WO2010110143A1 - 石炭ガス化排水の処理方法 - Google Patents
石炭ガス化排水の処理方法 Download PDFInfo
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- WO2010110143A1 WO2010110143A1 PCT/JP2010/054539 JP2010054539W WO2010110143A1 WO 2010110143 A1 WO2010110143 A1 WO 2010110143A1 JP 2010054539 W JP2010054539 W JP 2010054539W WO 2010110143 A1 WO2010110143 A1 WO 2010110143A1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/70—Treatment of water, waste water, or sewage by reduction
- C02F1/705—Reduction by metals
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/06—Treatment of sludge; Devices therefor by oxidation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/106—Selenium compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
- C02F2101/14—Fluorine or fluorine-containing compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
Definitions
- the present invention relates to a method for treating coal gasification wastewater, and more specifically, efficiently removes COD components such as SS, fluorine, cyanide, selenium and ammonia contained in the gas washing wastewater generated in the coal gasification step,
- the present invention relates to a method for treating coal gasification wastewater to obtain treated water of good water quality that can be discharged or reused.
- Coal is the richest reserve of fossil fuels, has a wide range of existence on the earth, and is said to become the main fuel for thermal power generation in the future.
- Coal gasification combined power generation that combines gas turbine power generation and steam turbine power generation, which are more efficient than conventional thermal power generation, and coal gas that incorporates fuel cell power generation in order to effectively use limited fossil fuels Fuel cell power generation is attracting attention.
- Coal gasification combined power generation is a coal gasification furnace that converts carbon monoxide and hydrogen into gas fuels by partially oxidizing the coal, and a gas purification device that removes dust, sulfur, etc. from the generated gas
- This is a power generation system that combines a gas turbine combined cycle power plant using the refined gas as fuel.
- Coal gas is required to use the same gas turbine body as the liquefied natural gas-fired gas turbine.
- FIG. 7 is a process system diagram of an example of a coal gasification combined power generation facility.
- pulverized coal is conveyed from the pulverized coal conveying device 101 by an air stream, and sent to the coal gasification furnace 102 together with oxygen.
- the pulverized coal is partially oxidized at 1,500 to 1,800 ° C. and 2 to 3 MPa, and the generated gas containing carbon monoxide and hydrogen as main components is sent to the syngas cooler 103 from the top of the furnace.
- the generated slag is discharged from the furnace bottom.
- the gas passes through the dust filter 104 and the dust is removed, the gas is washed with water in the washing tower 105. Waste water generated in the water washing tower 105 is sent to the waste water treatment device 106.
- the water-washed gas is sent to the desulfurization tower 108 through the COS converter 107, and the sulfur content is removed.
- the purified gas is sent to the gas turbine 109 and combusted to drive the turbine 109.
- the exhaust from the gas turbine 109 is sent to the exhaust heat recovery boiler 110, and the steam turbine 111 is driven by the steam generated by recovering the exhaust heat.
- coal gasification wastewater contains COD components such as SS, fluorine, cyanide and ammonia, selenium, etc. It is necessary to remove and treat to the quality of water that can be discharged or water that can be reused.
- coal gasification wastewater treatment technology includes thermal hydrolysis of coal gasification wastewater, decomposition of cyanide, removal of metals separated and precipitated from the cyano complex, and wet catalytic oxidation of COD components.
- a removal method has been proposed (Patent Document 1).
- Patent Document 2 a method of performing catalytic wet oxidation treatment on non-catalytic wet oxidation treatment for cyanide-containing wastewater has been proposed.
- a method for treating fluorine in wastewater a method of coagulating and precipitating by adding a calcium compound, a magnesium compound, or an aluminum compound to the wastewater is known, and an ammonia stripping method is known for treating ammonia. ing.
- the coal gasification wastewater to be treated in the present invention contains high-concentration SS, COD components such as fluorine, cyanide, and ammonia, selenium, etc. in addition to high-concentration SS.
- COD components such as fluorine, cyanide, and ammonia, selenium, etc.
- JP 2007-289841 A JP-A-8-290174 Japanese Patent Laid-Open No. 9-290297
- the present invention has been made in view of the above-described conventional situation, and includes SS, fluorine, cyanide, selenium, ammonia, and COD components contained in coal gasification wastewater such as gas washing wastewater generated in the coal gasification step. It aims at providing the processing method of the coal gasification waste_water
- the method for treating coal gasification wastewater of the present invention is a method for treating coal gasification wastewater, (1) Fluorine removal step for removing fluorine by coagulation precipitation; (2) a cyanide decomposition step for decomposing cyanide by wet oxidation or thermal hydrolysis; (3) a selenium treatment step for reducing selenate ions with a metal reductant, and (4) a COD / ammonia removal step for removing COD and / or ammonia, wherein (1) is performed prior to (2) It is characterized by that.
- the method for treating coal gasification waste water according to claim 2 is the method according to claim 1, wherein the cyan decomposition step is a non-catalytic wet oxidation step, the COD / ammonia removal step is a catalytic wet oxidation step, (1), (2), (3), (4) in order.
- the method for treating coal gasification wastewater according to claim 3 is the method according to claim 1, wherein the cyan decomposition step is a non-catalytic wet oxidation step, the COD / ammonia removal step is a catalytic wet oxidation step, (1), (2), (4), (3) in that order.
- the method for treating coal gasification wastewater according to claim 4 is the method according to claim 1, wherein the cyan decomposition step is a non-catalytic wet oxidation step, the COD / ammonia removal step is an ammonia stripping step, Is in the order of (1), (2), (3), (4).
- the method for treating coal gasification wastewater according to claim 5 is the method according to claim 1, wherein the COD / ammonia removal step is a biological treatment step, and the order of each step is (1), (2), (3), (4) It is characterized by the order.
- a method for treating coal gasification wastewater according to claim 6 is the denitrification method according to claim 4, wherein the biological treatment step uses an autotrophic denitrifying bacterium having ammonia ions as electron donors and nitrite ions as electron acceptors. Including a process.
- the method for treating coal gasification wastewater according to claim 7 is characterized in that in any one of claims 1 to 6, it has an advanced treatment step of treating the treated water in the COD / ammonia removal step.
- coal gasification wastewater of the present invention According to the method for treating coal gasification wastewater of the present invention, SS, fluorine, cyanide, selenium, ammonia, and COD components contained in coal gasification wastewater such as gas washing wastewater generated in the coal gasification process are efficiently removed. Thus, it is possible to obtain treated water with good water quality that can be discharged or reused.
- the method for treating coal gasification wastewater of the present invention comprises the following steps (1) to (4), wherein step (1) is performed prior to step (2).
- Fluorine removal step for removing fluorine by coagulation precipitation
- Cyanide decomposition step for decomposing cyanide by wet oxidation or thermal hydrolysis
- Selenium treatment step for reducing selenate ions by metal reductant
- COD / ammonia removal step for removing COD and / or ammonia
- the coal gasification wastewater to be treated is wastewater discharged from a coal gasification process such as gas cleaning wastewater discharged from a water washing tower of the above-mentioned coal gasification combined power generation facility.
- a coal gasification process such as gas cleaning wastewater discharged from a water washing tower of the above-mentioned coal gasification combined power generation facility.
- the treatment method of the coal gasification process from which gasification wastewater is discharged For example, the moving bed type Lurgi method, the spouted bed type Copper-Stochek method, the fluidized bed type Winkler method, and the pressurized fluidized bed
- the high gas method of the type and the Texaco method of the pressurized spouted bed type can be exemplified.
- the method of the present invention is suitably applied to the treatment of coal gasification wastewater such as combined coal gasification combined power generation and coal gasification fuel cell power generation that require a large-scale coal gasification device and requires stable operation over a long period of time. be able to.
- the water quality of coal gasification wastewater discharged from such a coal gasification process is as follows. pH: 7-9 SS: 20-1000mg / L Fluorine: 20 to 2000 mg / L Cyan: 10-150mg / L Selenium: 0.5-10mg / L Ammonia: 2000 to 4000 mg / L (as N) COD: 200-1500 mg / L
- Examples of the method for removing fluorine by coagulation precipitation include the following methods. (1) A calcium compound is added to the waste water to form hardly soluble calcium fluoride by the following reaction, which is separated and removed. Ca 2+ + 2F ⁇ ⁇ CaF 2 (2) A magnesium compound is added to the waste water, and fluorine ions are adsorbed on magnesium hydroxide and removed by the following reaction. Mg 2+ + 2OH ⁇ + F ⁇ ⁇ Mg (OH) 2 ⁇ F ⁇ (3) An aluminum compound is added to the waste water, and fluorine ions are adsorbed and removed by aluminum hydroxide by the following reaction. Al 3+ + 3OH ⁇ + F ⁇ ⁇ Al (OH) 3 ⁇ F ⁇
- the above methods (1) to (3) can be carried out in combination of any two or more, and in particular, by removing the fluorine with the magnesium compound (2) after removing the fluorine with the calcium compound (1), Fluorine can be removed to a high degree. In the method using the magnesium compound (2) or the aluminum compound (3), fluorine can be highly removed only by this method.
- the treatment with the magnesium compound of (2) or the aluminum compound of (3) may be carried out at a subsequent stage of (1) as an advanced treatment after the treatment with the calcium compound of (1).
- SS in waste water can be removed at the same time as fluorine by performing a coagulation sedimentation treatment.
- the wastewater is not made acidic to pH.
- Neutral to alkaline treatment is required.
- the method of (1) using a calcium compound can be carried out at pH neutral to alkaline (specifically, pH 6 to 9)
- the method of (2) using a magnesium compound is alkaline (specifically Can be treated at a pH of 9 or more, preferably 11 or more
- the method (3) using an aluminum compound is preferred because the treatment can be carried out at a pH neutrality (specifically, pH 6 to 8).
- calcium salts such as calcium chloride (CaCl 2 ) can be used in addition to basic calcium compounds such as calcium oxide (CaO) and calcium hydroxide (Ca (OH) 2 ).
- the amount added is preferably about 1 to 3 times equivalent to the fluorine ions in the wastewater in terms of Ca.
- an acid such as hydrochloric acid (HCl) or sulfuric acid (H 2 SO 4 ) or an alkali such as sodium hydroxide (NaOH) or potassium hydroxide (KOH) is added as necessary so that the above pH condition is satisfied. It is preferable.
- nonionic polymer flocculants such as polyacrylamide, polyethylene oxide, urea-formalin resin, polyaminoalkyl methacrylate, polyethyleneimine, polydiallylammonium halide, Cationic polymer flocculants such as chitosan, anionic polymer flocculants such as sodium polyacrylate, polyacrylamide partial hydrolyzate, partially sulfomethylated polyacrylamide, poly (2-acrylamide) -2-methylpropane sulfate, etc. 1 type (s) or 2 or more types can be used.
- nonionic polymer flocculants such as polyacrylamide, polyethylene oxide, urea-formalin resin, polyaminoalkyl methacrylate, polyethyleneimine, polydiallylammonium halide, Cationic polymer flocculants such as chitosan, anionic polymer flocculants such as sodium polyacrylate, polyacrylamide partial hydrolyzate, partially sulfomethylated polyacrylamide
- anionic polymer flocculants are excellent in agglomeration effect and can be used particularly preferably.
- the amount of the polymer flocculant added is usually about 0.1 to 5 mg / L, although it varies depending on the quality of the wastewater to be treated and the type of polymer flocculant used.
- magnesium salts such as magnesium sulfate (MgSO 4 ) and magnesium chloride (MgCl 2 ) can be used, and the amount added is determined by experimentally determining the amount of fluorine adsorbed on magnesium hydroxide.
- the fluorine concentration of the treated water is 10 mg / L or less, it is 10 to 20 times (weight ratio) of the fluorine to be removed in terms of Mg.
- an alkali such as KOH.
- the flocculant used for the flocculation treatment after adding the magnesium compound to the wastewater the same one as in the case of the calcium compound can be used, and the amount added is the quality of the wastewater to be treated and the polymer flocculant used. Usually, it is about 0.1 to 5 mg / L although it varies depending on the type.
- an aluminum salt such as aluminum sulfate (Al 2 (SO 4 ) 3 , sulfate band), polyaluminum chloride (PAC), etc.
- Al 2 (SO 4 ) 3 sulfate band
- PAC polyaluminum chloride
- the addition amount thereof is fluorine of aluminum hydroxide.
- the adsorption amount is experimentally determined and determined. Generally, when the fluorine concentration of the treated water is 10 mg / L or less, it is 1 to 10 times (weight ratio) of fluorine to be removed in terms of Al. If necessary so that the pH conditions described above, HCl, acid or NaOH, such H 2 SO 4, it is preferable to add an alkali such as KOH.
- the aggregating agent used for the aggregating treatment after adding the aluminum compound to the waste water the same one as in the case of the calcium compound can be used, and the amount added is the quality of the waste water to be treated and the polymer aggregating agent used. Usually, it is about 0.1 to 5 mg / L although it varies depending on the type.
- the separated sludge separated by the coagulation sedimentation treatment is returned and added to the wastewater to be treated, and calcium fluoride is precipitated with the returned sludge as the core, thereby increasing the sludge concentration and reducing the sludge. Volume can be reduced.
- FIG. 1 is a system diagram showing an example of a fluorine removal step (1) suitable for the present invention.
- the method using the calcium compound (1) and the method (2) using the magnesium compound are used in combination.
- coal gasification wastewater which is raw water
- first reaction tank 2 of the Ca coagulation sedimentation step I coal gasification wastewater
- a calcium compound such as Ca (OH) 2
- the solution is introduced into the first pH adjusting tank 3
- acid such as HCl and H 2 SO 4 is added, and stirred at pH 6-9 to precipitate CaF 2
- Aggregation treatment is performed by adding a polymer flocculant and stirring.
- the agglomerated water is subjected to solid-liquid separation in the first sedimentation tank 5, a part of the separated CaF 2 sludge is returned to the first reaction tank 2 and the remainder is discharged out of the system.
- the returned sludge may be introduced into the raw water tank 1. Further, the return sludge may be mixed with the calcium compound in advance and added to the first reaction tank 2. The amount of returned sludge is preferably about 20 to 50 times that of the generated sludge.
- the treated water of the Ca coagulation precipitation step I that is, the separated water of the first precipitation tank 5 is then introduced into the second reaction tank 6 of the Mg coagulation precipitation step II, and the magnesium compound such as MgSO 4 and the remaining calcium are removed.
- alkali such as NaOH and stir at pH 10-11.
- Mg (OH) 2 is precipitated, and fluorine is adsorbed on the Mg (OH) 2, and is then introduced into the second aggregating tank 8, and a polymer flocculant is added and agitation is performed.
- the agglomerated water is solid-liquid separated in the second sedimentation tank 9, a part of the separated sludge is returned to the second reaction tank 6, and the remainder is discharged out of the system.
- transduce return sludge into the 1st reaction tank 2 of a Ca coagulation sedimentation process.
- the amount of the returned sludge is preferably an amount so that the SS concentration in the reaction tank at the return destination is 2000 to 10,000 mg / L from the viewpoint of scale prevention.
- Na 2 CO 3 is added to remove Ca remaining in the treated water of the Ca coagulation precipitation step I, and carbon dioxide gas may be used in addition to Na 2 CO 3 .
- the addition amount is preferably about 1 to 2 times equivalent to Ca.
- the separated water in the second sedimentation tank 9 may be fed to the next process as it is, but as shown in FIG. 1, it is possible to highly remove SS by filtering with a filtration device 10 such as a sand filter. It is preferable in preventing clogging and scale failure due to SS in the subsequent process.
- fluorine in coal gasification wastewater is highly removed to 10 mg / L or less.
- fluorine in coal gasification wastewater it is preferable that fluorine in coal gasification wastewater is highly removed to 10 mg / L or less.
- the oxidative decomposition of cyan is carried out in a neutral or alkaline manner, but neutral is preferable when the COD component is also oxidized and decomposed at the same time. In the absence of an oxidizing agent, this cyanide hydrolysis is alkaline.
- an alkali such as NaOH is added to the wastewater to be treated as necessary, preferably at pH 9 or more, more preferably at pH 10 or more, most preferably at pH 11-12.
- the thermal hydrolysis treatment is preferably performed while heating to 101 to 210 ° C., more preferably 120 to 180 ° C., and maintaining the pressure to maintain the liquid phase of the wastewater to be treated.
- the reaction rate of thermal hydrolysis is slow, which is not preferable.
- the temperature of the thermal hydrolysis treatment is less than 101 ° C.
- the reaction rate is slow, and it may take a long time for the thermal hydrolysis treatment.
- the higher the temperature of the thermal hydrolysis treatment the faster the hydrolysis reaction.
- the temperature of the thermal hydrolysis treatment exceeds 210 ° C., a pressure-resistant structure of 2 MPa or more is required, and the cost of equipment and operation management increases. There is a fear.
- the temperature of the thermal hydrolysis treatment is 180 ° C. or less, the treatment can be performed at a pressure of 1 MPa or less.
- the time for the thermal hydrolysis treatment can be appropriately selected according to the temperature of the thermal hydrolysis treatment. For example, when the thermal hydrolysis treatment is continuously performed at 160 ° C., the average residence time in the thermal hydrolysis treatment system is preferably 1 hour or longer.
- the oxidizing agent used for wet oxidation is not particularly limited, and examples thereof include oxygen gas, oxygen-enriched air, air, and hydrogen peroxide. These may be used alone or in combination of two or more. Of these, hydrogen peroxide is particularly preferably used because it is liquid and easy to handle and has good oxidative decomposition performance of the COD component.
- the amount of oxidant used is not particularly limited, but it should be 1.1 to 3 times, especially 1.5 to 2.5 times the theoretical amount required for oxidative decomposition of cyanide in the wastewater and COD components. It is preferable.
- the heating temperature condition in this wet oxidation may be the same as in the above-mentioned thermal hydrolysis, but the pH condition may be neutral to alkaline as described above, but the COD component is also oxidized and decomposed simultaneously. It is preferable to use neutral conditions. Therefore, when the treated water in the fluorine removal step (1) is alkaline, an acid such as HCl or H 2 SO 4 is added to adjust the pH to near neutrality, and then subjected to a wet oxidation treatment. Is preferred.
- Cyanide in the waste water supplied to the cyan decomposition step (2) exists as an iron cyanide complex.
- this cyan decomposition step (2) is preferably a non-catalytic wet oxidation step without using a catalyst.
- FIG. 2 is a system diagram showing an example of a cyan decomposition step (2) suitable for the present invention.
- wastewater to be treated (treated water in the fluorine removal step (1) in the present invention) is first introduced into the pH adjustment tank 11.
- an acid such as H 2 SO 4 is added to adjust the pH to about pH 7, and then heated by the heat exchanger 12 (and a heater (not shown)) and introduced into the wet oxidation reaction tower 13.
- An oxidant such as H 2 O 2 is injected into the inflow water of the reaction tower 13, and cyanide in the waste water is wet oxidatively decomposed in the presence of the oxidant in the reaction tower 13.
- the effluent water (treated water) of the reaction tower 13 is heat-exchanged with the inflow water of the reaction tower 13 by the heat exchanger 12 and then fed to the next step. Nitrogen gas and carbon dioxide generated by the decomposition of cyan are discharged from the upper part of the reaction tower 13.
- cyan decomposition step (2) it is preferable to highly remove cyan in the coal gasification wastewater to 1 mg / L or less.
- Specific treatment methods in the selenium treatment step (3) include a method using metal iron as the metal reductant and a method using an alloy or mixture of metal titanium and other metals such as aluminum.
- the method using iron reductant is to bring wastewater adjusted to pH 5 or less into contact with iron, reduce selenate by the following reaction, and co-precipitate the precipitated selenium together with iron ions by the following reaction.
- iron reductant metallic iron
- a pH adjuster is added to the wastewater to be treated to adjust the pH to 5 or less, preferably 2 to 3.
- the pH adjusting agent used can be suitably used HCl, and H 2 SO 4 and the like. If the pH of the wastewater to be treated exceeds 5, when it is brought into contact with iron, it may take time to elute the iron into the wastewater to be treated or iron may not be sufficiently eluted into the wastewater to be treated.
- the pH of the wastewater to be treated is 5 or less, it is not always necessary to adjust the pH. It is preferable that the wastewater to be treated has a pH of 2 to 3 because iron is eluted quickly and contributes to the reaction.
- iron with which the wastewater adjusted to pH 5 or less is brought into contact examples include pure iron, crude steel, alloy steel, and other iron alloys.
- the iron is preferably in the form of a large surface area such as iron fine particles, iron wire, and granular iron, the maximum diameter is preferably 3 mm or less, and more preferably 0.1 to 1 mm.
- the content rate of iron is 85 weight% or more.
- the wastewater can be brought into contact with a column filled with iron fine particles, iron wire, granular iron or the like.
- contact can be made by adding fine iron particles, iron wire, granular iron or the like to the wastewater to be treated in the reaction tank.
- the contact time between wastewater and iron is usually preferably 2 to 30 minutes, but can be controlled by measuring the pH value or oxidation-reduction potential of the wastewater to be treated. That is, when the acid is consumed due to dissolution of iron, the pH in the system rises to pH 5 to 7 as a criterion for determining an appropriate contact time. Since the oxidation-reduction potential decreases as the oxidizing substance is reduced, the arrival of the oxidation-reduction potential below ⁇ 100 mV can be used as a reference for determining an appropriate contact time.
- the temperature of the waste water when contacting with iron is not particularly limited. However, heating to 40 ° C. or higher, particularly about 60 to 70 ° C., can increase the reduction efficiency of selenic acid. It is preferable to warm.
- the pH of the water to be treated is preferably 9 or more by adding an alkali agent. If the pH is less than 9, there is a possibility that aggregation of iron flocks and the like is insufficient.
- divalent iron ions in water become water-insoluble ferrous hydroxide, and trivalent iron ions become water-insoluble ferric hydroxide.
- the reduced selenium is adsorbed on the flocs of iron hydroxide to be produced, and is agglomerated and separated. Further, when fluorine is present in the waste water, a part of the fluorine is also adsorbed on the iron floc and is aggregated and separated. In addition, by setting the pH to 9 or more, other metal ions in which the hydroxide is water-insoluble also become hydroxide and form a floc. At this time, suspended substances, reduced selenium, fluoride components and the like contained in the wastewater are adsorbed on the iron floc and aggregate at the same time. Furthermore, when iron ultrafine particles are suspended in water, the iron ultrafine particles are also adsorbed and aggregated by the iron flocs. In addition, when the reaction system is open to the air, the divalent iron ions undergo air oxidation, and some of them become ferric oxide fine particles, and the ferric oxide fine particles are adsorbed on the iron floc. Aggregate.
- the alkali agent for the pH of the waste water after contact with iron 9 or more is not particularly limited, for example, NaOH, KOH, slaked lime (Ca (OH) 2), sodium carbonate (Na 2 CO 3), carbonate Potassium (K 2 CO 3 ), carbide soot and the like can be used, but NaOH or Ca (OH) 2 can be particularly preferably used.
- a polymer flocculant can be further added.
- the polymer flocculant to be used is not particularly limited, and examples thereof include nonionic polymer flocculants such as polyacrylamide, polyethylene oxide, urea-formalin resin, polyaminoalkyl methacrylate, polyethyleneimine, polydiallylammonium halide, chitosan and the like.
- anionic polymer flocculant such as cationic polymer flocculant, polyacrylic acid sodium, polyacrylamide partial hydrolyzate, partially sulfomethylated polyacrylamide, poly (2-acrylamide) -2-methylpropane sulfate Or 2 or more types can be used.
- anionic polymer flocculants are excellent in agglomeration effect and can be used particularly preferably.
- the amount of the polymer flocculant added is usually about 0.1 to 5 mg / L, although it varies depending on the quality of the wastewater and the type of polymer flocculant used.
- solid-liquid separation is performed to remove flocs generated by the flocculation treatment and to separate water to be treated.
- Arbitrary solid-liquid separation methods such as precipitation, filtration, centrifugation, and membrane separation, can be used.
- the separated sludge obtained by solid-liquid separation may be returned to the coagulation process.
- the separated sludge may be added to the waste water after contact with iron after being modified by adding alkali.
- FIG. 3 is a system diagram showing an example of the selenium treatment step (3) suitable for the present invention.
- the wastewater to be treated (for example, the water to be treated in the cyan decomposition step (2)) is treated with HCl or the like in the pH adjustment tank 21.
- the acid is added to adjust the pH to 5 or lower, and then heated by the heat exchanger 22, and then introduced into the iron packed tower 23. While passing through the iron packed tower 23, selenic acid in the waste water is reduced.
- the effluent water of the iron packed tower 23 is heat-exchanged with the inflow water of the iron packed tower 23 by the heat exchanger 23, and then introduced into the reaction tank 24, and the pH is adjusted to 9 or more by adding an alkaline agent such as NaOH.
- the effluent water from the reaction tank 24 is then fed to the coagulation tank 25 and coagulated by addition of a polymer coagulant, and then the coagulated sludge is solid-liquid separated in the settling tank 26, and the separated water is treated as treated water outside the system. Is discharged.
- the separated water in the sedimentation tank 26 may be fed to the next process as it is, but may be fed to the next process after being filtered by the filtration device 27 to highly remove SS.
- a part of the separated sludge in the sedimentation tank 26 may be returned to the reaction tank 24. Moreover, you may add to the reaction tank, after mixing beforehand with NaOH added to the reaction tank 24 in that case. Further, the returned sludge may be added to the coagulation tank 25.
- the method using an alloy or a mixture of metal titanium and another metal other than metal titanium as the metal reductant makes the treated wastewater contact with an alloy or mixture of metal titanium and another metal, and the other Selenium is reduced by eluting part of the metal. Since most of the reduced selenium precipitates on the metal surface, the treated water can be treated water. However, if necessary, after the reduction treatment, the pH is adjusted to precipitate the eluted metal, which is separated by solid-liquid separation. The metal is removed to obtain treated water.
- an alloy or a mixture of titanium metal and another metal other than metal titanium is used.
- Various metals can be used as the metal to be alloyed with or mixed with titanium metal, but it is preferable that the sludge composed of hydroxide generated by pH adjustment after elution of metal exhibits a white color. When the sludge is white, it is easier to dispose of the sludge than when it is colored brown or the like.
- the metal that produces white sludge include aluminum, zinc, tin, and copper. In particular, aluminum, zinc, and tin are excellent in terms of solubility and can be suitably used.
- the metal other than metal titanium may be only one kind of metal, but may be a mixture or alloy of two or more kinds of metals.
- any of solid solution, intermetallic compound, and covalent alloy can be used.
- an alloying method for example, a method using a difference in ionization tendency of metal, an electrolytic method, a melting method, or the like can be employed.
- titanium metal and other metals can be used as a mixture without being alloyed.
- metallic titanium in the form of powder, granule, fiber, and other metals in the form of powder, granule, fiber, etc. are mixed in the same form Alternatively, different forms can be mixed to form a mixture.
- the shape of the alloy or mixture of titanium and another metal is preferably one having a large surface area.
- a powdery product, a granular material, a fibrous material, or a fine thin film having a particle size of about 10 ⁇ m to 5 mm is suitable.
- the reduction reactor may be, for example, a reduction reaction tank in which a selenium-containing wastewater is introduced into a reaction tank and a powdery, fine-grained alloy or mixture is added. It is also possible to use a packed tower in which waste water is passed through the packed bed.
- the other metal When the wastewater to be treated is brought into contact with an alloy or a mixture of titanium metal and another metal, the other metal is eluted and dissolved in the wastewater. When the metal elutes into ions, a strong reducing action occurs, and selenium in the wastewater is reduced. Since this metal elution is neutral and takes a long time, it is preferable to promote acid elution by adding an acid to the selenium-containing wastewater. Examples of the acid to be added include HCl and H 2 SO 4 .
- the amount of acid added is preferably set according to the amount of metal to be eluted.
- the metal elution amount is generally proportional to the acid addition amount, and the acid addition amount can be determined by a relational expression obtained in advance by experiments. Further, the elution amount of the metal can be set according to the hexavalent selenium concentration to be reduced.
- Al 0 , Zn 0 , and Se 0 represent zero-valent, that is, non-ionized Al, Zn, and Se, respectively.
- the selenium reduction treatment performance is greatly improved as compared with the treatment by single contact of metal titanium or other metal.
- metals other than titanium such as aluminum and zinc are dissolved, electrons move through titanium that hardly dissolves even in the presence of acid, and selenium is reduced on the titanium surface. It may be expressed.
- the ratio T / M between the volume T of metallic titanium and the volume M of other metals is preferably 1/3 or more, particularly preferably 1/2 or more.
- the ratio T / M is 1/3 or more, the selenium reduction performance is improved. The reason for this is that since the proportion of titanium metal is high, the amount of electrons generated during the dissolution of other metals moves to the surface of the titanium metal, and the amount of selenium reduced on the surface of the metallic titanium increases. It is thought to be to do.
- the ratio T / M is less than 1/3, the ratio of titanium metal is low, and thus electrons generated during dissolution of other metals are emitted from the surface of the other metals. It is considered that the performance of selenium reduction treatment decreases because the amount of electrons that increase and the amount of electrons that move to the metal titanium surface and contribute to the reduction of selenium decreases.
- this ratio T / M is preferably 3/1 or less, particularly 1/1 or less. More preferably, this ratio T / M is 1/3 to 3/1, in particular 1/2 to 1/1.
- Al is particularly suitable (hereinafter, a method using metal titanium and aluminum may be referred to as “Al / Ti method”).
- T a method using metal titanium and aluminum
- A a method using metal titanium and aluminum
- T / A is 1/3 to 3/1, particularly 1/2 to 2/1, selenium is removed very efficiently. be able to.
- Reduced selenium for example, hexavalent selenium
- hexavalent selenium is mostly converted to zero-valent selenium, which is deposited on the titanium surface of the alloy or mixture and removed from the waste water. Residual selenium is reduced from hexavalent to low valent selenium, for example, tetravalent selenium, and is easily precipitated by agglomeration.
- the treated wastewater it is preferable to subject the treated wastewater to a reduction treatment and then agglomerate the reduction treatment water.
- the agglomeration treatment is performed by adjusting the pH of the reduction treatment water, precipitating the eluted metal as an insoluble compound such as hydroxide, and solid-liquid separation of the precipitated metal compound.
- the pH of the reduced water is usually adjusted by adding an alkali such as NaOH, KOH, Ca (OH) 2 or the like.
- an alkali such as NaOH, KOH, Ca (OH) 2 or the like.
- the metal used with the metal titanium is aluminum
- an alkali is added to the reduction-treated water, and the dissolved aluminum is precipitated as aluminum hydroxide.
- the pH is preferably adjusted to 5 to 8 by adding an alkali. If the pH is too low or too high than this range, the aluminum hydroxide will dissolve, which is inappropriate.
- the metal used together with the metal titanium is zinc, the pH can be adjusted to 9 to 10, and in the case of tin, the pH can be adjusted to around pH 8 to precipitate these as hydroxides.
- an organic flocculant or an inorganic flocculant can be added to improve solid-liquid separation.
- the solid-liquid separation when performing the solid-liquid separation operation can adopt any commonly used method, and it can be treated with the treated water by precipitation, filtration, centrifugation, membrane separation, etc. Separated into sludge composed of insoluble metal compounds.
- the metal eluted during the reduction treatment is insolubilized by pH adjustment and solid-liquid separation of the reduced treated water, separated from the water, and discharged as treated water containing no metal. Further, when the eluted metal is precipitated as an insoluble compound, for example, aluminum hydroxide, reduced low-valent selenium remaining in the water is also adsorbed on the aluminum hydroxide flocs and is precipitated by a coprecipitation phenomenon.
- an insoluble compound for example, aluminum hydroxide
- Another preferred method for precipitating dissolved aluminum is a method of precipitating as calcium aluminate, adding a calcium compound to the reduction-treated water, adjusting the pH to 9 or higher, and coagulating.
- the calcium compound to be added include Ca (OH) 2 , CaO, and CaCl 2 .
- Use of Ca (OH) 2 is preferable because it becomes a calcium source and also acts as an alkali for pH adjustment.
- an arbitrary alkali is added to adjust the pH.
- the pH is adjusted to 9 or more, preferably 9-12. When the pH is lower than 9, it is difficult to produce calcium aluminate.
- coal gasification wastewater contains components other than cyan, such as thiocyanate and formic acid, and ammonia as a nitrogen component, these are removed in the COD / ammonia removal step (4).
- the following treatments (a) to (c) can be employed, and two or more of these can also be combined.
- oxidizing agent used, and examples thereof include oxygen gas, oxygen-enriched air, air, hydrogen peroxide, ozone, and hypochlorite.
- amount of oxidizer added it is preferably 1.1 to 3 times the theoretical amount necessary for oxidizing ammonia, COD components, etc., and 1.5 to 2.5 times. Is more preferable.
- the temperature of wet catalytic oxidation is not particularly limited, but is preferably 101 to 210 ° C, more preferably 120 to 180 ° C.
- the wastewater to be treated is pressurized to a pressure that maintains the liquid phase. If the wet catalytic oxidation temperature is less than 101 ° C., the rate of the oxidation reaction is slow, and it may take a long time to decompose and remove ammonia, COD components, and the like. The higher the wet catalyst oxidation temperature, the faster the oxidative decomposition proceeds. However, when the wet catalyst oxidation temperature exceeds 210 ° C, a pressure-resistant structure of 2 MPa or more is required, which may increase the cost of equipment and operation management. .
- the catalyst used for wet catalytic oxidation for example, ruthenium, rhodium, palladium, osmium, iridium, platinum, iron, cobalt, nickel, copper, gold, tungsten, and other metals, and these metals are insoluble or sparingly soluble in water. 1 type or 2 types or more, such as these compounds, can be mentioned.
- These metal catalysts or metal compound catalysts are preferably used by being supported on a carrier.
- the carrier include one or more of magnesia, alumina, titania, silica gel, silica-alumina, zirconia, activated carbon, diatomaceous earth, cordierite, and the supported amount is 0 with respect to the carrier. It is preferably about 2 to 1% by weight.
- FIG. 4 is a system diagram showing an example of a catalytic wet oxidation step as a COD / ammonia removal step (4) suitable for the present invention, where wastewater to be treated (for example, treated water in the selenium treatment step (3)) After heating from the storage tank 31 by a heat exchanger 32 (and a heater (not shown)), it is introduced into the catalyst packed tower 33 together with an oxidizing agent such as oxygen. While passing through the catalyst packed tower 33, ammonia and COD components in the wastewater are catalytically oxidized and decomposed in the presence of an oxidizing agent. The effluent water from the catalyst packed tower 33 is heat-exchanged by the heat exchanger 32, and then pH-adjusted in a pH-adjusting tank 34 as necessary, and discharged out of the system.
- wastewater to be treated for example, treated water in the selenium treatment step (3)
- ammonia stripping after adding alkali such as NaOH to the wastewater to be treated to adjust the alkalinity to about pH 10-12, the wastewater is brought into countercurrent contact with air in a diffusion tower. The ammonia ions in it are separated as ammonia gas.
- This stripping tower may be filled with a packing such as a cascade ring in order to increase the contact efficiency. Further, steam may be supplied to the stripping tower for heating together with air.
- the temperature be 40 to 90 ° C. and the gas (air) / liquid (drainage) flow rate ratio (G / L volume ratio) be 500 or more.
- ammonia in the waste water is removed, but other COD components remain. Therefore, when the ammonia stripping process is adopted as the COD / ammonia removal process (4) and the COD component is not removed in the preceding stage, an advanced treatment process such as catalytic wet oxidation is further provided in the subsequent stage.
- the COD component is preferably removed. However, the COD component can also be removed by employing wet oxidation in the above-described step (2).
- exhaust gas containing ammonia is discharged, and this exhaust gas is diluted with air to an ammonia concentration of 1% or less as necessary, and then heated to about 300 to 400 ° C. to produce iron, platinum, It is preferable to decompose ammonia into nitrogen by contacting with a gas treatment catalyst such as ruthenium, tungsten, or titanium oxide.
- a gas treatment catalyst such as ruthenium, tungsten, or titanium oxide.
- Biological treatment is not particularly limited, but because the treated wastewater contains ammonia, autotrophic denitrifying bacteria using ammonia ions as electron donors and nitrite ions as electron acceptors. It is preferable to perform biological treatment including a denitrification step using (ANAMMOX bacteria).
- ANAMMOX bacteria can generate nitrogen gas by reacting ammonia nitrogen as an electron donor and nitrite nitrogen as an electron acceptor under anoxic conditions (Microbiology 142 (1996), p2187-). 2196 etc.)
- ammonia nitrogen can be oxidized using the oxidizing power of nitrite nitrogen, so nitrogen can be removed with an oxygen consumption equivalent to the theoretical amount, saving energy. be able to.
- organic substances such as methanol, the cost can be saved.
- This ANAMOX bacteria is an autotrophic bacterium, and the amount of excess sludge generated per nitrite nitrogen to be reduced is less than one-fifth compared to denitrifying bacteria that use organic matter to denitrify, and waste Generation amount can be greatly reduced.
- Nitrite nitrogen as an electron acceptor involved in this reaction can be obtained by partially oxidizing ammonia nitrogen in wastewater, and may be introduced from other systems, or a separate chemical may be used. good.
- the type of reaction tank is a column filled with a carrier suitable for adhering microorganisms such as sand, synthetic resin, gel, etc., and the wastewater to be treated is passed in an upward or downward flow, and nitrogen on the surface of the carrier.
- a method is used in which a denitrification reaction proceeds by contacting a compound with a microorganism.
- the carrier used here is preferably one having a large specific surface area, and in particular, a granular shape having a particle size of about 0.1 to 10 mm, or a shape such as a string shape, a cylindrical shape, or a gear shape is known.
- the carrier is preferably flowed gently in water, and is flowed by a gas generated by denitrification, a gas injected from the outside, a stirrer, or the like.
- denitrifying microorganisms that grow in suspension in water can be used, and the reaction is achieved by increasing the concentration of microorganisms in the system by reducing the amount of microorganisms flowing out of the system by solid-liquid separation of the grown microorganisms. Increasing the reaction rate per tank volume is also preferred.
- various conventionally known methods such as precipitation, flotation, centrifugation, and filtration can be applied to the solid-liquid separation means used.
- raw water is injected upward from the bottom of the reaction tank, and sludge is blocked or granulated without using a bacterial adhesion carrier to form a sludge bed of granular sludge with a particle size of 0.5 to several mm.
- a USB (Upflow Sludge Bed) method is also suitable in which microorganisms are formed and retained at a high concentration in the reaction tank and subjected to high load treatment.
- the COD / ammonia removing step (4) highly removes ammonia in coal gasification wastewater to N to 60 mg / L or less, or COD components to 15 mg / L or less.
- the present invention is characterized in that among the steps (1) to (4) described above, the step (1) is performed before the step (2).
- the order of the other steps is not particularly limited, but it is preferable to employ the following aspects (A) to (C).
- the cyan decomposition step is a non-catalytic wet oxidation step
- the COD / ammonia removal step is a catalytic wet oxidation step
- the order of each step is (1), (2), (3), (4)
- the cyan decomposition step is a non-catalytic wet oxidation step
- the COD / ammonia removal step is a catalytic wet oxidation step
- the order of each step is (1), (2), (4), (3) To do.
- the cyanide decomposition step is a non-catalytic wet oxidation step
- the COD / ammonia removal step is an ammonia stripping step or a biological treatment step
- the order of each step is (1), (2), (3), The order is (4).
- the fluorine removal step (1) By making the fluorine removal step (1) by coagulation sedimentation the first step, it is possible to preferentially remove fluorine with high corrosiveness and prevent equipment corrosion at a later stage. That is, for example, if fluorine is present in the wet oxidation process, hydrofluoric acid is generated and causes corrosion of the apparatus, which is not preferable. Further, in steps (2) to (4), the processing efficiency is increased by raising the temperature by heating, but if fluorine is present under such high temperature conditions, titanium, stainless steel, etc. used in these steps Steel materials are corroded by high concentrations of fluorine. Therefore, it is preferable that the step (1) is the first step and fluorine is preferentially removed.
- SS in the coal gasification wastewater can also be removed in this step (1), and problems such as blockage of the subsequent catalyst packed tower and the like can be avoided. Also in the point which can do, it is preferable that a process (1) is made into the 1st process.
- step (3) an acid is added to the waste water to elute the metal in the metal reductant.
- the wastewater becomes acidic, and when cyanide is present in the wastewater, it is volatilized as hydrogen cyanide (HCN).
- Hydrogen cyanide is a harmful substance, and it is not preferable to volatilize it for safety and health. Therefore, it is preferable to remove cyan in step (2) prior to step (3).
- the precipitated SS component is dissolved by the addition of an acid, there is less fear of clogging due to the washing step of the reductant, etc.
- the free metal can then be removed.
- step (4) is a catalytic wet oxidation step
- the steps (3) and (4) May be performed first, even if it is in order of step (1) ⁇ step (2) ⁇ step (3) ⁇ step (4), step (1) ⁇ step (2) ⁇ step ( 4)
- the order of step (3) may be used.
- step (4) is a biological treatment step such as the denitrification step using the above-mentioned ANAMMOX bacteria, as in the case of the above-described catalytic wet oxidation step, if the steps (1) and (2) are prioritized, Either step (3) or step (4) may be performed first.
- the method of FIG. 5 is a wet process shown in FIG. 2 after removing SS and fluorine in the step (1) performed by combining the aggregation precipitation treatment with Ca salt and the aggregation precipitation treatment with Mg salt shown in FIG. Step (2) for decomposing cyanide by oxidation is performed. That is, after adjusting the pH in a pH adjusting tank, it is heated in a heat exchanger (not shown) and wet oxidized in the presence of an oxidizing agent in a wet oxidation reaction tower to decompose cyanide. At this time, the COD component is also decomposed. Subsequently, the treated water of this process (2) is sent to the selenium treatment process (3) shown in FIG. 3 through a relay tank.
- this step (3) passes through the relay tank and is sent to the catalyst wet oxidation treatment step (4) shown in FIG. 4 to decompose and remove the COD component and ammonia. Since this catalyst wet oxidation-treated water is usually alkaline with a pH of about 9 to 10, it is discharged after adjusting the pH to about 6 to 8 by adding an acid in a pH adjusting tank as necessary.
- the method shown in FIG. 6 is different from that shown in FIG. 5 in that ammonia stripping is performed instead of catalytic wet oxidation as step (4), and the other configurations are the same, and steps (1) to (3) are the same. The same is done.
- ammonia stripping step as described above, exhaust gas containing ammonia is discharged, and this is processed. Further, since the treated water is alkaline with a pH of about 10 to 11, it is discharged after adjusting the pH to about 6 to 8 by adding an acid in a pH adjusting tank as necessary.
- Fluorine concentration 15 mg / L or less Ammonia concentration: 60 mg / L or less (as N) COD concentration: 15 mg / L or less Selenium concentration: 0.1 mg / L or less Cyanide concentration: 1 mg / L or less high water quality treated water can be obtained, which can be discharged or reused as industrial water in some cases.
- Example 1 The coal gasification wastewater was treated by the treatment procedure shown in FIG.
- the processing conditions of each process are as follows.
- Step (1) SS, fluorine aggregation treatment>
- the aggregation precipitation treatment by adding Ca salt (using Ca (OH) 2 ) and the addition of Mg salt (using MgSO 4 ) shown in FIG. 1 were performed under the following conditions.
- Polymer flocculant Anionic polymer flocculant “Cliff Rock PA331” manufactured by Kurita Kogyo Co., Ltd., addition amount 3 mg / L
- Step (2) wet oxidation treatment>
- the wet oxidation treatment shown in FIG. 2 was performed on the treated water in step (1) under the following conditions. Hydrogen peroxide (H 2 O 2 ) was mixed with the effluent as an oxidizing agent and heated, and then passed through a pressure vessel (reaction tower). The treated water was cooled and the pressure was released.
- H 2 O 2 Hydrogen peroxide
- acid HCl
- NaOH alkali
- Water flow SV 15 / hr HCl addition amount: Added so that the iron elution amount is 3000 mg / L
- pH 10
- Polymer flocculant Anionic polymer flocculant “Cliff Rock PA331” manufactured by Kurita Kogyo Co., Ltd., addition amount 3 mg / L
- Step (4) Catalyst wet oxidation treatment>
- the catalyst wet oxidation treatment shown in FIG. 4 was performed on the treated water in step (3) under the following conditions.
- Oxygen (O 2 ) was used as the oxidizing agent.
- Table 1 shows the quality of treated wastewater and treated water in each process together with the discharge standard value.
- “-” indicates that no measurement is performed or no data is available. The same applies to Table 2 and later.
- the order of the step (3) and the step (4) is interchanged, and the processing is performed under the same conditions in the order of the step (1) ⁇ the step (2) ⁇ the step (4) ⁇ the step (3).
- similar processing results were obtained.
- Example 2 Simulating the treated water in step (2), the following simulated water drainage with the following water quality was prepared, and selenium treatment was performed by the Al / Ti method under the following conditions. This process is similarly performed except that aluminum and titanium are used as the metal reductant in FIG.
- Table 2 shows the processing results.
- Example 3 The coal gasification wastewater was treated by the treatment procedure shown in FIG. Of the steps (1) to (4), the processing conditions and processing procedures of the steps (1) to (3) are the same as those in the first embodiment. However, in step (2), the amount of H 2 O 2 added was 4000 mg / L, and the reaction time was 1 hr. In step (3), the amount of HCl added was such that the iron elution amount was 1600 mg / L.
- Process conditions for step (4) are as follows.
- the exhaust gas was diluted with air to an NH 3 concentration of 1% or less, heated, and decomposed into N 2 using a gas treatment catalyst (iron-based catalyst) under the following conditions.
- a gas treatment catalyst iron-based catalyst
- Table 3 shows the quality of treated wastewater and treated water in each process together with the discharge standard value. Table 3 also shows the properties of the treatment gas obtained by treating the exhaust gas discharged by ammonia stripping.
- the SS of the treated water of the step (2) is higher than that of the treated water of the step (1) because iron hydroxide precipitates from the iron cyanide complex salt. This is because T-Fe: 50 mg / L of the treated water of 1) becomes Fe (OH) 3 and is detected as SS at 96 mg / L.
- Table 4 The same applies to Table 4 below.
- Example 4 In Example 3, with respect to the coal gasification wastewater having a low water fluorine concentration shown in Table 4, the steps (2) to ( 4) and exhaust gas treatment were performed, and the results are shown in Table 4.
- SS fluorine aggregation treatment>
- aggregation precipitation was performed by adding Al salt (sulfuric acid band) with aggregation precipitation as a one-stage treatment.
- Polymer flocculant Anionic polymer flocculant “Cliff Rock PA331” manufactured by Kurita Kogyo Co., Ltd., addition amount 3 mg / L
- the present invention it is possible to efficiently remove all SS, fluorine, cyanide, selenium, ammonia and COD components in coal gasification wastewater, which can be discharged or reused. It turns out that the treated water of water quality can be obtained.
- the pH of the treated water in step (4) is slightly higher than the discharge standard value, but this treated water may be adjusted by adding an acid as appropriate.
- the method for treating coal gasification wastewater of the present invention it is possible to efficiently remove all pollutants in the coal gasification wastewater and to obtain treated water with good water quality that can be discharged or reused. it can.
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Abstract
Description
(1)凝集沈殿によりフッ素を除去するフッ素除去工程、
(2)湿式酸化または熱加水分解によりシアンを分解するシアン分解工程、
(3)金属還元体によりセレン酸イオンを還元処理するセレン処理工程、並びに
(4)CODおよび/またはアンモニアを除去するCOD/アンモニア除去工程
を含み、(1)を(2)よりも先に行うことを特徴とする。
(1)凝集沈殿によりフッ素を除去するフッ素除去工程
(2)湿式酸化または熱加水分解によりシアンを分解するシアン分解工程
(3)金属還元体によりセレン酸イオンを還元処理するセレン処理工程
(4)CODおよび/またはアンモニアを除去するCOD/アンモニア除去工程
pH:7~9
SS:20~1000mg/L
フッ素:20~2000mg/L
シアン:10~150mg/L
セレン:0.5~10mg/L
アンモニア:2000~4000mg/L(Nとして)
COD:200~1500mg/L
まず、凝集沈殿によりフッ素を除去するフッ素除去工程(1)について説明する。
(1) 排水にカルシウム化合物を添加して、以下の反応で難溶性のフッ化カルシウムを生成させ、これを分離除去する。
Ca2++2F- → CaF2
(2) 排水にマグネシウム化合物を添加して以下の反応でフッ素イオンを水酸化マグネシウムに吸着させて除去する。
Mg2++2OH-+F- → Mg(OH)2・F-
(3) 排水にアルミニウム化合物を添加して以下の反応で水酸化アルミニウムにフッ素イオンを吸着させて除去する。
Al3++3OH-+F- → Al(OH)3・F-
この点、(1)のカルシウム化合物による方法はpH中性~アルカリ性(具体的には、pH6~9)で処理を行うことができ、また、(2)のマグネシウム化合物による方法ではアルカリ性(具体的にはpH9以上、好ましくは11以上)で処理を行うことができ、(3)のアルミニウム化合物による方法はpH中性(具体的にはpH6~8)で処理を行うことができ好ましい。
また、上述のpH条件となるように必要に応じて、塩酸(HCl)、硫酸(H2SO4)等の酸または水酸化ナトリウム(NaOH)、水酸化カリウム(KOH)等のアルカリを添加することが好ましい。
また、上述のpH条件となるように必要に応じて、HCl、H2SO4等の酸またはNaOH、KOH等のアルカリを添加することが好ましい。
また、上述のpH条件となるように必要に応じて、HCl、H2SO4等の酸またはNaOH、KOH等のアルカリを添加することが好ましい。
図1は、本発明に好適なフッ素除去工程(1)の一例を示す系統図であり、前述の(1)のカルシウム化合物による方法と(2)のマグネシウム化合物による方法を併用するものである。
この返送汚泥量は、発生汚泥に対して20~50倍程度とすることが好ましい。
この返送汚泥量は、返送先の反応槽内のSS濃度が、2000~10000mg/Lとなるような量とするのが、スケール防止上、好ましい。
なお、第2沈殿槽9の分離水は、そのまま次工程に送給しても良いが、図1に示す如く、砂濾過器等の濾過装置10で濾過してSSを高度に除去することが、後工程におけるSSによる閉塞やスケール障害を防止する上で好ましい。
次に、湿式酸化または熱加水分解によりシアンを分解するシアン分解工程(2)について説明する。
2CN-+O2+H2O → 2HCO3 -+N2
CN-+2H2O → HCOO-+NH3
従って、このシアン分解工程(2)は触媒を用いない無触媒の湿式酸化工程であることが好ましい。
図2は、本発明に好適なシアン分解工程(2)の一例を示す系統図であり、被処理排水(本発明ではフッ素除去工程(1)の処理水)を、まずpH調整槽11に導入してH2SO4等の酸を添加してpH7程度にpH調整した後、熱交換器12(および図示しない加熱器)で加熱して湿式酸化反応塔13に導入する。この反応塔13の流入水には、H2O2等の酸化剤が注入され、排水中のシアンは反応塔13内で酸化剤の存在下、湿式酸化分解される。反応塔13の流出水(処理水)は、熱交換器12で反応塔13の流入水と熱交換された後、次工程へ送給される。シアンの分解で生成した窒素ガス、炭酸ガスは、反応塔13の上部から排出される。
次に、金属還元体によりセレン酸イオンを還元処理するセレン処理工程(3)について説明する。
3Fe0+SeO4 2-+8H+ → 3Fe2++Se0+4H2O
Fe2++Se0+2OH- → Fe(OH)2・Se0
Fe2++2NaOH → Fe(OH)2+2Na+
Fe3++3NaOH → Fe(OH)3+3Na+
3Zn0+SeO4 2-+8H+ → 3Zn2++Se0+4H2O
2Al(OH)3+Ca(OH)2+Se0 → CaAl2O4・Se0+4H2O
また、被処理排水にフッ素やホウ素が含まれている場合、アルミン酸カルシウムが析出する際、フッ素やホウ素も同時に析出させて除去することができる。
次に、石炭ガス化排水中のCODおよび/またはアンモニアを除去するCOD/アンモニア除去工程(4)について説明する。
(b) アンモニアストリッピング
(c) 生物処理
本発明においては、以上説明した工程(1)~(4)のうち、工程(1)を工程(2)よりも先に行うことを特徴とする。その他の工程順については特に制限はないが、次の(A)~(C)の態様を採用することが好ましい。
(B) シアン分解工程を無触媒の湿式酸化工程とし、COD/アンモニア除去工程を触媒湿式酸化工程とし、各工程の順序を(1)、(2)、(4)、(3)の順とする。
(C) シアン分解工程を無触媒の湿式酸化工程とし、COD/アンモニア除去工程工程をアンモニアのストリッピング工程または生物処理工程とし、各工程の順序を(1)、(2)、(3)、(4)の順とする。
また、排水中のシアンが、金属錯体の形態で存在する場合は、シアンの分解に伴い金属が遊離するため、条件によって析出する。特にアルカリ性で金属水酸化物として析出するものが多い。
このため、シアン処理後の排水をそのままアンモニアストリッピングで処理すると、放散塔内でSSや、スケール化による閉塞が懸念される。
以下に、本発明に係る工程(1)~(4)の処理手順の一例を示す図5,6を参照して、本発明に好適な処理手順を説明するが、本発明で採用し得る処理手順は何ら図5,6に示すものに限定されるものではない。
次いで、この工程(2)の処理水を中継槽を経て図3に示すセレン処理工程(3)に送給する。即ち、酸を添加してpH調整した後、金属還元体と接触させ、その後、凝集沈殿処理する。好ましくは更に濾過装置で濾過する。
この工程(3)の処理水は中継槽を経て、図4に示す触媒湿式酸化処理の工程(4)に送給してCOD成分とアンモニアの分解除去を行う。この触媒湿式酸化処理水は通常pH9~10程度のアルカリ性であるため、必要に応じてpH調整槽で酸を添加してpH6~8程度に調整した後放流する。
アンモニアストリッピング工程では、前述の如く、アンモニアを含む排ガスが排出されるため、これを処理する。また、処理水はpH10~11程度のアルカリ性であるため、必要に応じてpH調整槽で酸を添加してpH6~8程度に調整した後放流する。
フッ素濃度:15mg/L以下
アンモニア濃度:60mg/L以下(Nとして)
COD濃度:15mg/L以下
セレン濃度:0.1mg/L以下
シアン濃度:1mg/L以下
の高水質処理水を得、これを放流ないしは場合によっては工業用水として再利用することが可能となる。
図5に示す処理手順で石炭ガス化排水の処理を行った。
各工程の処理条件等は次の通りである。
図1に示すCa塩(Ca(OH)2を使用)添加による凝集沈殿処理とMg塩(MgSO4を使用)添加による凝集沈殿処理を以下の条件で行った。
Ca添加量=2500mg/L as Ca
pH=7
高分子凝集剤:栗田工業(株)製アニオン系高分子凝集剤「クリファームPA893」,添加量3mg/L
(Ca凝集沈殿処理上澄み水に対して実施)
Mg添加量=500mg/L as Mg
pH=11
高分子凝集剤:栗田工業(株)製アニオン系高分子凝集剤「クリフロックPA331」,添加量3mg/L
工程(1)の処理水に対して、図2に示す湿式酸化処理を以下の条件で実施した。
排水に酸化剤として過酸化水素(H2O2)を混合して加熱した後、圧力容器(反応塔)に通水し、処理水は冷却し、圧力開放した。
(湿式酸化処理条件)
温度=170℃
圧力=0.9MPa
初期pH=7
酸化剤(H2O2)添加量=8000mg/L
反応時間:2hr
工程(2)の湿式酸化処理水に対して、図3に示すセレン処理を以下の条件で実施した。
排水に酸(HCl)を添加した後、鉄を充填したカラムに通水した後、アルカリ(NaOH)を添加して凝集沈殿処理した。
還元体=鉄
温度=70℃(還元体通水後放冷)
通水SV=15/hr
HCl添加量:鉄溶出量が3000mg/Lとなるよう添加
pH=10
高分子凝集剤:栗田工業(株)製アニオン系高分子凝集剤「クリフロックPA331」,添加量3mg/L
工程(3)の処理水に対して、図4に示す触媒湿式酸化処理を以下の条件で実施した。酸化剤としては酸素(O2)を用いた。
温度=160℃
圧力=0.9MPa
充填物=1重量%Pt担持/TiO2
SV=2/hr
O2注入量=NH3,CODに対して1.2倍当量
なお、表1において「-」は測定を行っていないこと或いはデータ無しであることを示す。表2以降についても同様である。
工程(2)の処理水を模擬して、以下の水質の模擬排水を調製し、以下の条件でAl/Ti法によるセレン処理を行った。この処理は、図3において、金属還元体としてアルミニウムとチタンを用いること以外は同様に実施される。
T-Se=5mg/L(Se(VI))
CODMn=490mg/L(ギ酸=4900mg/L)
NH4-N=4900mg/L
還元体:Al/Ti=1/1(体積比)
温度:65℃
Al溶出量:1500mg/L
SV:5/hr(Alに対して)
(凝集条件)
pH=7
図6に示す処理手順で石炭ガス化排水の処理を行った。
工程(1)~(4)のうち、工程(1)~(3)の処理条件および処理手順は実施例1におけると同様である。
ただし、工程(2)において、H2O2添加量は4000mg/Lとし、反応時間は1hrとした。
また、工程(3)において、HCl添加量は、鉄溶出量が1600mg/Lとなるような量とした。
工程(3)の処理水に対して実施した。
排水にNaOHを添加してpH10とした後、カスケードリングの充填物を充填した充填塔式放散塔上部より供給し、下部よりスチームおよび空気を吹き込んだ。
(ストリッピング条件)
G/L=500(空気/排水体積比)
温度=80℃
充填物=カスケードリング
充填物充填高さ=4m
(排ガス処理条件)
温度=300~400℃
SV=5000/hr
表3には、アンモニアストリッピングで排出された排ガスを処理して得られた処理ガスの性状も併記した。
実施例3において、表4に示す水質のフッ素濃度が低い石炭ガス化排水に対して、工程(1)を以下のAl塩による凝集処理としたこと以外は同様にして、工程(2)~(4)と排ガス処理を行い、結果を表4に示した。
図1において、凝集沈殿を1段処理として、Al塩(硫酸バンド)添加による凝集沈殿処理を行った。
(Al凝集条件)
硫酸バンド添加量=10000mg/L
pH=7
高分子凝集剤:栗田工業(株)製アニオン系高分子凝集剤「クリフロックPA331」,添加量3mg/L
なお、本出願は、2009年3月24日付で出願された日本特許出願(特願2009-072215)に基づいており、その全体が引用により援用される。
Claims (12)
- 石炭ガス化排水を処理する方法であって、
(1)凝集沈殿によりフッ素を除去するフッ素除去工程、
(2)湿式酸化または熱加水分解によりシアンを分解するシアン分解工程、
(3)金属還元体によりセレン酸イオンを還元処理するセレン処理工程、並びに
(4)CODおよび/またはアンモニアを除去するCOD/アンモニア除去工程
を含み、(1)を(2)よりも先に行うことを特徴とする石炭ガス化排水の処理方法。 - シアン分解工程が無触媒の湿式酸化工程であり、COD/アンモニア除去工程が触媒湿式酸化工程であり、各工程の順序が、(1)、(2)、(3)、(4)の順であることを特徴とする請求項1に記載の石炭ガス化排水の処理方法。
- シアン分解工程が無触媒の湿式酸化工程であり、COD/アンモニア除去工程が触媒湿式酸化工程であり、各工程の順序が、(1)、(2)、(4)、(3)の順であることを特徴とする請求項1に記載の石炭ガス化排水の処理方法。
- シアン分解工程が無触媒の湿式酸化工程であり、COD/アンモニア除去工程工程がアンモニアのストリッピング工程であり、各工程の順序が(1)、(2)、(3)、(4)の順であることを特徴とする請求項1に記載の石炭ガス化排水の処理方法。
- COD/アンモニア除去工程が生物処理工程であり、各工程の順序が(1)、(2)、(3)、(4)の順であることを特徴とする請求項1に記載の石炭ガス化排水の処理方法。
- 生物処理工程が、アンモニアイオンを電子供与体、亜硝酸イオンを電子受容体とする独立栄養性脱窒細菌を用いた脱窒工程を含むことを特徴とする請求項5に記載の石炭ガス化排水の処理方法。
- COD/アンモニア除去工程の処理水を処理する高度処理工程を有することを特徴とする請求項1ないし6のいずれかに記載の石炭ガス化排水の処理方法。
- フッ素除去工程が、以下の(1)~(3)のいずれか1以上の工程を含むことを特徴とする請求項1ないし7のいずれかに記載の石炭ガス化排水の処理方法。
(1) 排水にカルシウム化合物を添加して、難溶性のフッ化カルシウムを生成させ、これを分離除去する工程
(2) 排水にマグネシウム化合物を添加してフッ素イオンを水酸化マグネシウムに吸着させて除去する工程
(3) 排水にアルミニウム化合物を添加して水酸化アルミニウムにフッ素イオンを吸着させて除去する工程 - フッ素除去工程が、(1)のカルシウム化合物によるフッ素除去後に、(2)のマグネシウム化合物によるフッ素除去または(3)のアルミニウム化合物によるフッ素除去を行う工程であることを特徴とする請求項8に記載の石炭ガス化排水の処理方法。
- シアン分解工程が、フッ素除去工程の処理水をpH中性条件に調整した後、酸化剤として過酸化水素を添加して加熱する湿式酸化工程であることを特徴とする請求項1ないし9のいずれかに記載の石炭ガス化排水の処理方法。
- セレン処理工程が、pH5以下に調整した排水を鉄と接触させて、セレン酸を還元処理し、析出したセレンを鉄イオンと共に、共沈させて凝集処理する工程であることを特徴とする請求項1ないし10のいずれかに記載の石炭ガス化排水の処理方法。
- セレン処理工程が、排水を、金属チタンとアルミニウム、亜鉛及びスズよりなる群から選ばれる1種又は2種以上の金属チタン以外の他の金属との合金または混合物と接触させて、該他の金属の一部を溶出させることによりセレンを還元する工程であることを特徴とする請求項1ないし10のいずれかに記載の石炭ガス化排水の処理方法。
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CN102348648B (zh) | 2014-06-04 |
CN102348648A (zh) | 2012-02-08 |
KR101653129B1 (ko) | 2016-09-01 |
JP2010221151A (ja) | 2010-10-07 |
KR20110129863A (ko) | 2011-12-02 |
JP5417927B2 (ja) | 2014-02-19 |
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