TW200932688A - Method and apparatus for biologically treating organic matter-containing water - Google Patents

Abstract

A method for biologically treating organic matter-containing water is provided to prevent membrane from contamination when biologically treating the organic matter-containing water as raw water for a pure water production. Herein, an anaerobic sludge containing methanogen is maintained in a reactor 110, and then the organic matter-containing water, which mainly contains monomer organism (s. g. tetramethylammonium hydroxide) which can be biologically decomposed by methanogen, as treated water is provided from a raw water tube 130 to the reactor 110 for using methanogen in an anaerobically biological treatment. In a membrane separation unit 112 disposed ouside the reactor 110, a solid-liquid separation is performed by a treating solution obtained by the anaerobically biological treatment, so that a separation water in which solids is separated is acquired. Thereafter, the separation water undergoes a desalinating treatment in a reverse osmosis membrane apparatus 114, thereby being a raw material of the pure water production.

Description

200932688 VI. Description of the Invention: [Technical Field] The present invention relates to a biological treatment method and apparatus for anaerobic treatment of water containing organic matter, and more particularly to a drainage The biological treatment is carried out and used as a biological treatment method for raw water for pure water production and cracking. [Prior Art] 参 一般 一般 一般 一般 一般 一般 一般 一般 一般 一般 一般 一般 一般 一般 一般 一般 一般 一般 一般 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需 需Suitable for the treatment of wastewater containing complex = polymer (polymer) compounds (eg food drainage). In addition, the hydrolysis rate of high molecular organic matter in the anaerobic biological treatment towel is slow, because the hydraulic retention time is required (Hydraulic Retenti〇) n Time) is set to 3 = two or more. For this, the standard hydraulic retention time for green biological treatment is short between the fathers and fathers, which is about 5 days. The body of the water is used to read and use pure water and discharge it. = In addition to the exclusive water recycling, that is, in the biological treatment of organic matter-containing water containing organic matter, the previous treatment ° when the organic matter-containing water contains nitrogen, the oxygen compound is oxidized under oxygen conditions The production of nitric acid and oxygen = denitrification. In addition, the aerobicity = temple preservation 4 is carried on the carrier to increase the biological treatment tank. Thus "the speed (for example, Japanese Patent Laid-Open No. 9-2009326) 88 187785. When using a carrier, for example, the removal rate of organic matter in each biological treatment tank can be increased to about 1 kg-COD/m3/day~2 kg-COD/m7day. When the obtained treatment liquid is reused in the production of pure water, the treatment liquid is treated by a solid-liquid separation device to separate the microorganisms, and then subjected to desalting treatment by a reverse osmosis membrane (R0 membrane) separation device or the like (for example, Japanese Patent Special) Open 20〇7—175582). As mentioned above

------- When you use the raw water produced by the non-intermediate pure water to reuse it, it is usually treated with a membrane separation device. However, the separation membrane is clogged due to the operating conditions or the quality of the water to be treated. In particular, when the membrane is separated from the biological treatment liquid, the microorganism itself and the viscous substance generated by the microorganism adhere to the membrane surface. The tendency to block. The viscous substance produced by microorganisms has a hard-to-dissociate property mainly composed of a polymer organic substance, and the amount of production thereof is roughly proportional to the amount of microorganisms to which the biological lasing is applied: the ground is enlarged. Therefore, in the case of using an aerobic microorganism biological treatment towel having a large proliferation rate, the amount of the polymer organic substance produced is also large. When the biological treatment tank to which the carrier is added, the amount of microorganisms is changed, so that the amount of production of molecular organic matter is increased. The increase in anaerobic microorganisms is relatively less than that of aerobic microorganisms. However, the anti-blue biological treatment material is a phenomenon in the liquid. Ding (4) Sexual biological treatment, there are due to the production of microorganisms 5 200932688 Qiao dyed reverse osmosis membrane. On the other hand, when performing anaerobic biological treatment, although the possibility of membrane fouling due to the production of microorganisms is low, the possibility of membrane fouling due to residual organic substances or decomposition intermediates in the treatment liquid becomes high. In addition, when the microorganisms contained in the treatment liquid are separated after biological treatment of the drainage, if a coagulation sedimentation or a pressurized floating method is used, the separation is not sufficient, and the separated water contains microorganisms. The body will contaminate the reverse osmosis membrane in the latter stage. In particular, when adding a carrier to the biological treatment tank, it is necessary to use a sieve or the like in order to carry out solid-liquid separation of the carrier, but the particle size of the carrier which increases the surface area and increases the activity is small, so that the grid is easily clogged, in order to avoid This phenomenon necessitates the use of a complex solid-liquid separation device or a large sink. On the other hand, when the biologically treated treatment liquid is subjected to solid-liquid separation by the impregnation membrane provided in the biological treatment tank, the microorganisms and the like can be well separated, so that the reverse osmosis membrane contamination in the latter stage can be prevented. However, there is a problem that the impregnated membrane itself is clogged, and in particular, when aerobic treatment is performed, there is a problem that the impregnation membrane is clogged by the polymer organic matter generated by the microorganism, and the amount of permeated water is lowered. Further, when the organic substance-containing water contains a nitrogen component, in the aerobic biological treatment for removing the nitrogen component, the organic nitrogen is inorganicized by the microorganism to generate ammonia, which is aerobic nitrifying bacteria ( Nitrifier) oxidizes to form nitrous acid or nitric acid, which reduces the positive value of the liquid in the tank. Therefore, it is necessary to add a base for neutralization. Then, when the denitrification treatment of nitric acid is carried out under anaerobic conditions, the nitric acid or nitrous acid is reduced to nitrogen by the anaerobic deuterium gas, and in the process, the pH is raised. Therefore, it is necessary to add an acid for neutralization in the denitrification step. Thus, the acid or the test added for neutralization during the biological treatment becomes the salt load of the reverse osmosis membrane (RO membrane) in the latter stage. As described above, when the reaction is carried out until nitrous acid or nitric acid is formed and then denitrified, nitrous acid or nitric acid which is a strong acid is produced, and as a strong OH ', it is necessary to neutralize a strong acid or a strong one. On the other hand, in the step of oxidizing the nitride, if the biological reaction is stopped at the time point when ammonia is generated, only the weakly-available ammonia is neutralized, and it is not necessary to neutralize the strong acid or the strong test. In order to stop the biological denitrification of the nitrogen compound at the stage of ammonia production, the nitrifying bacteria having a slower proliferation rate may not be propagated in the biological reaction tank. Specifically, if the residence time of the sludge in the biological reaction tank is shortened, the walled fines are washed out from the biological reaction tank without being retained in the tank, so that the reaction is stopped at the stage of ammonia formation. However, in order to allow the nitrifying bacteria to flow out, it is necessary to set the ice retention time of the sludge in the bioreactor to be 4 days or less. When the sludge is retained for about 4 days or less, the organic matter contained in the treated water is not sufficiently decomposed. Therefore, the biologically treated treatment liquid contains a large amount of residual organic matter, and the residual organic matter is used as a matrix in the reverse osmosis membrane device to make the microorganisms proliferate easily. The proliferating microorganisms cause clogging of the membrane in the reverse direction, thereby degrading the desalting performance of the reverse osmosis membrane. As described above, when the organic substance-containing water is biologically treated and reused in pure water production, the drainage treatment process adversely affects the treatment using the reverse osmosis membrane. In addition, when the organic liquid-containing 7 200932688 water is subjected to biological treatment and agglomerated under aerobic conditions, the load on the reverse osmosis membrane device increases due to the addition, and on the other hand, the conductance of the ruthenium and the ruthenium is progressed. The shortening of the sludge retention time is due to the suppression of the reverse side membrane permeability. It is an object of the present invention to prevent the water in the reverse osmosis membrane from being treated in the biological treatment of water containing organic matter in the treatment of water. A method and apparatus for the treatment of permeable membranes, thereby smoothly processing the membrane. In order to solve the above problems, the present invention solves the above problems by biologically treating with water of an anaesthetic substance, and removing the material of the water towel without removing the product. The ammonium salt of the liquid is concentrated in a reverse osmosis membrane unit and then treated separately. In addition, the === treatment is divided into: the use of acid-producing bacteria from the organic matter η: the use of methane-producing bacteria (methods, etc., found to be the cause of membrane fouling = formation, is the acid associated with the acid formation step The present invention is completed by using an acid generating step of an acid-producing microbial group, and the present invention is completed. Specifically, the present invention provides a biological treatment method of water having an organic substance in the following steps, which is to contain an organic substance in the following manner The water is introduced into the anaerobic biological treatment tank; 8 200932688 The anaerobic oxidizing organism is located in the fascinating group of the visceral surface group: =? The treatment liquid obtained by the anaerobic biological treatment is not processed in the biological organism In the case of membrane separation; = separation of _ _ _ silk lysed water. The biological treatment method of water containing organic matter, wherein the sample relative to (four) organic broken ratio method, water material treatment thief And the hoof 4 cut 丨 5c is less than or equal to =) the biological treatment of the water containing the villager as described in (3) it = the above anaerobic treatment process is warmed, and then the above: Reverse osmosis membrane treatment. Lu above the mi = the biological treatment of water with organic matter, where two = machine ==:, alkanolamine, saponin, methyl acetamide, dimethylformamide, dimethyl benzene And any one or more of the ethnic groups composed of acetic acid. (6) A biological treatment device for water containing organic matter, comprising: an anaerobic biological treatment tank, which introduces water containing organic matter, and generates methane by using the generated bacterial group; and the device on the pit is 'in contact with the anaerobic biological treatment tank described above The membrane is subjected to a membrane reverse osmosis membrane device for the treatment liquid discharged from the anaerobic biological treatment tank, and the separated water of the membrane separation device is subjected to treatment. (7) The biological treatment apparatus for organic-containing water according to (6), wherein the organic-containing water towel contains a monomer organic matter in a total organic matter ratio of 70% or more. (8) The biological treatment of the organic-containing water according to (6) or (7), wherein the anaerobic treatment tank has a temperature of the liquid in the tank of 15 or more. C is less than or equal to 4 〇. The operation is carried out, and the treatment liquid is supplied to the membrane separation device and the reverse osmosis membrane device while heating (4) in the anaerobic treatment tank. (9) The biological treatment apparatus for organic-containing water according to (8), further comprising a heat recovery heating device that permeates water of the reverse osmosis membrane device as described above, and uses the recovered heat to heat the anaerobic Sex processing tank. (10) The biological treatment apparatus of the organic substance-containing water according to (6), wherein the membrane separation apparatus comprises a trace amount of (mie na tmtiQn or an ultrafiltration membrane. (11) as described in (6) The biological treatment device for water containing organic matter further includes a cleaning device, and the rib is supplied to the bio-generated gas (biogas) generated in the above-mentioned biological treatment tank to aerate and clean the membrane separation device. (10) Knife-off device (12) - a biological treatment device for water containing organic matter, comprising: an anaerobic biological treatment tank for introducing a group of organic methane-forming bacteria to form decane; a membrane separation device, and the above anaerobic organism The treatment tank is connected for 10 200932688 to discharge the above-mentioned anaerobic biological treatment tank for treating the membrane separation treatment_nuclear, and for the above-mentioned organic matter in the upper surface of the county (four) shrinkage The biological treatment device for water includes a treatment device different from the above-described anaerobic biological treatment tank (: (10) or (10), the biological treatment of the organic-containing water, the second treatment, the concentrated water The apparatus includes an evaporator that guides the above-mentioned concentrated water and takes out eight lx and takes out the residual water. The biological treatment device with organic_water in the middle is '^. ^- Ϊ £ column), tUf, (4) of the above water towel Insoluble chemistry, and separation of solids. Shangchen Fine Water (16) - A biological treatment method for water containing organic matter, including: introduction of water into the anaerobic biological treatment tank containing the A-burning flora The anaerobic biological treatment is carried out, and the treatment liquid obtained by the above anaerobic biological treatment is subjected to membrane separation without aerobic biological treatment, and is carried out by using the separated water obtained by (17) The biological treatment method of the organic substance-containing water according to (16), wherein the organic substance-containing water contains a nitrogen compound. 200932688 (18) The method according to (16) or d 7), wherein the biological treatment of the above-mentioned Han shrink water into the tray t, t ^ of biological treatment; using the evaporator different from the above Make impurities insoluble In the present specification, the organic matter contained in the water to be treated is not specific, and contains not only ❹; The term "total organic carbon" refers to water; the general term for diorganic matter' includes not only non-volatile organic matter, but also volatile organic compounds measured by TOC (Total Organic Carbon) instrument. In addition, fa = compound, preferably a low molecular weight of microorganisms can be directly absorbed, and the proportion of organic molecules is "early organic matter" (for example, it is specific to 7G% with respect to total = j). The so-called "monomer organic matter" is a low-particulate organic substance in which all kinds of organic matter can be directly absorbed by the microorganisms, and the organic matter containing the organic matter is decomposed. Oxygen organisms = The acid-producing flora is difficult to proliferate in the step. According to the knowledge of the present inventors, if the growth of the acid-producing microflora is inhibited, the formation of metabolites by these microorganisms can be prevented from being prevented by the metabolites - the monomeric organic matter cannot be passed through the microbial cell wall. In the present invention, the use of "monomer organic matter" is a term used to mean an organic substance other than such a polymer organic substance. Monomer 12 200932688 A: Lift: used as: the low matrix of the microflora produced by the hospital, the ratio of single ethyl _, =: iso == amine, dimethyl ketoamine, dimethyl sapphire) The water of the machine becomes an appropriate treatment object. This door has 3 in the middle of the month, using the methane-producing flora to be f-line;; sexual biological treatment. The organic matter in the treated water is mainly composed of monomeric organic matter. Because the monomeric organic matter is produced by the hospital: = biodegradation, so n is left untreated by the characteristic of the water to be treated, and the post-separation is prevented by the use of the monomer as a monomer. = methylacetamide, dimethylformamide, dimethyl amide, which contains a relatively high proportion of organic-containing water as a treatment object, and inhibits it, thereby preventing the formation of a large amount of organic For the main body's anaerobic treatment, I have a nitrification reaction. Therefore, when the treated water contains nitriding characters, the 'minus scores in the biological treatment step are: found that when the treated water contains nitrogen compounds and is supplied to the reverse 13 200932688

When the liquid t contains a nitrogen component, the condition that the microorganisms are prone to proliferate in the reverse osmosis membrane device in the reverse osmosis membrane device (for example, the treated sputum water contains 10% 〜 About 30% of the polymer organic matter causes the treated water to contain nitrogen compounds.) It is actively in the anaerobic biological treatment tank, in order to be treated to be well biodegraded to prevent membrane fouling in the latter stage, preferably ^ I was admired by the money in the money. When the water to be treated contains ', 囷 or local molecular organic matter', it will cause decomposition of the organisms that are used as the &-producing flora, and the formation of membrane-contaminated organic molecules. The metabolite of the acid-producing flora, ^ temperature is less than hunger or = 40 CI 彳 30% or so solution, but if - ° is less than or equal to the thief money m is decomposed. (4) If the temperature of the m5 c treatment tank is set to be greater than or equal to hunger less than or equal to 40 words, the content of organic matter other than organic matter is relatively high, and may also be = ❹ as above equal to 3 (rc is less than or equal to thief. The decomposition efficiency of the metabolites of the aphid-producing flora is due to the temperature condition: the temperature condition changes the characteristics of the water to be treated. Specifically, the I condition is 15 ° C or more and less than 3 ° ° C, preferably The ratio of the organic matter in the treated water is greater than or equal to ^ additionally 'when the temperature condition is less than hunger or more than 4G, the proportion of organic matter is set to be greater than or equal to 90%. In addition, if the pH is greater than If it is equal to 6 or less than 9, it can decompose the metabolite of the acid-producing microflora well. If the ρΉ value molybdenum rate is reduced to about 鄕, the pH of the liquid in the tank of the better decomposition tank is adjusted to be equal to or greater than or equal to 9. 6 small substances, the formation of metabolites in the acid-producing microflora is small, that is, the case may be sufficiently high (substantially driven), etc., or the liquid in the tank of the anaerobic biological treatment tank may not be adjusted.

The ammonium salt or the organic salt contained in the water to be treated is a money salt formed by U. Such an ammonium salt reacts with carbon oxide in the anaerobic biological treatment tank to form ammonium hydrogencarbonate. Therefore, when the nitrogen content is contained in the treated water, the pH of the liquid in the tank of the anaerobic biological treatment tank may be in the vicinity of the case where no neutralizing chemicals are added. The treatment liquid towel from the anaerobic biological treatment contains micro-X, so after the separation, the material county is set to remove solids.

The water (separated water) that has been made is decontaminated and becomes a raw material for pure water production. A membrane separation device equipped with a _ can be used for solid-liquid separation. As the separation membrane, an ultrafiltration membrane (UF membrane) or a microfiltration membrane _ membrane may be used, and it is preferred to use a pore diameter (for example, 100 Å or less) having a diameter smaller than that of a normal generation group. membrane. Further, the treatment liquid from the anaerobic biological treatment tank contains carbon guanidine hydrochloride or an organic material which has not been biologically treated, such as anaerobic, biological treatment; The portions of the remaining material are removed in the apparatus, but the other portions are not removed in the membrane separation device and are carried into the reverse osmosis membrane device 15 200932688 for collapse. Therefore, from the reading and sandwiching, 'contains about (7), „: condensed water (salt water, which is different from the water to be treated, and uses ammonium hydrogen citrate or the like. Therefore, it is treated. Chemical or / and physical methods for the salt water into the φ ,,: the choice of oxygen characteristics, such as the biological nitrogen can make the treatment of oxygen-producing biological thieves. Biological removal of any-species microorganisms ^ GtIOphy) or from the # And the value contained in the salt is changed so that the chemical in the brine is added to the impurity in the brine to form a compound, and the chemical used in the second embodiment is as follows: The impurities in the brine are acidified _ sulfuric acid, the protein is two::: acid; (4) the reaction is a physical treatment 'may be steamed, can also be used by '. In order to prevent ammonia from volatilizing in the form of gas = wind (2) The heating can also be aerated. The treatment of the contact with the brine is as follows. For example, the acid is used to make ammonia (amine) not used, and the amount of waste generated by the museum is used. At the same time, the advantages of water recovery are also used. - In addition to semiconductors such as windy waste devices, they are also used in the liquid crystal display industry. In the process of draining the clothes, it is not as good as the food 16 200932688 or the money shaft, the high scores of the children, or all kinds of reason.! 1 μ, the 'anaerobic biological treatment is carried out efficiently. Things and pairs:: The organic-- and the relatively clear drainage contained in the water in the water of the chemical factory are used as the application object. These drainage advantages. Stone, therefore, it is possible to use laboratory experiments to know the processing ability [invention effect ] ❹ There are two conditions for the organic matter to be a monomeric organic matter, and to inhibit the increase of the nitrification reversal due to the addition of Dingsheng, which can inhibit the concentration of salt and the metabolites. Thereby, the separation membrane is prevented from decomposing the organic matter. In the present invention, after the abortion treatment, the aerobic biological treatment can be carried out: a tit; a biological treatment liquid which is sufficiently decomposed. It can suppress the formation of acid and U and f-new property groups. =:===: This can prevent: Unremoved substances in anaerobic treatment == two = other treatments are carried out, thereby improving water recovery rate ,,,,,,,,,,,,,,,, The features and advantages of the description can be more clearly understood, and the following is a detailed description of the present invention. The present invention is described in detail with reference to the present invention. (4) The following is a schematic diagram of a biological treatment device (hereinafter simply referred to as "treatment skirt") of water containing organic matter used in the present invention. The treatment apparatus 1A includes an anaerobic biological treatment tank (hereinafter referred to as "reactor"), a membrane separation device 112, and a reverse osmosis membrane device m. A raw water pipe 130 is connected to the inlet of the reactor at 11 Torr. The reactor 11 is connected to the membrane separation device 112 via a treatment liquid pipe 132, and the membrane separation device 112 is connected to the reverse membrane and the membrane membrane device 114 via a separation water pipe 134. A permeate pipe 136 is connected to the outlet of the reverse osmosis membrane unit 114. The first heat exchanger 121 is provided in the middle of the raw water pipe no, and the second heat exchanger 122 is provided in the middle of the seepage water 136. The first heat exchanger 121 and the second heat exchanger 122 are connected by a fluid tube, and the fluid used for heat exchange is looped between the second heat exchanger 121 and the second heat exchanger. The first heat exchanger 12, the second heat exchanger 122°, and the fluid tube 139 constitute a heat recovery heating device. The reactor 110 is connected to a drain pipe 135 and an exhaust pipe 13 to discharge the reactor (10)_ excess sludge from the sludge pipe 135, and the gas generated in the reactor 110 is discharged from the exhaust pipe 131. The exhaust pipe 131 is connected to the membrane separation device 112, and is configured to be aerated and cleaned by a separation membrane (not shown) provided in the membrane separation and polymerization, and functions as a cleaning device. Further, a return pipe 133 is also connected to the membrane separation device 112, and the outlet end of the return pipe 33 is connected to the reactor 11A. In the reverse osmosis membrane unit 114, a brine tube 137 is connected to the concentration side. In the present invention, the water to be treated is supplied from the raw water f 13G to the reactor 18 200932688 110. It is preferable to supply the water to be treated in which the monomer organic matter accounts for the entire organic matter or more to the reactor no. The suitable operating conditions for the reactor no are, as described above, a pH of 6 to 9 and a temperature of 15 ° C to 4 Torr. 〇 Especially 30 ° C ~ 40 ° C. Under such conditions, when a large amount of a polymer organic substance which does not become a matrix of the methane-producing microbial group is contained, it is possible to prevent membrane contamination by the acid-producing microbial metabolite. The sputum-producing microflora in the reaction 110 can be in the form of granules or floating. The smoldering bacterium is more difficult to form viscous buckwheat than the acid-producing bacterium, so it is difficult to form granulated sludge. . Therefore, the treatment liquid discharged from the anti-bank crying 110 easily contains the reaction in the reactor 110. In the present invention, the membrane separation device 112 is provided in the subsequent stage of the reactor 110, so that the microorganisms contained in the treatment liquid towel can be made good. Ground with separation. A preferred crucible is provided separately from the reactor no as shown in the present embodiment. As the membrane, an ultrafiltration membrane (UF membrane) or a trace amount (MF membrane) can be used, and it is preferable that the pore diameter is smaller than that of the normal acinogen-producing bacteria and the pore diameter is l〇〇nm41. 〇〇nm or less. The module form of the ® e-off device 112 is not particularly limited, but it is preferable that the sludge sent from the reactor 110 is formed in the inside of the membrane separation device η]. For example, a tubular shape can be suitably used: a flat film is used to separate the liquid component of the liquid film from the solid with the solid, and as shown in the present embodiment, if it is set on the reaction eve, it becomes the stomach groove. The type is easy to control the flow of the membrane surface, so that it is preferable from the viewpoint of preventing the membrane from being damaged. In the sample towel of the present embodiment, the membrane separation device 112 is connected to the exhaust pipe 131, and the process liquid is sent from the reactor 110 to the membrane separation device 112 together with the generated gas. The gas is aerated and cleaned while flowing along the water to be treated in the membrane separation device 112. The treatment liquid supplied to the membrane separation device 112 is subjected to solid-liquid separation while passing through the inside of the apparatus, and the separated water from which the solid component is removed is discharged from the permeate side to the outside of the apparatus. On the other hand, the solid concentrated concentrated sludge liquid moves together with the gas in the treated liquid flow path of the membrane separation device 112, and is returned from the return pipe 133 to the reactor n. The growth rate of the smoldering bacteria group is slower than that of the aerobic microorganisms. However, if the sludge concentration in the reactor 110 is maintained at about 4,000 mg/L to 10,000 mg/L by performing such sludge return, The decomposition rate was the same as that in the aerobic biological treatment of the aerobic activated sludge. Therefore, when the sludge concentration is in the above range, the hydraulic retention time of the reactor 11 () can be made to be about 5 days to 2 days. The excess sludge was appropriately extracted from the reactor 11 through the sludge discharger 135, and the sludge concentration in the reactor 11 was adjusted. The separated water of the solid component is separated from the membrane separation device 112, and is desalted in the reverse osmosis membrane device 114 provided in the subsequent stage of the membrane separation device 112 to be used as raw water for pure water production. In the present embodiment, the reactor 11 is operated at 30 C to 40 ° C, and the temperature of the treatment liquid is also 30. 〇40. (In the case where the aerobic treatment is not performed or the temperature is not artificially lowered, the treatment liquid discharged from the reactor 110 is sent to the membrane separation device 112 and the reverse osmosis membrane device 114. About 30 ° C Since the liquid is easily subjected to reverse osmosis membrane separation, the flux (1) ux of the reverse osmosis membrane device 114 can be increased by feeding the treatment liquid from the reactor 110 to the reverse osmosis membrane device 114' in a warm state. 20 200932688 = Inverse, the liquid removed from the membrane device 114 is still warm. Therefore, in the present embodiment, the heat exchange in the heat exchanger of the heat exchanger 122 is replaced by the heat exchange of the permeation money by the exchange of the permeated water pipe 136 which discharges the permeated water 136. The second shell is sent to the i-th heat exchanger 121 via the fluid pipe 139. In the first two = 121, the raw water sent from the raw water pipe 13 is heated by the heated heat exchange medium and sent to the reactor 110. e

The reverse osmosis county 114 is treated to remove the permeated water of the salt, and the raw water for the manufacture of the swill. Specifically, in the reverse osmosis membrane device 114, a device for arranging the desulfurization device sub-exchange device and the line sterilizing device pure water producing device in the rear stage, the permeated water discharged from the 2-permeation 114 is treated by the machine types. In this way, pure 7 can be produced. If the secret water is treated in the other (four) line, the water will be recycled through the water. <Examples [Embodiment 1] As Example 1, an experiment was carried out using the experimental device 3 of the processing device (10) shown in the figure. The reaction II 110 of the experimental apparatus was operated under the conditions of an effective volume and an m hydraulic retention time of 0.5 days. In the reactor U0, the granules discharged from the anaerobic reaction for treating methanol are sterilized in a liquid towel to be treated, which will be described later, to maintain the floating sludge. The concentration of the reactor-like rotary sludge was 4, _mg/L, and 4G% of the existing amount (wet weight comparison) was the formation of smoldering _, and 6 (%) was the self-decomposing residue of the smoldering group. 21 200932688 As the water to be treated, organic-containing water having a total organic carbon concentration of 750 mg/L, a nitrogen concentration of 218 mg/L, and a phosphorus concentration of 1.0 mg_P/L was used. The composition of total organic matter is: tetramethylammonium hydroxide concentration is 25〇mg/L, monoethanolamine concentration is 250mg/L, acetic acid concentration is 250mg/L, and the content ratio of monomer organic matter to total organic carbon is substantially 100. %. The treated water was warmed so that the temperature of the liquid in the tank in the reactor 11 was 35 C, and the pH of the liquid in the tank was adjusted to 75. One or four tubular UF membranes (ultrafiltration enthalpy, pore diameter: 30 nm) having a diameter of 0.52 cm were disposed in the membrane separation device ❹ n2, and the biological treatment liquid discharged from the reactor 110 was flowed into the tube together with the gas. Return to the reactor 11 with gas. The permeate amount (flux) of the membrane separation device 112 was 1 〇 m/day. Knife The continuation of the 30-day experiment under the above conditions revealed that the flux of the membrane separation device ii2 was maintained at the above value, and the water-passing resistance was at most 3 kPa. The concentration of T〇c of the separated water obtained from the membrane separation device 112 was in the range of 3 mg/L to 4 mg/L during the experiment, and the TOC removal rate was 99.5%. Further, the reverse osmosis membrane device 114 (a spiral reverse osmosis membrane device having a wholly aromatic polyamine-based ultra-low pressure membrane as a osmium membrane) was introduced into the separated water at 750 kPa.

Desalination treatment The amount of permeate water after 2 hours passed was maintained at 90% of the water supply. T J

[Example 2] In Example 2, an MF membrane having a pore diameter of 400 nm was used instead of the UF membrane used in Example 1. In the same manner as in the Example, the separation of the toc concentration from the membrane separation apparatus equipped with the MF membrane was in the range of 3 mg/L to 4 mg/L as in the first embodiment. In addition, 22, 2009, the membrane flux separation device 112 has a flux-recovery method using the reverse osmosis membrane device 114 for = water: the same amount as the application example 1, even if the water is passed through the fG treatment. In ancient times, I was still at the initial 90% 〇 ^ ^ maximum, M kPa, higher than Example 1. The average diameter of the smoldering bacteria in the sludge in the reactor 110 is 800 nm'. Therefore, it is presumed that when the MF membrane is used, the smoldering bacteria will leave the pores and cause membrane clogging. Gland ^

[Comparative Example 1] The characteristics of the water to be treated were changed in Comparative Example 1. Specifically, in the treated water used in Example 1, 5 〇〇 mg_T〇c/L of sewage sludge was added, and the ratio of monomer organic to total organic carbon was adjusted to 58%. Further, since such treated water is used, the composition of the sludge in the reactor 11 is also changed. Specifically, the sludge concentration of the floating sludge in the reactor 11 used in Comparative Example 1 was 8, 〇〇〇mg/L, and 20% of the existing amount (wet weight comparison) was the decane-forming bacteria group. The acid-producing flora is 2%. The remaining 60% is from bacteria and self-decomposing sludge from sewage sludge. Except that the characteristics of the water to be treated were changed in this way and the microbial phase in the reactor 11 was changed, the experiment was carried out under the same conditions as in Example 。. As a result, the flux of the membrane separation device 112 was slowly lowered, and the water flow resistance exceeded 30 kPa 20 days after the start of the experiment. In Comparative Example 1, the TOC concentration of the separated water of the membrane separation device 112 was 18 mg/L to 43 mg/L. [Example 3] In Example 3, the amount of sewage sludge added to the water to be treated was set to 300 mg-TOC/L (the ratio of monomer organic matter was about 71%). The composition of the sludge in the reactor 110 also changes with the change of the water supply. Specifically, the sludge concentration of the floating sludge in the reactor 11 used in Example 3 was 8,000 mg/L, and 3% of the existing amount (wet weight comparison) was a group of the toxin-producing bacteria, and acid generation The flora is 3〇〇/0. The experiment was carried out under the same conditions as in Comparative Example 1, except that the characteristics of the water to be treated and the microorganism phase in the reactor 11 were changed. As a result, the flux of the membrane separation device 112 exhibited the same behavior as in Example i, and the TOC concentration of the separated water was 3 mg/L to 5 mg/L, and the flux of the reverse-dialysis membrane device 114 for treating the separated water was maintained. At 88%. It is shown by the above-mentioned test that if the organic matter in the water to be treated is 7〇0/. When the above is a monomeric organic substance and the anaerobic treatment is carried out using the sludge containing the decane-producing microbial flora, the separation membrane in the latter stage of the biological treatment can be prevented from being clogged. [Reference Example 1] The temperature of the liquid in the tank of the reactor no in Example 3 was set to 沁 °C. As a result, the flux of the membrane separation device 112 decreased, and the water passage resistance exceeded 30 kPa after 7 days. Further, the temperature of the liquid in the tank of the reactor ι 10 was set to 50 〇C separately, and as a result, the flux of the membrane separation device 112 decreased. The water-passing resistance exceeded 30 kPa after 3 days. [Reference Example 2] The pH of the liquid in the tank of the reactor crucible in Example 3 was set to 5. As a result, the water passage resistance of the membrane separation device 112 rises sharply, and the water passage resistance exceeds 30 kPa in the day. Further, the pH value of the liquid in the tank of the reactor 11Q was set to 1 Torr, and as a result, the water-blocking resistance of the membrane separation device il2 was rapidly increased, and the water-passing resistance exceeded 3 kPa after 8 days. 24 200932688 [Comparative Example 2] Ο

In Comparative Example 2, a diffusing means for blowing air inside the reactor was provided, whereby the reactor was made into an aerobic biological treatment tank. The TOC concentration of the treatment liquid flowing out of the aerobic biological treatment tank was 3 mg/L as in the case of Example 1, except that the reactor was changed to aerobicity, and the experiment was carried out under the same conditions as in Example 1. 4 mg/L range. However, the flux ' of the membrane separation device 112 can maintain a predetermined flux for only 20 days. Further, in the liquid in the tank of the aerobic biological treatment tank, the soluble T〇C was contained at a concentration of 200 mg/L. On the other hand, the solubility TOC concentration of the liquid in the tank of the anaerobic reactor of Example 1 was about 1 〇 mg/L. As described above, in Comparative Example 2, the concentration of the soluble T〇c in the liquid in the tank was higher than that in Example i, and the amount of the polymer organic matter constituting the presently soluble TOC and the treated aqueous phase introduced into the aerobic biological treatment tank were as described in Example i. Than, to achieve about the same as the latter. The conversion ratio of the sludge (bacteria) to the organic matter in the water to be treated which is introduced into the biological treatment tank is 0.3 g/g in terms of the aerobic microorganism, whereas in the case of the microorganism, the reading is g/g. Since the polymer organic matter is formed by the recent self-decomposition, it is estimated that the higher the conversion rate, the more organic matter is generated. Further, in Comparative Example 2, in the same manner as in Example ,, the amount of permeated water after 2 G hours was decreased to the result of the treatment of the separated water 2 in which the membrane was separated in the membrane separation device 112. Start to pass water. In Comparative Example 2 and Example i, it was shown that the generation of the polymer organic matter of the dyeable separation membrane can be suppressed by performing the anaerobic biological treatment using the surrounding group instead of the aerobic biological treatment. 25 200932688 Further, in Comparative Example 2, in the microbial population of the aerobic biological treatment tank, the nitrogen component of the nitrifying bacteria in the microbial population of the aerobic biological treatment tank was Weihua. Therefore, the pH of the liquid in the tank of the oxygen-containing biological treatment tank is lowered, and the treatment liquid is ^

1 deteriorated. Therefore, the pH is adjusted to 7 at the time point when the liquid _ ρ Η value in the tank is lower than 5. Further, after continuing to maintain the aerobic condition, the supply of air to the biological treatment tank is stopped to become an anaerobic condition, thereby performing denitrification. When the oxygen transfer is on the job, add the acid acid to the pH tank to 7. Such a batch of Kawasaki: As a result of the treatment of the field and adjusting the pH, the concentration of salts in the treatment liquid is increased. Therefore, the osmotic pressure of the reverse osmosis membrane device in the latter stage of the membrane separation device is increased by about 100 kPa to about 200 kPa as compared with the example '. The rate of the wrist salt of the reverse osmosis membrane device is lowered, so it must be increased by about 15% to 20%. Reverse osmosis membrane device. According to the above experiment, according to the present invention, the anaerobic sludge caused by the organic matter in the treated water body and the anaerobic sludge containing the g group formed by the Jiayuan can be used to reduce the high molecular organic matter contained in the Wei towel. Or the amount of organic matter is not decomposed and the contamination of the separation membrane is prevented. (Second Embodiment) Fig. 2 is a schematic view showing a biological treatment apparatus 200 for water containing an organic substance according to a second embodiment of the present invention. The treatment apparatus 2A includes an anaerobic biological treatment tank (hereinafter referred to as "reactor") 21G, a membrane separation device, a reverse osmosis membrane package f 214, and an in-service tank such as a concentrated water treatment device. A raw water pipe 23 is connected to the inlet of the reactor 210. The reactor 21 is connected to the membrane separation device 212 (4) via a treatment liquid pipe 232, and the membrane separation device 212 is connected to the reverse osmosis membrane device 214 via a separation water pipe 234. A permeate pipe 236 is connected to the outlet of the reverse osmosis 26 200932688 membrane unit 214. The first heat exchanger 221 is provided in the middle of the original water officer 230, and the second heat exchanger 222 is provided in the middle of the seepage director 236. The first hot-parent 221 is connected to the second heat exchanger 222 by the fluid pipe 239, and the fluid used for heat exchange is looped between the first heat exchanger 221 and the second heat exchanger. The first heat exchanger 221, the second heat exchanger 222, and the fluid tube 239 constitute a heat recovery heating device. A drain pipe and an exhaust pipe 231 are connected to the reactor 210. The excess sludge in the reactor 21 is discharged from the sludge g 235, and the gas generated from the exhaust pipe 210 is discharged. The exhaust pipe 231 and the membrane separation device 231 are provided in the membrane separation device by aeration cleaning. In addition, the 臈 separating skirt 212 is also 233 ′. The outlet end of the return pipe 233 is 盥 吕 吕 詈 詈 詈 詈 , , , , , , , , , , , 。 。 。 。 。 In the reverse osmosis membrane f, a brine tube 237 is connected to the side of the wave. Brine tube 237盥

Anammox slot 241 connection. The ', = invention towel' is supplied to the reactor 2iq as an organic-containing water which is treated as water to be treated via a raw water pipe. For example, if U should be used, the preferred operating conditions of the thief 210 are: pH value of 6~$, B~40C, especially 30~4 (TCe if the plexus is at, the degree is == base: r(10) Contamination. It can prevent the hyperthyroidism-producing flora in the reactor 210 produced by the acid-producing metabolites from being granulated or floating in any state of 200932688. The methane-producing microflora is more difficult than the acid-producing microflora. The formation of the viscous material is therefore difficult to form the granular sludge. Therefore, the sludge discharged from the reactor 210 is likely to contain the sludge in the reactor 21. In the present invention, a membrane is provided in the latter stage of the reactor 210. Since the separation device 212 is used, it is preferable to perform solid-liquid separation of the microorganisms contained in the treatment liquid. Preferably, the membrane separation device 212 is provided separately from the reverse = 210 as in the present embodiment. The ruthenium film (10) film or the micro film (MF film) is preferably a straight U having a pore diameter smaller than that of the gamma-producing bacterium of the pass f. Specifically, the pore diameter is about or less than or equal to or less than nm. Therefore, the module material of the ίίΐ212 is not limited, but it is better to block 21. The sludge to be fed in the membrane separation device 212 is difficult to control the membrane surface flow rate by using the tubular method or the flat separation of the di-membrane and the solid component. Therefore, it is preferable to prevent film defects and δ. At the point where the separation device 212 is connected, the exhaust pipes 23!, 212 are connected. The gas is sent from the reactor 21G to the membrane separation device. The separation of the amine and the hydrazine is carried out by moving the device to the treated water flow path in the device 212. The separation of the component contained in the membrane separation device during the separation of κΓγ was separated by the liquid, and the concentrated condensed U was removed from the permeate side. On the other hand, the solid component is moved in the rich path, and is returned from the liquid to be treated k g 233 of the membrane separation device 212 to the reactor 21A. 200932688 The decane-producing microbial population has a slower proliferation rate than the aerobic microorganisms, but the sludge is returned to the right and the sludge concentration in the reactor 210 is maintained at 4,000 mg/L~10, 〇〇〇mg/ Around L, a decomposition rate which is the same as that in the case of aerobic biological treatment using aerobic activated sludge can be obtained. Therefore, when the sludge concentration is in the above range, the hydraulic retention time of the reactor 21A can be made 〇5 days to 2 days. The excess sludge is appropriately withdrawn from the reactor 210 via the sludge discharge pipe 235 to adjust the sludge concentration in the reactor 21. The separated water in which the solid component is separated from the apparatus 212 is desalted in the reverse osmosis membrane unit 214 disposed in the subsequent stage of the membrane separation unit 212 to be used as raw water for pure water production. In the present embodiment, the reactor 21 is operated at 30 C to 40 ° C, and the temperature of the treatment liquid is also 3 Torr to 4 ° C. When the aerobic treatment is not performed and the temperature is not artificially lowered, the treatment liquid discharged from the reactor 210 is sent to the membrane separation device 212 and the reverse osmosis device 214. The liquid of about 30 C is easily subjected to the reverse osmosis membrane. Separation, the flux of the reverse osmosis membrane device 214 can be increased by sending the treatment liquid from the reactor 210 to the reverse osmosis membrane crucible 214 in a warm state. ^ The liquid discharged from the reverse osmosis membrane device 214 is still warm. Therefore, in the present invention, the heat exchange of the permeated water is performed by the heat exchanger 222 placed in the middle of the permeated water pipe for discharging the permeated water, and the second heat exchanger 222 is returned. The heat exchanged by the heat exchange is sent to the first heat exchanger 221 via the fluid pipe 239. In the first converter 221, the raw water sent from the raw water pipe 230 is heated by the heated heat exchange medium, and then sent to the reactor 210. 29 200932688 The permeable water of the salt is removed by treatment in the reverse osmosis membrane device 214, and can be used as raw water for pure water production. Specifically, in the reverse section of the reverse osmosis membrane device, a type H of a pure water manufacturing apparatus such as a de-cleaning device and a purple sterilizing device is disposed, and the machine is discharged from the retro-permeability device 2U. The permeated water is treated, whereby tons of water can be produced: the salt discharged from the reverse osmosis membrane device 2M is discharged through the concentrated concentrated water pipe 237. In the processing apparatus 200 according to the second embodiment, the biological treatment tank holding the self-supporting biological (A_mQxm organism) is treated as concentrated water. In the Anammox tank 241, 'concentration 1 and (4) supplied from the brine tube 237 are partially oxidized to nitrous acid under microaerobic conditions, and the biological reaction of the Anammox microorganism is used to generate Rat gas and remove nitrogen. The effluent from the Anam_x tank (4) is discharged from the 攸 官, and it can be further processed to be used as raw water for pure water production. Alternatively, the effluent may be solid-liquidized in a solid-liquid separation (not shown): the solid component is returned to the sludge centrifugation, and the hull component is released or recovered. (Embodiment 3) The concentrated water discharged from the object 攸 钱 钱 214 214 _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ Fig. 3 is a schematic view showing a third embodiment of the apparatus 300 of the present invention. The treatment device lion has a reaction = 43 instead of the Α__ χ 241 as a concentrated water treatment device, "the treatment device 200 is different. The concentrated water is supplied to the reaction column such as the salt 30 200932688. The chemical injection device adds a chemical which reacts with ammonia in the concentrated water to form a solid. A phosphoric acid and a magnesium salt are added as a chemical to the concentrated water, and magnesium ammonium phosphate is formed in the reaction column 343 to produce struvite (struvite). Crystallization. The struvite crystals can be discharged from the reaction column 343 and used as a fertilizer, etc., and the ammonia dehydrogenated water can be removed and separated from the crystals, and can be recovered as raw water produced by pure water. (Embodiment 4) FIG. Mode of the processing apparatus 400 according to the fourth embodiment of the present invention. The processing apparatus 400 includes an evaporator 445 as a concentrated water treatment apparatus. In the processing apparatus 400, concentrated water is introduced into the evaporator 445 to perform vacuum distillation and distillation from the distillation water pipe. 446 Take distilled water for raw water for pure water production. Although it is not shown in the figure, it is also possible to add sulfuric acid to concentrated water before steaming. The concentrated water is treated by a method in which two or more kinds of biological treatment, chemical treatment, and physical treatment are combined in a state in which the pH of the concentrated water is about 4 to 6 and the ammonia is 4 ampere. In the processing device 500 of the fifth, the biological treatment tank (Anamm〇x tank 241) and the hair dryer 445 are combined to form a concentrated water treatment device. In the treatment device, the concentrated water is firstly used. The biological treatment can reduce the amount of acid required for pH adjustment of the water to be treated supplied to the hair dryer 445. [Embodiment] [Embodiment 4] In the fourth embodiment, the simulation is shown in FIG. The experimental device of the processing device 2 was tested. The reactor of the experimental device, 21〇, was operated under the conditions of an effective volume of 31 200932688 〇 3 1 m and a hydraulic retention time of 0.5 day. The reactor 210 will be treated in the reactor 210. The granular sludge discharged from the anaerobic reactor of the alcohol is cultured in a treatment liquid to be described later to maintain the floating sludge. The concentration of the floating sludge in the reactor 210 is 4,000 mg/L, and the existing amount is present. (wet weight comparison) 40% is the methane-producing flora, and 6〇% is the self-decomposing residue of the smoldering bacteria. As the treated water, the total organic carbon (TOC) concentration is 500 mg/L, and the nitrogen concentration is 152 mg/L. The inorganic salt has a concentration of mg/L of β-containing organic water. Carbon and nitrogen are basically derived from tetramethylammonium hydroxide at a concentration of 480 mg/L for TOC and 140 mg/L for hydrazine. The temperature of the liquid in the tank in the reactor 210 was brought to 35 C. Four membrane-shaped UF membranes having a diameter of cin52 cin (a pore diameter of 3 〇 nm) were disposed in the membrane separation device 212 to be discharged from the reactor 21 The biological treatment fluid flows into the tube together with the gas. The concentrate and gas are returned to the reactor 210. The amount of permeate water (flux) of the membrane separation device 212 is set to ι. The separated water obtained from the membrane separation device 212 is concentrated at 0.75 MPa by a reverse osmosis membrane device 214 (a spiral reverse osmosis membrane device having a wholly aromatic polyamine-based ultra-low pressure membrane as a reverse osmosis membrane) at 0.75 MPa. Times. Three days after the start of the experiment under the above conditions, tetraammonium hydroxide was decomposed, and the TOC concentration of the separated water from the membrane separation device 212 was 5 mg/L to form tridecylamine and ammonia. The TOC for separating water is essentially tridecylamine at a concentration of 4 mg/L. The remaining 1 mg/L is a high molecular organic compound produced by microorganisms. In addition, the ammonia concentration of the separated water is in the range of 135 mg_N/L to 140 mg-N/L. The ammonia is reacted with the 32 c 200932688 carbon (concentration of about 120 mg-C/L) produced by decane fermentation in the reactor 210 to form ammonium hydrogencarbonate. Therefore, the pH of the liquid in the tank of the reactor 210 can be maintained at pH 7.0 to pH 7.5 without adding a neutralizing reagent. The reverse osmosis membrane device 214 for desalting the separated water was operated at a flow rate of 〇 95 at 〇.75 MPa for 60 days from the start of the experiment. Concentrated water obtained from reverse osmosis membrane unit 214, pot pH

It is about 8.5, the concentration of trimethylamine is 40mg_c/L, the concentration of chlorine chloride is 1,400 mg-N/L, the concentration of molecular organic matter is 〇 〇 ton, the recovery of salt (recording salt) and organic matter is about 】 〇〇%. Concentrated water was biologically treated in micro-aerobic/anaerobic conditions in Anarmnox Trough 24! The load on the Anammox tank 24 i is 3 kg_N/m3/day. By the treatment of the towel in the Anammox tank 241, the trimethylamine and ammonia in the shrinking water of Han. The treatment solution which is biologically decomposed and flows out from Anamm〇x # 241 has a bod degree of 10 mg/L or less, an ss concentration of ι〇雄 or less, and a nitrogen concentration of 10 mg-N/L. [Example 5] An experiment was carried out in the same manner as in Example 4 except that the experimental apparatus which mimics the processing apparatus of Fig. 3 was used in Example 5. For the implementation: 1 Γ In the middle of the brine tube 237, a 2% chlorinated solution was added as an analge of 800 mg/L, and a citric acid (tetra) solution was added. In addition, === nano is used to make the pH value η, so that the carbonation gas is dissociated and the = is released. The capacity of the reaction column 343 was 20 L, and the _water of the above chemical was added to the person who was thin L/cut. As a result, the shop and the scale and the ', ’' produced struvite crystals having a diameter of about 2 mm to 3 mm. The concentration of t〇c of the treated water taken out in the reaction zone 343 of 200932688 = s 344^ is zig/L, and the nitrogen concentration is 140 mg/L' to remove the ammonia contained in the concentrated water. . In addition, 'the struvite crystals are taken out from the reaction column 343, and the fertilizer is divided into ammonia, H is almost free of heavy metals, and can be used in Example 6 only for the treatment of Figure 4. The experimental setup of the apparatus was carried out in the same conditions as in the case of Example 4. In the implementation of 夭6, '彳<the chemical addition I (not shown) is placed in the middle of the brine tube 3374], and the test of the condensed water supplied to the evaporator 445 by the sulfuric acid 1 becomes 〇(pH and Erlufa) Zhai 445 is by decompressing and warming the concentrated water to 4 〇〇c, and subtracting 'from the steaming water pipe 446 + to take out the steamed water. Steamed water t〇c twice, 0.01 mg-C/ L, the nitrogen degree is 〇2 mg_N/L. In addition, ammonium sulfate (IV) remaining in the heat generator 445 is recovered, and as a result, 98% of the money in the concentrated water can be recovered as an ammonium sulfate slurry. The treatment liquid obtained by the biological treatment of Anammox = of Example 4 was further distilled in a burst state 445 using the test apparatus simulating the treatment apparatus 500 of FIG. 5 in Example 7 in Example 7. In Example 7, supply, ° The ammonia concentration of the liquid to the 煞 煞 445 was 7 〇 mg_N/L, which was lower than that of the example 6. Therefore, the amount of acid necessary for lowering the pH was carried out, and 1/2 6 of 6 was corrected. (4) Water quality of steamed water discharged in 445 < TOC concentration is 〇mg-C/L, and nitrogen concentration is 〇湖胤. [Comparative Example 3] 34 200932688 In Comparative Example 3, in the opposite An air diffusing device that blows air is disposed inside the device, thereby making the reactor an aerobic biological treatment tank. Except that the reactor is changed to aerobicity, the experiment is carried out under the same conditions as in the example 4, and Since the pH adjustment of the aerobic biological treatment tank was not performed, the nitrification reaction was found to occur one week after the start of the experiment, and the pH of the liquid in the tank was lowered to about 5.0 to 5.5. The result 'flowed from the aerobic biological treatment tank. The TOC concentration of the treatment liquid was about 10 mg/L to 120 mg/L, and the turbulent flux of the reverse osmosis membrane device for desalting the separated water obtained from the membrane separation device was half that of Example 4. [Comparative Example] 4] In Comparative Example 3, sodium hydroxide was added to the aerobic biological treatment tank to adjust the pH of the liquid in the tank to a range of 6.5 to 7.5. As a result, it was allowed to flow out from the aerobic biological treatment tank. The concentration of T〇c in the treatment liquid was lowered to 10 mg/L. However, the treatment liquid contained nitric acid at a concentration of about 13 (1 lng/L to about 40 mg/L), and the sodium hydroxide added by adjusting the pH value was used. The salt concentration becomes higher. The flux of the reverse osmosis membrane device for separating the φ water obtained in the apparatus for desalination treatment was limited to 60% of Example 4. [Comparative Example 5] In Comparative Example 4, a denitrification tank was provided in the latter stage of the aerobic biological treatment tank. The treatment device treatment device 6 (8) having the configuration shown in Fig. 6 has an aerobic biological treatment tank (aerobic reactor 61A) instead of the anaerobic biological treatment device used in the embodiment / (reactor 21G) In the latter stage of the aerobic reactor 610, a denitrification tank 613 for retaining denitrifying bacteria and a re-aeration tank 200932688 〇 611 ° are added to the treatment liquid flowing out of the aerobic reactor 61 to add sterol. Sulfuric acid was added to the nitrogen tank 613 to maintain the pH at 6.5 to 7.5, and the denitrification treatment was carried out. The effluent from the denitrification tank 613 is sent to the re-aeration tank 611' via the pipe 632B and re-aerated in the re-aeration tank 611, and then sent to the membrane separation device 612 via the pipe 632C. As a result, the flux of the reverse osmosis membrane device 614 for desalting the separated water obtained from the membrane separation device 612 was 80% of that of Example 4 two weeks after the start of the experiment. However, the flux of the reverse osmosis membrane unit 614 was reduced to 50% of the Φ of Example 4 one month after the start of the experiment. Therefore, the reverse osmosis membrane was taken out for microscopic observation, and as a result, a large amount of biofilm adhered to the surface. Since the biofilm was hardly adhered to the reverse osmosis membrane of the reverse osmosis membrane device used in Example 4, it was estimated that the flux decreased due to the adhesion of the biofilm in Comparative Example 5. In the examples, the reason why the biofilm was not attached to the reverse osmosis membrane was considered to be the following two points. In the reverse osmosis, the membrane, the middle, and the concentration of the salt increase the 1) value of the brine to 8 5, so that the ammonia is removed from the carbon hydride and the ammonium hydride, and the growth of the microorganism is inhibited due to the toxicity of ammonia. For other reasons, the growth rate of the sputum-producing microbes is slower than that of the aerobic microorganisms, and it is difficult to form a biofilm. The anaerobic treatment of water containing organic matter is carried out by using the decane-producing microbial population as described above, whereby the organic matter can be biodegraded without adding a pH-viewing agent, and the dyeing can be suppressed. The amount of molecular weight produced by the shaft. In addition, in the anaerobic treatment step using the formazan-producing microflora, the carbon dioxide is generated by carbon dioxide, and the aerobic treatment is not performed, and the anaerobic treatment step in the reverse osmosis can be suppressed. In the case of a reverse osmosis membrane in the absence of concentration, it is concentrated in a reverse osmosis membrane apparatus, and a biofilm is formed in the membrane apparatus. Namely, it is possible to prevent the substance removed by the method from being contaminated in the reverse osmosis membrane device. [Industrial Applicability] The present invention can be used for the treatment of cut organic organisms containing organic substances and reused in pure water.

Although the present invention has been disclosed in the above embodiments, it is not intended to limit the invention to those skilled in the art, and it is possible to make a few changes and > without departing from the spirit and scope of the invention. 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 Fig. 2 is a schematic view of a biological treatment apparatus according to a second embodiment of the present invention. Fig. 3 is a schematic view of a biological treatment apparatus according to a third embodiment of the present invention. Fig. 4 is a schematic view showing a biological treatment apparatus according to a fourth embodiment of the present invention. Fig. 5 is a schematic view showing a biological treatment apparatus according to a fifth embodiment of the present invention. Fig. 6 is a schematic view showing an experimental apparatus used in Comparative Example 5. [Main component symbol description] 37 200932688 100, 200, 300, 400, 500: biological treatment device 110: anaerobic biological treatment tank 112, 212: membrane separation device 114, 214, 614: reverse osmosis membrane device 121, 22 621: 1st heat exchanger (heat recovery heating|setting) 122, 222, 622: 2nd heat exchanger (heat recovery heating discharge) 130, 230: raw water pipes 131 and 231: exhaust pipe ❹ 132, 232: Process liquid pipes 133, 233: return pipes 134, 234: separation water pipes 135, 235: mud pipes 136, 236: permeate pipes 137, 237: brine pipes 138, 238, 242, 344, 446, 630, 631, 632, 632B, 632C, 633, 634, 635, 636, 637, 638, 639, 642: piping φ 139, 239: fluid tube 210: anaerobic biological treatment tank (reactor) 241, 641: Anammox tank (concentrated water treatment Apparatus) 343: Reaction column 445: Evaporator 600: Biological treatment apparatus 610 of Comparative Example: Aerobic biological treatment tank (aerobic reactor) 611: Re-aeration layer c 200932688 612: Membrane separation apparatus 613: Denitrification groove

39

Claims (1)

200932688 VII. Patent application scope: l _ Biological treatment method for water containing organic matter, including · introducing water containing organic matter into anaerobic biological treatment tank; using oxygen in the anaerobic biological treatment tank to generate oxygen Sexual biological treatment; the paper preparation 〆 will use the treatment liquid obtained by the anaerobic biological treatment to perform membrane separation without aerobic biological treatment; 生 Reverse osmosis (4) to separate the lysate (4) separated water to carry out the raw material of the organic matter-containing water described in item 1 of the scope of the object. The tree-heated water towel, the ratio of organic matter to v, organic carbon is greater than Equal to 7〇〇/. . The second aliquot of the first or second item containing the organic matter, 7 and the method A, wherein the liquidity in the anaerobic biological treatment tank is set to be less than a thief, and the anaerobic is performed. The object is: the raw material of the organic substance-containing water described in item 3 of the Qing 2 range. The process of the oxygen treatment is heated, and the membrane separation and the reverse osmosis treatment are further carried out. The raw material method of the organic matter-containing water described in Item 2, wherein the monomer is organically selected from the group consisting of tetramethylammonium hydroxide, diethylene glycol monobutyl ether, isopropanol, dimethyl Any of the group consisting of B-, diamine, dimethyl sulfoxide, and acetic acid 200932688 6. A biological treatment device for water containing organic matter, comprising: a field biological treatment tank for introducing water containing organic matter and The sputum group is formed by the smoldering to generate a sputum, and the membrane separation device is connected to the anaerobic biological treatment tank for membrane separation of the treatment liquid discharged from the anaerobic biological treatment tank. The device 'is used to treat the separated water of the membrane separation device. _ = The raw material of the organic-containing water described in Item 6 of the patent scope, wherein the content of the monomeric organic matter in the organic-containing water is 70% or more. 8. A biological treatment apparatus for applying organic water according to item 6 or item 7 of the patent application, comprising: The anaerobic treatment tank is operated by setting the temperature of the liquid in the tank to 15 C or more and 401 or less. ▲ The treatment liquid is supplied to the membrane in the anaerobic treatment tank under heating. The separation device and the reverse osmosis membrane device. 9. The raw material processing device for water containing organic matter according to claim 8 of the patent application, further comprising a heat recovery heating device for heat recovery of the permeated water of the reverse osmosis membrane device, and using the recovered heat to add Warm the anaerobic treatment tank. = a membrane & ampere device for water containing organic matter as described in claim 6 wherein the membrane separation device comprises microfiltration, membrane or super-organic water containing organic matter as described in claim 6 The biological treatment device further includes a cleaning device for supplying the bio-generated gas generated in the anaerobic raw material 200932688 treatment tank to the membrane separation device for aeration cleaning. In the biological treatment device for the organic matter-containing water, the anaerobic biological treatment tank is used to introduce the water containing the organic matter formed by the smoldering group and using the membrane separation device, and the anaerobic The biological biological treatment tank from the anaerobic thief _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ Concentration 13. The biological treatment device of claim 12, wherein the Han shrink water treatment: two = different treatment tanks of the spoon treatment tank. In the case of claim 12, the biological treatment device, wherein the concentrated water device is introduced into the concentrated water to evaporate and take the device to include the treatment. According to the item 12 of the scope = k biological treatment device with organic matter, in which the concentrated water treatment == the separation of water. The biological treatment method of the water added to the concentrated water and the organic matter, including: introducing 3 organic water into the containing biological treatment tank for anaerobic biological treatment. The solution will be treated with the treatment liquid of the diarrhea bioremediation treatment without any 42 200932688 aerobic biological treatment, and the isolation water obtained by the membrane separation and the spirometry separation/penetration treatment; Scope No. 16 & Shrinkage Treatment _ Biological treatment method, wherein the organic substance-containing t contains organic water. 18. For example, the biological treatment method of the water containing the nitrogen compound in item 16 or the L of the application , wherein the biological treatment different from the organic biological treatment described in the item *; using the anaerobic residual treatment; and/or _ concentrated water is treated by steaming with 13 = water. 43