JP4678831B2 - Process for treating waste liquid from sugarmaking waste, sugar production liquid, or fermentation process of sugar production - Google Patents

Description

  The present invention relates to a method for treating a waste liquid from a fermentation process of sugar-making waste, sugar-making waste liquid, or sugar-making waste.

  Various waste liquids are discharged at food manufacturing plants. In particular, waste liquids (organic waste liquids) containing a large amount of organic matter are discharged from factories that manufacture plants and animals as raw materials and produce processed agricultural foods, processed livestock foods and processed fishery foods. Among these, a part of the waste liquids such as shochu lees, fermentation waste liquid, sugar-making waste nectar, and umezuke seasoning waste liquid are disposed of by ocean dumping. However, in accordance with the “Convention on the Prevention of Marine Pollution Caused by the Disposal of Waste and Others (London Convention)”, which came into effect in 1975 based on the viewpoint of protecting the global natural environment and was revised in 1993. Was banned. Japan has not yet ratified the treaty. However, studies are underway to ratify the treaty between 2004 and 2005. Therefore, organic waste liquid treatment methods have been developed to replace ocean dumping.

  Sugarmaking waste, sugarmaking wastewater, and wastewater from the fermentation process of sugarmaking waste contain high concentrations of organic substances derived from proteins or sugars, coloring substances, and inorganic substances such as chlorine and potassium. In order to treat the waste liquid and discharge it into the environment, it is necessary to reduce the content of organic and inorganic substances to below the emission standard. Conventionally, as a treatment method of these waste liquids, (1) biological treatment method, (2) incineration treatment method, (3) use for feed and organic fertilizer, and (4) boiler combustion method have been performed.

  In general, biological treatment is known to be effective as a method for treating organic wastewater at low cost. Moreover, the activated sludge method, the membrane separation activated sludge method, the biofilm method, etc. are known. Since the sugarmaking waste, the sugarmaking waste liquid, and the waste liquid from the fermentation process of the sugarmaking waste have a very high organic substance concentration compared with general organic wastewater, methane fermentation treatment has been used for a long time. In recent years, high-speed processing has become possible by the methane fermentation method using the UASB method (Non-Patent Document 1).

  Further, spray incineration, submerged combustion, fluidized bed incineration, and the like have been developed as waste liquid incineration methods. The spray incineration method is a method in which high-concentration organic waste liquid is sprayed into the furnace and incinerated. Specifically, the organic waste liquid is fluidized by holding it at high temperature and high pressure, and this fluidized product is spray incinerated. (Patent documents 1 to 3 and non-patent document 2). The submerged combustion method is a method in which high-temperature combustion gas generated by combustion is ejected into the liquid at once, and heat transfer, absorption of combustion gas components, and the like are efficiently performed by direct contact between the liquid and the combustion gas bubbles ( Patent Documents 4 to 7 and Non-Patent Documents 3 and 4). The fluidized-bed incineration method is a method in which silica sand or aluminum oxide is used as a fluid medium to maintain a high-temperature fluid state in a furnace, and incineration is put into the furnace to instantaneously completely incinerate (Patent Documents 8 and 9). . In the incineration treatment method as described above, dedicated equipment and devices have been developed and sold.

  As a feed and an organic fertilizer, a sugar-making waste liquid is used for livestock feed. Moreover, the fertilizer manufactured by adding the stefene waste liquid and bentonite discharged | emitted from a beet sugar manufacturing process to the aggregates and sediment discharged | emitted from an aquatic processing wastewater treatment plant, and granulating (patent document 10), and There is known a fertilizer (Patent Document 11) obtained by electrodialyzing a sugar-making waste liquid.

  A method of burning in a boiler with a special furnace using sugar-making waste as a fuel was also tested. When only molasses is burned, the fuel value is reported to be 1/5 that of coal (Non-patent Document 5).

So far, sugar factories have been researching the use of ultrafiltration membranes made of organic polymers and ceramic materials to clean sugar solutions in the sugar production process (Non-Patent Documents 6 and 7), and research on recovering sugar from waste nectar (Non-Patent Documents). 8 and 9) have been performed.
According to the description in Non-Patent Documents 6 and 7, the purification of the sugar solution in the sugar production process was intended to remove a polymer substance larger than the coloring component derived from the raw material, unlike the decolorization / desalting of the waste solution. Therefore, ultrafiltration membranes or microfiltration membranes (MF membranes) were studied and it was concluded that ultrafiltration membranes were more suitable. This is because when a liquid containing a large amount of impurities is processed, a microfiltration membrane having a molecular weight close to that of the polymer substance to be separated is likely to be clogged. It was because it was less likely to clog when used. In this prior art, in order to remove a coloring component having a molecular weight of several thousand, a resin or granular charcoal is used as a decoloring adsorbent. Therefore, no membrane is used to separate the colored components. Moreover, the film to be used is mainly a ceramic film, and an organic polymer film can also be used. However, since the lifetime is short and the heat resistance and chemical resistance are low, it has been considered difficult to put to practical use. This is because, at that time, ceramic membranes were considered to be suitable for cleaning sugar solutions because of their higher heat resistance and chemical resistance. As described above, in this method, both the coloring component and the salt permeate the membrane and cannot be separated.

  Next, according to the description of Non-Patent Documents 8 and 9, regarding the research for recovering sugar from molasses, the polymer substance was removed by ultrafiltration, followed by desalting by electrodialysis. The ultrafiltration membrane used was a polyethersulfone tubular membrane with a molecular weight cut off of 40,000, and a polyethersulfone hollow fiber membrane with a molecular weight cut off of 30,000 and an acrylonitrile tubular membrane with a molecular weight cut off of 20,000. It has been. Membrane separation by ultrafiltration membrane was aimed at removing relatively large substances, as can be seen from the molecular weight cut-off. Further, electrodialysis is used for desalting. Therefore, in this method, both the coloring component and the salt permeate the membrane and cannot be separated.

  In the fermentation industry, removal of coloring components from fermentation waste liquid derived from molasses has also been studied (Non-Patent Documents 10 and 11). In addition, when using waste honey derived from a sugar factory as a fermentation raw material, the coloring components in the waste honey move to the yeast product, so it has been studied to decolorize the molasses and use it for fermentation (non- Patent Document 11).

  According to the description of Non-Patent Document 10, in the examination of the membrane treatment method for decolorizing molasses used for fermentation, three types of membranes were selected at the laboratory level. A polysulfone hollow fiber membrane with a molecular weight cut off of 5,000 and a flat membrane of polysulfone with a molecular weight cut off of 2,000 (spiral type module) are selected as the ultrafiltration membrane, and a polysulfone tubular membrane (tubular type module) is selected as the reverse osmosis membrane. It was. The decolorization of molasses means the removal of colored components, and since the peak of the molecular weight of the colored components in molasses is in the range of 3,000 to 5,000, the goal was to remove colored components with a molecular weight of about 3,000. However, the former of the ultrafiltration membranes has a large molecular weight cut off compared to the molecular weight of the coloring component (fraction molecular weight 5,000), and the decolorization rate is 56%, which is not a desirable result. Of the ultrafiltration membranes, the latter was also used in practical tests. On the other hand, the reverse osmosis membrane has problems such as membrane breakage and ceramic / membrane separation, and the final test was not performed. However, in any of the three types of membranes, there remains a problem of economics due to a decrease in membrane life due to fouling and a decrease in permeation flux.

  According to the description of Non-Patent Document 11, the use of an ultrafiltration membrane or a reverse osmosis membrane for decolorizing the molasses of fermentation raw materials was examined, and several ultrafiltration membranes and reverse osmosis membranes were examined. Even with the polysulfone reverse osmosis membranes selected by the above, there is a problem in terms of economy because it requires a pretreatment by centrifugation before the filtration treatment and frequent membrane washing because the processing capacity is reduced by fouling. It was difficult to put it to practical use. In addition, the same document describes decolorization by a membrane of yeast culture waste liquid (fermentation waste liquid), and is a reverse osmosis membrane (charged membrane) of a sulfonated polyether sulfone of a synthetic polymer composite membrane as a usable membrane. A membrane having a salt rejection of 5% when measured at 0.5 MPa and 25 ° C. using a 0.2% (w / v) sodium chloride aqueous solution as an evaluation solution was selected. As can be seen from the salt rejection, this membrane was very permeable and had a large amount of permeated water.

JP-A-11-304125 Japanese Patent Laid-Open No. 10-253034 JP-A-5-337497 JP 2002-89820 A Japanese Patent Publication No.52-3232 JP 51-142877 A JP 49-46576 A JP 59-138804 A Japanese Patent Laid-Open No. 57-16715 Japanese Patent Laid-Open No. 52-50878 JP-A-1-38193 Edited by Food Equipment and Equipment Encyclopedia Editorial Committee, “Chapter 2 Wastewater Treatment Technology and Equipment”, Food Equipment and Equipment Encyclopedia, Industry Research Association Encyclopedia Publishing Center, 1006-1026, July 2002 Yoshiaki Kinoshita, "Concentrated waste liquid treatment by spray combustion method", Water pollution research (Japan Water Environment Society) Vol.12 (2), 79-86, 1989 Yoichi Ozawa, "Waste / Recycling Waste Liquid Incineration Equipment Introduction of Waste Liquid Incineration Technology Using In-Liquid Combustion", Environmental Purification Technology Vol.2 (12), 60-64, 2003. Masao Deguchi, “Submerged combustion type inorganic salt-containing waste liquid incinerator”, Industrial Heating Vol.36 (1), 46-54, 1999 “Queensland Society of Sugar Technologists” The International Sugar Journal, pp. 62-64, 1932 Nagakase Hirokazu, Hino Masao, Fujita Hirohisa, “Sugar Solution Cleaning Process Using Membrane Separation Technology”, Journal of Refined Sugar Technology, Vol. 50, pp. 5-9, 2002 Kishihara Shiro, Okuno Masahiro, Yoshimoto Satoshi, Hosokawa Tomohiro, Fujimoto Toshiko, Fujii Satoshi, "Effects of Membrane Separation on Sugar Crystallization and Adsorption Decolorization", Journal of Refining Sugar Technology, Vol.48, 27 ~ 34, 2001 Supervised by Hiroshi Shimizu and Masato Nishimura, "Section 8 Sugar Purification", Latest Membrane Processing Technology and Its Applications, Fuji Techno System Co., Ltd., 634-638, August 1984 Supervised by Masayuki Nakagaki, “Part IV: Examples of membrane applications and applications 6. Desalination of sugar solutions”, Popular membrane treatment technology, Fuji Techno System Co., Ltd., pages 144-152, February 1999 Edited by Editorial Committee of Food Industry Membrane Utilization Technology Research Association, “12. Clarification and Decolorization of Molasses”, Published by Food Industry Membrane Utilization Technology Research Association, pages 353-372, September 1987 Edited by Membrane Utilization Technology Study Group, “Development of Decolorization of Yeast Manufacturing Wastewater and Water Circulation System”, Membrane Treatment System in Food Industry, pp. 143-195, November 1989

  (1) The waste liquid from the fermentation process of sugar-making waste liquid and sugar-making waste nectar is mostly water, but contains a high concentration of insoluble solids, organic substances such as microbial-degradable coloring substances, or ash. The waste liquid was usually treated with activated sludge after methane fermentation. However, in this method, the microbial difficult-to-decompose colored substance is transferred as it is to the treated liquid. It is known that the colored substance contained in the sugar liquid is distributed in a molecular weight range of about 1,000 to 25,000, and in particular, a high-molecular colored substance having a molecular weight of 3,000 or more is hardly decomposed by microorganisms. Since this coloring substance is very strongly colored and the chromaticity reaches several tens of thousands of times of the treated water in the sewage treatment plant, it is necessary to decompose and remove the coloring substance or dilute and discharge by other methods. However, an inexpensive method for decomposing colored substances has not been put to practical use. (2) Although various waste liquid incineration treatment methods are counted as one of the low-pollution type excellent treatment methods, the initial investment cost for the equipment is high and the operation cost is also high. Therefore, the various waste liquid incineration treatment methods have a problem that the cost burden on products such as sugar or fermentation products increases, and it is difficult to use in the food industry. (3) In use for fertilizer and feed, the supply-demand relationship between the amount of waste liquid generated (supply side) and the amount of fertilizer / feed consumption (consumption side) changes significantly. In recent years, the switch to other fertilizers and feeds has progressed in terms of economic efficiency, and the consumption of fertilizer derived from sugar-making waste liquid and sugar-making waste nectar has been steadily decreasing. The danger is great. (4) In a method of burning in a boiler such as a bagasse-fired boiler, a lot of inorganic salts are contained in the fermentation waste liquid made from sugar-making waste liquid or sugar-making waste nectar, especially chlorine ions that cause corrosion in boiler combustion And a large amount of potassium that promotes corrosion has the disadvantage of causing corrosion in the superheater and damaging the boiler. In addition, these inorganic salts adhere to the furnace unless maintained at the melting temperature or higher in the furnace. Therefore, the furnace needs to be able to withstand high temperatures. Further, a furnace having a hearth needs to be a special furnace because an inorganic salt solidified on the bottom of the furnace accumulates and operation failure occurs. Furthermore, chlorine ions are known to generate dioxins depending on the incineration conditions, and it is not preferable to incinerate waste liquids that contain a lot of chlorine in general boilers that do not meet the structural standards and maintenance management standards of waste incineration facilities. .

Therefore, in order to incinerate the sugarmaking waste, the sugarmaking waste liquid, and the waste liquid from the fermentation process of the sugarmaking waste, salt, in particular, chlorine ions are separated from these waste or waste liquid, and the waste liquid containing chlorine ions is treated with waste water. Need to do and incinerate the rest. At this time, it is necessary that a colored component is contained in the waste liquid on the incineration side. This is because the coloring component is not decomposed by ordinary waste water treatment as described in the background art. Therefore, it is necessary to easily separate the coloring component and chloride ion.
In order to separate colored substances and chloride ions, membrane treatment, separation by ion exchange resin, and separation by electrodialysis can be considered. However, most of the membrane treatment techniques that have been studied in sugar mills or fermentation factories so far use ultrafiltration membranes. Since the molecular weight cut-off at this time is a unit of several tens of thousands, the object was to remove foreign matters much larger than the coloring components and salts from the waste liquid. Therefore, the coloring component and the salt were not separated. In addition, electrodialysis is used to remove salts from these waste honey and waste liquid after membrane treatment, and membrane treatment is positioned as a pre-stage of electrodialysis. That is, the conventional method is a membrane treatment technique that combines ultrafiltration and electrodialysis. Since these liquids are high-concentration organic waste liquids, they tend to cause fouling of membranes used in electrodialysis and ultrafiltration, and electrodialysis requires large equipment and high running costs. Therefore, it is difficult to desalinate these solutions in one step of either electrodialysis or ultrafiltration. As another technique, the use of a reverse osmosis membrane for removing colored components was studied, but it was difficult to put it to practical use due to fouling problems, and the behavior of salts was unknown.

  In order to remove chlorine ions, a method using an ion exchange resin can be considered. However, wastewater with a very high salt concentration, for example, chromatographic separation wastewater whose salt concentration exceeds 30% by weight per solid content, requires a large amount of resin, and it takes a great deal of cost to regenerate the resin. Not practical.

  As described above, there has been no known technique for separating sugar-making waste, sugar-making waste liquid, and coloring components and inorganic salts, particularly chloride ions, from the fermentation process of sugar-making waste by a single-stage membrane treatment.

  From the above, the conventional methods as described above have problems, and no effective waste liquid treatment means for solving these problems has been proposed yet. Therefore, the present invention should be able to solve the problem of providing an effective processing means that is economically feasible with respect to the sugar beet waste, the sugar bean waste liquid, and the waste liquid from the fermentation process of the sugar bean waste. It is to be an issue.

As a result of intensive studies, the present inventors have found that sugar-making waste, sugar-making waste liquid, or waste liquid from the fermentation process of sugar-making waste is colored using an ultrafiltration membrane or a reverse osmosis membrane that is a synthetic polymer composite membrane. The present invention has been completed by finding that the above-mentioned problems can be effectively solved by separating the concentrate into a concentrate containing chlorine and a permeate containing chlorine ions.
In addition, the present invention provides a sugarmaking waste, a sugarmaking waste liquid, or a waste liquid from a fermentation process of sugarmaking waste using an ultrafiltration membrane having a fractional molecular weight of 2,000 to 4,000 and being a synthetic polymer composite membrane. Provided is a method for treating a waste liquid, comprising separating into a concentrated liquid containing a coloring component and a permeate containing chlorine ions.
Furthermore, the present invention provides a salt inhibition rate of a sodium chloride aqueous solution of 0.05% (w / v) or more and 3.5% (w / v) or less of sugar cane waste, sugar waste liquid, or waste liquid produced by fermenting sugar waste. A concentrated solution containing colored components and chloride ions using a reverse osmosis membrane that is a synthetic polymer composite membrane that is 40% to 60% under a pressure of 0.3 MPa to 5.6 MPa and a temperature of 25 ° C. Provided is a method for treating a waste liquid, comprising separating the permeated liquid.

ADVANTAGE OF THE INVENTION According to this invention, the simple and economical process of the waste liquid from the fermentation process of sugar-making waste liquid, sugar-making waste liquid, and sugar-making waste liquid is attained. Specifically, the following advantages are obtained.
(1) Since the separation of chlorine ions and colored components can be performed by one-stage membrane treatment, the process is simplified.
(2) Since the amount of coloring components in the permeate is reduced, wastewater treatment by a normal biological treatment method is possible.
(3) Since the concentration of chlorine ions in the concentrated liquid is reduced, when the concentrated liquid is incinerated with a boiler, corrosion and depletion of the boiler water pipe and generation of harmful substances due to chlorine ions can be reduced.
(4) In a sugar factory, the amount of capital investment can be reduced by incinerating the concentrated liquid using an existing bagasse-fired boiler, thereby reducing the cost burden on the product.
(5) The load on the natural environment due to ocean dumping can be prevented.

Hereinafter, preferred embodiments for carrying out the present invention will be described in detail.
"Sugar-making waste honey" means 1st honey, 2nd honey and sugar-making honey generated at raw sugar manufacturing factories, molasses honey, 1-7th honey and refined sugar honey generated at refined sugar manufacturing plants, and sugar beet sugar It means beet honey generated in manufacturing plants, but includes honey similar to these.
“Sugar-making waste liquid” is a waste liquid containing colored components produced in the sugar production process, and means various waste liquids derived from the sugar production process, such as the remaining chromatographic separation waste liquid obtained by chromatographic separation and recovering sucrose. In addition, waste liquids similar to these are also included. The sugar-making waste liquid contains, as its components, organic substances such as proteins, sugars, amino acids, and organic acids, biologically difficult-to-decompose coloring components, and inorganic salts.
“Waste liquor from fermentation process of sugar-making waste honey” means waste liquid from fermentation process such as alcoholic fermentation, amino acid fermentation, and baker's yeast fermentation using sugar-making waste honey as a raw material. Including. Various fermentation waste liquids contain proteins, carbohydrates, amino acids, organic acids such as organic acids, biologically difficult-to-decompose coloring components, and inorganic salts as components.

  An example of the analytical value of sugar cane raw sugar is, for example, 21.6 wt% moisture, 10.8 wt% reducing sugar (glucose and fructose), 32.1 wt% sucrose, 1.5% potassium, 560 ppm sodium , Calcium 888 ppm, magnesium 1,200 mg / kg, iron 19 ppm, chloride ion 7,600 mg / kg, sulfate ion 9,300 mg / kg.

Among the sugar manufacturing waste liquids, for example, the analysis values of the chromatographic separation waste liquid are, for example, 56.0% by weight of water, 3.1% by weight of reducing sugar (glucose and fructose), 3.9% by weight of sucrose, 24.7% by weight of organic substances, 1,306 mg / kg of sodium, potassium They were 2,645 mg / kg, calcium 56.6 mg / kg, magnesium 44.2 mg / kg, chloride ion 2,841 mg / kg, iron 1,073 mg / kg, sulfate ion 3,261 mg / kg, and liquid density 1200 kg / m ² .

  As an example of the analysis value of the waste liquid from the fermentation process of sugar beet waste, the waste liquid obtained by distilling raw sugar waste nectar after alcohol fermentation is 90% moisture, 8.5% organic matter, 1.3 mg / kg sodium, They were potassium 41.0 mg / kg, calcium 13.3 mg / kg, iron 5.3 mg / kg, silicon dioxide 5.2 mg / kg, chloride ion 17.9 mg / kg, phosphate ion 3.3 mg / kg, sulfate ion 16.4 mg / kg.

  The types of membranes used in the present invention include ultrafiltration membranes (separating polymer coloring components and chloride ions due to differences in molecular weight) and reverse osmosis membranes (depending on differences in molecular weight and charge), which are synthetic polymer composite membranes. Separating the polymer coloring component and the chlorine ion) can be used. In the present invention, “synthetic polymer composite membrane” means an organic polymer membrane in which the membrane body is composed of a functional layer (dense layer or skin layer) and a support layer (porous layer), both of which are made of a synthetic polymer. means. In addition, it is not preferable to use an inorganic membrane such as ceramic or metal for membrane treatment of molasses or sugar-derived waste liquid because of the following problems. That is, the inorganic film has a much higher specific gravity than the synthetic polymer composite film. Therefore, there is a problem that the equipment becomes large and heavy in order to secure an effective film area. Further, when an effective film area cannot be secured, the inorganic film is immediately clogged (fouling). Therefore, it takes time to clean the chemicals, resulting in a problem that the filtration efficiency is deteriorated.

  In the present invention, an “ultrafiltration membrane (UF membrane)” is a membrane generally used for pressure filtration in which separation is performed based on the size of molecular weight, and is a membrane in which a separation level is expressed by a fractional molecular weight. is there. Usually, the molecular weight is fractionated in the region of several thousand to several million, which corresponds to the size of the particles in the range of several nm to several hundred nm as the molecular size.

  In the present invention, a “reverse osmosis membrane (RO membrane)” generally applies a pressure higher than the osmotic pressure difference between solutions passing through the membrane to the high concentration liquid side to prevent the permeation of the solute, ) Is a membrane used in a liquid separation method that permeates, and the separation level is expressed by a salt rejection. There are membranes used to produce pure water by allowing only water to pass through, membranes used for concentration of solutes, membranes that permeate and separate salts and low-molecular substances, and permeate and separate molecules smaller than ultrafiltration membranes. Used when doing.

  In the present invention, the ultrafiltration membrane is preferably capable of separating a color component which is said to have a peak at a molecular weight of 3,000 to 5,000 from chloride ions. The concentrated liquid separated by this membrane contains high-molecular organic substances containing colored components with poor biodegradability, while low-molecular organic substances such as salts containing chlorine ions and inorganic substances migrate to the permeate.

As the ultrafiltration membrane, a synthetic polymer composite membrane having a fractional molecular weight of 2,000 or more and 4,000 or less can be used. In the synthetic polymer composite membrane, the membrane body is preferably a flat membrane.
In the present invention, the “flat membrane” of the flat membrane-like synthetic polymer composite membrane is an expression used to distinguish from a tubular membrane and a hollow fiber membrane, and does not indicate a module type. Synthetic polymer membranes include cellulose-based membranes, polyacrylonitrile-based membranes, polyolefin-based membranes, polysulfone-based membranes, polyethersulfone-based membranes, polyamide-based membranes, polyimide-based membranes, etc., and various organic polymers are used as materials. Is done.

  The ultrafiltration membrane is preferably a polyamide membrane. Furthermore, the ultrafiltration membrane is preferably a spiral module. A polyamide-based film is a film in which the polymer constituting the functional layer of the film is mainly polyamide. Even if other materials are used in combination, those using polyamide as the main component are included in this category. . Examples of what are referred to as polyamide-based membranes are: aromatic polyamides composed of terephthalic acid, m-aminobenzamide, and m-phenylenediamide, polyamide hydrazides composed of isophthalic acid and m-aminobenzohydrazide, polypiperazines composed of fumaric acid and dimethylpiperazine There are membranes composed of amides as well as m-phenylene isophthalamide-terephthalamide copolymers. The polyamide film in the present invention includes these films and those generally sold as polyamide films.

  In the present invention, the ultrafiltration membrane is preferably a membrane that concentrates colored components on the concentrate side and concentrates chloride ions on the permeate side. Ultrafiltration membranes that are difficult to pass colored components are less likely to pass salts and tend to have a low permeation rate, so it is necessary to select a membrane that can satisfy these opposing conditions as much as possible. In order to satisfy this condition, the decolorization rate on the permeate side of the ultrafiltration membrane at 420 nm and 520 nm is preferably 85% or more, and more preferably 90% or more. Absorbances 420 nm and 560 nm are wavelengths at which absorption of colored components in the sugar production process is large. The chloride ion concentration rate on the permeate side of the ultrafiltration membrane is preferably 105% or more, more preferably 110% or more.

  Specifically, a DESALGH UF element having a molecular weight cut off of 2,500 (manufactured by GE Water Technologies) and a DESAL GK UF element having a molecular weight cut off of 3,500 (manufactured by GE Water Technologies) can be used as the ultrafiltration membrane. DESAL GH and DESAL GK membranes are polyamide membranes of flat membrane-like synthetic polymer composite membranes. The maximum operating temperature of DESAL GH and DESAL GK membranes is 80 ° C, and they have fouling resistance and chemical resistance.

  The maximum use temperature (° C.) indicates the heat resistant temperature of the film, and is the highest temperature at which the film can be used. This temperature represents the highest temperature that can be used when the membrane is modularized. When a membrane is used industrially, it is necessary to form a module in which a membrane having a large area is compactly housed in an exterior. The module is also called an element, and includes a membrane, an outer package (outer wrap), a water collection pipe, a spacer through which the stock solution passes, and a spacer through which the permeate passes. The maximum use temperature of the membrane is defined by the heat resistance of these components. The heat resistance of the polyamide film itself is generally said to be 90 ° C. However, since the heat resistance of components other than the film constituting the module is usually lower than that of the film, the heat resistance temperature of the film as a module is higher than this. Shown low. Except in special cases, the heat-resistant temperature of a membrane is the maximum operating temperature of a typical module of the membrane.

  When fouling occurs, the permeability of the membrane deteriorates, and the substance to be permeated does not permeate, so the separation of the membrane worsens, the liquid solvent becomes difficult to pass through, the permeation flow rate tends to decrease, and more frequent washing is performed. Deterioration due to the cleaning liquid and a stop of the processing for cleaning are required, and the lifetime of the film is short and the cost is increased.

  By using a membrane with a molecular weight cut-off of 2,000 or more and 4,000 or less as an ultrafiltration membrane, coloring components and chloride ions can be separated, and using a synthetic polymer composite membrane increases the durability of the membrane. Costs can be reduced. Moreover, by using a polyamide film, antifouling, heat resistance, and chemical resistance can be satisfied. Furthermore, the ultrafiltration membrane can be made into a spiral type module using a flat membrane-like membrane, thereby making it possible to make a compact facility with a wide membrane area.

As a reverse osmosis membrane, salt rejection of 0.05% (w / v) to 3.5% (w / v) sodium chloride aqueous solution is 40% to 60% at a pressure of 0.3 MPa to 5.6 MPa and a temperature of 25 ° C. %, And a synthetic polymer composite membrane can be used. In the synthetic polymer composite membrane, the membrane body is preferably a flat membrane.
In the present invention, the salt rejection is the same as the salt removal rate or the salt rejection rate, and is 0.05% (w / v) to 3.5% (w / v) at a pressure of 0.3 MPa to 5.6 MPa and a temperature of 25 ° C. v) The salt permeation difficulty is expressed as a percentage when the following aqueous sodium chloride solution is used, and the salt permeation ratio is subtracted from 100%. That is, what percentage of the salt in the solution has permeated is the salt permeation ratio, and the ratio of the salt that has not permeated is the salt rejection.

  The reverse osmosis membrane is preferably a polyamide membrane or a sulfonated polyethersulfone membrane. The polyamide film is as described above. The sulfonated polyethersulfone membrane is a charged membrane obtained by sulfonating a polyethersulfone membrane, and is a membrane having heat resistance, fouling resistance, and chemical resistance like a polyamide membrane. Sulfonated polyethersulfone membranes are marketed as charged membranes using sulfonated polyethersulfone, even if other materials are used in combination, even if the polymer constituting the functional layer of the membrane contains sulfonated polyethersulfone. Are included in this category.

  In the present invention, the reverse osmosis membrane is preferably a membrane that concentrates colored components on the concentrate side and concentrates chloride ions on the permeate side. A reverse osmosis membrane that hardly allows coloring components to pass through is less likely to pass salts and tends to have a low permeation rate. Therefore, it is necessary to select a membrane that can satisfy these opposing conditions as much as possible. In order to satisfy this condition, the decolorization rate of the reverse osmosis membrane on the permeate side at 420 nm and 520 nm is preferably 90% or more, and more preferably 94% or more. The chloride ion concentration rate on the permeate side of the reverse osmosis membrane is preferably 105% or more, more preferably 110% or more, and most preferably 120% or more.

Specifically, NTR-7450 (manufactured by Nitto Denko Corporation), NF270 (manufactured by Dow Chemical Company), SW04 (DRA4510) (Daisen Membrane Systems Co., Ltd.) can be used as the reverse osmosis membrane. NTR-7450 is a sulfonated polyethersulfone membrane that is a flat membrane-like synthetic polymer composite membrane, has a salt rejection of 40%, a maximum operating temperature of 90 ° C., and has fouling resistance. NF270 is a polyamide membrane of a flat membrane-like synthetic polymer composite membrane, having a salt rejection of 40 to 60% and a maximum use temperature of 45 ° C. SW04 is a polyamide membrane of a flat membrane-like synthetic polymer composite membrane, having a salt rejection of 15 to 60% and a maximum use temperature of 45 ° C.
In Examples 2 and 5 below, the permeation rate of SW04 was 8 ml / 30 minutes when the chromatographic separation waste solution of Brix 5 was treated at 65 ° C. under a pressure of about 0.5 MPa, and other membranes ( NTR-7450, NF-270) is lower than the transmission speed. However, the permeation rate varies depending on temperature, pressure, waste liquid properties such as Brix and viscosity. Therefore, there is a possibility of practical use by adjusting the temperature and pressure.

  In the present invention, the salt rejection of an aqueous sodium chloride solution of 0.05% (w / v) to 3.5% (w / v) is 40% to 60% under a pressure of 0.3 MPa to 5.6 MPa and a temperature of 25 ° C. By using a reverse osmosis membrane, the color components and chloride ions can be suitably separated. By using a synthetic polymer composite membrane, the durability of the membrane is increased and the cost is reduced. By using this film, a spiral type module can be obtained, and a large area and compact equipment can be obtained. Furthermore, prevention of fouling, heat resistance, and chemical resistance can be satisfied by using either a polyamide film or a sulfonated polyethersulfone film.

  In the present invention, as "incineration disposal", methods known to those skilled in the art such as spray incineration method, submerged combustion method, catalytic wet oxidation process, rotary kiln incineration, organic waste liquid / water emulsion incineration, fluidized bed incineration method and ordinary boiler incineration Can be used. Further, the concentrate obtained by the membrane treatment and bagasse discharged from the sugar factory may be burned together, that is, by spraying the concentrate on bagasse. The concentrate containing the coloring component obtained by the membrane treatment of the present invention contains almost no chloride ions. Therefore, even if combustion is performed with a normal boiler, there is no need to worry about boiler corrosion and operational problems, and there is no need for special specifications. Ordinary boilers are usually burned at 1,000 to 1,200 ° C. using coal, heavy oil, city gas, propane gas or the like as fuel.

  In the present invention, as the “waste water treatment”, a known waste water treatment such as a general biological treatment such as an activated sludge method or a methane fermentation method or an ozone oxidation method can be used. The permeate concentrated with chloride ions obtained by the membrane treatment of the present invention does not contain a hardly decomposable coloring substance. Thus, the permeate can be treated with the known waste water treatment.

[Example]
EXAMPLES Hereinafter, although an Example demonstrates this invention, this invention is not limited to these. In the examples, “%” means “% by weight” unless otherwise specified. Ash (salt) was measured using an ignition residue (550 ° C., 3 hours) measurement method. The amount of chloride ions was measured by anion chromatography. Specifically, DIONEX ion chromatograph (model number QIC analyzer), DIONEX guard column (IonPacAG4A-SC 4mm x 50mm, 10-32), DIONEX column (IonPacAS4A-SC 4mm x 50mm, 10-32), and Using a suppressor (AMMS III 4 mm) manufactured by DIONEX, measurement was performed at room temperature at a flow rate of 1.6 ml / min. The amount of sodium ion and potassium ion was measured by cation chromatography. Specifically, DIONEX ion chromatograph (model number QIC analyzer), DIONEX guard column (IonPac CG12 4mm x 50mm, 10-32), DIONEX column (IonPac CS12 4mm x 50mm, 10-32), and DIONEX Measurement was performed using a suppressor (CMMS II) at room temperature and a flow rate of 1.1 ml / min.

  The UF membranes (diameter 76 mm) shown in Table 1 below were attached to the stirring type ultra holder UHP-76K (manufactured by Advantech Toyo Co., Ltd.). Use 300 ml (65 ° C) of the chromatographic separation waste solution (see Table 2 below) from the second honey of the sugarcane production process by ion exchange chromatography as a stock solution and stir the stirring bar at a constant speed. Then, filtration was performed by applying a pressure of about 0.5 MPa with helium to obtain a concentrate and a permeate. During filtration, the stirring ultra holder was immersed in water at 65 ° C., and the liquid temperature during filtration was kept at 65 ° C. The initial permeation rate in each membrane was measured as the permeation amount per 30 minutes. Moreover, the color of the permeate was visually evaluated. The control is a chromatographic separation effluent without membrane treatment. The color of the permeated liquid was evaluated in four stages of dark brown, brown, light yellow, and colorless. The results are shown in Table 3 below.

DESAL GK、DESAL GH（ＧＥウォーター・テクノロジーズ社製）

DESAL GK, DESAL GH (manufactured by GE Water Technologies)

  All of the UF membranes of Example 1 had a permeation rate of 20 ml / 30 min or more, and the transmitted color was pale yellow (Table 3). If the heat resistance of the membrane is low, the high-temperature (60 ° C. or higher) molasses or waste liquid immediately after being obtained from the process cannot be treated. In addition, when the fouling resistance is low, the membrane is easily clogged and the permeation rate is low, so that the amount of waste liquid treated per unit time is reduced, and the washing is repeated, so that a running cost is required. Furthermore, if the chemical resistance is low, the film is likely to be deteriorated by a chemical used for cleaning the film, such as sodium hypochlorite, and the film life is shortened. The UF membrane of Example 1 has no problem in terms of these characteristics (Table 1).

  Using the RO membrane (diameter 76 mm) shown in Table 4 below, the initial permeation rate was measured and the permeate was evaluated by the same method as in Example 1. The stock solution is the same as in Example 1. The results are shown in Table 5.

NTR-7450（日東電工株式会社製）
NF270（ダウ・ケミカル・カンパニー製）
SW04（ダイセン・メンブレン・システムズ株式会社）

NTR-7450 (Nitto Denko Corporation)
NF270 (manufactured by Dow Chemical Company)
SW04 (Daisen Membrane Systems Co., Ltd.)

  The RO membrane of Example 2 had a pale yellow permeate (Table 5). NTR-7450 has no problem in terms of the above characteristics (Table 4).

[Comparative Example 1]
Using the RO membrane (diameter 76 mm) shown in Table 6 below, the initial permeation rate was measured and the color of the permeate was evaluated in the same manner as in Example 1. The stock solution is the same as in Example 1. The results are shown in Table 7.

NTR-7410（日東電工株式会社製）
DESAL DK（ＧＥウォーター・テクノロジーズ社製）
DRC3000（ダイセン・メンブレン・システムズ株式会社）
NF90（ダウ・ケミカル・カンパニー製）
PES10（ナディアフィルトレーション社製）

NTR-7410 (Nitto Denko Corporation)
DESAL DK (manufactured by GE Water Technologies)
DRC3000 (Daisen Membrane Systems Co., Ltd.)
NF90 (manufactured by Dow Chemical Company)
PES10 (manufactured by Nadia Filtration)

[Discussion]
Non-Patent Document 11 discusses the use of NTR-7410 for decolorization of yeast fermentation wastewater. However, as described in the comparative example, the permeability was too high, and the coloring component was considerably transmitted, so that a satisfactory result could not be obtained for the purpose of the present invention.

The same DESAL GK membrane (diameter 76 mm) as in Example 1 was attached to a stirring type ultra holder UHP-76K (manufactured by Advantech Toyo Co., Ltd.). A 300 ml (65 ° C) solution of molasses (Brix 81.4) from the sugarcane production process diluted to Brix 5 is placed in a stirring type ultra holder and the pressure is about 0.5 MPa with helium while stirring the stirring bar at a constant speed. And filtered. During filtration, the stirring type ultra holder was immersed in water at 65 ° C., and the liquid temperature during filtration was kept at 65 ° C. When the amount of the concentrated liquid reached 100 ml, 200 ml of distilled water was added to the concentrated liquid side and filtration was performed again. This operation was repeated twice to obtain a concentrated liquid and a permeated liquid.
In order to measure the ash content and chloride ion amount of the obtained concentrated liquid, 100 ml of the concentrated liquid was lyophilized to obtain 1.1 g of a brown powder. The results are shown in Table 8.

As a result, the amount of ash and chloride ions in the concentrate decreased compared to the molasses as the raw material.
This can reduce the corrosion and wear of the boiler water pipe when incinerated with the boiler.

Using the UF membrane (diameter 76 mm) shown in Table 9 below, in the same manner as in Example 1, the chromatographic separation waste solution (different from the chromatographic separation waste solution of Example 1 in a lot) is used as a stock solution for laboratory membrane permeation. Tests were conducted to determine the decolorization rate, chloride ion concentration rate, and permeation rate. The absorbance at 420 nm and 560 nm of the stock solution was 1.373 and 0.300, respectively, and the chloride ion concentration was 2,628 (ppm).
(Decolorization rate)
The decolorization rate was calculated according to the following equation by measuring the absorbance of the stock solution and the absorbance of the permeate at 420 nm and 560 nm, respectively. The absorbances of 420 nmm and 560 nm are wavelengths at which absorption of colored components in the sugar production process is large.
Decolorization rate (%) = (absorbance of stock solution−absorbance of permeate) ÷ absorbance of stock solution × 100
The absorbance of the stock solution was measured by diluting the stock solution 10 times with distilled water. The absorbance of the permeate was measured by diluting the permeate 10 times with distilled water.
The evaluation criteria for the decolorization rate are as follows.
○: Decolorization rate at 420 nm is 90% or more and decoloration rate at 520 nm is 90% or more ×: Decoloration rate at 420 nm is less than 90% or decoloration rate at 520 nm is less than 90% (Cl ion concentration rate)
The chloride ion concentration ratio was calculated by taking the permeate solution until 80 ml of permeate solution was obtained and thoroughly homogenizing it, measuring the chloride ion concentration, and setting the chlorine ion concentration of the stock solution as 100%.
The evaluation criteria of the chloride ion concentration rate are as follows.
○: 105% or more ×: Less than 105% (transmission speed)
The initial permeation rate indicates the amount of permeate obtained in 30 minutes from the start of permeation.
The evaluation criteria for the transmission speed are as follows.
○: 5 ml or more ×: Less than 5 ml The results are shown in Table 9.

  Both DESAL GK and DESAL GH had a decolorization rate (420 nm, 560 nm) of 90% or more, and in particular, the decolorization rate at 560 nm was 97% or more. Further, since the chloride ion concentration rate was increased, the salt was concentrated on the permeate side. From these results, the coloring component and the chlorine ion are separated (ie, concentrated) on the concentrated liquid side and the permeated liquid side, respectively. Furthermore, the initial permeation rate was as high as 19 ml and 34 ml.

[Comparative Example 2]
Using a UF membrane (diameter: 76 mm) shown in Table 10 below, a membrane permeation test at the laboratory level was conducted using the chromatographic separation waste solution as a stock solution by the same method as in Example 1, and the decolorization rate, chloride ion concentration rate, The transmission speed was determined for each. The evaluation criteria for the decolorization rate, chloride ion concentration rate, and permeation rate are the same as in Example 4. The stock solution is the same as in Example 4.
The results are shown in Table 10.

DESAL GE、DESAL GM、DESAL PW（ＧＥウォーター・テクノロジーズ社製）
UK-10（アドバンテック東洋株式会社製）
NTU-3150（日東電工株式会社製）

DESAL GE, DESAL GM, DESAL PW (manufactured by GE Water Technologies)
UK-10 (manufactured by Advantech Toyo Corporation)
NTU-3150 (manufactured by Nitto Denko Corporation)

  DESAL GE had an initial transmission rate as low as 15, and a decolorization rate at 420 nm of less than 90%. Membranes other than DESAL GE are excellent in that the initial permeation rate exceeds 40. However, the decolorization rate at 420 nm and 560 nm was 90% or less. Further, the concentration rate of chloride ions was not concentrated in DESAL PW and NTU-3150. Therefore, in the membrane shown in Table 10, it is difficult to separate chlorine ions and colored components.

Using a RO membrane (diameter: 76 mm) shown in Table 11 below, a membrane permeation test at the laboratory level was conducted using the chromatographic separation waste solution as a stock solution in the same manner as in Example 1, and the decolorization rate, chloride ion concentration rate, permeation rate were measured. I asked for speed. The evaluation criteria for the decolorization rate, chloride ion concentration rate, and permeation rate are the same as in Example 4. The stock solution is the same as in Example 4.
The results are shown in Table 11.

  In any of the NTR-7450, NF270, and SW04 films, the decolorization rate (420 nm, 560 nm) was 94% or more, and in particular, the decoloration rate at 560 nm was 99% or more. Moreover, since the chloride ion concentration rate is 115% or more, chloride ions are concentrated on the permeate side. This separates (that is, concentrates) the coloring components and chloride ions on the concentrate side and the permeate side, respectively. Furthermore, the initial permeation rate was 8 to 33 ml.

[Comparative Example 3]
Using a RO membrane (diameter 76 mm) shown in Table 12 below, a membrane permeation test at the laboratory level was conducted using the chromatographic separation waste solution as a stock solution by the same method as in Example 1, and the decolorization rate, chloride ion concentration rate, The transmission speed was determined for each. The evaluation criteria for the decolorization rate, chloride ion concentration rate, and permeation rate are the same as in Example 4. The stock solution is the same as in Example 4.
The results are shown in Table 12.

DRC-1000S（ダイセン・メンブレン・システムズ株式会社）

DRC-1000S (Daisen Membrane Systems Co., Ltd.)

  NTR-7410, DRC-1000S, and PES10 were excellent in that the initial transmission rate exceeded 20, but DESL DK had an initial transmission rate of 4, which was not a sufficient initial transmission rate. Except for DESAL DK and NTR-7410, the decolorization rate was less than 90%. Further, the chloride ion concentration rate was not concentrated in DRC-1000S. Accordingly, these membranes are inferior in any one or more of decolorization rate, chloride ion concentration rate, and permeation rate.

(Desalination rate test using actual machine)
Diluted 18 kg of molasses (Brix 86.2) obtained from a sugar factory to Brix 20 with distilled water, inoculated with baker's yeast (Saccharomyces cerevisiae IFO3040), and then cultured at 37 ° C for 24 hours under aerobic conditions did. The obtained culture broth was centrifuged at 8,000 × g for 15 minutes, and the supernatant was suction filtered with Toyo filter paper No.2. As a result of freeze-drying this filtrate, 8.0 kg of brown powder (waste liquid from the fermentation process) was obtained. 200 L of pure water was added to this powder, and ultrafiltration was performed at 60 ° C. with a spiral ultrafiltration module DESAL GK8040 (manufactured by GE Water Technologies) to obtain 50 L of a concentrated solution. After adding 150 L of pure water to this concentrate, ultrafiltration was again performed using a spiral ultrafiltration module DESAL GK8040 to obtain 50 L of concentrate and permeate.
The spiral ultrafiltration module DESAL GK8040 is a module type using the same membrane as the DESAL GK membrane used in Examples 1 and 3.
In order to measure the ash content and chloride ion content of the obtained concentrated liquid, the total amount (50 L) of the obtained concentrated liquid was freeze-dried to obtain 2.7 kg of a brown powder. The results are shown in Table 13.

As a result, the amount of ash and chloride ions in the concentrated liquid decreased compared to the waste liquid in the fermentation process.
This can reduce the corrosion and wear of the boiler water pipe when incinerated with the boiler.

(Desalination rate test using actual machine)
10 m ³ of chromatographic separation waste solution (Brix5, 75 ℃), the waste solution after collecting sugar by ion-exchange chromatography from the second honey in the sugarcane sugar production process, is used for spiral ultrafiltration module DESAL GK8040 (membrane area 22.3 m ² , Membrane inlet pressure 1 MPa) (manufactured by GE Water Technologies). Filtration conditions were set such that the flow rate through the membrane at the beginning of the flow was 6.3 m ³ / hr, the permeate recovery flow rate was 0.6 m ³ / hr, and the concentrate recovery flow rate was 0.3 m ³ / hr. As a result, to recover the permeate 6 m ³ and concentrate 3 m ³ (Step 1). After adding 3 m ³ of water to the collected concentrated liquid 3 m ³ and mixing, it was filtered with a spiral ultrafiltration module DESAL GK8040 (membrane area 22.3 m ² ) (membrane inlet pressure 1 MPa) in the same manner as above. . Filtration conditions were set such that the flow rate through the membrane at the beginning of the flow was 5.3 m ³ / hr, the permeate recovery flow rate was 0.6 m ³ / hr, and the concentrate recovery flow rate was 0.4 m ³ / hr. As a result, 3 m ^{3 of} concentrated liquid and 2 m ³ of permeate were recovered (step 2).
In order to measure the amount of sodium ion, potassium ion and chlorine ion in the obtained concentrated liquid, 1 kg of the concentrated liquid recovered in Step 1 and Step 2 was freeze-dried to obtain 64.46 g and 51.56 g of brown powder, respectively. It was. The results are shown in Table 14.

As a result, the content of sodium ion, potassium ion and chloride ion in the concentrate recovered in step 1 is reduced compared to the chromatographic separation waste solution, and the content of sodium ion, potassium ion and chloride ion in the concentrate recovered in step 2 Decreased compared to the concentrate recovered in step 1.
This can reduce the corrosion and wear of the boiler water pipe when incinerated with the boiler.

(Incineration test of membrane desalination waste liquid)
The same membrane treatment as in Example 7 was performed, and the concentrated liquid in Step 2 was recovered. The concentrate was concentrated under reduced pressure to about Brix 50. The liquid was sprayed onto bagasse generated at 8.3 t / hr at 150 L / hr and burned in a stalker-type bagasse-fired boiler (trade name: N-900 natural circulation boiler, manufactured by Takuma) Approximately 900 t / day sugar factory). Compared to before and after combustion of the waste liquid, there was some slag adhesion to the water pipe, and no significant change in boiler operation was observed. After burning continuously for 14 days, the boiler was stopped and the inside was observed. As a result, no corrosion of the super heater was observed, and no large clinker was generated on the stalker. From this result, it was confirmed that the waste liquid subjected to membrane treatment has no trouble in combustion.

(Long-term continuous treatment test with actual machine)
A long-term continuous membrane treatment test was conducted using chromatographic separation waste liquid (Brix 3.5 to 5.5, about 75 ° C.) continuously discharged from the sugar cane sugar production process. The chromatographic separation waste solution was subjected to membrane treatment using an UF apparatus incorporating 16 spiral ultrafiltration modules DESAR GK8040. Two UF devices of the same type (No. 1 and No. 2) were installed, and the operation and washing were switched every 6 hours so that one UF device was washed while the other UF device was washed. After passing through the membrane, the permeated liquid and a part of the concentrated liquid were discharged out of the apparatus, and the remaining concentrated liquid was permeated again as a processing liquid into the UF apparatus as a circulating liquid. The remaining concentrated liquid is processed again as a circulating liquid in order to increase the linear velocity of the filtration process. A new chromatographic separation waste liquid was added to the circulating liquid flow so that the total amount of the permeated liquid and the discharged concentrated liquid was the same (that is, additional chromatographic waste liquid = amount of permeated liquid + concentrated concentration to be discharged). Liquid volume). FIG. 3 shows a conceptual diagram of the flow of chromatographic separation waste liquid, concentrated liquid, permeate and circulating liquid in the UF apparatus.

Liquid temperature (° C) of UF device No. 1 and No. 2, UF device inlet pressure (MPa), concentration (out) liquid pressure (MPa), permeate (out) liquid flow rate (m ³ / h), concentration (out ) The liquid flow rate (m ³ / h) and the circulating fluid (before supply liquid addition) flow rate (m ³ / h) were measured every other day, and the changes are shown in FIGS. 1 and 2, respectively. The UF apparatus was washed with water, washed with 100 ppm sodium hypochlorite solution containing 0.1% sodium hydroxide, and finally washed with water.

In addition, in order to confirm how the membrane processing capacity changed before and after long-term treatment, absorbance at 420 nm, absorbance at 560 nm, chloride ion concentration, sulfate ion concentration, sodium ion concentration, potassium ion concentration , Conductivity, and total dissolved solids (TDS) were measured. Absorbance showed the measured value of the liquid diluted 50 times with distilled water.
The results are shown in Table 15.

  As a result, the liquid temperature, UF inlet pressure, concentrate pressure, permeate flow rate, concentrate flow rate, and circulating fluid flow rate were stable during the test period (68 days) in both UF devices. Moreover, the decolorization ability and chloride ion concentration ability of the membrane were not reduced by the long-term treatment.

  The present invention relates to a waste liquid treatment comprising separating a sugar liquid waste, a sugar liquid waste liquid, or a waste liquid from a fermentation process of the sugar liquid waste liquid into a concentrated liquid containing coloring components and a permeate containing chloride ions by membrane treatment. Provide a method. Therefore, the present invention has industrial applicability.

It is a figure which shows the amount of permeated liquid of UF apparatus No. 1, a concentrated flow volume, a circulating flow volume, and a liquid temperature. It is a figure which shows UF inlet pressure, concentrated liquid pressure, and liquid sound of UF apparatus No.1. It is a figure which shows the amount of permeated liquid of UF apparatus No. 2, a concentrated flow volume, a circulating flow volume, and a liquid temperature. It is a figure which shows UF inlet pressure, concentrated liquid pressure, and liquid sound of UF apparatus No.2. It is a conceptual diagram of the flow of chromatographic separation waste liquid, concentrated liquid, permeated liquid, and circulating liquid in UF apparatuses No. 1 and No. 2.

Explanation of symbols

1 UF equipment 2 UF membrane module

Claims (9)

Sugar waste honey, sugar waste, or waste from the fermentation process of sugar waste honey, Ri fractional molecular weight of 2,000 or more 4,000 or less der, concentrate and chlorine containing coloring components using an ultrafiltration membrane is a polyamide-based film A method for treating a waste liquid, comprising separating into a permeate containing ions. Ultrafiltration membrane is a spiral module, the processing method of the waste liquid of claim 1. The salt rejection of 0.05% (w / v) to 3.5% (w / v) sodium chloride aqueous solution is 0.3 MPa or more and 5.6 MPa or less for sugar making waste, sugar making waste liquid, or waste liquid from fermentation process of sugar making waste. of Ri der 40% to 60% or less at a temperature of pressure and 25 ° C., that is separated into a permeate containing concentrate and chlorine ions containing a coloring component using a reverse osmosis membrane is a polyamide-based film Including waste liquid treatment methods. The waste liquid treatment method according to claim 3 , wherein the reverse osmosis membrane is a nanofiltration membrane. The waste liquid treatment method according to claim 1 or 2 , wherein the polyamide-based membrane is a flat membrane-like composite membrane . The waste liquid treatment method according to claim 3 or 4, wherein the polyamide-based membrane is a flat membrane-like composite membrane. The processing method of the waste liquid as described in any one of Claims 1-6 including incinerating a concentrate. The processing method of the waste liquid as described in any one of Claims 1-7 including draining a permeate. The waste liquid treatment method according to claim 7 , wherein the incineration disposes the concentrated liquid and bagasse together.

Images