CN107055773A - A kind of method of cassava alcohol wastewater anaerobic effluent advanced treating - Google Patents
A kind of method of cassava alcohol wastewater anaerobic effluent advanced treating Download PDFInfo
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- CN107055773A CN107055773A CN201710457535.5A CN201710457535A CN107055773A CN 107055773 A CN107055773 A CN 107055773A CN 201710457535 A CN201710457535 A CN 201710457535A CN 107055773 A CN107055773 A CN 107055773A
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
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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
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- Biodiversity & Conservation Biology (AREA)
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- Environmental & Geological Engineering (AREA)
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- Chemical & Material Sciences (AREA)
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- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention discloses a kind of method of cassava alcohol wastewater anaerobic effluent advanced treating, belong to dirty water decontamination handles technical field.Seed sludge of the present invention is the anaeration in normal temperature granule sludge of food processing factory, reactor is used as using up-flow anaerobic sludge blanket UASB, pass through continuous Anaerobic Treatment under the conditions of middle 35 DEG C of temperature, analyze its fermentation character, kinetic model is set up simultaneously and provides optimization operational factor for fermentation process, and reliable operational management theoretical direction is provided for the processing of actual cassava alcohol wastewater.The fermentation of anaerobic waste water depth can produce substantial amounts of biogas, can effectively dispose one stage of cassava alcohol high temperature anaerobic and go out aqueous waste solution, realize the innoxious of high concentrated organic wastewater, minimizing and recycling.This method is simply easily operated, and stability is high, can effectively handle the waste liquid of one stage of cassava alcohol high temperature anaerobic water outlet.
Description
Technical field
The present invention relates to a kind of method of cassava alcohol wastewater anaerobic effluent advanced treating, belong to the dirty water decontamination handles technology
Field.
Background technology
According to related report, cassava alcohol fuel will play more and more important during following energy source configuration
Effect.Due to contain in the root of cassava, stem can be produced in substantial amounts of carbohydrate and starch, ethanol alcohol production process it is a large amount of
Organic wastewater, wherein the nutriment containing substantial amounts of reproducible utilization, is the nontoxic high concentrated organic wastewater of a class.In wood
During potato fuel ethanol production, about 15t alcohol waste water can be discharged by generating alcohol per ton, and such waste water has Gao Hangu
The features such as rate, high COD and low pH, be the industry high-concentration organic wastewater of a class difficult degradation, can not only influence waste water to receive water body
Ecological environment, and be also one of the influence factor for restricting enterprise development, therefore, how to solve the problem and turned into enterprise to send out
An important topic during exhibition.Anaerobic fermentation is the technology for converting biomass into bioenergy, can be produced reproducible clear
Clean energy biogas, has turned into one of effective ways of processing alcohol waste water at present
Compared to other processing disposal technologies, anaerobic digestion is more advantageous, and it not only can effectively handle cassava alcohol
Waste liquid, and can obtain and clean biogas energy, the minimizing of cassava alcohol wastewater, innoxious and recycling are realized, to ring
Border and economic sustainable development have great importance.
In cassava alcohol wastewater anaerobic fermentation process, although part organic matter can be degraded after one-level Anaerobic Treatment,
But organic substance in one-level anaerobic effluent is still higher, biodegradability is good, SS contents are low, pH is moderate etc., therefore to cassiri
The processing method of smart one stage of waste liquid anaerobic fermentation water outlet stills need to improve.The current high organic concentrations high stage of SS anaerobic fermentations one
Anaerobic effluent processing is still faced with many problems, is mainly shown as two aspects：On the one hand it is due to a stage anaerobic fermentation system
Waste water quality characteristic is different in water outlet, and the disposal type of the successive depths processing used is different；On the other hand in actual waste liquid
Need to consider the principles such as economy and operability in processing procedure, it is desirable to which successive depths processing unit not only needs efficiently
Disposal ability, while but also with the features such as economic cost is low, management is simple, in addition, for the operating condition of anaerobic fermentation process
Optimization problem, how to set up optimal way and method is also the problem encountered during processing alcohol effluent.
The content of the invention
Technical problem solved by the invention is dissolved organic matter in the water outlet for a stage high temperature CSTR reactor
The problem of matter content is higher is there is provided a kind of method of cassava alcohol wastewater anaerobic effluent advanced treating, and methods described is using upper
Flow anaerobic sludge bed reactor UASB, inoculation granule sludge carries out middle temperature continuous anaerobic fermentation methane production.
In one embodiment of the invention, the TS of the middle temperature granule sludge be 100~110mg/L, VS be 80~
90mg/L, pH are 7.5~8.0.
In one embodiment of the invention, the inoculum concentration is 8~10gVS sludge/L waste water.
In one embodiment of the invention, the inoculum concentration is that 72gVS dirts are inoculated with 7.2L reactor volume
Mud.
In one embodiment of the invention, the anaeration in normal temperature UASB of the middle temperature granule sludge from food processing factory
In reactor, the inoculum concentration is 72gVS strains in retort.
In one embodiment of the invention, the VS of the cassava alcohol wastewater anaerobic fermentation is 10g/L, cassava alcohol
Anaerobic fermentation waste liquid carries out continuous feed by peristaltic pump, and water outlet is 2 with water inlet reflux ratio：1, pH is not adjusted in course of reaction.
In one embodiment of the invention, the inlet flow-patterm of the reactor is 7.4~7.62, total COD 15000~
2200~2700mg/ of 15400mg/L, soluble 10000~11000mg/L of COD, 6200~6500CaO of basicity mg/L, VFA
L。
In one embodiment of the invention, the running temperature of the UASB anaerobic reactors is 33~35 DEG C.
In one embodiment of the invention, the method for operation of the UASB anaerobic reactors is negative for graduated increasing volume
The mode of lotus, in 3kgCOD/ (m3.d 5~10d) is run, 5kgCOD/ (m are promoted to3.d 10~15d) is run, then is promoted to
7kgCOD/(m3.d 30~35d) is run.
In one embodiment of the invention, the HRT and factor of created gase of the UASB reactors are calculated as follows：Y=
5.2441x2+2.29x；Wherein, y is y (t)/ym；Y (t) is unit time factor of created gase, ymFor maximum factor of created gase；X is hydraulic retention
Time HRT；By giving factor of created gase, the hydraulic detention time needed for acquisition is calculated.
The present invention also provide designed according to methods described, the processing for cassava alcohol wastewater anaerobic effluent that manufactures is set
It is standby.
Beneficial effect：Seed sludge is derived from the anaeration in normal temperature granule sludge of food processing factory by the present invention, using up flow type
Anaerobic mud bed UASB reactors reclaim waste processing in line with maximum resource, operate simple, expense cost as processing equipment
Low theory, by carrying out comprehensive analysis to the mesostate produced during microbial growth, by nearly 60 days
Biological wastewater treatment, TCOD concentration is down to 1327.9mg/L from 15000mg/L, TCOD clearances reach 83.0%~
84.1%.The anaerobic fermentation method of operation that the present invention is lifted by volumetric loading, further reduces anaerobic fermentation outlet water organic substance
Matter concentration, improves the resource utilization degree of anaerobic fermentation water outlet.The technique of the present invention is simple, it is easy to control and operation, to carrying
The treatment effeciency and energy recovery rate of high cassava alcohol anaerobic fermentation waste liquid are significant, and will not produce secondary pollution,
Therefore can as the anaerobic fermentation water outlet of one stage of cassava alcohol wastewater subsequent treatment means, with good application and research
Prospect.
Brief description of the drawings
Fig. 1 is UASB anaerobic reactor schematic diagrames；
Fig. 2 is the situation of change of UASB reactor water outlets COD under different service conditions；
Fig. 3 is the Operating ettectiveness of UASB reactors under different condition；
Fig. 4 is UASB reactors organic acid and pH stability characteristic (quality)；
Fig. 5 is that UASB reaction systems organic acid constitutes dynamic change；
Fig. 6 is CSTR anaerobic reaction production rate of methane fitting a straight lines under different volumetric loadings；
Fig. 7 is the fitting a straight line between HRT and y (t)/(ym-y (t))；
Fig. 8 is the matched curve between k, HRT and y (t)/(ym-y (t)).
Embodiment
Methane content is determined using portable Methane determination instrument, TCOD, SCOD are determined using dichromate titration, is used
Liquid phase method determines VFA.
The fundamental characteristics such as table 1 of cassava alcohol wastewater, i.e. a stage high temperature CSTR anaerobic fermentation water outlet：
The cassava alcohol wastewater water quality characteristic of table 1
The middle temperature granule sludge that UASB anaerobic reactors are inoculated with present embodiment is derived from the anaeration in normal temperature of food processing factory
Retort, sludge fundamental characteristics such as table 2：
The property of the seed sludge of table 2
Embodiment 1
Using the up-flow anaerobic sludge blanket UASB reactor assemblies shown in Fig. 1, device is full glass material, and volume is
9.5L, actually active reaction volume is 7.2L.Reaction temperature is 35 DEG C, and water inlet is entered by pump from reactor bottom, reaction production
Raw biogas is separated by three phase separator, and draining into collection airbag from gas outlet pipe collects, and water outlet is with water inlet according to 2:1 ratio is entered
It is glass sandwich outside row backflow, reactor, maintains temperature to be run under the conditions of 35 DEG C using heating water bath mode.
UASB reactor water outlets COD situation of change under the different service conditions of embodiment 2
UASB reactor Operating ettectiveness is as shown in Figure 2.After stage CSTR anaerobic reactor processing, water outlet is according to institute
The corresponding hydraulic detention time and volumetric loading of setting enter UASB reactors by dilution, using pump and carry out anaerobic fermentation,
3kgCOD/(m3.d 10d) is run under load, 5kgCOD/ (m are promoted to3.d 15d) is run, then is promoted to 7kgCOD/ (m3.d) transport
Row 33d.By the processing of nearly 60 days, final reactor operating load was 7kgCOD/m3.d, TCOD and SCOD concentration point in water outlet
Not Wei 1327.9,551.2mg/L, TCOD clearances reach 83.0%~84.1%.During processing, go out Organic substance in water
Concentration is improved with the increase of water inlet volumetric loading.
As shown in figure 3, day biogas yield is improved with the raising of volumetric loading, when reactor volumetric loading be 3,
5、7kgCOD/m3.d under the conditions of during stable operation, day biogas output be respectively 6.9,12,17.1L/d, methane content respectively reaches
47.5%th, 52.3%, 51%, production rate of methane is respectively 0.358,0.315,0.31mL/g TCOD.With the progress of reaction,
Day biogas output does not occur big ups and downs, show reactor have under the volumetric loading good stable disposal ability with
Effect.
Methane phase anaerobic fermentation system is easily impacted by VFA concentration, under high-load condition, with VFA concentration
Accumulation can cause system pH reduction, so as to suppress the activity of methanogen so that organic substrates clearance and conversion ratio reduction.
Therefore, using the fermentation character of VFA concentration and pH metrics evaluation anaerobic fermentation systems.
As shown in figure 4, in the whole fermentation process of UASB anaerobic reactors, because inlet flow-patterm is always held at more than 7.4, appearance
Product load is within the scope of the disposal ability of the reactor, and therefore, pH is always held at more than 7.3 in water outlet, and basicity is maintained
1660~2325CaOmg/L or so because UASB inlet flow-patterms are higher, while the methanogenesis activity of institute's microbe inoculation compared with
Height, this explanation is under the regulation of suitable operating load, and the reaction system has good buffer capacity, does not have in the process of running
There is acidification phenomenon.
Organic acid composition in whole fermentation process is analyzed, as a result as shown in figure 5, lactic acid content is very low, most
Big value is 24.7mg/L, and main Determination of Organic Acids is acetic acid, is 7kgCOD/m in volumetric loading3When .d, acetic acid concentration exists
Between 532.9-1168.1mg/L, propionic acid and butyric acid content are relatively low and fluctuate smaller, pH change in stable system stage content
It is more consistent with each organic peracid forming composition dynamic change trend.In summary, in whole anaerobic fermentation process, when volume is negative
Lotus is 7kgCOD/m3When .d, reactor organic acid concentration is always maintained at relatively stable state, VFA concentration 900~
951.4mg/L between.
The kinetic model of CSTR anaerobic reaction production rate of methane under the different volumetric loadings of embodiment 3
The operational factor of the reactor is controlled according to following kinetic model：
The foundation of kinetic model is based on conservation of matter and obtained, then has：
In above-mentioned formula：
VRFor the volume (L) of reactor；moFor the inventory (L/d) added；C0To add the concentration of material organic substance
(g/L)；C is the concentration (g/L) of organic substance in reactor；R (c) is the speed (g/L.d) that substrate is digested；Y is that unit is former
Expect factor of created gase (L/gTCOD)；ymFor maximum unit raw material factor of created gase (L/gTCOD)；
According to first-order kinetics:
Wherein, k is first order reaction speed (d-1)。
According to HRT=m0.VR, under steady-state conditions, (1) (2) two formula can be obtained more than:
In addition, during anaerobic reaction, under the conditions of different time t, factor of created gase and substrate organic matter concentration have
Following relation:
Equation (4) conversion can be obtained,
Wherein, y (t) is unit raw material factor of created gase (L/gTCOD).
By (3) and (5), equation can be obtained:
In addition, according to volumetric loading and the relational expression Fr=m of hydraulic detention time0.HRT, (6) formula can be converted:
Under conditions of formula (7), k values can be according to HRT and y (t)/(ym- y (t)) between fitting a straight line figure and obtain,
Such as Fig. 7.
In addition it is also possible to obtain k, HRT and y (t)/(y by matched curve figurem- y (t)) graph of a relation between three, order
y(t)/ymFormula (6), can be converted into by=U,
Fit equation can be obtained for y=-0.004x+0.396 from factor of created gase matched curve Fig. 6, and maximum factor of created gase is 0.396L/
GTCOD, i.e. unit raw material factor of created gase, pass through HRT and y (t)/(ym- y (t)) between matched curve Fig. 7 (fit equation is y=
34.49x-2.06) first order kinetics parameter k*C can be obtained0It is worth for 34.49g/L.d, according to UASB entering organic matter of water matter concentration
C0For 15000mg/L, k values can be further obtained for 2.29d-1。
Make y (t)/ym=U, Fig. 8 can be obtained according to the relational expression of volumetric loading and hydraulic detention time.Fit curve equation
For y=5.2441x2+2.29x.It is 2.29d in k values again by Fig. 8-1When, according to given y (t) value 0.35L/gTCOD,
It is 3.3d that optimal HRT values under the conditions of this, which can be obtained, and Fr values are 4.5kgCOD/ (m3·d)。
Therefore, the model can calculate acquisition and reach the optimal of corresponding factor of created gase under the conditions of given pre- factor of created gase y
HRT and Fr, has certain directive significance to construction scale of projects and cost budgeting, while can also be provided for Practical Project operation
Certain theories technique support.
Although the present invention is disclosed as above with preferred embodiment, it is not limited to the present invention, any to be familiar with this skill
The people of art, without departing from the spirit and scope of the present invention, can do various changes and modification, therefore the protection model of the present invention
Enclose being defined of being defined by claims.
Claims (10)
1. a kind of method of cassava alcohol wastewater anaerobic effluent advanced treating, it is characterised in that methods described is to use up flow type
Anaerobic mud bed reactor UASB, is inoculated with middle temperature granule sludge and carries out middle temperature continuous anaerobic fermentation methane production；The middle temperature
The TS of grain sludge is 100~110mg/L, and VS is 80~90mg/L, and pH is 7.5~8.0.
2. according to the method described in claim 1, it is characterised in that the inoculum concentration is 8~10gVS sludge/L waste water.
3. according to the method described in claim 1, it is characterised in that the running temperature of the UASB anaerobic reactors is 33~35
℃。
4. according to the method described in claim 1, it is characterised in that the method for operation of the UASB anaerobic reactors carries for the stage
The mode of liter capacity load, the graduated increasing volumetric loading is respectively at 3kgCOD/ (m3.d)、5kgCOD/(m3.d)、
7kgCOD/(m3.d) operation a period of time.
5. according to the method described in claim 1, it is characterised in that the method for operation of the UASB anaerobic reactors carries for the stage
The mode of liter capacity load, in 3kgCOD/ (m3.d 5~10d) is run, 5kgCOD/ (m are promoted to3.d 10~15d) is run, then is carried
Rise to 7kgCOD/ (m3.d 30~35d) is run.
6. according to the method described in claim 1, it is characterised in that the inlet flow-patterm of the UASB anaerobic reactors is 7.4~
7.62, total COD are 15000~15400mg/L, and soluble COD is 10000~11000mg/L, and basicity is 6200~6500CaO
Mg/L, VFA are 2200~2700mg/L.
7. according to the method described in claim 1, it is characterised in that the TS of the middle temperature granule sludge is 108~110mg/L,
VS is 86~88mg/L, and pH is 7.8~8.0.
8. according to the method described in claim 1, it is characterised in that water outlet is 2 with water inlet reflux ratio：1, it is uncomfortable in course of reaction
Save pH.
9. according to the method described in claim 1, it is characterised in that the HRT and factor of created gase of the UASB reactors are counted as the following formula
Calculate：Y=5.2441x2+2.29x；Wherein, y is y (t)/ym；Y (t) is unit time factor of created gase, ymFor maximum factor of created gase；X is water
Power residence time HRT.
10. by the Slops treatment equipment of any methods described operations of claim 1-9.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111115964A (en) * | 2020-01-08 | 2020-05-08 | 中国科学院生态环境研究中心 | Wastewater anaerobic biological treatment system for seasonal strain preservation and recovery and application thereof |
| CN112209501A (en) * | 2020-10-10 | 2021-01-12 | 国投生物科技投资有限公司 | Method for reducing VFA production in wastewater during anaerobic treatment in IC reactor |
| CN118479698A (en) * | 2024-07-15 | 2024-08-13 | 杭州碟滤膜技术有限公司 | White spirit cellar bottom water treatment process and device |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101250005A (en) * | 2008-04-01 | 2008-08-27 | 同济大学 | Cassava grain stillage anaerobic treatment method |
| CN106630132A (en) * | 2016-12-29 | 2017-05-10 | 江南大学 | Method for high-temperature anaerobic treatment on cassava alcohol waste liquor by different inocula |
-
2017
- 2017-06-16 CN CN201710457535.5A patent/CN107055773B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101250005A (en) * | 2008-04-01 | 2008-08-27 | 同济大学 | Cassava grain stillage anaerobic treatment method |
| CN106630132A (en) * | 2016-12-29 | 2017-05-10 | 江南大学 | Method for high-temperature anaerobic treatment on cassava alcohol waste liquor by different inocula |
Non-Patent Citations (3)
| Title |
|---|
| 宁平: "《活性炭-微波处理典型有机废水》", 31 May 2015, 冶金工业出版社 * |
| 张庆华: "纤维质高效水解关键技术及其在木薯燃料乙醇产业中的应用", 《中国博士学位论文全文数据库 工程科技Ⅰ辑》 * |
| 陈金荣等: "高温CSTR—中温UASB两级厌氧处理木薯酒精废水", 《工业水处理》 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111115964A (en) * | 2020-01-08 | 2020-05-08 | 中国科学院生态环境研究中心 | Wastewater anaerobic biological treatment system for seasonal strain preservation and recovery and application thereof |
| CN112209501A (en) * | 2020-10-10 | 2021-01-12 | 国投生物科技投资有限公司 | Method for reducing VFA production in wastewater during anaerobic treatment in IC reactor |
| CN118479698A (en) * | 2024-07-15 | 2024-08-13 | 杭州碟滤膜技术有限公司 | White spirit cellar bottom water treatment process and device |
| CN118479698B (en) * | 2024-07-15 | 2024-09-27 | 杭州碟滤膜技术有限公司 | White spirit cellar bottom water treatment process and device |
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