CN114671519B - Method for repairing acidification system of anaerobic reactor under high-inflow COD concentration condition - Google Patents
Method for repairing acidification system of anaerobic reactor under high-inflow COD concentration condition Download PDFInfo
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Abstract
The invention discloses a method for repairing an acidification system of an anaerobic reactor under the condition of high COD concentration of inlet water, which comprises the following steps: firstly, maintaining the COD concentration of the inlet water at 6000-8000mg/L, and the organic load is higher than 1.5 kg/(m) 3 D) a step of; next, a trace amount of O is added to the system in a set ratio 2 The oxygen amount is maintained at 33 to 150gO 2 between/kgCOD; simultaneously adding exogenous nitrate, and controlling the ratio of C to N to be 20-65:1; controlling an anaerobic system to perform recovery culture at 33 ℃, and simultaneously accelerating acetate formation of waste water metabolic intermediate products through path regulation and control of carbon dioxide reductase gene expression; finally, based on the characteristics of pH and alkalinity rising, the recovery of COD removal rate to be normal and the obvious increase of the abundance of acetic acid nutrition type methanogens, the concentration of nitrate in the inlet water is gradually reduced until the normal operation of the reactor is realized. The method is based on facultative bacteria consumption O 2 Removing organic matters and consuming H by denitrification + And VFA, promote pH, realize the recovery of the anaerobic bioreactor acidification system of high inflow COD concentration, easy and simple to handle, the energy saving.
Description
Technical Field
The invention belongs to the technical field of sewage biological treatment, and particularly relates to a method for repairing an acidification system of an anaerobic reactor under the condition of high influent COD concentration.
Background
Anaerobic biological treatment technology is one of widely used technologies in the field of sewage treatment, and has the advantages of low sludge yield, energy recovery, good economy and the like. There are many factors affecting the operation of anaerobic bioreactors, including pH, temperature, ORP, salinity, etc. Under normal conditions, the acidogenic bacteria and methanogenic bacteria are kept in metabolic balance, and the metabolic products in the hydrolysis acidification stage can be timely utilized by the methanogenic bacteria and finally converted into inorganic matters such as methane. However, methanogens are relatively sensitive to pH, and suitable for growth at pH in the range of 6.5 to 3.8, and when pH is low, methanogen activity decreases, causing fatty acid accumulation, ultimately leading to reactor acidification. During operation, acidification of the reactor is caused by various reasons, such as toxic substances (heavy metals, free ammonia and the like), excessive load of the reactor, impact of low temperature and other environmental conditions, and the like. Under acidifying conditions, methanogen activity decreases and the reactor operation becomes less effective, and in some cases even completely stopped.
The current anaerobic acidification system regulation strategies include adding strong alkali, adding zero-valent iron, refluxing effluent water and the like (such as the prior art with patent application publication number or patent grant publication number of CN103435304B, CN106434824A, CN 105668380A). The pH can be rapidly increased in a short time by adding the reinforcing alkali, but the pH is difficult to keep stable after stopping adding, so that the problem can not be fundamentally solved; the zero-valent iron is added for too long to repair the acidification system, and the effluent backflow is only suitable for adjusting the micro-acidification anaerobic system. Exogenous nitrate addition to repair low influent COD concentration (COD=2000 mg.L) -1 ) Under the condition of the anaerobic acidification system (the prior art with the publication number of CN 113060896A), the method is only suitable for repairing the anaerobic acidification system when the COD concentration of the inlet water is low, and when repairing the high-concentration organic wastewater, the high-concentration organic wastewater needs to be diluted and then repaired and regulated, so that the repairing time is prolonged. If the method in the prior art with the publication number of CN113060896A is adopted to directly repair the high-concentration organic wastewater, the activity of methanogen is inhibited and even the cell membrane is destroyed to die due to the need of adding high-concentration nitrate, so that the purpose of repairing cannot be achieved. Therefore, how to repair the high-concentration organic wastewater under the condition of direct water inflowThe acidification system of the complex anaerobic reactor accelerates the repair efficiency and shortens the repair time, which is a problem to be solved in the field.
Disclosure of Invention
1. Problems to be solved
Aiming at the problem that the method for repairing the acidification of the anaerobic reactor in the prior art is difficult to be directly suitable for repairing the acidification of the anaerobic bioreactor under the condition of high inflow COD concentration, the invention provides the method for repairing the acidification system of the anaerobic reactor under the condition of high inflow COD concentration, which effectively avoids accumulation of organic acid, realizes repair of bacterial community structure and avoids failure of the reactor due to acidification under the condition of high inflow COD concentration.
2. Technical proposal
In order to solve the problems, the technical scheme adopted by the invention is as follows:
the invention adopts trace dissolved oxygen and nitrate to co-feed, can directly regulate and control the acidification of the anaerobic reactor to recover the methane production when the COD concentration of the water is high, and simultaneously quickly recover the pH value of the anaerobic acidification system.
By adding a small amount of oxygen and exogenous nitrate into the anaerobic acidification system, the facultative anaerobe can be utilized to consume oxygen through aerobic respiration, so that the organic matters such as volatile fatty acid and the like in the system can be degraded, the ammonia nitrogen removal effect can be improved, and the toxic effect on microorganisms in the system due to the too high ammonia nitrogen concentration can be avoided. Under the condition of a trace amount of oxygen, facultative bacteria on the outer layer of the granular sludge can quickly consume and protect anaerobic bacteria in the granular sludge from toxic action of oxygen, the aerobic reaction has higher efficiency compared with the anaerobic reaction, and denitrifying bacteria can consume H by taking VFA as an electron donor for denitrification + And alkalinity is generated, so that the repair of an anaerobic acidification system under the condition of high inflow COD concentration is realized.
The invention provides a method for repairing an acidification system of an anaerobic reactor under the condition of high COD concentration of inlet water, which is characterized in that: ph=3.5-6.5, proportion of propionate >16% of total VFA, which is volatile fatty acid, the method comprising the steps of:
s110, controlling the quality of inlet water: analyzing the water quality after acidification of the anaerobic wastewater treatment system, controlling the COD concentration of the inlet water to be 6000-8000mg/L, ensuring that the inlet water condition is a high COD concentration condition, and the organic load is higher than 1.5 kg/(m) 3 ·d)；
S120, controlling the addition amount of exogenous oxygen and nitrate: consumption of H according to denitrification process + Alkalinity producing facultative anaerobe consumption O 2 Under the condition, the concentration of exogenous nitrate and oxygen is designed to be added, the concentration of C and N is controlled to be between 20 and 65:1, the VFA in an anaerobic acidification system is removed through denitrification, the pH is improved, and the alkalinity is generated; the amount of added oxygen is controlled between 33 and 150gO 2 between/kgCOD, facultative bacteria consume O by aerobic respiration 2 Removing organic matters in the system; gibbs free energy due to oxygen redox reactions (1/4O 2 +H + +e - ＝1/2H 2 O,ΔG 0’ = -38.14 kJ/eeq) to nitrate (1/5 NO 3 - +6/5H + +e - ＝1/10N 2 +3/5H 2 O,ΔG 0’ = -31.63 kJ/eeq) is lower, so that facultative bacteria can more rapidly oxidize high concentrations of organic acids and ammonia nitrogen by consuming oxygen through aerobic respiration;
s130, metabolic path control based on a system microenvironment in the repairing process: in the repairing culture process, controlling the alkalinity of the anaerobic system to be more than or equal to 600mgCaCO 3 and/L, starting repair culture at 33deg.C, and removing CO by stirring and top air extracorporeal circulation alkali absorption 2 The dissolved gas is quickly released, the pressure in the system is reduced, and the CO is reduced 2 The effect of water-soluble on pH; the formation of acetate which is an intermediate product of waste water metabolism is accelerated through the path regulation and control of the gene expression of the carbon dioxide reductase;
quantitative qPCR analysis of denitrification gene narG, nirS, nirk and nos and carbon dioxide reduction in anaerobic granular sludge into acetic acid pathway gene acsA and acsB; regulating and controlling the adding proportion of the exogenous oxygen or nitrate in the step S120 to enable the acsA and acsB gene expression to present the highest transcriptional expression activity so as to promote the formation of acetate;
s140, metabolic product characteristics after repair is finished: detecting the concentration and components of the VFA of the effluent of the anaerobic system in the repairing process, and synchronously increasing the concentration of propionic acid and the concentration of acetic acid to serve as one of indexes for indicating that the anaerobic acidification reactor is successfully repaired by the repair of the micro-oxygen and nitrate;
s150, repairing and finishing microbial community characteristics: through analysis of community structure change in the anaerobic acidification system repaired by micro-oxygen and nitrate, screening the increase of the abundance of key acetogenic bacteria as one of indexes of restoring the ecological community of the system when the anaerobic acidification system is repaired by the cooperation of exogenous micro-oxygen and nitrate under the condition of high influent COD concentration;
s160, restoring normal COD removal effect based on pH rebound, increasing the abundance of acetic acid nutrition type methanogenic bacteria, gradually reducing nitrate in water to a normal state by taking one of S140 or S150 or the increase of the abundance of acsA and acsB genes as a sign, and stopping adding oxygen, so that the normal operation of the reactor under the condition of high water inflow COD concentration is realized under the condition of not depending on exogenous nitrate and oxygen.
Preferably, in the step S120, the concentration of the exogenous nitrate is between 40 and 100 mg/L.
Preferably, in the steps S140 and S160, the pH is raised to above 6.8, the removal rate of COD is greater than 80%, the propionic acid content in the effluent VFA is lower than 300mg/L, and the methanogen composition recovery characteristic is recovered to a normal level, i.e. the acidification regulation is completed.
Preferably, in the step S150, the key acetogenic bacteria include unclassified f Anaerolineaceae and norankf norank o SBR1031, but are not limited to the listed acetogenic bacteria.
Preferably, in the step S120, the COD concentration of the inlet water is controlled to 6000mg/L, the condition of high COD concentration of the inlet water is ensured, the HRT is 3d, and the recovery culture is performed at 33 ℃. Preferably, in the step S160, the pH is greater than 6.8, the COD removal rate is greater than 80%, the abundance of methanogens with acetic acid is increased, the nitrate in the water is gradually reduced to a normal state, and the addition of oxygen is stopped, so that the normal operation of the reactor under the condition of high COD concentration of the water is realized without depending on exogenous nitrate and oxygen.
3. Advantageous effects
Compared with the prior art, the invention has the beneficial effects that:
the method is based on that facultative bacteria degrade organic matters by aerobic respiration, and degrade the VFA by cooperating with denitrification, so that the accumulated VFA after acidification of an anaerobic reaction system can be removed, alkalinity is generated, acetate formation is promoted, and the rapid recovery of the acidification system of the anaerobic reactor under the condition of high inflow COD concentration is facilitated. By adding oxygen and exogenous nitrate, the pH is raised back and the reactor operates normally. The method is simple and convenient to operate, low in cost and easy to realize.
Drawings
FIG. 1 is a flow chart of the method for regulating and controlling the recovery of an anaerobic bioreactor after acidification;
FIG. 2 is a graph showing pH change during acidification remediation of the reactor with different COD concentration of incoming water in example 1;
FIG. 3 is a graph showing alkalinity changes during acidification remediation of the reactor with different COD concentrations in example 1;
FIG. 4 is a graph showing the COD removal rate change in the acidification recovery process of the reactor with different influent COD concentrations in example 1;
FIG. 5 is a graph showing the change of ammonia nitrogen removal rate in the acidification recovery procedure of the reactors with different COD concentrations of inflow water in example 1;
FIG. 6 is a graph showing the change of the abundance of main methanogens in the acidification repair process of reactors with different COD concentrations in example 1;
FIG. 7 shows the abundance of norank f Propionibacteriaceae, unclassified f Anaerolineaceae and norankf norank o SBR1031 in the different influent COD concentration reactors of example 1;
FIG. 8 is a graph showing the pH change during the long-term recovery culture in the high influent COD concentration reactor of example 2;
FIG. 9 is a graph showing the change in alkalinity of the high influent COD concentration reactor of example 2 during long-term recovery culture;
FIG. 10 is a graph showing the COD removal rate change in the acidification recovery process of the reactor with high influent COD concentration in example 2;
FIG. 11 is a graph showing the ammonia nitrogen concentration of the effluent during the acidification remediation process of the high influent COD concentration reactor in example 2;
FIG. 12 is a graph showing the change of functional gene abundance in the acidification repair process of the high influent COD concentration reactor in example 2;
FIG. 13 is a graph showing the change in propionic acid concentration after 15d of the high influent COD concentration reactor in example 2 was subjected to a recovery culture;
FIG. 14 is a graph showing the change in concentration and composition of VFA in the process of acidizing and repairing the high influent COD concentration reactor in example 2;
FIG. 15 is a graph showing the alkalinity versus pH during the UASB reactor acidification remediation process of example 3;
FIG. 16 is a graph showing the COD concentration and COD removal rate of effluent during the acidification recovery process of the UASB reactor in example 3.
Detailed Description
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs; the term "and/or" as used herein includes any and all combinations of one or more of the associated listed items.
For the purpose of facilitating an understanding of the embodiments of the present invention, reference will now be made to the following description of specific embodiments, taken in conjunction with the accompanying drawings, and the embodiments are not intended to limit the embodiments of the invention.
Example 1:
the comparison of the effect of the method for regulating and controlling the recovery of methane produced after acidification of the anaerobic bioreactor under different influent COD concentration conditions provided by the embodiment of the invention is shown in figure 1, and the method comprises the following treatment steps:
step S1, system characteristic analysis after acidification of anaerobic reactor
Analyzing the water quality after acidification of the anaerobic wastewater treatment system, wherein the pH=5.5, and the COD removal rate is less than or equal to 60 percent (the COD concentration of the original inlet water of the acidification reactor is more than 8000 mg/L);
s2, controlling the quality of the inlet water: the COD concentration of the initial inflow water is controlled to be 2000mg/L, and then the inflow water is gradually increased to 6000mg/L.
S3, adding exogenous nitrate and oxygen
Specifically, the addition of exogenous nitrate and O is designed 2 Concentration, total 8 experimental groups, CN is 22-33:1, and the oxygen amount is controlled between 33 and 111gO 2 between/kgCOD, the following are specific:
blank control group, designated R 0 Oxygen and nitrate are not added;
only adding oxygen group, setting 3 different oxygen concentrations, respectively named R 1 、R 2 、R 3 In the I-III stage, the total amount of oxygen introduced in a single period is 20, 40 and 60mg respectively, in the IV stage, 20, 40 and 60mg of oxygen are introduced into each experimental group respectively, and after each period (each water changing period, namely, HRT hydraulic retention time) is operated for 1d, the oxygen with the same concentration is introduced again, in the V stage, 20, 40 and 60mg of oxygen are introduced into each experimental group respectively, after each period is operated for 1.5d, the oxygen with the same concentration is introduced again, and the total amount of introduced oxygen is 40, 80 and 120mg respectively;
only the nitrate group, designated R, was added N In the first-second stage, nitrate concentration is 40mg/L, the third stage is raised to 80mg/L, the fourth stage is raised to 100mg/L, and after each period is operated for 1d, 100mg/L nitrate is added again, in the fifth stage, nitrate concentration is still 100mg/L, and after each period is operated for 1.5d, 100mg/L nitrate is added again;
oxygen and nitrate groups are added simultaneously, nitrate concentration and R are added at each stage in the experimental group N The same, and in each stage, the oxygen amount and R are introduced 1 、R 2 、R 3 The same, respectively named R 1 ’、R 2 ’、R 3 The specific addition concentrations are shown in Table 1.
TABLE 1 design of acidizing wastewater remediation experiments
* The oxygen content was calculated based on the COD content of the intake water and was 50mg O 2 /g COD； # The oxygen content was calculated based on the COD content of the inflow water and was 100mg O 2 /g COD； ** The oxygen content was calculated based on the COD content of the intake water and was 150mg O 2 /g COD；
Step S4, metabolic pathway control in repair process
Partial CO removal by stirring and headspace extracorporeal circulation lye absorption 2 Reducing the solubility of CO 2 Influence on the pH of the system. And by adding different amounts of micro-oxygen and exogenous nitrate, the expression effect of the carbon dioxide reductase gene is improved, and the formation of acetate is promoted.
Step S5, long-term recovery culture of the reactor
Under the experimental condition described in S3, carrying out repair culture on each experimental group reactor for 52 days at 33 ℃, and detecting indexes mainly including effluent water quality indexes, headspace gas components, acetic acid and propionic acid content in effluent VFA, main methanogenic archaea abundance, denitrification and CO 2 Reducing to acetic acid pathway gene abundance, and the like, and detecting the change condition of the abundance of key acetogenic bacteria in the system (figures 2-3). The results of the experiment are summarized as follows:
(1) The treatment effect of adding oxygen and nitrate simultaneously is superior to the application condition range of adding oxygen only, adding nitrate only and blank
As shown in FIG. 2, in stage I, COD concentration of the inlet water is 2000mg/L, and oxygen addition amount (50-150 mgO) 2 Under the conditions of/gCOD) and nitrate concentration (40 mg/L), oxygen and nitrate group (R) are added simultaneously 1 ’、R 2 ’、R 3 ') the pH value of the effluent is the highest (6.49-6.51); next, only the nitrate group (R N ) pH 6.46; adding oxygen group only (R 1 、R 2 、R 3 ) And blank group (R) 0 ) Similarly, the pH of the effluent is between 6.40 and 6.45.
Stage II, COD concentration of the inflow water is 3000mg/L, and oxygen addition amount (33-100 mgO) 2 /gCOD), nitrate addition (40 mg/L). Simultaneously adding oxygen and nitrate group R 1 ' average effluent pH was highest, 6.30-6.42, higher than that of the nitrate-only group R N 6.25-6.30 of (3); and R at this time 2 ’、R 3 ' the pH decreases with increasing oxygen concentration. As shown in FIG. 5, R 1 ’、R 2 ’、R 3 The average ammonia nitrogen removal rate is higher than that of the ammonia nitrogen removal rate obtained by adding nitrate only, and the lifting amplitude is 5.6-12.58%.
In stage III, COD concentration of the inflow water is 3000mg/L, and oxygen addition amount (33-100 mgO) 2 gCOD) and nitrate concentration (80 mg/L). 34d, adding oxygen and nitrate group R simultaneously 2 ’、R 3 ' the pH of the effluent reaches 6.41 and 6.49 respectively, and only nitrate group R is added N 6.38, R 1 ' is 6.33, the oxygen group is between 6.08 and 6.11, and the blank group is 6.12. This indicates that the pH of the high oxygen concentration effluent is higher in the presence of nitrate under this condition. As in fig. 3, 63d, average effluent alkalinity: r is R 1 ’(921mgCaCO 3 /L)>R N (911mgCaCO 3 /L)>R 2 ' and R 3 ’(868、856mgCaCO 3 /L)>Only oxygen group and blank group (541-594 mgCaCO) 3 L); as in fig. 4, 63d, average COD removal rate: r is R 3 ’(96.12％)>R 2 ’(94.38％)>R N (93.6％)>R 1 ' (91.96%). I.e. R 1 ' basicity is higher than R N However, the COD removal rate was lower than the latter, which suggests that the high alkalinity in the anaerobic remediation system is not a major factor in determining the COD removal rate. In summary, this stage R 1 ’、R 2 ’、R 3 ' COD removal Rate overall ratio R N The group height is 1.34-4.51%.
In the early stage of the IV stage, the COD concentration is 4500mg/L, and the oxygen addition amount ((22-63 mgO) 2 /gCOD). Times.2) and nitrate concentration (100 mg/L.times.2). The average effluent pH is higher when oxygen and low oxygen are added in the nitrate group simultaneously: simultaneously adding oxygen and nitrate group R 1 ' (6.34) =add nitrate only group R N (6.34)>R 2 ’、R 3 ’(6.31-6.32)>Adding oxygen group only (6.26-6.28)>Blank group.
Stage IV (81 d) with simultaneous addition of oxygen nitrate R 2 ' the pH of the effluent is highest: r is R 2 ’(6.81)>R 1 ’(6.77)＝R N (6.33)>R 3 ’(6.31)>Blank and oxygen only (6.29-6.36) groups, which indicate that at high concentrations of influent COD, an increase in the amount of oxygen in the presence of nitrate can promote pH elevation.
In summary, stage IV R 1 ’、R 2 ’、R 3 ' COD removal rate (90.4%, 94.5%, 96.3%) to R N The group height is 3-8.8%.
In the V stage, the COD concentration of the inlet water is 6000mg/L and the oxygen addition amount ((13-50 mgO) 2 /gCOD). Times.2) and nitrate concentration (100 mg/L.times.2). 105 th to 126 th days, the average effluent pH of the oxygen and nitrate group added simultaneously is higher than 6.30: r is R 1 ’(6.38)>R 2 ’(6.32)>R 3 ' (6.31). 129d, adding oxygen and nitrate group at the same time, wherein the average effluent pH is highest: r is R 3 ’(3.06)>R 1 ' and R 2 ’(3.03、3.04)>R N (3.00)>Adding oxygen group only (6.12-6.59)>Blank R 0 (4.83). 108d, average outlet alkalinity: r is R 1 ’(1463mgCaCO 3 /L)>R N (1350mgCaCO 3 /L)>R 2 ' and R 3 ’(1261、1299mgCaCO 3 /L)>Only oxygen group and blank group (656-845 mgCaCO) 3 /L)。
At stage V, 105-128d, R 2 ' the average COD removal rate is highest and reaches 90.6%; 121d, the removal rate of COD of the discharged water: r is R 1 ’、R 2 ' and R 3 ’(98.61％、98.53％、93.63％)>R N (85.16%). 95d, R 3’ The ammonia nitrogen removal rate is highest: r is R 3 ’、R 2 ’、R 1 ’(98.9％、94.0％、83.9％)>R N (50.9％)。
(2) Matters to be noted: under the following conditions, the transient pH value of the added nitrate group is higher than that of the added oxygen and nitrate groups, but the COD removal rate, ammonia nitrogen removal rate, alkalinity and other indexes are reduced
In the early stage of the III stage, the COD concentration of the inlet water is 3000mg/L, and the oxygen addition amount (33-100 mgO) 2 According to the concentration of/gCOD) and nitrate (80 mg/L multiplied by 2), namely under the condition of improving the nitrate concentration of the inlet water on the basis of II stage, only the nitrate group R is added N A transient pH higher than the simultaneous addition of oxygen and nitrate group (R 1 ’、R 2 ’、R 3 ’)：R N (6.38)>R 1 ’、R 2 ’、R 3 ’(6.32-6.34)>Adding oxygen onlyAir group>Blank R 0 The method comprises the steps of carrying out a first treatment on the surface of the However, no matter whether oxygen exists or not, the COD removal rate of the added nitrate group begins to decrease, which indicates that the excessive nitrate proportion in the COD of the unit water inflow starts to inhibit the acidogenic methanogen. At this time, only the nitrate group R was added N Average COD removal ratio while adding oxygen and nitrate group R 1 ’、R 2 ’、R 3 The COD removal rate (94-98%) of' is 1.34-4.51%.
Stage III 18d, R 3 ' the alkalinity of the effluent reaches the highest 643mgCaCO 3 /L，R 1 ' and R 2 ' 636 and 643mgCaCO 3 L, R N 625mgCaCO 3 and/L. 34d, R 2 ’、R 3 ' the pH of the effluent reaches 6.41 and 6.49 respectively, and R N 6.38, R 1 ' 6.33, the experimental group with only oxygen added was between 6.08 and 6.11, and the blank group was 6.12. This suggests that the addition of only high nitrate, the absence of oxygen, for long term operation, inhibits the anaerobic system, resulting in a drop in pH and alkalinity.
42d, R in stage III 2 ’、R 1 ' and R 3 ' Ammonia nitrogen removal rate (83.3%, 35.6%, 36.4%)>R N (30.8％)。
(3) Matters to be noted: under the following conditions, only the oxygen group added has short pH lower, and the COD concentration of the inlet water is 3000mg/L and the oxygen addition amount ((33-100 mgO) is 3000mg/L in the stage II caused by the existence of carbon dioxide gas pressure in the headspace 2 Per gCOD)) and nitrate concentration (40 mg/L), oxygen group (R) alone was added 1 、R 2 、R 3 ) The average effluent pH increased with increasing oxygen concentration: r is R 3 (6.18)>R 1 (6.14)>R 2 (6.13). I.e. this indicates that the anaerobic effluent pH is higher at high oxygen concentrations under this condition.
(4) Restoration of methanogen and bacterial community structure in restoration process
In the acidification and repair process of the anaerobic system, the change of the abundance of methanogenic archaea is shown in fig. 6 and 3. Stage II, 24d, the highest methanogenic archaea abundance of each group was Methanobacterium. Simultaneously adding oxygen and nitrate R 2 ' group (nitrate concentration 40 mg.L) -1 OxygenThe gas addition amount is 80 mg), and the Methanosaeta abundance is improved from 10.3 percent to 12.5 percent before repair.
32d in the IV stage, wherein the groups with high metanosaeta abundance are all in the group with higher oxygen concentration, and R is added in the group with oxygen and nitrate 2 ' the metasasa abundance is at most 6.3%; r is R 3 The metanosaeta abundance in the group increased from 1.1% to 10.1% in stage ii. Under the condition of the same oxygen concentration, the abundance of Methanobacterium in the group without adding nitrate is higher than that of the group with adding exogenous nitrate, which shows that the simultaneous addition of oxygen and nitrate is helpful for the restoration of acetic acid nutritional methanogens.
105d in stage IV, in the experimental group with simultaneous addition of oxygen and nitrate, R 3 The 'experimental group' had the highest Methanobacterium abundance, rising from 3.3% to 14.3%. The abundance of the oxygen and nitrate groups is improved when the methnolinea is added simultaneously, R N 、R 1 ’、R 2 ’、R 3 ' from 0.08%, 0.03%, 0.16% and 0.08% up to 0.42%, 0.40%, 1.2% and 0.43%, respectively. R is R N The group Candida-Methanofastidiosum abundance and Bathyarchaeia abundance increased significantly from 0.2% to 4.0% and 0.3% to 1.3%, respectively. .
Stage V113 d, the abundance of Methanosaeta for each group varies less, while the abundance of Methanosaacterium increases. Simultaneously adding oxygen and nitrate group R 2 ' and addition of oxygen group R only 3 The abundance of the Methanosaeta is 11.3% at the highest; whether nitrate is present or not, candida-metafastdiosum high abundance occurs in the higher oxygen concentration group. 113d,norankf norank o SBR1031 abundance is: r is R 1 、R 2 、R 3 (11.0%, 11.3% and 9.6%)>R 1 ' and R 3 ' (5.3% and 8.5%)>Blank R 0 (3.8％)>R N (3.4%). unclassified f Anaerolineaceae abundance: simultaneously adding oxygen and increasing with the increase of oxygen concentration in the nitrate group, R 1 ’、R 2 ’、R 3 ' 4.2%, 4.5% and 6.9%, respectively, and higher than the group R with nitrate alone N 2.3% of (3); and R is 1 、R 2 、R 3 6.4%, 6.2% and 3.1%. 113d, R N The group contained a higher norank f Propionibacteriaceae abundance (19.8%).
S6, restoring the reactor to a normal state
In the long-term culture process of S5, the pH, alkalinity, COD removal rate, gas components, methanogenic archaea community structure and the like in the reactor can be gradually restored to normal level, and the like, so that the abundance of key acetogenic bacteria is improved, and the anaerobic acidification reactor achieves a good restoration effect.
Example 2:
the method for recovering and regulating the acidified anaerobic bioreactor under the condition of high inflow COD concentration provided by the embodiment of the invention comprises the following steps:
step S1, system characteristic analysis after acidification of anaerobic reactor
Analyzing the water quality after acidification of the anaerobic wastewater treatment system, wherein the COD concentration of the inflow water is more than 8000mg/L, the pH value is=4.5, the COD removal rate is less than or equal to 60%, the propionate content is 533mg/L, and the propionate content accounts for 19% of the total amount of the VFA;
s2, controlling the quality of the inlet water: the COD concentration of the inlet water is controlled to be 6000mg/L and 8000mg/L respectively.
S3, adding exogenous nitrate and oxygen
Specifically, the addition of exogenous nitrate and O is designed 2 Concentration, 2 groups of high water inflow COD concentration are controlled: experimental group R6000-H with water inflow COD concentration of 6000mg/L 1 (hrt=1d) and R6000-L 1 (hrt=2d) C: N is 21 to 46:1, and blank control groups R6000-H are respectively set 0 And R6000-L 0 The method comprises the steps of carrying out a first treatment on the surface of the Experimental group R8000-H with COD concentration of water at 8000mg/L 1 (HRT＝1d)、R8000-L 1 (hrt=2d) C: N is 28 to 61:1, and a blank control group R8000-H is set 0 And R8000-L 0 . Setting different oxygen concentration at 33-111 gO 2 The ratio of the oxygen to the oxygen demand (kgCOD) is shown in Table 2.
TABLE 2 design of acidizing wastewater remediation experiments
* The COD of the inflow water is taken as a reference, and the oxygen addition amount is 30mg O 2 /g COD；
* The oxygen addition amount is 45mg O based on the COD amount of the inflow water 2 /g COD.
Step S4, metabolic pathway control in repair process
Partial CO removal by stirring and headspace extracorporeal circulation lye absorption 2 Reducing the solubility of CO 2 The influence on the pH of the system is improved, and the effect of expressing the carbon dioxide reductase gene is improved by adding micro-oxygen and exogenous nitrate, so that the formation of acetate is promoted.
Step S5, long-term recovery culture of the reactor
Under the experimental conditions described in S3, the reactors of each experimental group were cultured for a long period at 33 ℃ and the following indexes were detected, mainly including effluent pH, alkalinity, COD removal effect, and the abundance of the main denitrification and methanogenesis functional genes, etc., while detecting the change of VFA in the system (see FIGS. 8-14). The repair results are summarized below:
(1) The present example is based on an acidification system with ph=4.5, a COD removal rate of 23% and a propionate accumulation of 19% of the total VFA, starting to repair, i.e. the acidification is more severe at the start of repair. Second, the repair cases were compared under different organic load conditions (controlled with hrt=1d, 2 d) at high influent COD concentrations of 6000 and 8000mg/L.
In stage I, oxygen and nitrate are added (oxygen addition amount 30 mgO) 2 The pH, alkalinity and average COD removal rate of the effluent with the concentration of/gCOD and nitrate (40-80 mg/L) multiplied by 2) are higher than those of a blank group, and the rise amplitude is 0.90-0.98, 533.6-329.6mgCaCO 3 L and 14.35-18.34%. Under the condition that the COD concentration of the inflow water is the same, the alkalinity of the outflow water and the average COD removal rate of the experimental group with HRT of 2d are larger than those of the group with HRT of 1d, and the rising amplitude is 89.1-162.9mgCaCO respectively 3 L and 4.14-9.16%.
Stage I13 d, R6000-L 1 The highest alkalinity of the effluent is 1062mgCaCO 3 /L，R6000-H 1 1022mgCaCO 3 /L，R8000-H 1 And R8000-L 1 The alkalinity of the effluent is 598 mgCaCO and 836mgCaCO respectively 3 Blank groups are 38-32 only8mgCaCO 3 between/L.
31d, R6000-L 1 The pH of the effluent is the highest, R6000-L 1 (5.51)>R6000-H 1 (5.42)>R8000-H 1 And R8000-L 1 (5.05、4.91)>Blank (3.94-4.26); at this time, the COD removal rate sequence was: R6000-L 1 (53.5％)>R8000-L 1 (53.5％)>R8000-H 1 (46.5％)>R6000-H 1 (44.5％)>Blank (24-39.5%). From R6000-H 1 Having a relatively high pH, while a lower COD removal rate indicates that pH is not the only factor affecting COD removal rate.
And II, raising the nitrate concentration of the repairing group to 2 times of the original nitrate concentration, and aerating for 3min. The repair group added with oxygen and nitrate is respectively 0.08-0.39 and 605.8-311.1mgCaCO higher than the blank group 3 L, 1.40-12.90%. 60d, the alkalinity of the repair group is reduced to 658.5-868.0mgCaCO 3 and/L. Under the condition that the COD concentration of the inflow water is the same, the alkalinity of the outflow water of the group with HRT of 2d is still larger than that of the outflow water of the group with HRT of 1d, and the amplification is 3.8-10.4%. The average COD removal rate is reduced by 6.81-13.91%. R6000-H under the condition of same HRT 1 The average COD removal rate is higher than R8000-H 1 And R8000-L 1 And R6000-L 1 The difference is small.
And III, reducing the nitrate concentration by 25%, stopping aeration, and opening the fermentation bottle mouth to reduce the aeration degree. The pH, alkalinity and average COD removal rate of the effluent water of the oxygen and nitrate adding repair group (oxygen adding is in a bottleneck opening mode, nitrate concentration ((40-80 mg/L) ×3)) are higher than those of the blank group, and the rising amplitude is 0.11-0.23, 623-344mgCaCO 3 L and 23.3-26.8%. The COD removal rate of the repair group with added oxygen and nitrate is higher than 80%.
Stage III 85d, R6000-H 1 The pH of the effluent is highest: R6000-H 1 (6.82)>R6000-L 1 (6.66)>R8000-H 1 (6.61)>R8000-L 1 (6.60)>Blank (5.09-5.25); the COD of the inflow water is 6000mg/L group, R6000-H 1 、R6000-L 1 The alkalinity of the water output reaches the highest at 90d and 80d respectively, which are 1111.5 and 1131.2mgCaCO 3 L; COD of the inflow water is 8000mg/L group, R8000-H 1 、R8000-L 1 At the same time, the highest 90d is 1101.45 and 1283.0mgCaCO respectively 3 /L。
And IV, keeping the nitrate concentration unchanged, closing the fermentation bottle mouth, and improving the oxygen addition amount by 50% compared with the stage I. The low-load inflow COD6000mg/L group has the highest ammonia nitrogen removal rate, alkalinity and pH.
And in the IV stage 106d, the average alkalinity sequence of the effluent is as follows: R6000-L 1 (1026mgCaCO 3 /L)>R8000-L 1 (998mgCaCO 3 /L)>R6000-H 1 (965mgCaCO 3 /L)>R8000-H 1 (885mgCaCO 3 /L)>Blank group (395-416 mgCaCO) 3 L); at this time, the COD removal rate sequence was: R6000-L 1 (86.04％)>R8000-H 1 (83.88％)>R6000-H 1 (36.88％)>R8000-L 1 (35.35％)>Blank (53.13-58.13%). 109d, the ammonia nitrogen concentration sequence of the effluent is as follows: R6000-L 1 (13.0mg/L)>R8000-L 1 (13.60mg/L)>R8000-H 1 (17.70mg/L)>R6000-H 1 (18.45mg/L)>Blank (33.25-33.30 mg/L). From high load condition (HRT 1 d) of 8000mg/L of inflow water, R8000-H 1 Ratio R8000-L 1 And R6000-H 1 It can be seen that the COD removal rate is higher, the nitrate concentration of the influent water is 40mg/L×3 (the×3 is 3 times of single cycle HRT addition) and the oxygen addition amount (45 mgO) 2 /g COD) is a more suitable control condition.
116d in the IV stage, when the restoration is finished, the pH sequence of the effluent is as follows: R6000-L 1 (6.30)>R6000-H 1 (6.63)>R8000-H 1 (6.62)>R8000-L 1 (6.59)>Blank (4.62-5.21).
In summary, at the end of repair, the pH of each repair group was raised from extremely acidified 4.50 to 6.59-6.30, i.e. by 2 orders of magnitude; the COD removal rate is increased from 23% to 35-86%, namely, the removal rate is increased by 2-3 times.
(2) Typical denitrification functional genes, methanogenesis genes and carbon dioxide fixation functional gene change conditions in the repair process; the propionate content of the effluent gradually decreases along with repair
As can be seen from FIG. 12, the modification was carried out with the change in the concentration of exogenously added micro-oxygen and nitrateThe recombinant functional genes show larger difference, and the I and IV stages contain high abundance denitrification genes narG, nirS, methanogenic genes and carbon dioxide fixed genes, wherein R6000-H 1 All functional genes in the group were more abundant than in the blank group.
At the end of stage I, 51d, R6000H 1 Meanwhile, the highest denitrification genes (narG, nirS and nosZ), carbon dioxide fixed genes acsA and acsB, a methane-generating gene mcrA and an anaerobic ammoxidation gene hzo gene abundances are held, and the sequences of the gene abundances from high to low in a repairing group are the same: R6000H 1 ＞R8000H 1 ＞R8000L 1 ＞R6000L 1 。R6000H 1 The abundance of the functional gene is R8000H 1 1.5-14 times of (a).
R6000H 1 Repair of methane mcrA Gene abundance (2.38X10) 3 copies/ngDNA) and the carbon dioxide fixed gene acsA abundance (1.08X10) 3 cobies/ngDNA) are all their low load repair group R6000L 1 3 times of the abundance of the corresponding gene; while the methane-producing gene mcrA abundance under the high-load condition of R8000 group (R8000H) 1 ：1.66×10 3 copies/ngDNA) and acsA abundance (R8000H 1 ：6.46×10 6 cobies/ngDNA) are all higher than the low load condition R8000L 1 (mcrA：1.20×10 3 copies/ngDNA；acsA：5.03×10 6 cobies/ngDNA). This indicates that the amount of nitrate added per unit load cannot be too high, and that too high a nitrate concentration reduces the abundance of the functional gene.
At the end of stage III, 95d, R6000L 1 Meanwhile, the highest denitrification genes (narG, nirK and nosZ), carbon dioxide fixation genes acsA and acsB, methanogenesis gene mcrA and anaerobic ammoxidation gene hzo gene abundance are held. But at this time R8000L 1 The gene abundance treatment was at the lowest level, probably due to R8000L 1 The reason why the amount of oxygen added per COD group is insufficient. 113d in the IV stage, the oxygen addition amount is increased to 45mg O 2 /g COD. The added micro-oxygen and nitrate repair group has higher abundance of denitrification genes narG, nirS and nosZ than the blank group. R8000L 1 Methane-producing gene mcrA abundance (2.38X10) 3 cobies/ngDNA) and the carbon dioxide fixation function gene acsA abundanceHighest. The mcrA abundance sequence is: R8000L 1 (2.38×10 3 copies/ngDNA)>R8000H 1 (8.51×10 6 copies/ngDNA)>R6000H 1 (7.97×10 6 copies/ngDNA)>R6000L 1 (3.10×10 6 copies/ngDNA)。
R6000H 1 The group contains the highest abundance acsA genes, the acsA abundance sequence of which is: R6000H 1 (2.61×10 7 copies/ngDNA)＞R6000L 1 (1.85×10 7 copies/ngDNA)＞R8000L 1 (1.82×10 7 copies/ngDNA)＞R8000H 1 (3.69×10 6 cobies/ngDNA). In addition, as can be seen from FIG. 12f, the abundance of the acsA gene of the IV-phase repair group is greatly increased compared with that of the III-phase repair group, wherein R6000H 1 Group acsA gene abundance (2.6X10) 3 The copies/ngDNA) is its stage III value (6.4X10 6 cobies/ngDNA).
As can be seen from FIGS. 13 and 14, the propionic acid concentration of the anaerobic system at the beginning of the repair reaches 595mg/L, and the total VFA concentration reaches 3318mg.L -1 . 15d, propionic acid concentration in the fed micro-oxygen and nitrate recovery group was reduced to 1/9 of that in the blank group. Wherein R6000-H 1 Group and R6000-L 1 The concentration of propionic acid in the effluent is respectively reduced to 139mg/L and 30mg/L; blank R6000-H 0 And R6000-L 0 The concentration of propionic acid in the effluent is 428mg/L and 349mg/L respectively (and the proportion of propionic acid and butyric acid is high). 15d, when the COD of the inflow water is 8000mg/L, R8000-L 1 The concentration of the propionic acid in the effluent is 30.8mg/L, which is lower than that of the blank group R8000-L 0 284.3mg/L; and R8000-H 0 Although the concentration of the propionic acid is higher than that of R8000-H 1 Low but with a much higher butyric acid content than R8000-H 1 Group, which is also a refractory organic acid, and the carbon chain is longer. This indicates that the acidification system of the blank group is still inhibited by the accumulation of propionic acid in the VFA, while the propionic acid inhibition in the repair group has been released, at which time the COD removal rate, alkalinity and pH of the repair group are all increased.
113d, the VFA concentration of the repair group effluent is reduced compared with that of the previous stage, and the main components are recovered to acetic acid. Wherein, repair group effluent VFA concentration: R6000-H 1 (1333.9mg·L -1 )、R6000-L 1 Group (1233.8 mg.L) -1 )；R8000-H 1 (1613.0mg·L -1 ) And R8000-L 1 Group (1380.5 mg.L) -1 ). Blank VFA was based on butyric acid: R6000-H 0 (1282.1mg·L -1 )、R6000-L 0 Group (1453.6 mg.L) -1 )、R8000-H 0 (2430mg·L -1 ) And R8000-L 0 Group (1836.1 mg.L) -1 ) The effluent VFA concentration is higher.
In short, at the end of the restoration, the concentration of propionic acid in the VFA of the restoration group water with the added oxygen and nitrate is restored to be reduced, and the restoration group water is converted into acetic acid which is a methanogenic substrate and is used as a main component. The denitrification functional genes narG, nirS and nosZ abundance, the methanogenesis genes and the carbon dioxide fixation genes are all increased.
S6, restoring the reactor to a normal state
In the long-term culture process in S5, based on the increase of the pH value, the alkalinity and the COD removal rate in the reactor, the increase of the content of the acetate in the effluent and the decrease of the concentration of propionic acid, the normal level of the methanogenic gene mcrA is recovered, the fixed carbon dioxide acetogenic gene acsA is improved, and the better recovery effect of the anaerobic acidification reactor is realized.
Example 3:
the method for recovering and regulating the acidified UASB reactor provided by the embodiment of the invention comprises the following steps:
analyzing the acidified water quality of the anaerobic wastewater treatment system, and the COD concentration of the inflow water>8000mg/L, pH=5.3, COD removal rate less than or equal to 50%; the COD concentration of the initial water inlet is controlled to be 3000mg/L and 6000mg/L respectively. Two UASB reactors were respectively set with initial inflow COD concentration of 3000 (RL) and 6000mg/L (RH) and HRT of 2d. Wherein, the concentration of nitrate added into RL is 80mg/L, and the oxygen addition amount in a single period is 30mgO 2 gCOD; the concentration of nitrate added in RH is 80mg/L, nitrate is added twice in a single period, and the addition amount of oxygen is 30mgO 2 /gCOD. Repairing and culturing until the II stage (59-80 d), stopping adding oxygen and nitrate, culturing until the III stage (81-93 d), and increasing the concentration of RL and RH inflow water COD by 20%. Specifically, the results are shown in Table 3.
TABLE 3 design of acidizing wastewater remediation experiments
Partial CO removal by stirring and headspace extracorporeal circulation lye absorption 2 Reducing the solubility of CO 2 The influence on the pH of the system is improved, and the effect of expressing the carbon dioxide reductase gene is improved by adding micro-oxygen and exogenous nitrate, so that the formation of acetate is promoted. The reactors of each experimental group are cultivated for a long time at the temperature of 33 ℃ and the indexes of the reactors mainly comprise the pH value, the alkalinity, the COD removal effect, the abundance of key functional genes, the abundance of main methanogenic archaea and the like are detected. The repair results are summarized as follows:
(1) In the embodiment, based on the acidification system with the pH=5.7, the COD removal rate being less than 50% and the propionate accumulation accounting for 16% of the total amount of the VFA, the restoration is finished in the UASB reactor, and after nitrate and air are added for 2 weeks, all indexes can be restored to be normal.
As can be seen from FIG. 15, the pH value of the effluent of the UASB reactor is restored to be 11 to 14d which is higher than 6.8, and the alkalinity is simultaneously and rapidly increased to 800mgCaCO 3 and/L. The pH value of the reactor effluent after acidification is only 5.3, and the pH values of the reactor effluent of the two groups of reactors are gradually increased along with the progress of the repair reaction at the initial stage of the repair culture. RL group (COD concentration of inflow 3000 mg/L) and RH (COD concentration of inflow 6000 mg/L) are respectively cultured until the pH value of the water discharged from 11d and 14d reaches above 6.8 after repairing culture, and then the pH value of the water discharged can be kept stable.
The alkalinity of the reactor effluent after acidification is only 524mgCaCO 3 and/L. And (3) repairing the initial stage of culture, wherein the alkalinity of the reactor effluent is in an ascending trend. No. 12d, RL group (COD concentration of inflow 3000 mg/L) with the alkalinity of the effluent reaching the maximum value of 1122.4mgCaCO 3 L, then at 800-1000mgCaCO 3 Fluctuation in the range of/L. While the pH value of the effluent of the RH reactor (the COD concentration of the inlet water is 6000 mg/L) is cultivated to 22d, and the pH value reaches to the maximum of 1064.8mgCaCO 3 and/L, after which the value fluctuates.
The change in reactor COD removal rate during the repair process is shown in FIG. 16. The COD removal rate of the reactor is low in the initial stage of the repair culture and is only about 50%. In the repairing process, the COD removal rates of the two groups of reactors are gradually increased along with the repairing experiment. 14d, the removal rate of the RL group COD reaches 91%, and the removal rate of the RH group COD is 85%; and the COD removal rate of the RH group reaches 90.5%, and in the II stage, after the addition of oxygen and nitrate is gradually stopped, the COD removal rate can still be kept stable. And (3) repairing and culturing to a third stage, and lifting to lift the COD concentration of the RL and RH inflow water to reach 3600 mg/L and 3200mg/L respectively, wherein the COD removal rate of the reactor can still be kept above 90%.
In a word, the anaerobic acidification system is repaired by adopting externally added nitrate and aeration in the UASB reactor, and the result shows that the pH value can be quickly recovered to be normal in 14 days; the recovery is carried out under the condition of high COD concentration of the inlet water, and the COD removal rate can reach more than 85-90% within 2 weeks.
It should be noted that the foregoing examples, which are merely illustrative of the technical solutions of the present invention and are intended to enable those skilled in the art to understand the principles of the present invention and to implement the same, are not intended to limit the present invention in any way, and it will be appreciated that equivalent changes or modifications made by employing the spirit of the present invention fall within the scope of the present invention without departing from the spirit and scope of the technical solutions of the embodiments of the present invention.
Claims (6)
1. The method for repairing the acidification system of the anaerobic reactor under the condition of high COD concentration of the inlet water is characterized in that the acidification of the anaerobic reactor is characterized in that: ph=3.5-6.5, proportion of propionate >16% of total VFA, the method comprising the steps of:
s110, controlling the quality of inlet water: the COD concentration of the inlet water of the anaerobic reactor is controlled to be 6000-8000mg/L, and the organic load is higher than 1.5 kg/(m) 3 ·d)；
S120, controlling the addition amount of exogenous oxygen and nitrate: at 33-150 gO 2 Adding O to the System/kgCOD 2 Maintaining micro-oxygen conditions in the system; simultaneously adding exogenous nitrate in the proportion of 20-65:1 of C to N;
s130, metabolic path control based on a system microenvironment in the repairing process: in the repairing culture process, controlling the alkalinity of the anaerobic system to be more than or equal to 600mgCaCO 3 and/L, starting repair culture at 33deg.C, and removing CO by stirring and top air extracorporeal circulation alkali absorption 2 The method comprises the steps of carrying out a first treatment on the surface of the Quantitative qPCR, analyzing reduction of carbon dioxide in anaerobic granular sludge into acetic acid pathway genes acsA and acsB; regulating and controlling the adding proportion of the exogenous oxygen or nitrate in the step S120 to enable the acsA and acsB gene expression to present the highest transcriptional expression activity so as to promote the formation of acetate;
s140, metabolic product characteristics after repair is finished: detecting the concentration and components of the VFA of the effluent of the anaerobic system in the repairing process, and synchronously increasing the concentration of propionic acid and the concentration of acetic acid to serve as one of indexes for indicating that the anaerobic acidification reactor is successfully repaired by the repair of the micro-oxygen and nitrate;
s150, repairing and finishing microbial community characteristics: by analyzing the community structure change in the anaerobic acidification system repaired by the micro-oxygen and the nitrate, the increase of the abundance of the key acetogenic bacteria is used as one of indexes of the ecological community restoration of the system when the anaerobic acidification system is repaired by the cooperation of the exogenous micro-oxygen and the nitrate under the condition of high inflow COD concentration;
s160, gradually reducing nitrate in water to a normal state based on the condition that the pH value is raised to above 6.8, the COD removal rate is more than 80%, the abundance of acetic acid nutrition type methanogen is increased, and taking one of the rising characteristics of the abundance of the acsA and acsB genes in step S140 or step S150 as a sign, and stopping adding oxygen, so that the normal operation of the reactor under the condition of high COD concentration in water is realized under the condition of not depending on exogenous nitrate and oxygen.
2. The method for repairing an anaerobic reactor acidification system under high influent COD concentration conditions according to claim 1, wherein: in the step S120, the concentration of the added exogenous nitrate is 40-100 mg/L.
3. The method for repairing an anaerobic reactor acidification system under high influent COD concentration conditions according to claim 1, wherein: in the steps S140 and S160, the pH value is raised to above 6.8, the COD removal rate is more than 80%, the propionic acid content in the yielding water VFA is lower than 300mg/L, and the methanogen composition recovery characteristic is recovered to the normal level, namely the acidification regulation is completed.
4. The method for repairing an anaerobic reactor acidification system under high influent COD concentration conditions according to claim 1, wherein: in the step S150, the key acetogens include unclassified fAnaerolineaceae and norank f norank o SBR1031.
5. The method for repairing an anaerobic reactor acidification system under high influent COD concentration conditions according to claim 1, wherein: in the step S110, the COD concentration of the inlet water is controlled to be 6000mg/L, the condition of high COD concentration of the inlet water is ensured, in the step S120, the HRT is 3d, and the repair culture is carried out at the temperature of 33 ℃.
6. The method for repairing an acidification system of an anaerobic reactor under high influent COD concentration conditions according to any one of claims 1 to 5, wherein: in the step S160, the pH is greater than 6.8, the COD removal rate is greater than 80%, the abundance of acetic acid nutrition type methanogenic bacteria is increased, the nitrate in the water is gradually reduced to a normal state, and the addition of oxygen is stopped, so that the normal operation of the reactor under the condition of high water inflow COD concentration is realized without depending on exogenous nitrate and oxygen.
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