CN102910777B - Treatment method for wastewater generated in cellulosic ethanol production - Google Patents
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Abstract
The present invention relates to a treatment method for wastewater generated in cellulosic ethanol production. The method is used for treatment and reuse of wastewater generated by using corn stalks and other plant fibers as raw materials for ethanol production, and especially for salt-containing organic wastewater. A combined process of filter pressing - multi-effect evaporation - cooling - anaerobic fermentation - aerobic biotreatment - filtration is used for treating the wastewater generated in the cellulosic ethanol production. The water flowed out after the treatment can be directly reused in the processes such as acid liquor preparation, hydrolysis and fermentation of the cellulosic ethanol production, so purposes of saving water and zero liquid discharge in the cellulosic ethanol production are reached. The method of the present invention is characterized in that recycling of all the high salt concentration wastewater can be achieved, effective recovery and comprehensive utilization of waste materials in the wastewater is obtained, high concentration organic pollutants are converted into methane and the like for resource utilization, and requirements of circular economy, clean production and the like are met.
Description
Technical field
The present invention relates to a kind for the treatment of process of cellulose ethanol waste water, for take processing and the reuse that the vegetable fibres such as maize straw are the waste water of raw material production ethanol, particularly salt-containing organic wastewater.
Background technology
Along with the worsening shortages of global fossil energy, the general requirement of the aggravation of environmental pollution, recycling economy and minimizing carbon emission, the exploitation of renewable energy source has become the theme in these epoch, and take the vegetable fibres such as maize straw, Chinese sorghum straw, is one of important channel of renewable energy source exploitation as raw material production cellulose ethanol.
It is raw material that cellulose ethanol normally be take the vegetable fibres such as maize straw, Chinese sorghum straw, by steaming the techniques such as quick-fried pre-treatment, cellulase hydrolysis, saccharifying enzyme fermentation, ethanol rectifying and dehydration, obtain high purity ethanol, and mix production process of alcohol products in gasoline component, as clean fuel for vehicle.In this production process, owing to steaming quick-fried pre-treatment, the structure organization of the cellulosic component in raw material is destroyed and plays vital effect, to the energy consumption of the yield of the alcohol concn of the hydrolysis efficiency of follow-up lytic enzyme, fermentation liquid, alcohol product and whole production process, all will produce tremendous influence.Therefore, in concrete cellulose ethanol production technology optimization, steam quick-fried pretreatment condition and often especially paid attention to, the quick-fried route of acid steaming is one of them, with more than 1% sulfuric acid, fibrous material is carried out to dip treating in advance, then sends into steam explosion machine and steam quick-fried pre-treatment.Adopt after this route, by acidic conditions, destroyed preferably the Mierocrystalline cellulose weave construction in raw material, greatly improved cellulosic hydrolysis efficiency, alcohol yied, and reduced the consumption of energy consumption and zymin.Yet when obtaining above effect, along with adding of acid, hydrolysis, fermenting process will constantly carry out pH regulator with alkali, cause and in final draining, contain a large amount of vitriol and other inorganic salt, as sulfate radical can reach 10,000 mg/L left and right, inorganic salt content can reach more than 4%, to originally causing larger difficulty with regard to very unmanageable high concentrated organic wastewater.
Because cellulose ethanol production process is comparatively complicated, water of productive use and water displacement are all quite high, according to current state of the art analysis, produce one ton of alcohol product fresh water consumption amount and be about 25～30 tons, simultaneously by the high-concentration sewage of discharging nearly 25 tons, this not only can significantly increase the production cost of cellulose ethanol, and will bring a large amount of high-concentration sewages to process problem.Based on this, the processing of cellulose ethanol waste water and reuse have become key restraining factors of cellulose ethanol scale operation.The high-concentration sewage problem producing for solving cellulose ethanol production process, the main treatment process adopting is that high-concentration sewage is carried out to anaerobic treatment at present, some that remove in sewage has the material of severe inhibition to Mierocrystalline cellulose or hydrolysis of hemicellulose and liquid glucose fermenting enzyme, as carboxylic acid, furfural, furans, phenol etc., make to process rear water outlet reuse as much as possible.As CN01808115.0 and US6555350 all propose to adopt up-flow anaerobic sludge blanket (UASB) art breading sewage, make inhibitory substance carboxylic acid in sewage, furfural, furans, phenol etc. remove more than 80%, sewage after processing more than at least 5% is recycled, by anaerobically fermenting, produce methane, methane recovery is put forward high-octane utilization ratio simultaneously.Yet this inventive method is only applicable to process neutral (not adding soda acid) and steams the waste water that quick-fried pre-treating process produces, acidity is steamed to factory effluent under quick-fried pre-treatment route and make it to be not suitable for to adopt because of following three reasons.First, the total salt quantity that contains high density in waste water after adopting acid steaming quick-fried, as sodium sulfate, sodium acetate, Sodium.alpha.-hydroxypropionate etc., wherein inorganic salt content is up to more than 4%, the scope of application below 2% well beyond anaerobically fermenting treatment process, under this situation, growth and the activity of anaerobically fermenting microbial bacteria obtain severe inhibition, even cause the failure of anaerobic treatment process; Secondly, sulfate radical content in waste water is up to more than 10,000 mg/L, well beyond the required value below anaerobically fermenting treatment process 5000mg/L, under this situation, sulfate radical in waste water will be reduced to the hydrogen sulfide of high density by anerobe, thereby the methanation fermenting process of severe inhibition high-enriched organics, causes biogas production rate to decline rapidly, can not produce biogas even at all; In waste water, salts contg is high, and the water outlet after processing cannot reuse, causes the high water consumption of cellulose ethanol production process, the problem of maximum discharge not to be changed.
Comprehensive above analysis, adopts acid cellulose ethanol production technique of steaming quick-fried pre-treatment route in technology, have a larger advantage economically, but has also correspondingly brought larger waste water handling problem.Due to the relevant wastewater processing technology not still being applicable at present, the widespread use of acidity being steamed to the cellulose ethanol production technique of quick-fried pre-treatment route will cause huge environmental protection restriction undoubtedly.
Summary of the invention
The present invention is directed to the acid water quality characteristics that steams the cellulose ethanol production wastewater of quick-fried pre-treatment route, a kind for the treatment of process of cellulose ethanol waste water is proposed, the main combined treatment process such as press filtration, multiple-effect evaporation, cooling, anaerobically fermenting, aerobic biochemical, filtration that adopt, the water outlet of processing through said process is all made cellulose ethanol water of productive use and is recycled, thereby realizes the water-saving and emission-reducing object that cellulose ethanol is produced.
The treatment process of a kind of cellulose ethanol waste water of the present invention is mainly divided into six processing units:
(1) press filtration, after press filtration, waste water carries out multiple-effect evaporation processing, and press filtration charging is the mixture of concentrated solution after cellulose ethanol waste water and multiple-effect evaporation.To be cellulose ethanol waste water mix with cooling concentration liquid after multiple-effect evaporation detailed process delivers to pressure filter and carry out press filtration processing, and multiple-effect evaporator evaporation is sent in pressure filter water outlet after heat exchange; Filter residues of press filter fully utilizes disposal as Ordinary solid waste.Pressure filter can adopt conventional plate and frame(type)filter press, vacuum belt press filter, rotary drum pressure filter etc.Cellulose ethanol waste water is the acid cellulose ethanol production wastewater that steams quick-fried pretreatment process.
(2) multiple-effect evaporation is processed, and after press filtration, waste water enters multiple-effect evaporator after heat exchange, and the gaseous state material that multiple-effect evaporation obtains is condensed into liquid phase, and the concentrated solution after multiple-effect evaporation loops press filtration.Multiple-effect evaporation is transformed into gaseous state by liquid state by waste water and volatile organic matter wherein as ethanol, acetaldehyde, acetic acid, lactic acid, furfural, polycyclic aromatic hydrocarbons etc., and through with raw material heat exchange after again change into liquid state, send into cooling system and process; Evaporation concentration liquid, the concentrated waste water that contains various inorganic salt, organic salt, wood sugar, xylogen etc. is sent pressure filter and cellulose ethanol waste water combination treatment back to after heat exchange cooling.Multiple-effect evaporator can be selected two～six effects, but considers energy-conservation and plant investment, preferably selects five effects; Vaporizer can be selected film-type evaporation, dribble-feed evaporation or other various conventional evaporation patterns, but considers based on corrosion factor, preferably selects falling film type; One effect of multiple-effect evaporator adopts makes thermal source for steam outward, and the secondary steam that adopts successively last effect to generate after two effects is made thermal source, the secondary steam that each effect evaporation produces through with raw material heat exchange after obtain condensing cooling.
(3) cooling process, the condensation liquid phase of the gaseous state material that multiple-effect evaporation obtains is cooled to below 40 ℃, and cooling rear water outlet enters anaerobically fermenting and processes.Cooling tower adopts conventional natural ventilation type air cooling tower.
(4) anaerobically fermenting is processed, the cooled material that step (3) obtains enters reactor by the bottom of upflow anaerobic sludge blanket reactor, under anaerobically fermenting bacterium effect on anaerobic mud bed, methanation reaction occurs, methane gas is recycled outward by the pneumatic outlet discharger of reactor head; Processing water outlet enters aerobic treatment unit by reactor head liquid outlet and carries out subsequent disposal.The volumetric concentration of methane gas that this unit obtains is 40%～60%; The residence time of waste water in anaerobic reactor is 20～50h; Water inlet volumetric loading is 5～10kgCOD/m
3.d; In reactor, the service temperature of waste water is 30～40 ℃.
(5) aerobe is processed, and aerobic treatment is carried out in the water outlet after anaerobically fermenting is processed, and aerobic treatment adopts the aerobic treatment processes such as conventional activated sludge method or embrane method to process.
(6) filtration treatment, filters water outlet for cellulose ethanol production process.Filtration treatment adopts traditional sand-bed filter, more medium filter, fibrous bundle or fiber ball filter, shifting sand filter that also can adopt thermopnore form etc. is processed the water outlet of aerobe unit, after processing, water part or fully recovering are done cellulose ethanol production technique water, as complex acid water, hydrolysis and fermentation procedure water etc.
The inventive method adopts respectively press filtration, multiple-effect evaporation, cooling, anaerobically fermenting to produce methane, aerobe, filtration combined treatment flow process to cellulose ethanol waste water, after processing, water outlet can be made the process waters such as complex acid, hydrolysis and fermentation that cellulose ethanol is produced by direct reuse, because reuse water is not substantially containing inorganic salt, recycle for a long time the accumulation impact that can not cause salt, reach the object of water saving and the minimizing sewage discharge of cellulose ethanol production.
The method that the present invention proposes has high density saline sewage and can realize refuse material in fully recovering, waste water and obtained efficient recovery and comprehensive utilization, high concentration organic contaminant and be converted to methane etc. and obtain the utilization of resources, meets the requirement of recycling industries and clean production etc.
Accompanying drawing explanation
Fig. 1 is a kind of concrete cellulose ethanol sewage treatment technology process schematic diagram of the present invention.
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the inventive method is described.
Cellulose ethanol waste water is entered in pressure filter 1 continuously, and the solid waste in waste water, as xylogen, fermentation residue etc. is trapped within on the filter cloth of pressure filter, departs from and reclaims rear comprehensive utilization from filter cloth subsequently; The pressing filtering liquid of pressure filter 1 carries out consecutive evaporation processing by entering after interchanger and end effect steam heat-exchanging from multiple-effect evaporator 2 in multiple-effect evaporator 2.In multiple-effect evaporator 2, after preheating, first pressing filtering liquid enters an effect evaporation element, the primary steam (supplying steam outward) of take is indirect heating medium, the volatile organic matters such as ethanol contained in a part of waste water and waste water thereof, acetaldehyde, acetic acid, lactic acid, furfural, polycyclic aromatic hydrocarbons are transformed into steam state by liquid state, secondary indirect heating steam as two effect evaporation elements, in this process, an effect evaporation gas is converted into water of condensation; Concentrated solution after one effect evaporation directly enters two effect evaporation elements and proceeds evaporation process, and the steam steaming is as the second-heating steam of triple effect evaporation unit, and in this process, two effect evaporation gases are converted into water of condensation; Process by that analogy; Steam after end effect evaporation element evaporation process is by being become water of condensation after foregoing heat-exchange method heat exchange, and concentrated solution turns back to pressure filter 1 entrance and processes with cellulose ethanol waste water mixing press filtration after cooling.Evaporation condensed water after each effect and end effect evaporation process is directly sent into cooling tower 3 processing that further cools, and leaving water temperature(LWT) is controlled at below 40 ℃.The water outlet of cooling tower 3 is entered in reactor by the bottom of up-flow anaerobic sludge blanket (UASB) reactor 4, and under the zymogenic effect of anaerobic methane, the high-enriched organics in waste water is converted to organic acid and methane, and obtains methane by UASB aerogenesis mouth.Water outlet after UASB processes is delivered to aerobic biochemical unit 5 and is carried out biochemical degradation reaction, water outlet again after filter 6 filtration treatment reuse do the water of productive use such as the preparation of sulfuric acid liquid, hydrolysis and fermentation procedure.
Multiple-effect evaporator 2 of the present invention can be selected two～six effects, but considers steam consumption and plant investment impact, preferably selects five effect evaporation elements, controls ton and processes waste water primary steam consumption below 0.28 ton; Vaporizer can be selected film-type evaporation, dribble-feed evaporation or other various conventional evaporation patterns, but preferably selects falling film type evaporation; Based on energetic optimum utilization, consider, every effect evaporation element all will arrange evaporation preheater and interchanger; In the liquid cooling but of end effect evaporation concentration, salt parser to be set, the inorganic salt in state of saturation and organic salt in concentrated solution are crystallized out.Water outlet salts contg after multiple-effect evaporation is processed is very low, is generally below 100mg/L.
Cooling tower 3 of the present invention adopts conventional natural ventilation type air cooling tower, controls leaving water temperature(LWT) below 40 ℃.
Upflow anaerobic sludge blanket reactor 4 of the present invention is a kind of common anaerobic reactor structure, mainly four parts such as distribution plate, granule sludge treatment zone, bulking sludge breeding blanket, gas-solid-liquid separators, consists of.From the processing water outlet of cooling tower 3, by the bottom of UASB, enter reactor, on anaerobic mud bed, by anaerobically fermenting bacterium, complete after reaction, methane gas is recycled outward by the pneumatic outlet discharger of reactor head; Process water outlet and by reactor head liquid outlet, discharge cyclically utilizing, or further enter aerobic treatment unit and carry out subsequent disposal.The volumetric concentration of methane gas that this unit obtains is 40%～60%; The residence time of waste water in anaerobic reactor is 20～50h, is preferably 26～28h; The water inlet volumetric loading of anaerobic reactor is 5～10kgCOD/m
3.d, be preferably 6～9gCOD/m
3.d; In reactor, the service temperature of waste water is 30～40 ℃.
Aerobic treatment of the present invention unit 5 can be one or more combinations in traditional activated sludge process, intermittent activated sludge process (SBR), contact oxidation method, biomembrance process and any follow-on aerobe method.
Adopt the inventive method to carry out press filtration-multiple-effect evaporation-cooling-anaerobically fermenting-aerobe-filtration combined treatment to the cellulose ethanol waste water of the quick-fried pre-treatment production line of acid, can make pollutent COD main in treating high-concentration saline organic wastewater be reduced to below 60 mg/L by 130,000 mg/L, total salt quantity is reduced to below 100 mg/L by 100,000 mg/L, sulfate radical is reduced to below 5 mg/L by 10,000 mg/L, other fermentation inhibitor is all removed to below 10 mg/L, after processing, water outlet can be done the sulfuric acid liquid preparation that cellulose ethanol is produced by fully recovering, hydrolysis and fermenting process water, to reach the water saving of cellulose ethanol production and the object of sewage zero-discharge.
Below by embodiment, further illustrate the inventive method and effect.
Adopt treatment process of the present invention to process the cellulose ethanol production equipment waste water of domestic certain medium-sized test scale.This device be take maize straw as raw material, mainly adopts the explained hereafter cellulose ethanols such as the quick-fried pre-treatment of water vapor acid, enzymatic hydrolysis, liquid glucose fermentation, ethanol concentrate and rectification and purification, the principal pollutant COD 129050 mg/L(chromium methods in waste water, lower with), BOD
568600 mg/L, sulfate radical 9290 mg/L, total salt quantity 9.69%, ammonia nitrogen 38.8 mg/L, carboxylic acid 4600 mg/L, furans 230 mg/L, phenol 600 mg/L.
Adopt press filtration-multiple-effect evaporation of the present invention-cooling-anaerobically fermenting-aerobe-filtration combined treatment to carry out laboratory treatment test to above-mentioned waste water, wastewater treatment scale is 200 mL/h, and main experimental installation formation, operational conditions and the treatment effect of each processing unit are in Table 1.After processing by method of the present invention, COD in cellulose ethanol waste water can be reduced to 60mg/L, total salt quantity can be reduced to that 100mg/L is following, sulfate radical can be reduced to below 5 mg/L, inhibitory enzyme hydrolysis and zymogenic hazardous and noxious substances carboxylic acid, furans, phenols are all removed to below 5mg/L, reusing sewage be can meet and the requirement of the preparation of sulfuric acid liquid, hydrolysis and the fermenting process water of cellulose ethanol production, fully recovering made.
The main processing unit of table 1 embodiment 1 forms and treatment effect.
| processing unit title | treatment unit scale and chief component | main operational conditions and control parameter | process water outlet or |
| 1 press filtration | filter, treatment capacity 10L/h | periodical operation, vacuumizes, membrane filtration | water outlet COD11.7 ten thousand mg/L; Filter residue water ratio 80% |
| 2 multiple-effect evaporations | falling film type five effect evaporation test devices, glass material.Device wastewater treatment scale is 5L/h, mainly comprises column evaporator, preheater, condenser and enamel crystallizer tank. | operate continuously, outer for steam employing 0.6MPa saturation steam, consumption 1.3kg/h; Each is imitated evaporated water and is followed successively by 1.2,1.0,0.85,0.70,0.65 L/h; Concentrated solution 0.6 L/h adopts circulating water crystallization. | water outlet COD6.5 ten thousand mg/L, total salt quantity 38mg/L; |
| 3 is cooling | glass cools device, inside fills out Stainless Steel Helices | 40 ℃ of leaving water temperature(LWT)s | - |
| 4 anaerobically fermentings | adopt UASB, material synthetic glass, reactor volume 40L.Mainly comprise the formations such as bottom water distribution board, granule sludge bed, mud buffer layer, Gas-solid-liquid separater, vapor pipe, water shoot, screen cloth. | bottom is water inlet continuously; Water inlet flow velocity 200mL/h; Retention time of sewage 40h; Water inlet volumetric loading 7.8kgCOD/m 3.d; 39 ℃ of service temperatures; The methane gas average-volume concentration 55% of collecting. | water outlet COD 3000mg/L, organic acid 1000 mg/L, furans <1 mg/L, phenol <5 mg/ |
| 5 aerobic biochemicals | adopt traditional SBR, material synthetic glass, reactor volume 20L.Mainly comprise bottom micro-hole aerator oxygenic aeration, machine mixer, with magnetic valve, programmable logic controller (PLC) sequence control system, control entering of useless water and air. | be interrupted Inlet and outlet water; Two cycles of day operation; Periodic duty time 12h, water inlet 4h, aeration 10h, sedimentation 0.5h, draining 1h, idle 0.5h; Period treatment water yield 2.4L, water inlet flow velocity 0.6L/h; Blast volume 100mL/min. | water outlet COD 68mg/L, ammonia nitrogen <5 mg/L, total salt quantity 42 mg/L, organic acid <5 mg/L, furans <0.5mg/L, phenol <0.5 mg/ |
| 6 filter | quartz sand filtration post, diameter 20mm, high 50mm | ? | water outlet COD 58mg/L, ammonia nitrogen <5 mg/L, total salt quantity 42 mg/L, organic acid <5 mg/L, furans <0.5mg/L, phenol <0.5 mg/L, SS<20mg/L |
Adopt the treatment unit of embodiment 1, process the sewage identical with embodiment 1, the water treatment effect that the operational conditions of change each processing unit obtains is in Table 2.
The main processing unit of table 2 embodiment 2 forms and treatment effect
| processing unit title | treatment unit scale and chief component | main operational conditions and control parameter | process water outlet or |
| 1 press filtration | filter, treatment capacity 10L/h | periodical operation, vacuumizes, membrane filtration; In press filtration forward direction waste water, add the polymeric ferric sulfate flocculant of 50mg/L and carry out stirring for 3 minutes coagulating treatment | water outlet COD10.5 ten thousand mg/L; Filter residue water ratio 75% |
| 2 multiple-effect evaporations | falling film type five effect evaporation test devices, glass material.Device wastewater treatment scale is 5L/h, mainly comprises column evaporator, preheater, condenser and enamel crystallizer tank. | operate continuously, outer for steam employing 0.6MPa saturation steam, consumption 1.3kg/h; Each is imitated evaporated water and is followed successively by 1.22,1.03,0.87,0.76,0.62 L/h; Concentrated solution 0.5 L/h adopts circulating water crystallization. | water outlet COD5.8 ten thousand mg/L, total salt quantity 35mg/L; |
| 3 is cooling | glass cools device, inside fills out Stainless Steel Helices | 40 ℃ of leaving water temperature(LWT)s | - |
| 4 anaerobically fermentings | adopt UASB, material synthetic glass, reactor volume 40L.Mainly comprise the formations such as bottom water distribution board, granule sludge bed, mud buffer layer, Gas-solid-liquid separater, vapor pipe, water shoot, screen cloth. | bottom is water inlet continuously; Water inlet flow velocity 200mL/h; Retention time of sewage 40h; Water inlet volumetric loading 7.0kgCOD/m 3.d; 39 ℃ of service temperatures; The methane gas average-volume concentration 55% of collecting. | water outlet COD 2650mg/L, organic acid 950 mg/L, furans <1 mg/L, phenol <5 mg/ |
| 5 aerobic biochemicals | adopt traditional SBR, material synthetic glass, reactor volume 10L.Mainly comprise bottom micro-hole aerator oxygenic aeration, machine mixer, with magnetic valve, programmable logic controller (PLC) sequence control system, control entering of useless water and air. | be interrupted Inlet and outlet water; Two cycles of day operation; Periodic duty time 12h, water inlet 4h, aeration 10h, sedimentation 0.5h, draining 1h, idle 0.5h; Period treatment water yield 2.4L, water inlet flow velocity 0.6L/h; Blast volume 100mL/min. | water outlet COD 62mg/L, ammonia nitrogen <5 mg/L, total salt quantity 40 mg/L, organic acid <5 mg/L, furans <0.5mg/L, phenol <0.5 mg/ |
| 6 filter | quartz sand filtration post, diameter 20mm, high 50mm | ? | water outlet COD 56mg/L, ammonia nitrogen <5 mg/L, total salt quantity 40 mg/L, organic acid <5 mg/L, furans <0.5mg/L, phenol <0.5 mg/L, SS<20mg/L |
Claims (9)
1. a treatment process for cellulose ethanol waste water, is characterized in that comprising following process:
(1) press filtration, after press filtration, waste water carries out multiple-effect evaporation processing, and press filtration charging is the mixture of concentrated solution after cellulose ethanol waste water and multiple-effect evaporation;
(2) multiple-effect evaporation is processed, and the waste water pressing filtering liquid after press filtration enters multiple-effect evaporator after heat exchange, and the gaseous state material that multiple-effect evaporation obtains is condensed into liquid phase, and the concentrated solution after multiple-effect evaporation loops press filtration;
(3) cooling process, the condensation liquid phase of the gaseous state material that multiple-effect evaporation obtains is cooled to below 40 ℃;
(4) anaerobically fermenting is processed, the cooled material that step (3) obtains enters reactor by the bottom of upflow anaerobic sludge blanket reactor, under anaerobically fermenting bacterium effect on anaerobic mud bed, methanation reaction occurs, methane gas is recycled outward by the pneumatic outlet discharger of reactor head; During anaerobically fermenting is processed, the residence time of waste water in anaerobic reactor is 20～50h, and water inlet volumetric loading is 5～10kgCOD/m
3.d, in reactor, the service temperature of waste water is 30～40 ℃;
(5) aerobic treatment, aerobic treatment is carried out in the water outlet after anaerobically fermenting is processed;
(6) filtration treatment, filters out water section or all for cellulose ethanol production process.
2. in accordance with the method for claim 1, it is characterized in that: the pressure-filtering process of step (1) is: cellulose ethanol waste water mixes with cooling concentration liquid after multiple-effect evaporation to be delivered to pressure filter and carry out press filtration processing, and multiple-effect evaporator evaporation is sent in pressure filter water outlet after heat exchange; Filter residues of press filter fully utilizes disposal as solid waste.
3. it is characterized in that in accordance with the method for claim 2: pressure filter adopts plate and frame(type)filter press, vacuum belt press filter or rotary drum pressure filter.
4. in accordance with the method for claim 1, it is characterized in that: the multiple-effect evaporation of step (2) is processed, pressing filtering liquid from pressure filter enters multiple-effect evaporator after heat exchange, waste water and volatile organic matter are wherein transformed into gaseous state by liquid state, and through with raw material heat exchange after again change into liquid state, send into cooling system and process.
5. according to the method described in claim 1 or 4, it is characterized in that: step (2) multiple-effect evaporation is processed the concentrated solution obtaining, after heat exchange cooling, send pressure filter and cellulose ethanol waste water combination treatment back to.
6. in accordance with the method for claim 1, it is characterized in that: the multiple-effect evaporator of step (2) is selected two～six effects, multiple-effect evaporator is selected film-type evaporation, dribble-feed evaporation.
7. according to the method described in claim 1 or 6, it is characterized in that: an effect of multiple-effect evaporator adopts the outer steam that supplies to make thermal source, the secondary steam that adopts successively last effect to generate after two effects is made thermal source, the secondary steam that each effect evaporation produces through with raw material heat exchange after obtain condensing cooling.
8. it is characterized in that in accordance with the method for claim 1: step (5) aerobic treatment is activated sludge process or embrane method aerobic treatment process.
9. in accordance with the method for claim 1, it is characterized in that: the filtration treatment of step (6) adopts sand-bed filter, more medium filter, fibrous bundle or fiber ball filter, or adopt the shifting sand filter of thermopnore form.
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| JP2004283127A (en) * | 2003-03-25 | 2004-10-14 | Hitachi Kiden Kogyo Ltd | Method for producing ethanol from sewage sludge |
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