluidized aeration tank 2 by the pump 8 and supplied to the chemical oxidation reaction tank 10 using ozone 9 alone or in combination with the ozone 9 to coexist with the high silica adsorbent. Under the chemical oxidation treatment. Furthermore, the chemically oxidized water (having a high silica adsorbent) 11 is returned from the chemical oxidation reaction tank 10 to the suspended fluidized aeration tank 2 again. Since aerobic microorganisms are present in the aeration tank 2, the COD component which has been degraded by chemical oxidation treatment and has improved biodegradability is subjected to biodegradation and removed. The concentration of the high silica adsorbent in the suspension fluidized aeration tank 2 is 1,000 to 10,000 mg.
Per liter is preferred.
【０００９】難生物分解性ＣＯＤ成分とオゾン９を吸着
する高シリカ吸着材の例としては、高シリカペンタシル
ゼオライト（シリカライト又はＳｉＯ2 ／Ａｌ2 Ｏ3
比が高いＺＳＭ−５）、脱アルミニウムフォージャサ
イト（超安定Ｙ型ゼオライト：ＵＳＹ）、及びメソポー
ラスシリケート（ＭＣＭ−４１、ＦＳＭ−１６、テトラ
エトキシシランをシリカ源とする低温酸性合成メソポー
ラスシリケート、又は低分子ケイ酸をシリカ源とする低
温酸性合成メソポーラスシリケートなど）などの高シリ
カ吸着剤を挙げることができる。本発明において使用す
る高シリカ吸着材は、曝気水流によって容易に流動し、
ポンプ移送が容易な粉末状又は微粒子状であることが重
要である。高シリカ吸着材の粒径の範囲は、０．１μｍ
〜１ｍｍがよく、好ましくは０．５μｍ〜０．１ｍｍで
ある。粒径が数ｍｍ以上のものは、曝気によって流動し
難く、配管につまり易く、ポンプ移送が難しいので避け
るべきである。また、高シリカ吸着材細孔径は、約６〜
８オングストロームであることが望ましい。Examples of the high silica adsorbent for adsorbing the biodegradable COD component and ozone 9 include high silica pentasil zeolite (silicalite or SiO 2 / Al 2 O 3).
Low-temperature acidic synthetic mesoporous silicate using silica as a source of ZSM-5), dealuminated faujasite (ultrastable Y-type zeolite: USY), and mesoporous silicate (MCM-41, FSM-16, tetraethoxysilane), or And high silica adsorbents such as low-temperature acidic synthetic mesoporous silicates using low molecular silicic acid as a silica source. The high silica adsorbent used in the present invention flows easily by the aerated water flow,
It is important that the powder or particulate form is easy to pump. The range of the particle size of the high silica adsorbent is 0.1 μm
To 1 mm, preferably 0.5 μm to 0.1 mm. Particles having a particle size of several mm or more should be avoided because they hardly flow due to aeration, are easily clogged with piping, and are difficult to pump. The pore size of the high silica adsorbent is about 6 to
Preferably, it is 8 Å.
【００１０】懸濁流動曝気槽２内に設置されている中空
糸膜、平膜などの分離膜を用いたろ過体６により、高シ
リカ吸着材、微生物、及び原水に含まれていたＳＳをろ
過し、極めて清澄な膜ろ過水（処理水）１２を得る。化
学酸化反応には、酸化剤を用いるが、酸化力が強力でか
つ水に有害な物質を残さない点で、オゾンを用いること
が好ましい。さらに、その化学酸化反応を強力にするた
めには促進酸化処理方法を用いることができる。促進酸
化処理方法としては、オゾンガス９と紫外線と過酸化水
素のうちのいずれか２つ以上の組合せの反応によって、
ヒドロキシラジカルなどの活性酸素を発生させる方法を
挙げることができる。鉄イオンなどの均一触媒、二酸化
チタン、鉄酸化物に代表される金属酸化物などの不均一
触媒を併用しても良い。化学酸化反応槽１０は、オゾン
注入手段単独、またはオゾン注入手段に加えてＵＶラン
プまたは過酸化水素注入手段を備えるものを挙げること
ができる。オゾン９を注入する槽と紫外線照射を行う槽
を分ける場合は、化学酸化反応槽１０は複数の槽から構
成されていても良い。[0010] A filter 6 using a separation membrane such as a hollow fiber membrane or a flat membrane installed in the suspension fluidized aeration tank 2 filters high silica adsorbent, microorganisms, and SS contained in raw water. Then, extremely clear membrane filtered water (treated water) 12 is obtained. An oxidizing agent is used in the chemical oxidation reaction, but it is preferable to use ozone because it has strong oxidizing power and does not leave harmful substances in water. Further, in order to strengthen the chemical oxidation reaction, an accelerated oxidation treatment method can be used. As the accelerated oxidation treatment method, the reaction of a combination of two or more of ozone gas 9, ultraviolet light, and hydrogen peroxide,
A method for generating active oxygen such as a hydroxy radical can be given. A heterogeneous catalyst such as a uniform catalyst such as iron ions and a metal oxide represented by titanium dioxide and iron oxide may be used in combination. The chemical oxidation reaction tank 10 may be a tank provided with a UV lamp or hydrogen peroxide injection means in addition to the ozone injection means alone or in addition to the ozone injection means. When the tank for injecting ozone 9 and the tank for irradiating ultraviolet rays are separated, the chemical oxidation reaction tank 10 may be composed of a plurality of tanks.
【００１１】懸濁流動曝気槽２と化学酸化反応槽１０の
間の循環水量は、水循環率［循環水量（ｍ3 ／ｄａｙ）
／曝気槽容積（ｍ3 ）］として、少なくとも０．５ｄａ
ｙ-1以上とするのがよい。化学酸化反応槽１０の滞留時
間は短い方が良く、少なくとも０．５ｈｒ以下、好まし
くは０．２５ｈｒ以下とするのがよい。膜は、透過水フ
ラックスの確保および維持管理性の容易さの観点から、
孔径がサブミクロンオーダーであるＭＦ膜であることが
好ましい。原水１は、はじめに化学酸化反応槽１０に流
入させても構わない。The amount of circulating water between the suspension fluidized aeration tank 2 and the chemical oxidation reaction tank 10 is determined by the water circulation rate [circulating water amount (m 3 / day)
/ Aeration tank volume (m 3 )] at least 0.5 da
It is better to be y- 1 or more. The shorter the residence time of the chemical oxidation reactor 10 is, the better it is, at least 0.5 hr or less, preferably 0.25 hr or less. From the viewpoint of securing of permeate flux and ease of maintenance,
It is preferable that the MF film has a pore size on the order of submicron. The raw water 1 may first flow into the chemical oxidation reaction tank 10.
【００１２】本発明における実施例の別の形態を、図２
に示す。なお、図１で示した部分と同一部分は同一符号
を用いて示す。この例は、図１の懸濁流動曝気槽２及び
化学酸化反応槽１０の代わりに、一つの処理槽１３内に
仕切り板１４で区画して懸濁流動部１５と化学酸化反応
部１６を設けたものである。図２では、懸濁流動部１５
では散気装置５から散気される空気により高シリカ吸着
材粒子が水中で懸濁流動している。化学酸化反応部１６
ではその下部から供給されるオゾン９のガスにより懸濁
水が図２に示すように上昇して、懸濁流動部１５と化学
酸化反応部１６に水が循環される。この装置では、一つ
の槽ですみ、かつポンプ８や循環用の配管を要しない
で、図１の懸濁流動曝気槽２と化学酸化反応槽１０との
場合と同様の作用が行われる。Another embodiment of the present invention is shown in FIG.
Shown in The same parts as those shown in FIG. 1 are denoted by the same reference numerals. In this example, instead of the suspension flow aeration tank 2 and the chemical oxidation reaction tank 10 of FIG. 1, a suspension flow section 15 and a chemical oxidation reaction section 16 are provided in one processing tank 13 by partitioning with a partition plate 14. It is a thing. In FIG. 2, the suspension flow section 15
In this case, the high silica adsorbent particles are suspended and flow in water due to the air diffused from the diffuser 5. Chemical oxidation reaction section 16
In this case, the suspended water rises as shown in FIG. 2 by the gas of ozone 9 supplied from below, and the water is circulated to the suspended flow section 15 and the chemical oxidation reaction section 16. In this apparatus, the same operation as in the case of the suspension fluidized aeration tank 2 and the chemical oxidation reaction tank 10 in FIG.
【００１３】本発明では、前記に示すような構成とする
ことにより、高シリカ吸着材にオゾンが吸着されるとと
もに、高シリカ吸着材に吸着されているＣＯＤ成分が吸
着オゾン又はオゾンと過酸化水素、オゾンと紫外線によ
って発生するラジカル種によって、効率よく酸化され低
分子化されて、生物分解性が向上する。また、一部のＣ
ＯＤは炭酸ガス、塩素イオン等に無機化される。In the present invention, by adopting the above-described structure, ozone is adsorbed on the high silica adsorbent, and COD adsorbed on the high silica adsorbent is adsorbed ozone or ozone and hydrogen peroxide. In addition, the radical species generated by ozone and ultraviolet light efficiently oxidize and reduce the molecular weight, thereby improving biodegradability. Also, some C
OD is mineralized into carbon dioxide, chlorine ions, and the like.
【００１４】生物分解性が向上した有機物は、懸濁流動
曝気槽の内部および高シリカ吸着剤の表面に繁殖した微
生物により生物学的に分解することができ、ＣＯＤ分解
に要する酸化剤投入量、紫外線照射量などを低く抑える
ことができる。高シリカ吸着材はＣＯＤ成分も吸着する
ため、処理水ＣＯＤを低値で安定させることができる。
また、高シリカ吸着材表面では、オゾン濃度およびＣＯ
Ｄ濃度共に高くなるので反応効率が向上する。さらに、
オゾンによる排水の殺菌効果も得られる。なお、高シリ
カ吸着材は、無機物であるためオゾンによる劣化は殆ど
生じない。また、オゾンが高シリカ吸着材表面に吸着さ
れるため、水中の溶存オゾン濃度が低下し、溶存オゾン
による懸濁流動曝気槽および同曝気槽内のろ過体の膜劣
化を防ぐことができる。The organic matter having improved biodegradability can be biologically decomposed by microorganisms propagated inside the suspension fluidized aeration tank and on the surface of the high silica adsorbent. It is possible to reduce the amount of ultraviolet irradiation and the like. Since the high silica adsorbent also adsorbs the COD component, the treated water COD can be stabilized at a low value.
On the surface of the high silica adsorbent, the ozone concentration and CO
Since the D concentration increases, the reaction efficiency improves. further,
Ozone also has a sterilizing effect on wastewater. Since the high silica adsorbent is an inorganic substance, it hardly deteriorates due to ozone. In addition, since ozone is adsorbed on the surface of the high silica adsorbent, the concentration of dissolved ozone in the water is reduced, and it is possible to prevent membrane deterioration of the suspended flow aeration tank and the filter in the aeration tank due to the dissolved ozone.
【００１５】[0015]
【実施例】以下に本発明の実施例の一例を示すが、本発
明はこの実施例により限定されるものではない。DESCRIPTION OF THE PREFERRED EMBODIMENTS An embodiment of the present invention will be described below, but the present invention is not limited to this embodiment.
【００１６】実施例１ 図１に示すフローにより、難生物分解性ＣＯＤ含有排水
としてダイオキシン類含有排水の処理を行った。懸濁流
動曝気槽容積は６ｍ3 であった。前記曝気槽にはシリカ
ライト粉末を前記排水に５０００ｍｇ／リットルになる
ように投入した。前記曝気槽には分離膜が孔径０．４ミ
クロンのＭＦ膜であり、膜面積は１６０ｍ2 としたろ過
体を浸漬して、液圧式でろ過水を取り出した。シリカラ
イト粉末は、組成がＳｉＯ2 対Ａｌ2 Ｏ3 のモル比
が５０：１の高シリカであるシリカ・アルミナで、平均
粒径が２μｍのものであり、曝気によって容易に流動し
た。Example 1 According to the flow shown in FIG. 1, dioxin-containing wastewater was treated as the hardly biodegradable COD-containing wastewater. The volume of the suspension flow aeration tank was 6 m 3 . Silicalite powder was introduced into the aeration tank so as to be 5000 mg / liter in the wastewater. In the aeration tank, a filtration membrane having a pore size of 0.4 μm and a membrane area of 160 m 2 was immersed in a filtration membrane, and filtered water was taken out by a hydraulic system. The silicalite powder was silica-alumina, a high silica having a composition of SiO 2 to Al 2 O 3 having a molar ratio of 50: 1, an average particle size of 2 μm, and easily flowed by aeration.
【００１７】化学酸化反応槽は容量８０リットルのもの
を使用した。化学酸化処理は、オゾンと紫外線を組み合
わせる方法であり、オゾンガス流量は４リットル／ｍｉ
ｎ、オゾンガス濃度は３０ｍｇ／リットルとした。ま
た、紫外線ランプは、入力電力１００Ｗの低圧水銀ラン
プを用いた。曝気槽と化学酸化反応槽の循環水量は、１
０００リットル／ｈｒとした。この場合における水循環
率は約４ｄａｙ-1、促進酸化反応槽の滞留時間は約５分
であった。第１表にダイオキシン類含有排水の水質およ
び水量を示す。The chemical oxidation reaction tank used had a capacity of 80 liters. The chemical oxidation treatment is a method in which ozone and ultraviolet light are combined, and the flow rate of ozone gas is 4 liter / mi.
n, the ozone gas concentration was 30 mg / liter. A low-pressure mercury lamp having an input power of 100 W was used as the ultraviolet lamp. The amount of circulating water in the aeration tank and the chemical oxidation reaction tank is 1
000 liter / hr. In this case, the water circulation rate was about 4 day -1 , and the residence time in the accelerated oxidation reaction tank was about 5 minutes. Table 1 shows the water quality and amount of dioxin-containing wastewater.
【００１８】該排水を原水として処理運転を行ったとこ
ろ、処理水である膜透過水のダイオキシン類濃度は１ｐ
ｇ−ＴＥＱ／リットル以下、ＣＯＤは２ｍｇ／リットル
以下、ＢＯＤは３ｍｇ／リットル以下で定常的に安定し
た。また、曝気槽のダイオキシン類濃度も、運転初期は
徐々に上昇したが、その後は１５０ｐｇ−ＴＥＱ／リッ
トルで定常化した。When the wastewater was used as raw water for a treatment operation, the concentration of dioxins in the permeated water of the treated water was 1 p.
g-TEQ / liter or less, COD was 2 mg / liter or less, and BOD was 3 mg / liter or less, and was constantly stabilized. In addition, the concentration of dioxins in the aeration tank gradually increased in the initial stage of the operation, but thereafter became steady at 150 pg-TEQ / liter.
【００１９】[0019]
【表１】 [Table 1]
【００２０】比較例１ 比較例として、高シリカ吸着材を懸濁流動曝気槽に投入
しないこと以外は、実施例１と同条件で運転を行った。
この場合、運転初期においては、処理水である膜透過水
のダイオキシン類濃度は１〜５ｐｇ−ＴＥＱ／リット
ル、ＣＯＤは２〜５ｍｇ／リットル、ＢＯＤは５〜８ｍ
ｇ／リットルであり、本発明による実施例１に比べて高
かった。しかも、膜が溶存オゾンにより損傷し運転の安
定継続は不可能であった。Comparative Example 1 As a comparative example, the operation was performed under the same conditions as in Example 1 except that the high silica adsorbent was not charged into the suspension fluidized aeration tank.
In this case, in the initial stage of operation, the concentration of dioxins in the membrane permeated water as the treated water is 1 to 5 pg-TEQ / liter, COD is 2 to 5 mg / liter, and BOD is 5 to 8 m.
g / liter, which was higher than that of Example 1 according to the present invention. Moreover, the membrane was damaged by the dissolved ozone, and it was impossible to continue the operation stably.
【００２１】以上により、高シリカ吸着材を懸濁流動曝
気槽に投入することにより、オゾンによる高シリカ吸着
剤の劣化および水中有機物膜の損傷防止、および処理水
質の高度化が達成できることが示された。As described above, it is shown that by introducing a high silica adsorbent into a suspension fluidized aeration tank, it is possible to prevent deterioration of the high silica adsorbent due to ozone, prevent damage to organic matter films in water, and enhance the quality of treated water. Was.
【００２２】[0022]
【発明の効果】本発明によれば、前記に示すような構成
とすることにより、化学酸化反応において高シリカ吸着
材にオゾンが吸着されるとともに、高シリカ吸着材に吸
着されているＣＯＤ成分が吸着オゾン又はオゾンと過酸
化水素、オゾンと紫外線によって発生するラジカル種に
よって、効率よく酸化され低分子化されることにより、
生物分解性が向上し、それによりＣＯＤ成分が減少した
処理水を得ることができる。また、一部のＣＯＤは炭酸
ガス、塩素イオン等に無機化される。According to the present invention, with the above-described structure, ozone is adsorbed on the high silica adsorbent in the chemical oxidation reaction, and the COD component adsorbed on the high silica adsorbent is eliminated. By radicals generated by adsorbed ozone or ozone and hydrogen peroxide, ozone and ultraviolet rays, it is efficiently oxidized and reduced in molecular weight,
Biodegradability is improved, and thereby treated water having a reduced COD component can be obtained. Further, some CODs are mineralized into carbon dioxide, chlorine ions, and the like.
【００２３】また、化学酸化反応において生物分解性が
向上した有機物は、懸濁流動曝気域に戻って同曝気域の
内部および高シリカ吸着材の表面に繁殖した微生物によ
り生物学的に分解することができるので、ＣＯＤ分解に
要する酸化剤投入量、紫外線照射量などを低く抑えるこ
とができる。高シリカ吸着材はＣＯＤ成分も吸着するた
め、高シリカ吸着材表面では、オゾン濃度およびＣＯＤ
濃度共に高くなるので反応効率が向上し、処理水のＣＯ
Ｄを低値で安定させることができる。さらに、オゾンに
よる排水の殺菌効果も得られる。また、高シリカ吸着材
は、無機物であるためオゾンによる劣化は殆ど生じな
い。オゾンが高シリカ吸着剤表面に吸着されるため、水
中の溶存オゾン濃度が低下し、溶存オゾンによる曝気域
内のろ過体を構成するの分離膜の劣化を防ぐことができ
る。Further, the organic matter having improved biodegradability in the chemical oxidation reaction returns to the suspension fluidized aeration zone and is biologically degraded by microorganisms propagated inside the aeration zone and on the surface of the high silica adsorbent. Therefore, the amount of the oxidizing agent required for COD decomposition, the amount of ultraviolet irradiation, and the like can be reduced. Since the high silica adsorbent also adsorbs COD components, the ozone concentration and COD
As the concentration increases, the reaction efficiency improves, and the CO
D can be stabilized at a low value. Furthermore, the sterilization effect of the wastewater by ozone is also obtained. In addition, since the high silica adsorbent is an inorganic substance, deterioration due to ozone hardly occurs. Since ozone is adsorbed on the surface of the high silica adsorbent, the concentration of dissolved ozone in water is reduced, and the degradation of the separation membrane constituting the filter in the aeration zone due to the dissolved ozone can be prevented.
【図１】本発明によるＣＯＤ含有排水の処理方法のフロ
ー図を示す。FIG. 1 shows a flowchart of a method for treating COD-containing wastewater according to the present invention.
【図２】本発明によるＣＯＤ含有排水の処理方法におけ
る別の一例を示すフロー図を示す。FIG. 2 is a flowchart showing another example of the method for treating COD-containing wastewater according to the present invention.
１ 難生物分解性ＣＯＤ含有排水（原水） ２ 懸濁流動曝気槽 ３ 空気 ４ 曝気ブロワ ５ 散気装置 ６ ろ過体 ７ 高シリカ吸着材懸濁水 ８ ポンプ ９ オゾン １０ 化学酸化反応槽 １１ 化学酸化処理水 １２ 処理水 １３ 処理槽 １４ 仕切り板 １５ 懸濁流動曝気部 １６ 化学酸化反応部 Reference Signs List 1 Wastewater (raw water) containing hardly biodegradable COD 2 Suspended fluidized aeration tank 3 Air 4 Aeration blower 5 Aerator 6 Filter 7 High silica adsorbent suspended water 8 Pump 9 Ozone 10 Chemical oxidation reaction tank 11 Chemical oxidation treatment water 12 treated water 13 treatment tank 14 partition plate 15 suspension flow aeration unit 16 chemical oxidation reaction unit
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ テーマコート゛(参考） Ｃ０２Ｆ 3/10 Ｃ０２Ｆ 3/10 Ａ Ｃ０７Ｄ 319/24 Ｃ０７Ｄ 319/24 (72)発明者 小林 琢也 東京都大田区羽田旭町11番１号 株式会社 荏原製作所内 (72)発明者 田中 俊博 東京都大田区羽田旭町11番１号 株式会社 荏原製作所内 Ｆターム(参考） 4D003 AA12 AB12 BA02 CA10 DA07 EA14 EA23 FA01 FA07 4D006 GA07 HA93 JA01 KB12 KB22 KB30 MA01 MA03 PB20 PC63 4D024 AA04 AB11 AB13 BA05 BA07 BB01 BC04 DA06 DA07 DB05 DB10 DB15 DB24 4D050 AA12 AB13 AB17 AB19 BB02 BB09 BC09 CA07 CA09 CA17──────────────────────────────────────────────────の Continued on the front page (51) Int.Cl. 7 Identification symbol FI Theme coat ゛ (Reference) C02F 3/10 C02F 3/10 A C07D 319/24 C07D 319/24 (72) Inventor Takuya Kobayashi Ota, Tokyo 11-1 Haneda Asahi-cho, Ward Inside Ebara Works Co., Ltd. (72) Inventor Toshihiro Tanaka 11-1 Haneda Asahi-cho, Ota-ku, Tokyo F-term inside Ebara Works 4D003 AA12 AB12 BA02 CA10 DA07 EA14 EA23 FA01 FA07 4D006 GA07 HA93 JA01 KB12 KB22 KB30 MA01 MA03 PB20 PC63 4D024 AA04 AB11 AB13 BA05 BA07 BB01 BC04 DA06 DA07 DB05 DB10 DB15 DB24 4D050 AA12 AB13 AB17 AB19 BB02 BB09 BC09 CA07 CA09 CA17
Claims (4)
部と膜分離部を持つ懸濁流動曝気域内でＣＯＤ含有排水
を生物処理し、該生物処理された高シリカ吸着材微粒子
の懸濁水の一部を化学酸化反応域に供給し、該化学酸化
反応域からの処理液を前記高シリカ吸着材微粒子の懸濁
流動曝気域に返送し、該膜分離部からの膜透過水を処理
水として得ることを特徴とするＣＯＤ含有排水処理方
法。A biological treatment of COD-containing wastewater in a suspension-flow aeration zone having an aerobic suspension-flow portion and a membrane separation portion of high silica adsorbent fine particles, and a suspension of the biotreated high silica adsorbent fine particles. Is supplied to the chemical oxidation reaction zone, the processing liquid from the chemical oxidation reaction zone is returned to the suspension flow aeration zone of the high silica adsorbent fine particles, and the membrane permeated water from the membrane separation section is treated water. COD-containing wastewater treatment method characterized in that it is obtained as:
オゾンを併用する促進酸化処理を行う域であることを特
徴とする請求項１記載のＣＯＤ含有排水処理方法。2. The COD-containing wastewater treatment method according to claim 1, wherein the chemical oxidation reaction zone is a zone for performing ozone oxidation or accelerated oxidation treatment using ozone together.
子の好気性懸濁流動曝気槽と化学酸化反応槽より構成さ
れ、前記好気性懸濁流動曝気槽がＣＯＤ含有排水の導入
管、化学酸化反応槽への循環装置及び散気装置を槽底部
に有し、前記膜分離部がろ過水を系外へ排出する処理水
排出管を具備し、前記化学酸化反応槽が少なくともオゾ
ンガス注入手段を備えていることを特徴とするＣＯＤ含
有排水の処理装置。3. An aerobic suspension-flow aeration tank of high silica adsorbent fine particles immersed in a membrane separation section and a chemical oxidation reaction tank, wherein the aerobic suspension-flow aeration tank is an inlet pipe for COD-containing wastewater, A circulation device and an air diffuser to the oxidation reaction tank are provided at the bottom of the tank, the membrane separation unit is provided with a treated water discharge pipe for discharging filtered water out of the system, and the chemical oxidation reaction tank has at least an ozone gas injection means. An apparatus for treating COD-containing wastewater, comprising:
リカ吸着剤微粒子の好気性懸濁流動曝気槽が仕切り板に
よって膜分離部が浸漬された曝気部と化学酸化反応部と
に区画され、かつ曝気部と化学酸化反応部とは仕切り板
の上下で連通しており、前記曝気部に散気装置を設け、
化学酸化反応部にオゾンガス注入管を設置し、前記膜分
離部がろ過水を系外へ排出する処理水排出管を具備した
ことを特徴とするＣＯＤ含有排水の処理装置。4. An aerobic suspension-flow aeration tank of high silica adsorbent fine particles having a COD-containing drainage inlet pipe is partitioned by a partition plate into an aeration section in which a membrane separation section is immersed and a chemical oxidation reaction section, And the aeration unit and the chemical oxidation reaction unit communicate with each other at the top and bottom of the partition plate, and provided with a diffuser in the aeration unit,
An apparatus for treating COD-containing wastewater, wherein an ozone gas injection pipe is provided in a chemical oxidation reaction section, and the membrane separation section is provided with a treated water discharge pipe for discharging filtered water out of the system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2001174215A JP2002361237A (en) | 2001-06-08 | 2001-06-08 | Method and device for treating waste water containing cod component |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2001174215A JP2002361237A (en) | 2001-06-08 | 2001-06-08 | Method and device for treating waste water containing cod component |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JP2002361237A true JP2002361237A (en) | 2002-12-17 |
Family
ID=19015532
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2001174215A Pending JP2002361237A (en) | 2001-06-08 | 2001-06-08 | Method and device for treating waste water containing cod component |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2002361237A (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008055312A (en) * | 2006-08-31 | 2008-03-13 | Kyuchaku Gijutsu Kogyo Kk | Method and apparatus for treating harmful component-containing liquid |
| JP2008508093A (en) * | 2004-08-04 | 2008-03-21 | ユー・エス・フィルター・ウェイストウォーター・グループ・インコーポレイテッド | Method for cleaning membranes and chemicals therefor |
| WO2010049971A1 (en) * | 2008-10-29 | 2010-05-06 | Asaoka Keiichiro | Apparatus for treating organic wastewater and method of treating organic wastewater |
| CN104193114A (en) * | 2014-09-18 | 2014-12-10 | 广东溢达纺织有限公司 | Sewage treatment method and sewage treatment system |
| WO2014196151A1 (en) * | 2013-06-03 | 2014-12-11 | パナソニックＩｐマネジメント株式会社 | Waste water treatment device |
| CN104386775A (en) * | 2014-10-27 | 2015-03-04 | 安徽农业大学 | Adsorption reactor with separated internal recycle combined membranes, and water treatment device |
| CN105565559A (en) * | 2016-01-18 | 2016-05-11 | 四川师范大学 | Technology for removing acidic high-concentration mercury-containing waste water |
| CN110272745A (en) * | 2019-07-04 | 2019-09-24 | 湖南科技大学 | A kind of humic acid heavy metal deactivator oxidation modification device and its application method |
| CN111392991A (en) * | 2020-05-20 | 2020-07-10 | 福建龙净环保股份有限公司 | An integrated sewage treatment device and sewage treatment method |
| CN113562899A (en) * | 2021-07-13 | 2021-10-29 | 华南理工大学 | A method for treating organic pollutants in water bodies |
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2001
- 2001-06-08 JP JP2001174215A patent/JP2002361237A/en active Pending
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008508093A (en) * | 2004-08-04 | 2008-03-21 | ユー・エス・フィルター・ウェイストウォーター・グループ・インコーポレイテッド | Method for cleaning membranes and chemicals therefor |
| JP2008055312A (en) * | 2006-08-31 | 2008-03-13 | Kyuchaku Gijutsu Kogyo Kk | Method and apparatus for treating harmful component-containing liquid |
| WO2010049971A1 (en) * | 2008-10-29 | 2010-05-06 | Asaoka Keiichiro | Apparatus for treating organic wastewater and method of treating organic wastewater |
| WO2014196151A1 (en) * | 2013-06-03 | 2014-12-11 | パナソニックＩｐマネジメント株式会社 | Waste water treatment device |
| JP2014233686A (en) * | 2013-06-03 | 2014-12-15 | パナソニック株式会社 | Effluent treatment apparatus |
| CN104193114A (en) * | 2014-09-18 | 2014-12-10 | 广东溢达纺织有限公司 | Sewage treatment method and sewage treatment system |
| CN104386775A (en) * | 2014-10-27 | 2015-03-04 | 安徽农业大学 | Adsorption reactor with separated internal recycle combined membranes, and water treatment device |
| CN105565559A (en) * | 2016-01-18 | 2016-05-11 | 四川师范大学 | Technology for removing acidic high-concentration mercury-containing waste water |
| CN105565559B (en) * | 2016-01-18 | 2018-02-02 | 四川师范大学 | A kind of technology for removing mercury in acidic high-strength mercury-containing waste water |
| CN110272745A (en) * | 2019-07-04 | 2019-09-24 | 湖南科技大学 | A kind of humic acid heavy metal deactivator oxidation modification device and its application method |
| CN111392991A (en) * | 2020-05-20 | 2020-07-10 | 福建龙净环保股份有限公司 | An integrated sewage treatment device and sewage treatment method |
| CN113562899A (en) * | 2021-07-13 | 2021-10-29 | 华南理工大学 | A method for treating organic pollutants in water bodies |
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