CN101274809B - Treatment apparatus for organic wastewater - Google Patents

Treatment apparatus for organic wastewater Download PDF

Info

Publication number
CN101274809B
CN101274809B CN 200810088041 CN200810088041A CN101274809B CN 101274809 B CN101274809 B CN 101274809B CN 200810088041 CN200810088041 CN 200810088041 CN 200810088041 A CN200810088041 A CN 200810088041A CN 101274809 B CN101274809 B CN 101274809B
Authority
CN
China
Prior art keywords
biological treatment
tank
water
separation
organic
Prior art date
Application number
CN 200810088041
Other languages
Chinese (zh)
Other versions
CN101274809A (en
Inventor
安池友时
山田聪
田中伦明
Original Assignee
栗田工业株式会社
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Priority to JP2007091666A priority Critical patent/JP5223219B2/en
Priority to JP2007-091666 priority
Application filed by 栗田工业株式会社 filed Critical 栗田工业株式会社
Publication of CN101274809A publication Critical patent/CN101274809A/en
Application granted granted Critical
Publication of CN101274809B publication Critical patent/CN101274809B/en

Links

Classifications

    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00Water conservation; Efficient water supply; Efficient water use
    • Y02A20/10Relating to general water supply, e.g. municipal or domestic water supply
    • Y02A20/208Off-grid powered water treatment
    • Y02A20/212Solar-powered wastewater sewage treatment, e.g. spray evaporation
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02WCLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00Technologies for wastewater treatment
    • Y02W10/10Biological treatment of water, waste water, or sewage
    • Y02W10/15Aerobic processes

Abstract

本发明的有机性排水的处理装置,在第1生物处理反应槽1中对有机性排水进行生物处理,在第1浮选槽2中对生物处理水无凝集地进行浮选分离。 Treatment of organic waste water according to the present invention, biological treatment of organic discharged in the first biological treatment tank reactor 1, in the first biological treatment tank 2 flotation water flotation separation performed without agglomeration. 在第2生物处理反应槽3、8中对第1浮选槽2的分离水进行生物处理之后,进行固液分离。 After separation of the aqueous flotation tank 2 of the first biological treatment in the second biological treatment tank reactor 3, 8, the solid-liquid separation. 即便对于第1生物处理反应槽的处理水中的微生物体无凝集地进行固液分离,只要是浮选分离方式,则可充分地将所述微生物体分离并去除,因不使用凝集剂,所以可避免产生第2段生物处理反应槽中的有机物负荷增加以及凝集剂析出这些问题,而且也可减小装置设置面积以及曝气量。 Even for microorganisms in the treated water in the first biological treatment tank without agglutination reaction to solid-liquid separation, as long as the flotation separation method, it can be sufficiently separated from the microorganisms and removed, because the coagulant is not used, it is possible paragraph avoid the second biological treatment tank to increase the organic load reaction and a flocculant precipitate these problems, and the device installation area can be reduced and the amount of aeration.

Description

有机性排水的处理装置 Treatment of organic waste water

技术领域 FIELD

[0001] 本发明涉及一种含有溶解性有机物的有机性排水的处理装置,特别是涉及一种下述有机性排水的处理装置,即,在设为2段的生物处理反应槽中对含有溶解性有机物的排水进行生物处理时,不仅可维持处理水的水质且减轻生物处理负荷,而且可减小装置设置面积。 [0001] The present invention relates to treatment of organic waste water containing dissolved organic matter, particularly relates to a processing apparatus following organic discharged, i.e., in two-stage biological treatment is set to a reaction vessel containing dissolved when drainage biologically treated organic substance, the treated water not only to maintain the quality and reduce the processing load on the biological and apparatus installation area can be reduced.

背景技术 Background technique

[0002] 在有机性排水的处理中,一般实施生物处理,具体来说是采用活性污泥法(activated sludge process)及生物膜法(biofilm process)。 [0002] In the processing of organic waste water, the biological treatment is generally embodiment, specifically, activated sludge (activated sludge process) and biofilm (biofilm process). 在此类生物处理中,近年来,为了减轻环境负荷或通过回收水来节水,需要进一步经过高度处理的处理水。 In such a biological treatment, in recent years, in order to reduce the environmental load or by recycling water saving, the need for further processing highly treated water.

[0003] 为了提高生物处理水的水质,以前提出一种将生物处理反应槽分割成多段的多段式生物处理装置(例如,日本专利特开昭55-28759号公报、日本专利特开2000-42584号公报)。 [0003] In order to improve water quality in the biologically treated water, previously proposed a method of processing a biological reaction tank into a plurality of multi-stage biological treatment apparatus (e.g., Japanese Patent Laid-Open Publication No. 55-28759, Japanese Patent Laid-Open 2000-42584 No. Gazette). 与I段式的生物处理装置相比,多段式的生物处理装置可获得水质更高的处理水。 Compared to the biological treatment stage I, the multi-stage biological treatment means a higher quality of the treated water can be obtained.

[0004] 然而,在仅将生物处理反应槽设为多段的常规的多段式生物处理装置中,可获得水质比I段式生物处理装置更高的处理水,但仍然存在需要较大的设置面积以及大量的曝气(aeration)这些问题。 [0004] However, in the conventional multi-stage biological treatment apparatus only the biological treatment tank to the multistage reaction, the obtained quality higher than the biological treatment stage I treated water, there are still requires a large installation area and plenty of aeration (aeration) these problems. 以下对其理由进行说明。 The reason will be explained below.

[0005] 也就是说,在第I段生物处理反应槽中所生成的微生物体流入到第2段生物处理反应槽内,而成为第2段生物处理反应槽的有机物负荷(organicloading),但在BOD (Biochemical Oxygen Demand,生化需氧量)低的第2段生物处理反应槽中,微生物体开始自我消化,溶析出已灭绝的微生物体的构成成分,引起水质恶化。 [0005] That is, in paragraph I microorganism biological treatment tank generated by the reaction flows into the biological treatment section of the reaction tank 2, paragraph organic load becomes the second biological treatment tank reactor (organicloading), but BOD (biochemical Oxygen Demand, BOD) in paragraph 2 low biological treatment reaction tank, the microorganisms begin to self-digestion, precipitation of soluble constituents of microorganisms extinct, causing deterioration of water quality. 已灭绝的微生物体的构成成分中包含胡敏素(humin)类等难分解性有机物,对这些难分解性有机物进行微生物式的分解时需要延长HRT (hydraulic retention time,水力滞留时间),且设置面积变宽。 Constituents extinct microorganisms contained humin (Humin) the like recalcitrant organics, we need to extend the HRT (hydraulic retention time, the hydraulic retention time) microbial formula decomposing these hardly decomposable organic substances, and the installation area becomes width.

[0006] 而且,第2生物处理反应槽中,因为氧化微生物体内积存物质,而消耗溶解氧(dissolved oxygen),所以使曝气动力加大。 [0006] Further, the second biological treatment tank reactor, since the microorganisms in the accumulation of oxidized material consumed dissolved oxygen (dissolved oxygen), so that the power increase aeration.

[0007] 对此,提出以下方案:在多段式生物处理装置中,对来自第I段生物处理反应槽的生物处理水进行凝集处理,在第2段生物处理反应槽中对经固液分离机构分离的分离水进行生物处理(日本专利特愿2005-360619)。 [0007] In this regard, the following scheme: In the multi-stage biological treatment, biological treatment of water from biological treatment Stage I reaction vessel agglutination process, treating the reaction vessel in paragraph 2 of the solid-liquid separation mechanism of biological a separator for separating biologically treated water (Japanese Patent Application No. 2005-360619).

[0008] 此方案中,对第I段生物处理反应槽的处理水进行凝集处理使其固液分离,以此来去除微生物体,由此,可降低第2段生物处理反应槽的有机物负荷,解决上述常规的多段式生物处理装置的问题。 [0008] In this embodiment, the process of Stage I water biological treatment tank agglutination reaction treated to solid-liquid separation, in order to remove microorganisms, thereby, paragraph 2 can be reduced organic load biological treatment reaction vessel, multi-stage biological treatment problem solving the above conventional apparatus.

[0009] 然而,日本专利特愿2005-360619所述的方案中,存在以下问题。 [0009] However, Japanese Patent No. 2005-360619 in the embodiment, the following problem.

[0010] 也就是说,第I段生物处理反应槽的处理水的凝集处理中,当使用无机凝集剂作为凝集剂时,在对处理水进行固液分离而得的分离水中残留有溶解金属盐,此溶解金属盐在第2段生物处理反应槽的污泥或散气管中析出。 [0010] That is, the aggregation processing of Stage I water biological treatment in the reaction tank, when an inorganic flocculant as flocculant in water, separating a solid-liquid separation of the treated water obtained by dissolving the metal salt remains this was dissolved in paragraph 2 metal salt deposited biological treatment or sludge reaction tank Powder trachea.

[0011] 因污泥中的金属盐析出,使污泥的比重增大,从而使曝气等搅拌时所需的动力增大。 [0011] The precipitated metal sludge because the specific gravity of the sludge is increased, so that the power required for stirring increases aeration and the like. 特别是,有载体(carrier)的流动床式的生物处理反应槽中,载体的比重变大,因此载体会堆积在反应槽下部,无法充分地流动。 In particular, there is a carrier (Carrier) of the fluidized bed biological treatment reaction vessel, the gravity of the carrier becomes large, the carrier will accumulate in the lower portion of the reaction vessel, can not flow sufficiently.

[0012] 而且,散气管中金属盐的析出,使得因曝气量降低而导致溶解氧不足,或者因差压(differential pressure)上升而导致曝气动力增大。 [0012] Further, in the diffuser tube precipitated metal salt, such that due to a decrease caused by insufficient aeration of dissolved oxygen, or due to differential pressure (differential pressure) rise caused by increased aeration power.

[0013] 有机凝集剂中的大多数具有生物难分解性,当有机凝集剂流入第2段生物处理反应槽中时,会附着在载体表面,所以会导致妨碍氧透过、或降低生物活性。 [0013] Most of the organic aggregating agent is a biologically non-biodegradable, the organic aggregating agent flows when paragraph biological treatment reaction tank 2, will be attached to the support surface, the oxygen permeability will lead to hinder or reduce the biological activity.

发明内容 SUMMARY

[0014] 因此,本发明的目的在于提供一种能够解决因如上的日本专利特愿2005-360619所述的多段式生物处理装置中的凝集处理所引起的问题的有机性排水的处理装置。 [0014] Accordingly, an object of the present invention is to provide a solution by the above Japanese Patent No. treatment of organic waste water flocculating multi-stage biological treatment apparatus according 2005-360619 are caused problems.

[0015] 本发明者等人,为了解决所述问题进行了潜心研究,结果发现:在第I段生物处理反应槽中分解了大部分溶解性有机物之后,对在此生物处理反应槽中生成的微生物体无凝集地进行固液分离,且进一步在第2段生物处理反应槽中对已将此微生物体分离出的分离水进行生物处理,这样,即使对微生物体无凝集地进行固液分离,只要是浮选分离方式,则可以充分地将所述微生物体分离去除,因不使用凝集剂,所以可避免产生第2段生物处理反应槽中的有机物负荷增加及凝集剂析出这些问题,而且可减小装置设置面积及曝气量。 [0015] The present inventors, in order to solve the problem of the intensive studies, and found that: after the Stage I reaction vessel biological treatment of most dissolved organic matter decomposition, the reaction of this biological treatment tank generated microorganisms aggregated manner without solid-liquid separation and further processing in the reaction vessel for separating biological paragraph 2 the water has separated this microorganism is biologically treated, so that, even when no agglutination of microorganisms to solid-liquid separation, as long as the flotation separation method, it is possible to sufficiently separate and remove the microorganisms, because the coagulant is not used, it is possible to avoid the second paragraph and biological organic load increases coagulant precipitation treatment of the reaction vessel of these problems, but also and means is provided to reduce the area of ​​aeration.

[0016] 本发明是根据如上观点而完成的,以下说明本发明的要点。 [0016] According to the present invention is accomplished as described above viewpoint, the following description of the gist of the invention.

[0017] [I] 一种有机性排水的处理装置,其特征在于包括: [0017] [I] a device for processing organic waste water, comprising:

[0018] 具有生物膜的流动床式的第I生物处理反应槽,对有机性排水进行生物处理; [0018] I first fluidized bed biofilm process has a biological reaction tank, to biologically treating organic drainage;

[0019] 无凝集且浮选分离方式的第I固液分离机构,对从所述第I生物处理反应槽流出的生物处理水进行固液分离;以及 [0019] No aggregation and the first solid-liquid separation means I floatation separation method, the biological treatment of the reaction effluent from the first tank I biologically treated water by solid-liquid separation; and

[0020] 流动床式或膜分离活性污泥式的第2生物处理反应槽,对经该第I固液分离机构分离的分离水进行生物处理。 [0020] or a fluidized bed type membrane separation activated sludge biological treatment in the second reaction tank, solid-liquid separation means for separating the water separated by the second I biological treatment.

[0021] [2]如[I]所述的有机性排水的处理装置,其特征在于还包括: [0021] [2] [I] the treatment of organic waste water, characterized by further comprising:

[0022] 第2固液分离机构,对从所述第2生物处理反应槽流出的生物处理水进行固液分离;以及 [0022] The second solid-liquid separation means, solid-liquid separation tank for biological treatment of the reaction effluent from the second biological treatment of water; and

[0023] 高度处理机构,去除经所述第2固液分离机构分离的分离水中所含的溶解物。 [0023] The height of the processing means, remove solutes contained in the second solid-liquid separation by the separation means separating the water.

[0024] [3]如[I]或[2]所述的有机性排水的处理装置,其特征在于: [0024] [3] [I] or [2], wherein the treatment of organic waste water, comprising:

[0025] 所述第I生物处理反应槽的溶解性BOD去除率为30〜99%。 [0025] The biosoluble I of BOD removal reaction vessel was treated 30~99%.

[0026] [4]如[I]至[3]中任一项所述的有机性排水的处理装置,其特征在于还包括: [0026] [4] [I] to [3] according to any one of the treatment of organic waste water, characterized by further comprising:

[0027] 向由所述第I固液分离机构固液分离的水中添加浮选助剂的机构。 [0027] added to aid flotation separation means by means of the first solid-liquid separation I water.

[0028] [5]如[2]至[4]中任一项所述的有机性排水的处理装置,其特征在于还包括: [0028] [5] [2] to [4] according to any one of the treatment of organic waste water, characterized by further comprising:

[0029] 向由所述第2固液分离机构固液分离的水中添加凝集剂的机构。 [0029] adding a coagulant in the separating means by the second solid-liquid separation means water.

[0030] [6]如[2]至[5]中任一项所述的有机性排水的处理装置,其特征在于: [0030] [6] [2] to [5] The treatment of organic waste water according to any preceding claim, wherein:

[0031 ] 所述高度处理机构包括膜分离机构。 The [0031] processing means comprises a height membrane separation means.

[0032] 根据本发明,在第I生物处理反应槽中使大部分溶解性有机物质分解之后,利用第I固液分离机构使第I生物处理反应槽中所生成的微生物体无凝集地分离,进一步在第2生物处理反应槽中对已去除该微生物体的分离水进行生物处理之后,利用第2固液分离机构对第2生物处理反应槽中所生成的微生物体进行分离。 [0032] According to the present invention, the reaction vessel at the process I that most biological decomposition after dissolved organic matter by means of the first solid-liquid separation I I reaction vessel biological treatment microorganisms generated without separating aggregated, after further processing in the second reaction vessel for separating water the biological microorganism is biologically treated has been removed by the second solid-liquid separation means to the second biological treatment tank reactor resulting microorganisms were isolated. 这样,通过进行生物处理、固液分离这2段处理,可减少生物代谢物质量,且可降低流入高度处理机构中的有机物质浓度,从而可稳定地进行排水处理。 Thus, by biological treatment, this two-stage solid-liquid separation process, a bio-metabolite can be reduced by mass, and can reduce the concentration of organic substances in the inflow height processing means so that wastewater treatment can be stably performed.

[0033] 而且,第I固液分离机构中,不使用凝集剂,而是无凝集地进行浮选分离,由此,可有效地去除第I生物处理反应槽的处理水中的SS(SuspendedSubstance,悬浮物),且可以避免使用凝集剂时第2生物处理反应槽中的有机物负荷的增大或由凝集剂而引起金属盐析出这些问题,而且,可降低用于凝集处理的药剂成本且减少装置设备,从而可有效地进行处理。 [0033] Further, the first solid-liquid separation mechanism I, the coagulant is not used, but without agglomeration flotation separation performed, thereby effectively removing the SS-I biological treatment of water treatment of the reaction tank (SuspendedSubstance, suspended increases thereof), and avoid the use of organic load coagulant second biological treatment tank or a reaction caused by the metal salt coagulant precipitation problems, but also, can reduce the cost of reagents used in the aggregation process and reduces plant equipment so as to be effectively treated.

[0034] 本发明的有机性排水的处理装置,通过如上所述的2段生物处理,在须进一步对已充分去除有机物质的水进行高度处理时较有效,通过后续的高度处理,可获得水质良好的处理水。 [0034] The treatment of organic waste water according to the present invention, by a two-stage biological treatment as described above, to be more effective when the height of the further processing of the water has been sufficiently removed organic material, by subsequent processing of the height, the water quality can be obtained a good deal of water. 此高度处理机构的处理水的水质极佳,因此可直接用作再利用的水,或者回收作为纯水、超纯水的原水(rawwater)。 This highly water treatment water treatment means excellent, it can be directly used as a water reuse, recycling or as pure water, ultra pure raw water (rawwater).

[0035] 而且,利用高度处理机构,对已充分降低有机物质浓度的水进行处理,所以可减轻高度处理的负荷,如果高度处理机构为膜分离装置,则可防止膜污染,使通量(flux)随着时间降低的程度减小、长期保持稳定的处理。 [0035] Further, the use of height processing means for processing have been sufficiently reduced concentration of organic substances in water, which greatly reduces the processing load of the height, if the height of the processing means of the membrane separation means, membrane fouling can be prevented, so that the flux (Flux ) the degree of reduction decreases over time, long-term stability of the process. 而且,如果所述高度处理机构是离子交换装置,则通过减小有机物负荷、有机污染,而可实现提高处理水质、降低树脂再生频率、降低树脂交换频率。 Further, if the height of the processing means is an ion exchange device, the organic load by reducing the organic contamination, the treated water can be improved, reducing the frequency of regeneration of the resin, the resin to reduce the frequency of exchange. 而且,如果所述高度处理机构是氧化装置,则通过降低有机物负荷,可节省氧化剂的使用量、且使装置实现小型化。 Further, if the height of the processing means is an oxidation apparatus, by decreasing the organic load, the amount of oxidizing agent used can be saved, and the downsizing of the apparatus.

附图说明 BRIEF DESCRIPTION

[0036] 图I (a)及图I (b)是表示本发明的有机性排水的处理装置的实施形态的系统图。 [0036] FIG I (a) and FIG. I (b) is a system diagram of the embodiment of the organic processing apparatus of the present invention the drain.

[0037] I :第I生物处理反应槽 IA :散气管 [0037] I: I first biological treatment tank reactor IA: diffusing pipe

[0038] 2 :第I浮选槽 3 ••第2生物处理反应槽 [0038] 2: 3 •• flotation I, the second biological treatment tank reactor

[0039] 3A :散气管 4 :凝集槽 [0039] 3A: diffusing tubes 4: coagulation tank

[0040] 4A :第I凝集部 4B :第2凝集部 [0040] 4A: Part I aggregated portions 4B: second aggregated portion

[0041] 5 :第2浮选槽 6 :过滤装置 [0041] 5: second flotation cell 6: filter means

[0042] 7 :R0膜分离装置 8 :第2生物处理反应槽 [0042] 7: R0 membrane separation apparatus 8: the second biological treatment tank reactor

[0043] 8A :散气管 10 :载体 [0043] 8A: San tube 10: support

[0044] 20 :槽外膜组件 [0044] 20: groove outer membrane

具体实施方式 Detailed ways

[0045] 以下,对于本发明的有机性排水的处理装置的处理方法的实施形态进行详细说明。 [0045] Hereinafter, the embodiment of the processing method of processing an organic drainage apparatus of the present invention will be described in detail.

[0046][有机性排水] [0046] [organic discharged]

[0047] 本发明中,作为处理对象的有机性排水,只要是进行普通生物处理的包含有机物的排水即可,并无特别限定,可列举例如:电子产业排水、化学工厂排水、食品工厂排水等。 [0047] In the present invention, as an organic waste water treatment object, as long as the biological treatment is subjected to ordinary drainage containing organic matter can be, not particularly limited, and include for example: electronics industry drainage, drainage chemical plants, food factories drainage . 例如,电子零件制造过程中,从显影工序、剥离工序、蚀刻工序、清洗工序等,大量产生各种有机性排水,而人们希望回收排水,将其净化处理成纯水的程度后再次使用,所以,这些排水适合用作本发明的处理对象的排水。 For example, electronic parts manufacturing process, from the developing step, stripping step, an etching step, a washing step, etc., to produce a large number of various organic drainage, drainage and it is desired to recover, which will be used again after the purification treatment extent into pure water, so these drainage suitable for drainage of the processing object of the present invention.

[0048] 对于这样的有机性排水,可列举例如:包含异丙醇、乙醇等的有机性排水,包含一乙醇胺(MEA, Mono Ethanol Amine)、四甲基氢氧化铵(TMAH, Tetramethyl ammoniumhydroxide)等有机态氮、氨态氮的有机性排水,包含二甲亚砜(DMSO,Dimethyl Sulfoxide)等有机硫化合物的有机性排水。 [0048] For this organic discharged, for example, include: organic drain comprises isopropanol, ethanol and the like, comprising monoethanolamine (MEA, Mono Ethanol Amine), tetramethylammonium hydroxide (TMAH, Tetramethyl ammoniumhydroxide), etc. organic nitrogen, ammonia, organic nitrogen drainage, drainage containing organic dimethylsulfoxide (DMSO, dimethyl sulfoxide) and other organic sulfur compounds.

[0049] 本发明的有机性排水的有机物浓度并无特别限定,但本发明特别适用于溶解性TOC (Total Organic Carbon,总有机碳)大于等于100mg/L,例如为200 〜25000mg/L 的含高浓度有机物的排水的处理。 [0049] The concentration of the organic matter of the present invention, organic discharged is not particularly limited, but the present invention is particularly applicable to the solubility of TOC (Total Organic Carbon, total organic carbon) is equal to greater than 100mg / L, for example 200 ~25000mg / L containing treated waste water of a high concentration of organic matter.

[0050][生物处理反应槽] [0050] [Reaction biological treatment tank]

[0051]〈第I生物处理反应槽〉 [0051] <Reaction I of biological treatment tank>

[0052] 作为用于对排水进行生物处理的生物处理反应槽,只要有机物的分解效率优异即可,可采用现有的需氧性或厌氧性的生物处理反应槽,但本发明中,作为第I生物处理反应槽,使用生物膜方式的流动床式生物处理反应槽。 [0052] The reaction tank for biological treatment biological drainage treatment, as long as the organic substance decomposition efficiency superior to, may be employed conventional aerobic or anaerobic biological treatment of the reaction tank, the present invention, I first biological treatment tank reactor, biofilm embodiment using the fluidized bed biological treatment of the reaction vessel. 作为第I生物处理反应槽,优选对菌体进行造粒的UASB (upf low anaerobicsludge bed,升流式厌氧污泥床)方式或使用载体的生物处理反应槽。 I as the biological treatment reaction tank, preferably of pelletized cells of UASB (upf low anaerobicsludge bed, upflow anaerobic sludge blanket) system using a carrier or biological treatment reaction tank.

[0053] 作为载体,可使用活性炭、各种塑料载体、海绵载体等任一种,但优选使用海绵载体。 [0053] As the carrier, activated carbon may be used any of a variety of plastic carriers, carriers and the like sponges, they are preferable to use sponge carrier. 如果使用海绵载体,则可使微生物维持高浓度。 If a sponge carrier, the microorganism can maintain a high concentration. 对于海绵材料也无特别限定,但优选酯系聚氨酯。 For the sponge material is not particularly limited, but is preferably an ester-based polyurethane. 对于载体的投入量也无特别制限,但是,通常,优选生物处理反应槽中的载体相对于槽容量的表观容量(apparent capacity)为10〜50%左右,特别优选是30〜50%左右。 For inputs carrier is also not particularly limited, and however, generally, the reaction is preferably a biological treatment tank carrier relative to the nominal capacity of the tank capacity (apparent capacity) of about 10~50%, particularly preferably about 30 ~ 50%.

[0054] 作为在需氧性状态下微生物式地对有机物进行分解的需氧性生物处理反应槽,可使用设有用于向槽内供给氧(空气)的散气管、曝气机等氧气(空气)供给机构的曝气槽。 [0054] As the reaction aerobic biological treatment tank to decompose organic matter in the aerobic microorganisms formula state may be used provided into the chamber for supplying oxygen (air) diffusion pipe, and the like aerator oxygen (air ) supplying the aeration tank means.

[0055] 另一方面,作为在厌氧性状态下微生物式地对有机物进行分解的厌氧性生物处理反应槽,可使用UASB方式或保持载体的厌氧槽。 [0055] On the other hand, as to the type of organic matter microbial anaerobic decomposition of biological treatment reaction tank under anaerobic state, or mode can be used to maintain the anaerobic UASB tank carrier.

[0056] 第I生物处理反应槽,可为需氧性生物处理反应槽或厌氧性生物处理反应槽的I槽式,也可为需氧性生物处理反应槽及/或厌氧性生物处理反应槽的多槽式,而且,在I槽式的情况下,也可在槽内设置分隔壁。 [0056] The reaction of I biological treatment tank, aerobic biological treatment may be a reaction tank or anaerobic biological treatment tank I reaction trough, can also be aerobic biological treatment reaction tank and / or anaerobic biological treatment multi-tank reactor tank, and, in the case of I trough, the partition wall may be provided in the groove. 也就是说,本发明中,作为第I生物处理反应槽,可采用多槽式。 That is, the present invention, I first biological treatment tank reactor, multi-slot may be employed.

[0057] <第2生物处理反应槽> [0057] <2 Reaction biological treatment tank>

[0058] 本发明中,作为第2生物处理反应槽,使用流动床式或膜分离活性污泥式的生物处理反应槽。 [0058] In the present invention, as the second biological treatment tank reactor using a fluidized bed type or membrane separation activated sludge biological treatment reaction tank. 关于流动床式生物处理反应槽,与上述第I生物处理反应槽中的流动床式生物处理反应槽相同,也可为具有载体的生物膜式生物处理反应槽。 Biological treatment on a fluidized bed reaction vessel, with the first I biological treatment tank reactor fluidized bed biological treatment the same reaction vessel, the reaction vessel may be treated with biofilm biological carrier. 此时,关于使用的载体的种类及其投入量,也与上述第I生物处理反应槽中的相同。 At this time, the type and amount of the input vector used, the reaction vessel is also the same as the first I biological processing.

[0059] 而且,作为膜分离活性污泥式的生物处理反应槽,可采用在生物处理反应槽的槽外设有膜组件的槽外型MBR (Membrane Bioreactor,膜生物反应器)方式,也可采用在生物处理反应槽的槽内浸溃配置有膜组件的浸溃型MBR。 [0059] Further, as the membrane separation activated sludge biological treatment type reaction tank, biological treatment tank may be employed in the reaction tank has a peripheral groove membrane appearance MBR (Membrane Bioreactor, MBR) embodiment, may also be in the reaction vessel using biological treatment tank dipping the membrane module is disposed impregnation type MBR. 如果使用膜分离活性污泥式生物处理反应槽,可在槽内将活性污泥高度浓缩,提高生物处理效率。 If a membrane separation activated sludge biological treatment reaction vessel, it may be highly concentrated in the activated sludge tank, to improve the efficiency of the biological treatment.

[0060] 作为第2生物处理反应槽,采用利用载体的流动床式或膜分离活性污泥式生物处理反应槽,这样,可将难分解成分分解菌体保持在槽内,且可有效地进行处理。 [0060] As the second biological treatment tank reactor, using a fluidized bed or a membrane separation activated sludge biological treatment reaction vessel using a carrier, such may be difficult to break down into components held within the slot cell, and can effectively deal with. 特别是当使用膜分离活性污泥式的生物处理反应槽时,是将作为后段的第2固液分离机构的浸溃膜配置在此生物处理反应槽内,这样可使装置设置小型化。 In particular, when using membrane separation activated sludge biological treatment type reaction tank, is arranged to collapse as the film is immersed in the second-stage solid-liquid separation mechanism of this reaction is a biological treatment tank, so that the size of the device can set.

[0061] 该第2生物处理反应槽与第I生物处理反应槽相同,可为设有在需氧性状态下微生物式地对有机物进行分解的需氧性生物处理反应槽(槽内设有用于供给氧(空气)的散气管、曝气机等氧气(空气)供给机构的曝气槽),也可为在厌氧性状态下微生物式地对有机物进行分解的厌氧性生物处理反应槽。 [0061] The reaction of the second biological treatment tank to the first biological treatment reaction tank same as I, may be provided for the aerobic biological treatment of organic matter decomposing reaction tank type microorganisms in the aerobic state (provided with a slot supplying oxygen (air) diffusion pipe, and the like aerator oxygen (air) supply means aeration tank), the reaction vessel may be treated for the anaerobic biodegradation of organic matter of formula microorganisms under anaerobic state.

[0062] 第2生物处理反应槽,可采用需氧性生物处理反应槽或厌氧性生物处理反应槽的I槽式,也可采用需氧性生物处理反应槽及/或厌氧性生物处理反应槽的多槽式,而且,在I槽式的情况下,也可在槽内设置分隔壁。 [0062] The reaction of the second biological treatment tank may be employed aerobic biological treatment reaction I trough anaerobic biological treatment tank or a reaction tank may also be employed aerobic biological treatment reaction tank and / or anaerobic biological treatment multi-tank reactor tank, and, in the case of I trough, the partition wall may be provided in the groove. 也就是说,本发明中,作为第2生物处理反应槽,可米用多槽式。 That is, the present invention, the second biological treatment tank reactor, can be a multi-meter trough.

[0063][第I固液分离机构] [0063] [I, solid-liquid separation mechanism]

[0064] 本发明中,作为对来自第I生物处理反应槽的生物处理水进行固液分离的第I固液分离机构,在不添加凝集剂的无凝集处理中,采用的是浮选分离方式的固液分离机构。 [0064] In the present invention, a biological reaction from the first biological treatment tank I treated water for the first solid-liquid separation I liquid separation mechanism, without adding coagulant without aggregation process, using the flotation separation method solid-liquid separation mechanism. 对于浮选分离方式而言,特别优选加压浮选分离方式,为了使浮选分离稳定,也可添加介面活性剂(interfacial activeagent)等浮选助剂。 For flotation separation method, it is particularly preferred pressurized flotation separation system, in order to make stable floatation separation, may be added to the active agent interface (interfacial activeagent) flotation aid and the like.

[0065] 根据本发明,可利用无凝集的浮选分离而高效地对来自第I生物处理反应槽的生物处理污泥进行固液分离,其理由如下所述。 [0065] According to the present invention may be utilized without aggregation flotation separation process efficient solid-liquid separation of biological sludge from the biological treatment of the reaction tank I, the following reason.

[0066] 多段式生物处理装置的第I生物处理反应槽,通过反应槽分割而达到有机物负荷高的条件,第I生物处理反应槽中生成的微生物体处于对数增殖期(logarithmic growthphase)。 [0066] Biological Section I multistage biological treatment means treating the reaction tank, by dividing the reaction vessel to achieve a high organic load conditions, the reaction of the biological treatment tank I produced in the microorganism in the logarithmic growth phase (logarithmic growthphase). 对数增殖期的微生物体的状态为,具有亲水基团的细胞外多糖类的分泌量少、斥水性增强。 The state of the microorganisms to the logarithmic growth phase, with less secretion of an extracellular polysaccharide hydrophilic group, the water repellency is enhanced. 斥水性增强的微生物体,因受到斥水的相互作用而容易吸附气泡,即使无凝集,只要是浮选分离,那么就能够以快于沉淀分离的通水速度(LV)进行固液分离。 Microorganisms enhanced water repellency, water repellency due to the interaction being easily adsorbed bubbles, even without aggregation, as long as the flotation separation, the solid-liquid separation can be performed through the water at velocity (LV) faster than the precipitation.

[0067]另外,对数增殖期的微生物体,因未形成块体(block)所以在水中呈分散状态,无凝集的沉淀分离必须达到极低LV,处理效率明显变差。 [0067] Moreover, microorganisms of the logarithmic growth phase, because the block (block) is formed so not being dispersed in water, without precipitation must be aggregated for very low LV, the processing efficiency is significantly deteriorated.

[0068] 作为浮选分离、优选加压浮选分离的处理条件,并无特别制限,但优选例如通水LV为5〜25m/hr。 [0068] As flotation separation, preferably pressurized flotation separation treatment conditions, and is not especially limited, but is preferably, for example water passing LV 5~25m / hr. 当LV高出此范围时会有SS流出,而当低于此范围时在经济性不佳。 When the LV outflow SS will be higher than this range, and when lower than this range in the poor economy.

[0069] 而且,当使用浮选助剂时,作为浮选助剂,可使用I种或者2种或2种以上的不饱和脂肪酸盐等,对于原水,所述浮选助剂的添加量优选为O. I〜10mg/L左右。 [0069] Further, when using the flotation aids, as flotation aids, I may be used or two or more kinds or unsaturated fatty acid salts two kinds, for the raw water, the amount of flotation aid was added preferably about O. I~10mg / L. 另外,通常,浮选助剂是在加压浮选分离之前添加。 Further, generally, the flotation aid is added prior to the pressurized flotation separation.

[0070] 一般来说,污泥的固液分离采用的是按照常规方法添加凝集剂的凝集处理,本发明中,为了避免在添加了聚合氯化招(PAC, Poly AluminumChloride)或氯化铁(III)等无机凝集剂或有机凝集剂时所产生的问题,而实施无凝集的浮选分离,其理由如下所述。 [0070] In general, the solid-liquid separated sludge is employed flocculating aggregating agent is added according to conventional methods, the present invention, in order to avoid the addition polymerization strokes chloride (PAC, Poly AluminumChloride) or ferric chloride ( when III) an inorganic flocculant or an organic flocculant problems arising, while no agglutination of flotation separation embodiment, the following reason.

[0071] 也就是说,如果添加无机凝集剂,则如上所述,凝集处理的处理水中残留有由无机凝集剂而来的溶解金属盐,在第2生物处理反应槽中,所述溶解金属盐会在载体或散气管中产生析出。 [0071] That is, if the inorganic coagulant, as described above, the residue treated water from the agglomeration process are dissolved from the metal salts of inorganic flocculant, and the second biological treatment in the reaction vessel, the metal salt is dissolved It will produce precipitates or bulk carrier trachea.

[0072] 溶解金属盐在载体上的析出,会减少微生物体的附着部,从而减少附着的微生物量,因此会引起有机物分解速度的降低。 [0072] dissolving the metal deposited on the carrier, it will reduce the microbial attachment portion of the body, thereby reducing the amount of attachment of microorganisms, and therefore cause a decrease of the rate of decomposition of organic matter. 而且,因载体的比重加大,所以载体堆积在第2生物处理反应槽下部,无法充分流动,而使曝气等搅拌时所需的动力增大。 Further, due to increase the proportion of the carrier, the carriers accumulated in the lower portion of the second biological treatment tank reactor, not sufficiently flow, the power required for stirring increases aeration and the like.

[0073] 而且,金属盐在散气管上的析出,会使得因曝气量降低而导致溶解氧不足,或者因差压上升而导致曝气动力增大。 [0073] Further, the metal salt is deposited on the diffuser tube, so that due to a decrease may result in insufficient amount of dissolved oxygen aeration, or because rising pressure caused by increased aeration power.

[0074] 另一方面,当凝集剂不足而凝集不充分时,微小絮凝体(flock)增大,流出到固液分离机构的分离水中的絮凝体增多。 [0074] On the other hand, when there is insufficient aggregating agent is not sufficiently aggregated, tiny floc (Flock) in the increase flocs flows out solid-liquid separation mechanism to separate the water. 当第2生物处理反应槽为MBR方式时,凝集剂的泄漏部分附着在膜面,导致膜面堵塞。 When the second reaction tank is a biological treatment MBR embodiment, the leak portion coagulant adhered to the film surface, leading to clogging of the membrane surface.

[0075] 这样,因存在溶解金属盐,所以可能引起损害第2生物处理反应槽功能的严重问题,因此,本发明中的第I固液分离机构中,未使用无机凝集剂。 [0075] Thus, due to the presence of dissolved salts, it may cause serious damage to the second biological treatment tank reactor problems function, therefore, I, solid-liquid separation mechanism in the present invention, the inorganic coagulant is not used.

[0076] 而且,大多数有机凝集剂具有生物难分解性,当其流入到生物处理反应槽中时,如上所述,会附着在载体表面,从而可能导致阻止氧透过或使生物活性降低,因此,本发明中的第I固液分离机构中,与无机凝集剂同样,也未添加有机凝集剂。 [0076] Also, aggregating agents most organic biologically non-biodegradable, when it flows into the reaction vessel during the biological treatment, as described above, will be attached to the support surface, which may lead to prevent oxygen permeability decreases or biologically active, Thus, the solid-liquid separation mechanism I of the present invention, similarly with the inorganic flocculant, organic flocculant has not added.

[0077] 利用第I固液分离机构无凝集地进行处理,由此,可起到以下效果:减少凝集剂、用于调整PH值的药品、以及包含凝集反应所需要的反应槽及计量仪的设备。 [0077] The solid-liquid separating means by the first I performed without agglomeration process, whereby the following advantages are: reduced aggregating agent, drug for adjusting the PH value, and the meter comprising a reaction vessel and the desired agglutination of device.

[0078] 而且,当对原水TOC浓度大于等于100mg/L的含高浓度有机物的排水进行生物处理时,悬浊物质浓度增大,凝集沉淀分离时因添加了大量的凝集剂,所以污泥(sludge)容积增大,使得污泥界面增高,固液分离变得困难,但本发明中的无凝集的浮选分离中污泥容 [0078] Further, when the raw water is drained TOC concentration greater than or equal 100mg / L containing a high concentration of biological treatment of organic matter, suspended matter concentration is increased, by the addition of a large amount of agglomerated coagulant, the sludge precipitation separation ( sludge) volume increases, so that the sludge interface increases, it becomes difficult to solid-liquid separation, flotation separation, but in the present invention accommodating non-agglomerated sludge

积未增大,可容易地进行固液分离。 The product is not increased, solid-liquid separation can be easily performed.

[0079][第2固液分离机构] [0079] [Second solid-liquid separation mechanism]

[0080] 当对于来自第2生物处理反应槽的生物处理水进行固液分离时,可无凝集地进行处理,也可进行凝集处理,但为了利用第2固液分离机构可靠地去除微生物体和高分子有机物质,优选在固液分离之前进行凝集处理。 [0080] When the solid-liquid separation for the biological treatment reaction from the second biological treatment tank of water, can be handled without aggregation, the aggregation process may be performed, but in order to use the second solid-liquid separation mechanism and reliably remove microorganisms polymeric organic substance, preferably solid-liquid separation treatment prior to aggregation. 在后段实施高度处理时,特别优选添加凝集剂进行凝集处理。 In the practice of the height-stage process, particularly preferably a flocculant is added for aggregation treatment.

[0081] 生物处理水的凝集处理中,使用的是通常的凝集处理装置。 [0081] Biological aggregation processing water, is generally used in the flocculating means. 该凝集处理装置的凝集槽可仅为I槽,也可多段地设为2槽或2槽以上。 The coagulation tank flocculating means may only I groove, the second groove is also set to 2 or more grooves may be multiple stages.

[0082] 一般来说,凝集处理装置是由用于使凝集剂与被处理水充分接触的急速搅拌槽、和使凝集絮凝体成长的慢速搅拌槽构成。 [0082] In general, the aggregation processing means is for aggregating agent with rapid agitation tank water to be treated sufficient contact, and the aggregated floc growth slow stirring tank configuration. 因此,当将2槽或2槽以上的凝集槽设为多段时,优选将前段凝集槽作为急速搅拌槽,而将后段凝集槽作为慢速搅拌槽。 Thus, when 2 or more grooves of the second groove set multistage coagulation tank, preferably a pre-stage coagulation tank rapid agitation tank, and the rear stage stirring tank as a slow coagulation tank.

[0083] 作为凝集处理中使用的无机凝集剂,可列举三氯化铁、聚硫酸铁等铁系凝集剂,硫酸铝、氯化铝、聚合氯化铝等铝系凝集剂,但从凝集效果方面考虑,优选铁系凝集剂。 [0083] As the inorganic flocculant aggregation process used include ferric chloride, ferric sulfate and other iron-based poly-coagulant, aluminum sulfate, aluminum chloride, polyaluminum chloride and other aluminum based coagulant, but the effect of agglutination viewpoint, preferably iron-based coagulant. 这些无机凝集剂,可单独使用I种,也可同时使用2种或2种以上。 These inorganic coagulant, Type I may be used alone, or two or more kinds may be used simultaneously or in combination.

[0084] 进行凝集处理时,根据需要而添加pH值调整剂,以调整为所使用的无机凝集剂所适合的PH值。 When [0084] performing an agglutination process, if necessary to add a pH adjusting agent and, for adjusting an inorganic aggregating agent used for the PH value. 也就是说,作为pH值条件,例如,铁系凝集剂中,以pH 4〜8的pH值进行反应是有效的;铝系凝集剂中,以小于等于PH 5.0的pH值进行反应之后,调整为大于等于pH That is, as the pH conditions, e.g., iron based aggregating agent, the pH of the reaction is pH 4 to 8 is effective; after the aluminum-based coagulant, a pH of less than or equal to PH 5.0 is reacted, adjusted pH greater than or equal

6. O的pH值后有效,所以,优选根据需要,添加盐酸(HC1)、硫酸(H2SO4)等酸,或者氢氧化钠(NaOH)等碱来调整pH值。 After the pH value of 6. O valid, it is preferable according to need, hydrochloric acid (HC1 is), sulfuric acid (H2SO4) and the like acids, or sodium hydroxide (NaOH), alkali to adjust the pH. 在这样的pH值条件下进行凝集处理,可获得良好的处理水质,其详细理由尚不明确,但可推断,与生物代谢物中的蛋白质(albuminoid)成分的电荷被中和有关。 Is carried out at such pH values ​​aggregation process, to obtain good processing quality, the detailed reason is not clear, but inferred charge and biological metabolites protein (albuminoid) related component is neutralized.

[0085] 通过凝集处理,使生物处理水中的溶解性有机物和悬浊物变成絮凝体。 [0085] By aggregating treatment, biological treatment of water and dissolved organic matter suspended solids into flocs. 为了使所述凝集絮凝体成长,可在第I凝集槽中添加无机凝集剂,在第2凝集槽中添加高分子凝集剂。 In order to make the aggregated floc growth, an inorganic flocculant may be added at the aggregated vessel I, the polymer flocculant is added in the second coagulation vessel.

[0086] 作为对第2生物处理反应槽的生物处理水、优选对该生物处理水进行凝集处理后所得的凝集处理水进行固液分离的第2固液分离机构,并不限定为沉淀槽、浮选槽、离心分离机等,只要是生物处理水的凝集絮凝体容易浮选分离、且面积小于沉淀槽的装置即可,所以,特别优选加压浮选槽。 After [0086] As the second biological treatment of biological reaction tank of treated water, preferably water of the biological treatment process resulting agglomerated water flocculating second solid-liquid separation in solid-liquid separation means, not limited to the sedimentation tank, flotation, centrifugation, etc., as long as the biologically treated water easy aggregated floc flotation separation, and the apparatus can be smaller than the area of ​​the sedimentation tank, it is particularly preferred pressurized flotation. 而且,作为第2固液分离机构,特别优选使用浸溃膜等膜分离机构。 Further, as the second solid-liquid separation means, membrane separation means impregnated film is particularly preferably used. 此时,如上所述,使用浸溃型MBR来作为第2生物处理反应槽,这样,将作为第2固液分离机构的浸溃膜配置在第2生物处理反应槽内,从而可使装置小型化。 At this time, as described above, using the MBR impregnated type as the second biological treatment tank reactor, so that the collapse of the second film is disposed as the biological treatment reaction vessel immersed in the second solid-liquid separation means, so that the apparatus can be small of.

[0087][高度处理机构] [0087] [height of the processing means]

[0088] 另外,本发明中,也可进行高度处理,以此去除对第2生物处理反应槽的生物处理水进行固液分离后所得的分离水中所含的溶解物。 [0088] Further, the present invention can also be highly treated, this lysate is removed after the biological reaction of the second biological treatment tank water liquid separation process separating the water contained in the resultant.

[0089] 关于高度处理机构,可为进一步去除利用第I、第2生物处理机构、第I、第2固液分离机构去除排水中的有机物后所得的处理水中所残留的溶解有机物(dissolvedorganic matter)的类型,而且,可为去除处理水中所含的溶剂盐类的类型,也可为去除上述两者的类型。 [0089] For highly processing means may be further removed using the first I, second biological treatment means, the first I, second solid-liquid separation means is removed after draining the resulting treated water in the organic residue dissolved organic matter (dissolvedorganic matter) type, but also, the type of solvent removal process may be salts contained in the water, but also to remove the above-mentioned two types.

[0090] 作为高度处理机构,可列举如下类型。 [0090] As the height of the processing means, include the following types. [0091] 膜分离装置:例如,用于去除有机物或脱盐的RO膜(Reverse Osmosismembrane,反浸透膜)、NF 膜(nano-filter membrane,纳米过滤膜)、UF 膜(ultrafiltrationmembrane,超过滤膜)分离装置等 [0091] The membrane separation apparatus: RO membrane (Reverse Osmosismembrane, reverse osmosis membrane), for removal of organic or desalination, of NF membranes (nano-filter membrane, nanofiltration membrane), the UF membrane (ultrafiltrationmembrane, ultrafiltration) isolating devices, etc.

[0092] 离子交换装置:例如,用于脱盐或去除有机物的阴离子交换树脂塔、阳离子交换树脂塔、阳离子交换树脂与阴离子交换树脂混合填充而成的混床塔、电脱盐装置等 [0092] The ion exchange apparatus: for example, for desalting or anionic exchange resin column to remove organic matter, cation exchange resin column, an anion exchange resin and a cation exchange resin obtained by mixing a mixed bed column filled, like desalter

[0093] 氧化装置:例如,用于去除有机物的臭氧氧化装置、过氧化氢氧化装置、氯氧化装置、紫外线氧化装置等、或者同时使用这些装置的氧化装置。 [0093] Oxidation means: e.g., ozone-oxidation means for removing organic matter, means hydrogen peroxide, chlorine oxidation means, an ultraviolet oxidation device and the like, or the use of these means of oxidation. 另外,通常来说,多数情况下,在此氧化装置的后段设有用于离子交换、膜分离等的装置。 Further, generally speaking, in most cases, the latter stage of the oxidation apparatus is provided with means for ion exchange, membrane separation and the like.

[0094] 这些高度处理机构,也可适当地组合使用2种或2种以上。 [0094] The height of the processing means may be appropriately used in combination of two or more thereof. 而且,作为高度处理机构的一部分,也可再添加过滤装置或活性炭处理装置等其他处理装置。 Further, as part of the height of the processing means, may be further added other processing means or activated carbon filtration apparatus processing device and the like.

[0095] 当使用RO膜分离装置作为高度处理机构时,特别优选在RO膜分离装置的前段设置过滤装置,来去除水中的SS。 [0095] When the RO membrane separator processing mechanism as height, particularly preferably provided in the front stage filter means RO membrane separator to remove SS in water. 作为过滤装置,可使用填充了砂、无烟煤(Anthracite)等滤材的填充层型过滤装置,使用MF膜(Microfiltration membrane,精密过滤膜)、UF膜等膜的膜过滤装置等。 As a filtration apparatus, it may be filled using sand, anthracite (Anthracite) filter like filling layer type filtration apparatus using an MF membrane (Microfiltration membrane, microfiltration membrane), the membrane filtering device UF membrane film and the like.

[0096][有机性排水的处理装置] [0096] [treatment of organic waste water]

[0097] 以下,参照附图说明本发明的有机性排水的处理装置的一例。 [0097] Hereinafter, referring to the drawings of an example of processing organic waste water apparatus according to the invention.

[0098] 图I (a)及图I (b)是表示本发明的有机性排水的处理装置的实施形态的系统图。 [0098] FIG I (a) and FIG. I (b) is a system diagram of the embodiment of the organic processing apparatus of the present invention the drain. 另外,图I是本发明的有机性排水的处理装置的一例,本发明的有机性排水的处理装置并不限于图I所示的装置。 Further, FIG. I is an example of organic waste water treatment apparatus of the present invention, the treatment of organic waste water according to the present invention is not limited to the device I shown in FIG. 例如,高度处理机构并不限于RO膜分离装置,也可为离子交换装置或氧化装置,生物处理反应槽并不限于曝气槽,也可为厌氧性生物处理反应槽。 For example, the height of the processing means is not limited to RO membrane separation apparatus, device, or may be an ion exchange device oxidation, biological treatment is not limited to the aeration tank reaction vessel, the reaction vessel may be treated as anaerobic organisms.

[0099] 图I (a)中的有机性排水的处理装置包括:作为第I生物处理反应槽的曝气槽(以下称作“第I生物处理反应槽”)I;对于来自第I生物处理反应槽I的生物处理水,无凝集地、也就是说不添加任何凝集剂地进行固液分离的第I浮选槽(以下称作“第I浮选槽”)2 ;导入有来自第I浮选槽2的分离水的、作为第2生物处理反应槽的曝气槽(以下称作“第2生物处理反应槽”)3 ;对来自第2生物处理反应槽3的生物处理水进行凝集处理的凝集槽4 ;对来自凝集槽4的凝集处理水进行固液分离的、作为第2固液分离机构的浮选槽(以下称作“第2浮选槽”)5 ;导入有第2浮选槽的分离水的过滤装置6 ;以及导入有过滤装置6的过滤水的作为高度处理机构的RO膜分离装置7。 [0099] Figure I treatment of organic waste water (a) comprises: I a first biological treatment tank to the aeration tank reactor (hereinafter referred to as "the first biological treatment reaction tank I") I; I for from the first biological treatment I bioreactor treated water without agglomeration, the aggregating agent that is without adding any solid-liquid separation of the flotation tank I (hereinafter referred to as "first flotation tank I") 2; introduced from the first I have flotation separation of water, as the second biological treatment tank 2 aeration reaction tank (hereinafter, referred to as "the second biological treatment tank reactor") 3; biological reaction from the second biological treatment tank 3 for aggregation treatment water aggregation processing tank 4; agglutination agglutination treated water from the tank 4 solid-liquid separation, flotation tank as the second solid-liquid separation mechanism (hereinafter referred to as "second flotation cell") 5; into which a second water separation filter means 6 of the flotation tank; RO membrane separation apparatus and a filter for filtering the water introduced with the device 6 as the height of the processing means 7.

[0100] 另外,图I (a)及图I (b)中,第I生物处理反应槽I及第2浮选槽2可分别配置成2段或2段以上,按照生物处理反应槽一浮选槽一生物处理反应槽一浮选槽的顺序进行多段处理。 [0100] Further, FIG I (a) and FIG. I (B), the first biological treatment reactor I I and the second flotation tank 2, respectively, may be configured to segment or more than 22, according to a floating biological treatment tank reactor a biological treatment tank sequence selected from the reaction tank is a flotation tank multistage process.

[0101] 将原水(有机性排水)导入到第I生物处理反应槽I中,在散气管IA的曝气下,进行需氧性生物处理。 [0101] raw water (organic discharged) is introduced into a first biological treatment reactor I I, in the aeration diffusing pipe of IA, is subjected to aerobic biological treatment. 该第I生物处理反应槽I中,去除原水中的大部分溶解性有机物质(S-TOC),由此可降低流入到后段的第2生物处理反应槽3的溶解性有机物质浓度。 The second I biological treatment reactor I, removing most of the dissolved organic substance (S-TOC) of the raw water, thereby reducing the concentration of dissolved organic matter flows into the second stage after the biological treatment of the reaction tank 3. 该第I生物处理反应槽I是位于最前段的生物处理槽,所以,槽内每一微生物量的BOD负荷量变高,因此抑制了微生物间的食物链的自我分解。 The second biological treatment reactor I I is located at the first stage of the biological treatment tank, so that each groove microbial biomass high BOD load amount, thereby suppressing the autolysis of the microorganism between the food chain.

[0102] 第I生物处理反应槽I的较佳运转形态,根据原水中所含的有机物质的分解性而有些不同,但优选以BOD槽负荷I. 5〜60Kg-B0D/m3/day,TOC槽负荷O. 6〜24Kg-C/m3/day,去除原水中的30〜99%的溶解性BOD(S-BOD)的负荷量。 [0102] Biological Section I preferred form of operation of the process reactor I, exploded organic substances contained in the raw water and some different, but preferably the groove BOD load I. 5~60Kg-B0D / m3 / day, TOC load groove O. 6~24Kg-C / m3 / day, 30~99% removal of soluble BOD (S-BOD) load in the raw water.

[0103] 而且,如果在第I生物处理反应槽I中进行上述高负荷运转,将难以形成沉淀性优良的微生物絮凝体,因此,如图所示,优选向槽内投入载体10,以稳定地保持微生物量。 [0103] Further, if the high-load operation in the first biological treatment reactor I I, the precipitate is difficult to form an excellent microorganism flocs, thus, as shown, preferably into the carrier 10 into the slot, to be stably keep the microbial biomass. 添加了载体时的保持污泥量会根据载体及填充率而有所不同,但一般来说,当以槽容量的30〜 50%的表观容量而填充有海绵状的载体时,每一槽的污泥保持量达到2500〜6000mg-VSS/L左右,因此,当槽负荷为I. 5〜60Kg-B0D/m3/day时,污泥负荷达到O. 5〜IOKg-BOD/Kg-VSS/day,成为分散菌的发生区域。 Sludge retention time of adding the carrier will vary depending on the filling factor and the carrier, but in general, when 30~ 50% to the apparent capacity of tank volume filled with sponge-like carriers, each slot sludge holding volume reached about 2500~6000mg-VSS / L, and therefore, when the load of the groove I. 5~60Kg-B0D / m3 / day, the sludge load reached O. 5~IOKg-BOD / Kg-VSS / day, the bacteria become dispersed generation region.

[0104] 接着,对于来自第I生物处理反应槽I的生物处理水,在第I浮选槽2中无凝集地添加浮选助剂进行浮选分离,然后,第I浮选槽2的分离水被导入到第2生物处理反应槽3中,在散气管3A的曝气下,进行需氧性生物处理。 [0104] Next, from the second bio-reactor I I biological treatment of treated water in the flotation tank I, no agglutination was added 2 flotation aid flotation separation, then, I, flotation separation tank 2 water is introduced into the reaction in the second biological treatment tank 3, in the aeration diffusing pipe. 3A, aerobic biological treatment. 该第2生物处理反应槽3中,对经过第I生物处理反应槽I的生物处理后所残留的溶解性有机物质进行分解。 The reaction of the second biological treatment tank 3, through the first I for biological treatment of the biological residual dissolved organic substance treatment reactor I is decomposed. 该第2生物处理反应槽3中,较理想的是可靠地进行分解,以尽可能地降低流入到作为后段高度处理机构的RO膜分离装置7中的有机物浓度。 The second biological treatment tank 3 in the reaction, it is desirable to reliably decomposed, to reduce the concentration of organic matter in a subsequent stage 7 flows into the height of the processing means of the RO membrane separation apparatus as much as possible. 该第2生物处理反应槽3,特别优选将载体10保持在槽内的类型、或者以MBR方式保持菌体的类型,这样,在低负荷下也能稳定地保持微生物量。 The reaction of the second biological treatment tank 3, particularly preferred type of carrier 10 is held in a tank, or in a manner to maintain MBR types of cells, so that, at low load can be held stably microbial biomass. 该第2生物处理反应槽3的槽负荷为O. 03〜2Kg-B0D/m3/day,特别好的是O. I〜I. 2Kg-B0D/m3/day。 The reaction of the second biological treatment tank 3 is a tank load of O. 03~2Kg-B0D / m3 / day, particularly preferably O. I~I. 2Kg-B0D / m3 / day. 而且,当采用使用载体的生物处理反应槽时,优选以槽容量的30〜50%的表观容量来填充载体;当采用MBR方式是,优选MLSS浓度为2000〜12000mg/L。 Further, when a carrier is used in biological treatment reaction tank, preferably 30 ~ 50% of the apparent capacity of the tank volume filling carrier; mode when using the MBR, the MLSS concentration of preferably 2000~12000mg / L.

[0105] 接着,来自第2生物处理反应槽3的生物处理水被导入到凝集槽4中。 [0105] Next, a biological reaction from the second biological treatment tank 3 is introduced into the treated water in the coagulation tank 4. 该凝集槽4是由导入有生物处理水的第I凝集部(后述的表I中记作“No. 2-1凝集部”)4A与导入有来自第I凝集部4A的水的第2凝集部4B(后述的表I中记作“No. 2-2凝集部”)构成的双槽式生物处理反应槽,生物处理水首先在第I凝集部4A中添加无机凝集剂后受到凝集处理,之后,进一步在第2凝集部4B中添加pH值调整剂及/或高分子凝集剂,而使絮凝体粗大,然后,凝集处理水被送到第2浮选槽5,添加浮选助剂且利用浮选法使凝集絮凝体固液分离。 The coagulation tank 4 is introduced with a first portion I aggregated biologically treated water (to be described later in Table I, referred to as "No. 2-1 aggregated portion") and 4A into which water from the first I aggregated second portion 4A after the aggregated portion 4B (described later in table I, referred to as "No. 2-2 aggregated portion") Dual Chamber biological treatment reaction tank constituted biologically treated water is first added an inorganic coagulant in section I of 4A aggregated by aggregation process, then, is further added in the second aggregated portions 4B pH value adjustment agent and / or a polymer flocculant, the coarse flocs, and then, the treated water is supplied to the aggregation of the second flotation tank 5, a flotation aid was added agent and the aggregated floc solid-liquid separation using flotation.

[0106] 然后,对于第2浮选槽5的分离水,在过滤装置6中去除残留SS,之后在RO膜分离装置7中进行RO膜分离处理,取出渗透水作为处理水。 [0106] Then, for the second flotation separation of the water groove 5 in the filter device 6 to remove residual SS, followed by RO membrane separation processing in the RO membrane separation apparatus 7, the permeated water taken out as treated water.

[0107] 图1(b)中的有机性排水的处理装置中,代替图1(a)中的第2生物处理反应槽3的曝气槽,而设置散气管8A以及槽外具有膜组件20的槽外型MBR方式生物处理反应槽,作为第2生物处理反应槽8,且利用泵(bump) P,将第2生物处理反应槽8中的混合液传送给膜组件20,使其浓缩、循环,省略了凝集槽4以及第2浮选槽,而其他结构均与图1(a)所示的装置相同。 Processing means (b) in the organic discharged [0107] FIG. 1 in place of 1 (a) in the second biological treatment in the aeration tank 3 reaction tank, is provided outside the diffusing tube having a membrane 20 and a groove 8A MBR groove shape of biological treatment of the reaction tank, the reaction as the second biological treatment tank 8, and a pump (bump) P, the second biological treatment tank the reaction mixture was transferred to a membrane module 8 20, it was concentrated, cycle, the coagulation tank 4 is omitted and the second flotation cells, while other configurations are the same as shown in FIG. 1 (a) device. 图1(b)中,对于与图1(a)所示的部件具有相同功能的部件,使用相同符号。 FIG 1 (b), for the member shown in FIG. 1 (a) components having the same functions, the same reference numerals.

[0108] 图I (b)所示的有机性排水的处理装置中,第I浮选槽2的分离水被导入到作为第2生物处理反应槽8的槽外型MBR方式生物处理反应槽中,实施相同的处理。 [0108] FIG. I (B) shown in treatment of organic waste water, the water is separated I, flotation tank 2 is introduced into the second biological treatment tank as the exo manner MBR bioreactor treating the reaction vessel 8 , the same process. 关于该槽外型MBR方式生物处理反应槽的处理条件,优选MLSS浓度为5000mg/L、槽负荷为I. 0Kg-B0D/m3/day、通量为O. 4m3/m2 · day。 MBR process conditions for the appearance of biological reaction tank of the processing tank, MLSS concentration is preferably 5000mg / L, slot load I. 0Kg-B0D / m3 / day, flux O. 4m3 / m2 · day.

[0109] 来自该槽外型MBR方式生物处理反应槽8的生物处理水,在经过生物处理后由槽外的膜组件20进行膜过滤,因此,如图1(a)所示,可不经过凝集处理、浮选分离,而直接导入到RO膜分离装置7内进行处理。 Biological [0109] exo MBR process of biological reaction tank from the treated water tank 8, a membrane module for membrane filtration of the outer groove 20 after the biological treatment, and therefore, FIG. 1 (a) as shown, without going through aggregation treatment, flotation separation, introduced directly to the RO membrane separation device 7 for processing.

[0110] 图1(a)及图1(b)所示的装置中,在RO膜分离装置7的前段进行生物处理及固液分离这2段处理,由此可获得高水质的处理水,而且,可将FI值低的水供给到RO膜分离装置7中,所以,可抑制RO膜分离装置7的膜通量的降低,且可长期稳定地获得处理水。 Means [0110] FIG. 1 (a) and FIG. (B) 1, a biological treatment section 2 and the solid-liquid separation process in which pre-stage RO membrane separation device 7, whereby the high quality of the treated water is obtained, Further, the FI of low water may be supplied to the RO membrane separation apparatus 7, so that the film can be suppressed to reduce flux RO membrane separation apparatus 7, and the long-term stability can be obtained treated water.

[0111] 另外,所谓FI值是用作如下指标,此指标用来判断将水通入RO膜分离装置中进行去离子(deioniztion)处理时,供给到RO膜分离装置的水的水质是否适于RO膜处理。 [0111] The term FI index value is used as follows, this metric is used to determine when water is introduced into deionized (deioniztion) RO membrane separation processing apparatus, the water quality of water supplied to an RO membrane separation device is suitable for RO membrane treatment. 即使水中的溶解有机物或SS的量大致相等,当对所述水进行RO膜处理时,也可能出现膜通量会在处理的早期就降低、以及不会降低的情况,这时,供给到RO的水的FI值会产生差异。 Even if the amount of dissolved organic matter in the water or SS substantially equal to the water when the RO membrane treatment, the flux may also occur in the early treatment is lowered, without degrading and, then, supplied to the RO FI value of water will produce differences.

[0112] FI值可根据以下方法求出:进行操作,即,向具有预定孔径的滤膜(membranefilter)通入样品水,计测过滤预定量所需要的时间后,根据初期的需要时间及通入水预定时间之后的需要时间而求出,该FI值用于判断水质是容易还是不易引起膜污染、膜堵塞。 [0112] FI value can be determined according to the following method: the operation, i.e., the membrane (membranefilter) having a predetermined aperture into the sample water, a predetermined amount of time measured by filtration required, and the time required according to the initial pass after a predetermined time into the water required time is determined, the value of FI for determining water quality is easy or difficult to cause membrane fouling, clogging of the membrane. 一般来说,即便是FI值小于等于5的水质,也有时会被允许作为供给到RO的水(即RO的供水),但通常来说,希望是FI值小于等于3的水质。 In general, even if the quality is equal to FI value of less than 5, it may also be allowed as the water supplied to the RO (i.e., RO water supply), but generally it is desirable quality is smaller than or equal FI 3. 因此,本发明中,当使用RO膜分离装置作为高度处理机构时,优选利用生物处理及固液分离这2段处理来获得FI值小于等于3的水,而作为供给到RO膜分离装置的水。 Accordingly, the present invention, when used as a RO membrane separator processing mechanism height, preferably using biological treatment and solid-liquid separation process to obtain these two segments FI of 3 or less water, as water is supplied to the RO membrane separation apparatus .

[0113][实施例] [0113] [Example]

[0114] 以下,列举实施例及比较例,对本发明进行更具体的说明。 [0114] Hereinafter, Examples and Comparative Examples mentioned embodiment, the present invention will be more specifically described.

[0115][实施例I] [0115] [Example I]

[0116] 图1(a)所示的装置中,将主成分为四甲基氢氧化铵(TMAH)的为如下水质的工厂排水作为原水,以2000L/day的处理水量进行处理。 Means [0116] shown in FIG. (A) 1, a main component is tetramethylammonium hydroxide (TMAH) for water quality as factory wastewater as raw water, process water to 2000L / day processed. 另外,可推断,该原水的生物处理中磷的量不足,因此,以使TOC : P=IOO : 3的方式向原水中添加磷酸进行处理。 Further, inferred, an insufficient amount of the raw water is biologically treated phosphorus, therefore, to make the TOC: P = IOO: 3 embodiment the phosphoric acid treated raw water. 另外,作为浮选助剂,使用油酸钾。 Further, as flotation aids, using potassium oleate.

[0117] <原水水质> [0117] <raw water>

[0118] S-TOC :328mg/L [0118] S-TOC: 328mg / L

[0119] Kj-N :76mg/L [0119] Kj-N: 76mg / L

[0120] PO4-P :0. 8mg/L [0120] PO4-P:. 0 8mg / L

[0121] 表I中表示所使用的装置的规格及处理条件。 [0121] Table I indicates the specifications and the processing conditions used in the apparatus.

[0122] 而且,表2中表示各部分的水质,表3中表示添加到第I、第2生物处理反应槽中的载体的比重。 [0122] Further, Table 2 shows the quality of each part, in Table 3 is added to the first I, second biological treatment tank reaction gravity of the carrier.

[0123][实施例2] [0123] [Example 2]

[0124] 图1(b)所示的装置中,与实施例I中的处理情况相同,将工厂排水作为原水,以2000L/day的处理水量进行处理。 Apparatus shown in [0124] FIG. 1 (b), the same process as in the case of Example I, the factory wastewater as raw water, process water to 2000L / day processed. 另外,可推断,该原水的生物处理中磷的量不足,所以,以使TOC : P = IOO : 3的方式将磷酸添加到原水中进行处理。 Further, inferred, an insufficient amount of biological treatment of the phosphorus raw water, so as to make the TOC: P = IOO: 3 embodiment is added to the raw water is processed phosphoric acid. 作为浮选助剂,与实施例I相同,使用油酸钾。 As flotation aids, the same as in Example I, using potassium oleate.

[0125] 表I中表示所使用的装置的规格及处理条件。 [0125] Table I indicates the specifications and the processing conditions used in the apparatus.

[0126] 而且,表2中表示各部分的水质,表3中表示添加到第I生物处理反应槽中的载体的比重。 [0126] Further, Table 2 shows the quality of each part of Table 3 indicates the proportion of I is added to the biological treatment tank to support the reaction.

[0127][比较例I] [0127] [Comparative Example I]

[0128] 设置沉淀槽(以下称作“第I沉淀槽”)来代替实施例I中的第I浮选槽,在沉淀槽中对第I生物处理反应槽的生物处理水进行固液分离,除此以外,均以与实施例I相同的方式进行处理。 [0128] provided precipitation tank (hereinafter referred to as "first precipitation tank I") was used instead of Example I I flotation embodiment, solid-liquid separation in a precipitation tank I the first biological treatment tank reactor biological treatment of water, in addition, they are treated in the same manner as in Example I embodiment.

[0129] 表I中表示所使用的装置的规格及处理条件。 [0129] Table I indicates the specifications and the processing conditions of the device used.

[0130] 而且,表2中表示各部分的水质,表3中表示添加到第I、第2生物处理反应槽中的载体的比重。 [0130] Further, Table 2 shows the quality of each part, in Table 3 is added to the first I, second biological treatment tank reaction gravity of the carrier.

[0131][比较例2] [0131] [Comparative Example 2]

[0132] 设置凝集槽及沉淀槽(第I沉淀槽)来代替实施例I中的第I浮选槽,在凝集槽(包括第I凝集部(后述的表I中记作“No. 1-1凝集部”)及第2凝集部(后述的表I中记作“No. 1-2凝集部”)的双槽式的凝集槽)中,对第I生物处理反应槽I的生物处理水进行凝集处理,之后在沉淀槽进行固液分离,除此以外,均以与实施例I相同的方式进行处理。 [0132] flocculating tank and a settling tank provided (first precipitation tank I) instead of the first flotation cell I Example I embodiment, in the coagulation tank (including the first I aggregated portion (described later in Table I, referred to as "No. 1 ) -1 is aggregated portion ") and a second table I aggregated portion (described later referred to as" No. 1-2 aggregated portion ") of the dual-slot aggregation tank, biological treatment of the first bioreactor I I of water treatment aggregation treatment, followed by solid-liquid separation in the precipitation vessel, except, are treated in the same manner as in Example I embodiment.

[0133] 表I中表示所使用的装置的规格及处理条件。 [0133] Table I indicates the specifications and the processing conditions of the device used.

[0134] 而且,表2中表示各部分的水质,表3中表示添加到第I、第2生物处理反应槽中的载体的比重。 [0134] Further, Table 2 shows the quality of each part, in Table 3 is added to the first I, second biological treatment tank reaction gravity of the carrier.

[0135] [表I] [0135] [Table I]

[0136] [0136]

Figure CN101274809BD00121

[0137] [0137]

Figure CN101274809BD00131

[0138] ※I :3mm见方的聚氨酯海绵表观容量 [0138] ※ I: 3mm square urethane sponge apparent capacity

[0139] ※2 :38wt% (重量百分比)的三氯化铁水溶液 [0139] ※ 2: 38wt% (by weight) aqueous solution of ferric chloride

[0140] ※3 :通过添加NaOH进行调整 [0140] ※ 3: adjusted by adding NaOH

[0141] ※彳:填充有砂、无烟煤的双层过滤装置 [0141] ※ left foot: filled with sand, anthracite double filter means

[0142] ※5 :浮选助剂:油酸钾4mg/L [0142] ※ 5: Flotation aid: potassium oleate 4mg / L

[0143][表 2] [0143] [Table 2]

[0144] [0144]

Figure CN101274809BD00141

[0145]※测试方法:ASTM D4189-95 [0145] ※ Test Method: ASTM D4189-95

[0146][表 3] [0146] [Table 3]

[0147] [0147]

Figure CN101274809BD00142

[0148] 根据以上结果,可知如下内容。 [0148] From the above results, it was found the following.

[0149] 实施例1、2中,在第I生物处理反应槽I中,可去除原水中的大部分有机物,而且可在进行自我消化之前将微生物体作为SS,在第I浮选槽2中对所述微生物体无凝集地进行固液分离并去除。 [0149] Examples 1 and 2, in the first biological treatment reactor I I in, can remove most of the organic raw water, but may be performed before the self-digestion microorganisms as SS, I, in the flotation tank 2 the aggregation of microorganisms without the solid-liquid separated and removed. 而且,实施例I中,进一步在第2生物处理反应槽3中对第I生物处理反应槽I的无凝集的分离水进行处理,这样,可避免因溶解金属盐的析出所产生的载体比重增加及载体沉淀,进一步高度分解所残留的有机物,并且,通过在第2浮选槽5中去除SS,结果相比于比较例I及2,可获得S-TOC更低的处理水。 Further, in Example I, no further separation of water treated in the reaction tank 3 aggregation process in the first reactor I I biological organisms in the second process, so that the carrier can avoid an increase in the proportion of the metal salt due to dissolution and deposition of the resulting the precipitate and a carrier, further decomposition of the remaining organic height, and, by removing the SS in the second flotation tank 5, as compared to the results of Comparative Examples I and 2, a lower S-TOC obtained treated water.

[0150] 与此相对,比较例I中,因使用了沉淀槽而非浮选槽,所以,SS的分离性较差,对后段生物处理造成负荷,使有机物的去除性、凝集性、过滤性恶化。 [0150] On the other hand, in Comparative Example I, instead of the use of a flotation cell sedimentation tank, so that poor separability SS, causing the load to the latter stage biological treatment, the removal of organic substances, cohesiveness, filtered deterioration. 比较例2中,因使用了凝集槽及沉淀槽来代替浮选槽,所以,SS的去除性优良,但后段载体流动性明显恶化,所以,S-TOC恶化。 In Comparative Example 2, the use of the flocculating tank and a settling tank in place of the flotation tank, so that, SS removal is excellent, but a marked deterioration in the segment carrier mobility, therefore, S-TOC deteriorated.

[0151] 另外,在使用槽外型MBR方式生物处理反应槽来作为第2生物处理反应槽的实施例2中,S-TOC的去除性及RO膜处理水质良好,而且通量(渗透通量(permeation flux))也稳定。 [0151] Further, the use of biological treatment tank shape MBR reaction tank as in Example 2 Reaction biological treatment tank 2, the removal of the S-TOC RO membrane treatment and water quality is good, and the flux (permeation flux (permeation flux)) is also stable.

Claims (3)

1. 一种有机性排水的处理装置,其特征在于包括: 具有生物膜的流动床式的第I生物处理反应槽,对有机性排水进行生物处理,所述有机性排水的溶解性总有机碳的浓度为200〜25000mg/L ; 无凝集且加压浮选分离方式的第I固液分离机构,对从所述第I生物处理反应槽流出的生物处理水进行固液分离; 膜分离活性污泥式的第2生物处理反应槽,对经所述第I固液分离机构分离的分离水进行生物处理;以及高度处理机构,包括膜分离机构,且对来自所述第2生物处理反应槽的生物处理水进行处理。 An apparatus of processing organic waste water, comprising: I a first biological treatment tank biofilm reactor fluidized bed, the organic discharged water biological treatment, the soluble organic discharged TOC concentration 200~25000mg / L; I no agglutination of solid-liquid separation, and the pressing mechanism floatation separation method, the biological treatment of the reaction effluent from the first tank I biologically treated water solid-liquid separation; membrane separation active fouling mud-type second biological treatment tank reactor, separation of water through the solid-liquid separation mechanism I is isolated biological treatment; and a height processing means comprises a membrane separation means, and from said second biological treatment tank reactor biological treatment of water for processing.
2.根据权利要求I所述的有机性排水的处理装置,其特征在于其中所述的第I生物处理反应槽的溶解性BOD去除率为30〜99%。 The treatment of organic waste water according to claim I, characterized in that the soluble BOD removal I wherein said biological treatment of the reaction vessel is 30~99%.
3.根据权利要求I所述的有机性排水的处理装置,其特征在于还包括: 向由所述第I固液分离机构固液分离的水中添加浮选助剂的机构。 3. The treatment of organic waste water according to claim I, characterized by further comprising: adding a flotation aid the separation means by means of the solid-liquid separation I of water.
CN 200810088041 2007-03-30 2008-03-27 Treatment apparatus for organic wastewater CN101274809B (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
JP2007091666A JP5223219B2 (en) 2007-03-30 2007-03-30 Organic wastewater treatment equipment
JP2007-091666 2007-03-30

Publications (2)

Publication Number Publication Date
CN101274809A CN101274809A (en) 2008-10-01
CN101274809B true CN101274809B (en) 2013-01-09

Family

ID=39971971

Family Applications (1)

Application Number Title Priority Date Filing Date
CN 200810088041 CN101274809B (en) 2007-03-30 2008-03-27 Treatment apparatus for organic wastewater

Country Status (3)

Country Link
JP (1) JP5223219B2 (en)
CN (1) CN101274809B (en)
TW (1) TWI494281B (en)

Families Citing this family (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP5444684B2 (en) * 2008-10-21 2014-03-19 栗田工業株式会社 Organic wastewater treatment method and treatment equipment
TWI385128B (en) * 2008-12-19 2013-02-11 Ind Tech Res Inst Anaerobic non-woven membrane bioreactor and method for treating wastewater
JP5581669B2 (en) * 2009-03-10 2014-09-03 株式会社日立製作所 Water treatment method, water treatment member and water treatment facility
JP5205316B2 (en) * 2009-03-23 2013-06-05 株式会社神鋼環境ソリューション Wastewater treatment method
TWI568687B (en) * 2009-06-15 2017-02-01 沙烏地阿拉伯油品公司 Suspended media membrane biological reactor system and process including suspension system and multiple biological reactor zones
CN102781850B (en) * 2010-03-05 2014-12-24 栗田工业株式会社 Water treatment method and process for producing ultrapure water
JP5753668B2 (en) * 2010-06-22 2015-07-22 株式会社神鋼環境ソリューション Waste water treatment method and waste water treatment equipment
JP5914964B2 (en) * 2010-10-18 2016-05-11 栗田工業株式会社 Ultrapure water production method
JP2012205990A (en) * 2011-03-29 2012-10-25 Kurita Water Ind Ltd Treatment apparatus of organic wastewater
KR102021627B1 (en) 2012-01-11 2019-11-04 쿠리타 고교 가부시키가이샤 Reverse osmosis treatment process
JP5986819B2 (en) * 2012-06-18 2016-09-06 前澤工業株式会社 Water treatment method and equipment
JP5828327B2 (en) * 2013-02-13 2015-12-02 栗田工業株式会社 Method for processing development wastewater in color filter manufacturing process
CN103693730B (en) * 2013-11-28 2015-08-05 内蒙古工业大学 A kind of device and method of supercritical water oxidation method process high concentration hard-degraded organic waste water
JP6554781B2 (en) * 2013-12-26 2019-08-07 栗田工業株式会社 Operation method of reverse osmosis membrane device and reverse osmosis membrane device
JP2016117017A (en) * 2014-12-19 2016-06-30 三浦工業株式会社 Recovery filtration unit
JP2016117018A (en) * 2014-12-19 2016-06-30 三浦工業株式会社 Recovery filtration unit
JP2016117016A (en) * 2014-12-19 2016-06-30 三浦工業株式会社 Recovery filtration unit
JP6015811B1 (en) * 2015-05-19 2016-10-26 栗田工業株式会社 Water treatment method and water treatment apparatus
JP6318193B2 (en) * 2016-05-18 2018-04-25 前澤工業株式会社 Water treatment method and equipment

Family Cites Families (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6139120B2 (en) * 1978-02-15 1986-09-02 Mitsui Miike Machinery Co Ltd
JPH0729115B2 (en) * 1990-03-23 1995-04-05 株式会社荏原総合研究所 Processing method of raw sewage system sewage
JP3335500B2 (en) * 1994-08-03 2002-10-15 シャープ株式会社 Wastewater treatment device and a wastewater treatment method
TW387864B (en) * 1996-10-09 2000-04-21 Hoechst Ag Biological waste water treatment at high sludge concentrations
JPH10202281A (en) * 1997-01-28 1998-08-04 Maezawa Ind Inc Waste water treating device
JP3947588B2 (en) * 1997-01-30 2007-07-25 前澤工業株式会社 Wastewater treatment equipment
JPH10296287A (en) * 1997-04-30 1998-11-10 Shinko Pantec Co Ltd Method and device for treating water containing organic matter
JP3258600B2 (en) * 1997-06-30 2002-02-18 神鋼パンテツク株式会社 Of organic matter-containing water treatment method and apparatus
JP2002307088A (en) * 2001-04-11 2002-10-22 Hitachi Plant Eng & Constr Co Ltd Wastewater treatment apparatus
JP4552482B2 (en) * 2004-03-31 2010-09-29 栗田工業株式会社 Organic wastewater treatment method
JP2006000828A (en) * 2004-06-21 2006-01-05 Japan Organo Co Ltd Organic wastewater treatment method
JP4591678B2 (en) * 2004-12-14 2010-12-01 栗田工業株式会社 Biological treatment equipment
TWI300059B (en) * 2004-12-20 2008-08-21 Ind Tech Res Inst Anaerobic biological wastewater treatment system and process
JP4997724B2 (en) * 2005-08-02 2012-08-08 栗田工業株式会社 Organic wastewater treatment method

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
JP特开平10-296287A 1998.11.10

Also Published As

Publication number Publication date
CN101274809A (en) 2008-10-01
TWI494281B (en) 2015-08-01
TW200848375A (en) 2008-12-16
JP5223219B2 (en) 2013-06-26
JP2008246386A (en) 2008-10-16

Similar Documents

Publication Publication Date Title
Stephenson et al. Membrane bioreactors for wastewater treatment
US6416668B1 (en) Water treatment process for membranes
EP1461141B1 (en) Method of using water soluble polymers in a membrane biological reactor
Gander et al. Aerobic MBRs for domestic wastewater treatment: a review with cost considerations
RU2342330C2 (en) System and method for treatment of acid sewage waters
Trussell et al. The effect of organic loading on process performance and membrane fouling in a submerged membrane bioreactor treating municipal wastewater
Mutamim et al. Membrane bioreactor: Applications and limitations in treating high strength industrial wastewater
TWI410378B (en) Wastewater treatment plant containing organic matter and its handling method
US20020003116A1 (en) System and method for removal of arsenic from aqueous solutions
US4956093A (en) Wastewater treatment process
US7931808B2 (en) Sequencing batch reactor with continuous membrane filtration and solids reduction
Li et al. Treatment of synthetic wastewater by a novel MBR with granular sludge developed for controlling membrane fouling
AU2004289490B2 (en) Installation and method for the purification of an aqueous effluent by means of oxidation and membrane filtration
Skouteris et al. The effect of activated carbon addition on membrane bioreactor processes for wastewater treatment and reclamation–a critical review
Mutamim et al. Application of membrane bioreactor technology in treating high strength industrial wastewater: a performance review
JP4508694B2 (en) Water treatment method and apparatus
CN1980728A (en) Method and apparatus providing improved throughput and operating life of submerged membranes
WO2007019617A1 (en) Biological phosphorous removal
JP2002320979A (en) Method and system for treating metal-containing drainage
KR20080109860A (en) Hybrid membrane module, system and process for treatment of industrial wastewater
Choi et al. The effects on operation conditions of sludge retention time and carbon/nitrogen ratio in an intermittently aerated membrane bioreactor (IAMBR)
Chmiel et al. Concepts for the treatment of spent process water in the food and beverage industries
JP2001070967A (en) Cleaning system for laundry waste water
JP4492268B2 (en) Biological treatment equipment
Ng et al. Optimization of membrane bioreactors by the addition of powdered activated carbon

Legal Events

Date Code Title Description
C06 Publication
C10 Entry into substantive examination
C14 Grant of patent or utility model