CN112979061A - CNBB (CNBB) treatment process and equipment for wastewater in process of alcohol extraction of effective ingredients of plants - Google Patents
CNBB (CNBB) treatment process and equipment for wastewater in process of alcohol extraction of effective ingredients of plants Download PDFInfo
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Abstract
The invention relates to the technical field of wastewater treatment, and discloses a CNBB (CNBB) process and equipment for wastewater treatment in the process of alcohol extraction of plant active ingredients. Compared with the prior art, the invention does not use a coagulant for coagulating sedimentation, does not need to continuously add nutrients, saves the cost, reduces the production of sludge, reduces aeration biological filter equipment and shortens the process route; the treatment sequence of the AOPS advanced oxidation process is adjusted, and a screening bioreactor is added in the DSBB device, so that the long-time running stability of the facility is further fully ensured, and the stable effect and standard discharge of the effluent quality are ensured.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a CNBB (CNBB) treatment process and equipment for wastewater treatment in the process of alcohol extraction of plant effective ingredients.
Background
It is a common technical means to extract the components in the plant tissue by using alcohol solvent, and the effective components in the plant are dissolved in the ethanol solution by soaking the plant in alcohol (such as ethanol) with a certain concentration at a certain temperature and time, and then the effective components are separated from the ethanol by various technical means. During the soaking and separating process, a large amount of waste water is produced, and the main components of the waste water are ethanol, plant nutrients, suspended matters formed in the production process, inorganic acids, organic acids, inorganic bases, salts, esters, phenols, hydrocarbons, aromatic hydrocarbons and ketones. The wastewater has the characteristics of unstable water quality, unstable water quantity, high organic matter concentration, high suspended matter concentration and difficult biodegradation.
For the wastewater generated in the process, the prior art generally adopts biochemical means for treatment, for example, chinese patent CN201611135970.8 discloses an ICBB process for wastewater treatment in the extraction process of ginkgo biloba extract, which comprises the steps of coagulation, advanced oxidation, hydrolytic acidification, anaerobic treatment, aerobic treatment and the like as shown in fig. 1, however, the treatment process has the problems of low treatment efficiency, high investment and operation cost and the like.
For the above technical solution, the process has the following technical defects:
(1) in order to prevent the filler or particle electrode of the AOPs advanced oxidation device from being blocked by suspended matters (SS) in inlet water, the concentration of the suspended matters (SS) in the inlet water of the AOPs advanced oxidation device is required to be low, and in order to meet the requirement, the DSIC coagulating sedimentation treatment effect is required to be ideal and stable, in fact, the suspended matters contained in the ginkgo biloba leaf extract ginkgo ketoester wastewater are extremely high, and the dosage of a DSIC coagulant is required to be larger objectively; while producing a large amount of sludge. The electrode plate and the particle electrode of the existing AOPs device are easy to pollute, the existing AOPs device can not indicate the concentration of the instantaneously generated hydroxyl, and therefore the treatment effect of the AOPs device can not be judged at any time and any place.
(2) The method adopts a microbiological method to decompose organic matters in wastewater, adopts an alcohol extraction process to extract effective components of plants, has high total organic carbon content in the wastewater of the extraction process, has inconsistent proportions of carbon (C), nitrogen (N) and phosphorus (P) in the wastewater, does not meet the synthesis requirement of microbial nutrient components, and has the following requirements on the utilization of nutrients of microorganisms, namely C: N: P is 100:5: 1; more nutrients (N, P) must be added to finish the treatment of the total organic carbon, which objectively increases the operating cost.
(3) In the prior art, a large amount of excess sludge (microorganisms) is generated in the treatment process, the sludge amount generated in the whole sewage treatment process is large, and a large amount of secondary pollution is generated.
Disclosure of Invention
The first purpose of the invention is to provide a CNBB (CNBB) process for treating wastewater, which is suitable for green treatment of wastewater generated in the process of extracting effective ingredients of plants by alcohol, so as to overcome the defect that more nutrients (N, P) must be added in the treatment process in the prior art; the use of a large amount of inorganic coagulant; the amount of sludge produced is large; the pollution frequency of the AOPs electrode plate and the electrode particles is increased, so that the device cannot be normally used; the concentration of the hydroxyl group generated instantly can not be indicated, and the like.
According to the technical scheme, the treatment sequence of the advanced oxidation process of the AOPs is adjusted, so that the frequency of pollution of the electrode plates and the third granular particles in the AOPs is reduced, and the burden of coagulation mixing is reduced; the electrode reversing device is arranged in the AOPs device to change the polarity of the electrode plate, so that the precipitate deposited on the electrode plate is dissolved, and the effectiveness of the electrode plate is recovered; in the AOPs apparatus, an electrode potential measuring device is provided for indicating the concentration of instantaneously generated hydroxyl groups.
In order to achieve the purpose, the CNBB technology for treating the wastewater adopted by the invention comprises the following steps:
introducing the wastewater generated by each process into respective tempering and homogenizing treatment units respectively to carry out tempering and homogenizing treatment on the wastewater; and the step of tempering and homogenizing treatment is to collect the wastewater of each process according to the production cycle. The tempering time is a production period, pollutants in the tempering and homogenizing unit are relatively stable, the effluent of the tempering and homogenizing unit enters a mixing and coagulating treatment unit for mixing and coagulating treatment, and wastewater generated by each process is mixed and neutralized in the process;
optionally, the pH of the wastewater may be adjusted by adding an alkaline aqueous solution or an acidic aqueous solution to the wastewater;
optionally, in the step of mixed coagulation treatment, the pH is 7-9, the coagulation stirring time is 10-30 minutes, and the precipitation time is 30-100 minutes;
preferably, the coagulation pH is 8-9, the coagulation stirring time is 15-20 minutes, and the precipitation time is 40-65 minutes.
Optionally, the coagulation pH is 8, 8.2, 8.5, 8.8, or 9;
optionally, the coagulation stirring time is 10 minutes, 15 minutes, 18 minutes, 20 minutes, 22 minutes, or 25 minutes;
alternatively, the precipitation time is 30 minutes, 40 minutes, 50 minutes, 60 minutes, 70 minutes, 80 minutes, 90 minutes, or 100 minutes.
The effluent of the mixed coagulation treatment unit enters a biological bacterium treatment unit, biological bacteria are added into the biological bacterium treatment unit for biochemical treatment, and a microbial inoculum does not need to be added subsequently when the growth of the compound microbial bacteria is good; in an alternative embodiment of the invention, the Biological bacterial treatment is a DSBB Biological bacterial treatment (DSBB stands for dispersed solution Biological Bacteria), i.e. a complex microbial strain with diffusive solubility.
The biological bacteria processing unit is a DSBB biological bacteria processor, the DSBB biological bacteria processor also comprises a screening type biological reactor which is arranged at the front end of the internal processing procedure of the DSBB biological bacteria processor, when sewage enters the DSBB biological bacteria processor, the biological processing with high substrate concentration and high microorganism concentration is firstly carried out at the front end, namely the screening type biological reactor, and the microorganism which is suitable for sewage organisms is screened at the stage, and then the sewage enters the back end biological processing.
Furthermore, the biological bacteria are composite microbial bacteria, the composite microbial bacteria comprise more than two of ammonifying bacteria, nitrifying bacteria, sphaerotheca, achromobacter, flavobacterium, denitrifying bacteria, phosphophilic bacteria and actinomycetes, and the adding amount of the composite microbial bacteria accounts for 0.002-0.013% of the weight of the wastewater.
Optionally, the adding amount of the compound microorganism bacteria accounts for 0.002%, 0.003%, 0.004%, 0.005%, 0.006%, 0.008%, 0.01%, 0.012% or 0.013% of the weight of the wastewater. The effluent of the biological bacteria treatment unit enters an anaerobic treatment unit to carry out anaerobic treatment on organic matters in the sewage;
preferably, in the anaerobic treatment step, an anaerobic reactor at least provided with two anaerobic zones is adopted for anaerobic treatment;
the effluent of the anaerobic treatment unit enters a hydrolysis treatment unit for hydrolysis treatment, and in the hydrolysis treatment process, the concentration of dissolved oxygen is less than 0.5mg/L, and the pH value is 5-8;
optionally, the dissolved oxygen concentration is 0.1, 0.2, 0.3, 0.4 or 0.45mg/L, and the pH is controlled to be 5, 5.5, 6.5, 7, 7.5 or 8.
The effluent of the hydrolysis treatment unit sequentially enters a first aerobic treatment unit, an advanced oxidation treatment unit and a second aerobic treatment unit, and is respectively subjected to primary aerobic treatment, advanced oxidation treatment and secondary aerobic treatment;
further, in the processes of primary aerobic treatment and secondary aerobic treatment, the concentration of dissolved oxygen is controlled to be more than 2 mg/L;
further, in the advanced oxidation treatment process, the advanced oxidation treatment is AOPs advanced oxidation treatment (AOPs stands for advanced oxidation Processes), and oxidation is performed by an electrochemical oxidation method which is a three-dimensional electrode method.
The AOPs advanced oxidation apparatus is an electrochemical reaction apparatus, and oxidation is performed by an electrochemical oxidation method using a three-dimensional electrode method, and a granular third electrode is filled between two main electrodes, and the third electrode is a square or round particle electrode made of a composite material.
Further, an electrode potential measuring device is arranged in the AOPs advanced oxidation device and used for indicating the concentration of the hydroxyl groups generated instantly, if the electrode potential can not meet the requirement, namely the preset value of the electrode potential can not be reached, the polarity of an electrode plate of the AOPs is changed by a pole reversing device arranged in the AOPs advanced oxidation device, so that the precipitate deposited on the electrode plate is dissolved, and the effectiveness of the electrode is recovered. In the process, after the polarity of the AOPs electrode plates is changed, precipitates on the electrode plates are dissolved, the electrode potential is recovered to be larger than or equal to a set value, the effectiveness of the electrodes is recovered, and the electrode reversing device is started again until the electrode potential falls below the set value again, so that the polarity of the AOPs electrode plates is changed again. The adjustment of the sequence of the AOPs device firstly reduces the pollution frequency of AOPs electrode plates and electrode particles, improves the service life and the treatment efficiency, secondly lightens the burden of mixed coagulation, and thirdly improves the B/C ratio of organic matters which are difficult to be biochemically treated after anaerobic treatment, hydrolysis and primary aerobic treatment, thereby ensuring the stable increase of the subsequent water outlet effect.
Further, in the advanced oxidation treatment process, the PH range is controlled to be 6-9;
optionally, in the advanced oxidation treatment process, the PH is controlled to be 6, 6.5, 7, 8, 8.5, or 9.
Furthermore, in the advanced oxidation treatment process, the voltage range of the pole plates is controlled to be 0-50V, and the distance range of the pole plates is controlled to be 100mm-800 mm.
Preferably, in the advanced oxidation treatment process, the voltage range of the pole plates is controlled to be 20-45V, and the distance range of the pole plates is controlled to be 250mm-750 mm.
Optionally, in the advanced oxidation treatment process, the plate voltage is controlled to be 20, 30, 40 or 45 v, and the plate distance is controlled to be 250, 300, 400, 500, 600 or 750 mm.
In the present invention, CNBB means (Cell, nutrient, Biological Bacteria). The invention uses advanced oxidation device, nutrient circulation and biological bacteria treatment to treat the waste water with alcohol extract plant effective components, which has the advantages of reducing equipment investment, saving operation cost, shortening process route, reducing sludge amount, ensuring continuous and stable operation of the whole process route, ensuring water outlet effect and stable water quality, etc.
The effluent of the second aerobic treatment unit is discharged into a sewage outlet pipeline network;
the sludge produced by the mixed coagulation treatment unit enters a sludge acidification unit for sludge acidification treatment;
further, in the sludge acidification treatment process, the pH value range is controlled to be 5.5-7; the temperature is controlled within the range of 10-30 ℃.
Optionally, in the sludge acidification treatment process, the PH value is controlled to be 5.5, 6, 6.5 or 7; the temperature is controlled at 10 deg.C, 15 deg.C, 20 deg.C, 25 deg.C, or 30 deg.C. The method comprises the following steps that sludge generated by a biological bacteria treatment unit, an anaerobic unit, a first aerobic treatment unit and a second aerobic treatment unit enters a sludge autolysis treatment unit, sludge autolysis treatment is carried out under the action of a sludge autolysate, cell walls of microorganisms are damaged, lysosomes are dissolved out, sludge autolysis is carried out, after the sludge autolysis treatment unit is used for treating the sludge, the upper layer effluent enters the biological bacteria treatment unit, the lower layer sludge enters a sludge acidification unit, the effluent of the sludge acidification treatment unit enters the biological bacteria treatment unit, after the sludge autolysis treatment, part of cytoplasm exists in a small molecule soluble state, cell walls, cell membranes and organelles of the microorganisms still exist in a large molecule state, and the substances generated after autolysis treatment are shunted to the sludge acidification treatment unit and the biological bacteria treatment unit. In this section, N, P nutrients in the sludge are fed back into the biological bacteria treatment unit during the sludge autolysis treatment.
Furthermore, in the sludge autolysis treatment process, the cell wall of the microorganism is damaged, the autolysis treatment is carried out under the action of lysosomes, the pH is controlled to be 5-9, and the dissolved oxygen is controlled to be 0.5-8 mg/L.
Optionally, in the sludge autolysis treatment process, the sludge autolysis solvent adopts ClO2And O3。
Optionally, the pH is 5, 5.5, 6, 7, 8, or 9 and the dissolved oxygen is 0.5, 2, 3, 4, 5, 6, 7, 7.5, or 8 mg/L.
In the process, a nitrogen and phosphorus detector is used for monitoring N, P content in a DSBB biological bacteria treatment section, when the content of N or P is too high, supernatant produced by sludge autolysis treatment can be partially or completely discharged into a primary aerobic treatment section through a regulating valve arranged on a pipeline, a subsequent section discharge system is used, particularly, when the content of P is too high, part or all of the supernatant can be discharged out of the system after lower-layer sludge produced by sludge autolysis treatment is subjected to phosphorus treatment, the rest part enters a sludge acidification device, a calcium phosphate precipitation method is used in the phosphorus treatment process to enable P to be discharged out of the system in a calcium phosphate form, the part of sludge (containing N, P) can be directly discharged out of the system, and for the N with too high content, a denitrification discharge system can be also be used in an anoxic pond contained in a DSBB biological bacteria pond.
According to the CNBB process for treating the wastewater, N, P nutrients in the system are refluxed and recycled through sludge autolysis treatment, so that the technical problem that more N, P nutrients need to be added in the prior art is solved. Coagulating sedimentation is carried out without using a coagulant, so that the material cost of the process is saved, the sludge production is reduced, the treatment sequence of the AOPs advanced oxidation process is adjusted, the frequency of pollution of the electrode plate and the particulate third electrode in the AOPs is reduced, and the burden of coagulating and mixing is reduced; the electrode reversing device is arranged in the AOPs device to change the polarity of the electrode plate, so that the precipitate deposited on the electrode plate is dissolved, and the effectiveness of the electrode plate is recovered; an electrode potential measuring device is arranged in the AOPs device and is used for indicating the concentration of the hydroxyl groups generated instantly; after the anaerobic treatment, the hydrolysis treatment and the primary aerobic treatment, the B/C ratio of organic matters which are difficult to be biochemically treated is improved, so that the subsequent secondary aerobic effect is ensured, the stability of the effluent effect is improved, the number of aeration biofilters is reduced, the process route is shortened, a screening type bioreactor is added in a DSBB (double-stranded aerobic bacteria) device, the biological treatment with high substrate concentration and high microorganism concentration is ensured, the facility stability of the whole process route is further ensured, and the stable effect and the standard discharge of the effluent quality are ensured.
The invention also provides sewage treatment equipment, which is applied to the CNBB (CNBB) green treatment process of the wastewater generated in the process of extracting the effective ingredients of the plants by alcohol, and comprises a regulating and homogenizing tank, a mixing and coagulating tank, a biological bacteria treatment tank, an anaerobic reactor, a hydrolysis treatment tank, a first aerobic tank, a high-grade oxidation treatment device and a second aerobic tank which are sequentially communicated, and further comprises a first sludge tank, a second sludge tank, a sludge acidification device and a sludge autolysis device, wherein the mixing and coagulating tank is sequentially communicated with the first sludge tank and the sludge acidification device, the biological bacteria treatment tank is sequentially communicated with the second sludge tank and the sludge autolysis device, the anaerobic reactor, the first aerobic tank and the second aerobic tank are respectively communicated with the second sludge tank, the sludge acidification device is communicated with the biological bacteria treatment tank, and the sludge autolysis device is respectively communicated with the sludge acidification device and the biological bacteria treatment tank, the sludge autolysis device is also communicated with the first aerobic tank, and a regulating valve is arranged on a pipeline of the sludge autolysis device.
Preferably, in one embodiment of the present invention, the anaerobic reactor is provided with at least two anaerobic reaction zones, i.e., a first anaerobic zone and a second anaerobic zone. The biological bacteria treating pond is a DSBB biological bacteria processor, and also comprises a screening type bioreactor and a nitrogen and phosphorus detector.
Further, the advanced oxidation treatment device comprises an electrode potential measuring device and a pole reversing device which are respectively used for indicating that the concentration of the hydroxyl instantaneously generated by the oxidation treatment unit is changed and the polarity of the electrode plate of the oxidation treatment unit is changed.
Further, the sewage treatment equipment also comprises a dephosphorization treatment device which is respectively communicated with the sludge autolysis device and the sludge acidification device.
Compared with the prior art, the CNBB green treatment process for the wastewater generated in the process of extracting the effective ingredients of the plants by alcohol adopts a sludge autolysis technology to realize the cyclic utilization of the nutrients (N, P) in a system, achieves the purpose of not adding the nutrients (N, P) in the wastewater treatment, saves the material cost and reduces the sludge amount generated in the sewage treatment process.
The AOPs advanced oxidation process has higher requirements on the water quality index of inlet water, and in the prior art, the SS value is reduced by adding a DSIC (cationic dye-sensitized IC) coagulant. In the technical scheme of the invention, the AOPs advanced oxidation process treatment sequence is arranged after biological bacteria are subjected to biochemical treatment, anaerobic treatment and primary aerobic treatment, so that the concentration of SS at the inlet of an AOPs advanced oxidation device meets the requirement, thereby achieving the aim of not using a DSIC (solid State organic acid) flocculant, on the other hand, the generation of inorganic sludge in the process of using the flocculant is avoided, and the sludge amount is further reduced. The wastewater after the secondary aerobic treatment can directly meet the treatment target requirement without being treated by a DS terminal.
In the technical scheme, the materialized sludge generated in the mixing process can enter the DSBB biological bacteria treatment device after being subjected to peracid treatment by adopting an organic sludge acidification method.
Compared with the prior art, the CNBB process for sewage treatment shortens the treatment process route, reduces the dosing system, reduces the biological aerated filter and the DS terminal, further reduces the operation cost, and ensures that the system is easy to operate and the effluent is more stable.
Drawings
FIG. 1 is a process flow diagram shown in patent CN 201611135970.8;
FIG. 2 is a flow diagram of a wastewater treatment process according to the present invention;
FIG. 3 shows an anaerobic reactor used in an embodiment of the present invention and patent CN 201611135970.8.
In the figure: 1. an air outlet pipe; 2. a gas-liquid separator; 3. a reactor shell; 4. an effluent weir; 5. a second riser; 6. a second three-phase separator; 7. a second anaerobic zone; 8. a first riser; 9. a first three-phase separator; 10. a water inlet pipe; 11. a water outlet pipe; 12. a return pipe; 13. a first anaerobic zone; 14. a water distributor.
Detailed Description
The technical solution in the embodiment of the present invention will be clearly and completely described below with reference to the table data and the accompanying drawings in the embodiment of the present invention; it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments, and all other embodiments obtained by those skilled in the art without any inventive work are within the scope of the present invention.
Example 1:
in the biochemical treatment process of sewage, proper nutrient element proportion is generally required, namely C: N: P is 100:5: 1. The element ratio of the wastewater generated in the process of extracting the effective ingredients of the plants by alcohol relative to the elements has the following constituent characteristics: it has high total organic carbon content and low nitrogen and phosphorus content. The carbon nitrogen phosphorus ratio in the sewage is unbalanced, and based on the unbalance, the embodiment provides the following wastewater treatment scheme:
as shown in fig. 2, in one aspect, the present invention provides a CNBB process for green treatment of wastewater generated during alcohol extraction of plant effective ingredients, the CNBB process comprising the steps of:
introducing the wastewater into a tempering and homogenizing treatment unit for carrying out tempering and homogenizing treatment on the wastewater;
the effluent of the conditioning and homogenizing treatment unit enters a mixing and coagulating treatment unit for mixing and coagulating treatment, in the process, the wastewater generated by each process is mixed and neutralized, the quality and the quantity of the mixed and neutralized wastewater are more uniform and stable, the wastewater is subjected to mixing, mixing and neutralization, the property of the wastewater is changed, the colloid charge in the wastewater is changed, part of colloid is destabilized to generate precipitate to form sludge I, the sludge is materialized sludge, and the main component of the sludge is plant organic matter;
in the step of mixing and coagulating treatment, the pH is 9, the coagulating and stirring time is 12 minutes, and the precipitation time is 35 minutes;
the effluent of the mixed coagulation treatment unit, namely supernatant precipitated in the mixed coagulation treatment unit enters a DSBB biological bacterium treatment unit (DSBB stands for dispersublents biologicalcalcalia), namely, diffusible and soluble composite microbial bacteria, DSBB biological bacteria are added into the DSBB biological bacterium treatment unit for biochemical treatment, initial nutrients are supplemented, organic matters in the wastewater are degraded through metabolism of the microorganisms under the action of the microorganisms, in the step, the added biological bacteria are composite microbial bacteria and comprise ammonifying bacteria, nitrifying bacteria, sphaerotheca bacteria and denitrifying bacteria, the addition amount of microbial inoculum is 0.06g/l on the first day, 0.04g/l on the third day and 0.02g/l on the fifth day, the growth condition of the microorganisms is good, and the microbial inoculum is not added any more later.
The biological bacteria processing unit is a DSBB biological bacteria processor, the DSBB biological bacteria processor also comprises a screening type biological reactor which is arranged at the front end of the internal processing procedure of the DSBB biological bacteria processor, after sewage enters the DSBB biological bacteria processor, the biological processing with high substrate concentration and high biomass concentration is firstly carried out on the front end, namely the screening type biological reactor, the microorganism which is suitable for the sewage organism is screened at the stage, then the sewage enters the back end biological processing, and in the process, the screening type biological reactor is used as a biological selector, namely a section of area which is arranged at an inlet of an aeration tank and aims to maintain higher substrate concentration and is used for promoting the growth of fast growing bacteria (non-filamentous bacteria) and inhibiting the growth of the slow growing bacteria (filamentous bacteria).
The water treated by the DSBB enters an anaerobic treatment unit, an anaerobic reactor provided with two anaerobic zones is adopted to carry out anaerobic treatment on organic matters in the sewage, the organic matters are subjected to anaerobic decomposition under the condition of no oxygen, the anaerobic reaction efficiency is high, the proportion of N to P is relatively small, the amount of generated sludge is small, and the organic matters are discharged out of a wastewater treatment system in a methane decomposition mode.
The wastewater after the anaerobic treatment reaction enters a hydrolysis treatment unit, namely a hydrolysis tank; during the hydrolysis process, the concentration of dissolved oxygen is controlled to be 0.2mg/L, and the pH value is controlled to be 7.5. A small amount of sludge generated by anaerobic decomposition enters a sludge tank;
the effluent of the hydrolysis treatment unit sequentially enters a first aerobic treatment unit, an AOPs advanced oxidation treatment unit and a second aerobic treatment unit, and is respectively subjected to primary aerobic treatment, advanced oxidation treatment and secondary aerobic treatment. In the processes of primary aerobic treatment and secondary aerobic treatment, the concentration of dissolved oxygen is controlled to be 2mg/L and 4mg/L respectively, after the wastewater enters a combined section of hydrolysis treatment and primary aerobic treatment, on one hand, organic matters are further degraded, and on the other hand, the section can control the content of nitrogen (N) in the effluent by controlling the nitrification and denitrification levels. After primary aerobic treatment, the easily biodegradable organic matters in the wastewater are basically decomposed by microorganisms, and the rest organic matters are organic matters which are difficult to decompose by organisms, and some organic matters which are difficult to decompose by the microorganisms, pigments and the like. The organic matters are subjected to advanced oxidation treatment by AOPs, the matters are subjected to hydroxylation reaction, the biodegradability of the matters is improved after the hydroxylation reaction, and effluent enters subsequent secondary aerobic biochemical treatment. After secondary biochemical treatment, the organic matters are further degraded, the indexes of the organic matters in the effluent are lower, and the effluent realizes the standard discharge of the organic matters;
advanced Oxidation Processes (AOPs) are characterized in that hydroxyl radicals (OH) are generated through reaction, the OH radicals have extremely strong oxidizability, and organic pollutants can be effectively decomposed and even completely converted into harmless inorganic substances such as carbon dioxide, water and the like through the OH radicals.
In this embodiment, the AOPs advanced oxidation apparatus is an electrochemical reaction apparatus, and oxidation is performed by an electrochemical oxidation method using a three-dimensional electrode method, in which a granular third electrode is filled between two main electrodes, and the third electrode is a square or round particle electrode made of a composite material, and under an operating condition, a certain amount of hydroxyl radicals (· OH) having a very strong oxidation performance are generated in the apparatus.
In this embodiment, in the advanced oxidation process, the plate voltage range is controlled to be 20 v, and the plate pitch range is controlled to be 250 mm.
In this embodiment, an electrode potential measuring device is provided in the AOPs advanced oxidation apparatus to indicate the concentration of the hydroxyl groups instantaneously generated, and if the electrode potential is found to be not satisfactory, that is, not satisfactory to a set value, the polarity of the electrode plate of the AOPs is changed by a pole reversing device provided in the AOPs advanced oxidation apparatus to dissolve the precipitate deposited on the electrode plate, thereby recovering the effectiveness of the electrode. In the process, after the polarity of the AOPs electrode plate is changed, precipitates on the electrode plate are dissolved, the electrode potential is recovered to be equal to or above the set value, the effectiveness of the electrode is recovered, and the polarity of the AOPs electrode plate is changed again by starting the electrode reversing device again until the value of the electrode potential falls below the set value again.
The adjustment of the sequence of the AOPs device firstly reduces the pollution frequency of AOPs electrode plates and electrode particles, improves the service life and the treatment efficiency, secondly lightens the burden of mixed coagulation, and thirdly improves the B/C ratio of organic matters which are difficult to be biochemically treated after anaerobic treatment, hydrolysis and primary aerobic treatment, thereby ensuring the stable increase of the subsequent water outlet effect.
The sludge I produced by the mixed coagulation treatment unit enters a sludge acidification unit for sludge acidification treatment, and organic matter macromolecules are decomposed into micromolecules in the process;
controlling the pH value to be 5.5 in the sludge acidification treatment process; the temperature was controlled at 10 ℃.
Sludge I is mainly organic matter colloid particles, and is subjected to a sludge acidification treatment device, so that originally formed large-particle organic sludge is degraded into soluble nutrients such as fat, protein, starch and other macromolecular nutrients, enters a DSBB bacterial treatment unit and becomes DSBB nutrients;
sludge II generated by the biological bacteria treatment unit, the anaerobic unit, the first aerobic treatment unit and the second aerobic treatment unit enters the sludge autolysis treatment unit through a sludge tank for sludge autolysis treatment, and a sludge autolytic agent adopts ClO2And O3In the process, about 40% of organic carbon in a sewage system is converted into biochemical sludge, namely the sludge is subjected to subsequent sludge autolysis treatment in the form of sludge II, partial effluent of the sludge autolysis treatment unit enters a sludge acidification unit, and partial effluent of the sludge autolysis treatment unit and the effluent of the sludge acidification treatment unit enter a biological bacteria treatment unit.
In the sludge autolysis treatment process, the PH is controlled to be 5.5, and the dissolved oxygen is 8 mg/L.
And the effluent after the secondary aerobic treatment of the second aerobic treatment unit is discharged into a sewage outlet pipeline network.
In the wastewater treatment process, the sludge is the residual sludge generated by biochemical reaction, the conventional treatment mode mainly comprises sludge concentration, filter pressing dehydration and sludge drying, and the treatment is complex, the cost is high, the efficiency is low, and the resource utilization is avoided. The sludge is derived from microbial cells, contains proteins, is an organic nutrient, contains nitrogen and phosphorus, is finally decomposed into glycogen and is an indispensable nutrient for biological growth.
The biochemical reaction requires the coordination of the proportion of the nutrient components, and the total requirement is that C, N, P is 100, 5 and 1; the waste water contains abundant organic carbon C, N and P due to the alcohol extraction process, and particularly the content of phosphorus (P) is seriously deficient. In order to decompose the organic carbon C more fully, it is generally necessary to add nutrient N, P to the DSBB biological bacteria treatment system. The technical scheme utilizes the secondary sludge release N, P to realize the recycling of N and P. In this section, N, P nutrients in sludge two are fed back to the biological bacteria treatment unit during the sludge autolysis treatment.
Although N and P are relatively insufficient, especially the phosphorus (P) content is seriously insufficient, N, P is accumulated continuously with the continuous operation of the system, and in the embodiment, a nitrogen and phosphorus detector is used for monitoring the N, P content in the DSBB biological bacteria treatment section, when the N or P content is too high, the supernatant produced by the sludge autolysis treatment can be partially or completely discharged into a primary aerobic treatment section by arranging an adjusting valve on a pipeline, and then a discharge system of a subsequent section, particularly, when the P content is too high, part or all of the lower layer sludge generated by the sludge autolysis treatment can be discharged out of the system after the lower layer sludge is treated by phosphorus, the rest part enters a sludge acidification device, P is discharged out of the system in the form of calcium phosphate by using a calcium phosphate precipitation method in the phosphorus treatment process, the part of sludge (containing N, P) can also be directly discharged out of the system, for the N with too high content, a denitrification and denitrification discharge system can also be carried out in an anoxic pond contained in the DSBB biological bacteria pond.
In the embodiment, the invention provides equipment used in the CNBB process for wastewater treatment, which comprises a regulating and homogenizing tank, a mixing and coagulating tank, a biological bacteria treatment tank, an anaerobic reactor, a hydrolysis treatment tank, a first aerobic tank, a high-level oxidation treatment device, a second aerobic tank, a first sludge tank, a second sludge tank, a sludge acidification device and a sludge autolysis device, wherein the regulating and homogenizing tank, the mixing and coagulating tank, the anaerobic reactor, the hydrolysis treatment tank, the first aerobic tank, the high-level oxidation treatment device and the second aerobic tank are sequentially communicated, the mixing and coagulating tank is sequentially communicated with the first sludge tank and the sludge acidification device, the biological bacteria treatment tank is sequentially communicated with the second sludge tank and the sludge autolysis device, the anaerobic reactor, the first aerobic tank and the second aerobic tank are respectively communicated with the second sludge tank, the sludge acidification device is communicated with the biological bacteria treatment tank, the sludge autolysis device is also communicated with the first aerobic tank, the pipeline is provided with a regulating valve, and the anaerobic reactor is provided with a first anaerobic zone and a second anaerobic zone.
In this embodiment, the first sludge impoundment is used for holding mud one, and the second sludge impoundment is used for holding mud two.
In this embodiment, the advanced oxidation treatment apparatus includes an electrode potential measuring device and a polarity inverting device, which are respectively used to instruct to change the concentration of the hydroxyl radicals instantaneously generated by the oxidation treatment unit and to change the polarity of the electrode plate of the oxidation treatment unit.
In this embodiment, the above sewage treatment equipment further includes a dephosphorization device, and is respectively communicated with the sludge autolysis device and the sludge acidification device.
In this embodiment, the DSBB biological bacteria processor further comprises a screening bioreactor and a nitrogen-phosphorus detector.
In this embodiment, in order to facilitate the control regulation, still include industrial singlechip, its signal connection nitrogen phosphorus detector, electrode potential measuring device, fall utmost point device, governing valve etc..
In this embodiment, the anaerobic unit used in the sewage treatment process is the same anaerobic reactor as that used in CN201611135970.8, as shown in fig. 3, the anaerobic reactor includes a reactor shell 3, a water inlet pipe 10 and a water distributor 14 communicated with the water inlet pipe 10 are arranged at the bottom of the reactor shell 3, a gas-liquid separator 2 and an air outlet pipe 1 communicated with the gas-liquid separator 2 are arranged at the top of the reactor shell, a first three-phase separator 9, a second three-phase separator 6 and a water outlet weir 4 are sequentially arranged in the reactor shell 3 from bottom to top, the bottom of the gas-liquid separator 2 is communicated with the second three-phase separator 6 through a second riser 5, a first riser 8 communicated with the bottom of the first three-phase separator 9 is arranged in the second riser 5, a return pipe 12 is arranged in the first riser 8, and the first three-phase separator 9 is arranged in a first anaerobic zone 13, a second three-phase separator 6 is arranged in the second anaerobic zone 7.
The wastewater treated by the biological bacteria enters the reactor shell 3 through the water inlet pipe 10, and then the water distributor 14 distributes the inlet water in the mixing area in the reactor shell 3 to be mixed with the internal circulation muddy water mixed liquid from the return pipe 12, so as to dilute and homogenize the inlet water. Under the common push of inlet water and circulating water, the mixed wastewater and granular sludge enter a first anaerobic zone 13 (also called a granular sludge expanded bed zone) for biochemical degradation, the treatment zone has high volume load, and in addition, the reactor has larger ascending flow velocity due to larger height-diameter ratio, so that the granular sludge bed is in a fluidized state, at the moment, solid-liquid contact is sufficient, most organic matters in the wastewater are subjected to anaerobic digestion to generate biogas, and the generated biogas is collected by a first three-phase separator 9 and then ascends to a gas-liquid separator 2 along a first lifting pipe 8. Meanwhile, in the process of forming the methane bubbles, the liquid is expanded to generate the gas stripping effect, so that the volume of the muddy water mixed liquid at the position is increased, the density of the muddy water mixed liquid is reduced, and the mixed liquid rises into the gas-liquid separator 2 along the first lifting pipe 8 along with the methane under the effects of density difference and methane lifting. In the gas-liquid separator 2, gas-liquid separation occurs due to the density difference, and biogas is discharged from the biogas outlet pipe 1. At the moment, the density of the mud-water mixed liquid is increased, the mud-water mixed liquid flows back to the mixing area through the return pipe 12 under the action of density difference and gravity, and then the mud-water mixed liquid is fully mixed with the granular sludge and the inlet water at the bottom again and then continuously rises to realize an internal circulation. A small part of organic matters which are not anaerobically digested in the first anaerobic zone 13 automatically enter the second anaerobic reaction zone to continue anaerobic digestion and generate biogas, and the biogas is collected by the second three-phase separator 6 and then ascends to the gas-liquid separator 2 along the second riser pipe 5. In the gas-liquid separator 2, this portion of biogas is separated from the mixed liquor that also reaches the gas-liquid separator 2 along the second riser 5, and is also discharged from the biogas outlet conduit 1. The mixed liquor is also returned to the mixing zone through the return pipe 12, and continuously rises after being fully mixed with the granular sludge and the inlet water at the bottom, and enters the next internal circulation. The supernatant of the wastewater treated by the first anaerobic zone 13 and the second anaerobic zone 7 enters the effluent weir 4 and then flows out through the water outlet pipe 11.
In the embodiment, the anaerobic reactor can effectively improve the circulating strength and the treatment effect, so that the anaerobic reaction is more thorough, the quality and the efficiency of wastewater treatment are further improved, and reliable support is provided for the treated wastewater to reach the standard and be discharged; meanwhile, the reactor adopts a multi-layer sleeve form, the first lifting pipe 8, the second lifting pipe 5 and the return pipe 12 are coaxially arranged in the center of the reactor, the structure is simple, the occupied space is small, the three-phase separator can be effectively prevented from scaling, the service life is prolonged, and the maintenance is more convenient.
Example 2:
in this example, the difference from example 1 is:
in the step of mixed coagulation treatment, the pH value is 8, the coagulation stirring time is 25 minutes, and the precipitation time is 100 minutes;
the added biological bacteria are compound microbial bacteria, including ammonifying bacteria, nitrifying bacteria, phosphophilic bacteria, actinomycetes and denitrifying bacteria, the adding amount of the microbial inoculum is 0.04g/l on the first day and 0.04g/l on the third day, the growth of the microorganisms is found to be good, and the microbial inoculum is not added any more;
in the hydrolysis process, the concentration of dissolved oxygen is controlled to be 0.2mg/L, and the pH value is controlled to be 8.
In the processes of primary aerobic treatment and secondary aerobic treatment, the concentration of dissolved oxygen is controlled to be 3 mg/L;
controlling the pH value to be 7 in the sludge acidification treatment process; the temperature was controlled at 30 ℃.
Controlling the pH value to be 9 in the sludge autolysis treatment process; 2. dissolved oxygen 0.5 mg/L.
In the advanced oxidation treatment process, the voltage range of the pole plates is controlled to be 50V, and the distance range of the pole plates is controlled to be 800 mm.
The rest is the same as in example 1.
Example 3:
in this example, the difference from example 1 is:
in the step of mixed coagulation treatment, the pH value is 7.5, the coagulation stirring time is 18 minutes, and the precipitation time is 60 minutes;
the added biological bacteria are compound microbial bacteria, including ammonifying bacteria, nitrifying bacteria, phosphophilic bacteria, actinomycetes and denitrifying bacteria, the adding amount of the microbial inoculum is 0.02g/l in the first day, 0.01g/l in the third day and 0.01g/l in the fifth day, the growth of the microorganisms is found to be good, and the microbial inoculum is not added any more;
during the hydrolysis process, the dissolved oxygen concentration is controlled to be 0.45mg/L, and the pH value is controlled to be 5.
In the processes of primary aerobic treatment and secondary aerobic treatment, the concentration of dissolved oxygen is controlled to be 3mg/L and 5mg/L respectively;
controlling the pH value to be 6 in the sludge acidification treatment process; the temperature was controlled at 25 ℃.
In the sludge autolysis treatment process, the PH is controlled to be 6, and the dissolved oxygen is controlled to be 5 mg/L.
In the advanced oxidation treatment process, the voltage range of the polar plates is controlled to be 40V, and the distance range of the polar plates is controlled to be 500 mm.
The rest is the same as in example 1.
In examples 1 to 3, the main water quality index of the treated wastewater after the secondary aerobic treatment was as follows:
as can be seen from the above table, the technical scheme of the embodiment of the invention has good treatment effect on the wastewater generated in the process of extracting the effective substances by alcohol, and meets the actual requirement.
The invention recycles N, P nutrient in the system by refluxing and recycling sludge autolysis treatment, solves the technical problem that more N, P nutrient must be added in the prior art, saves the material cost of the process and reduces the sludge output.
The foregoing is only a preferred embodiment of the present invention; the scope of the invention is not limited thereto. Any person skilled in the art should be able to cover the technical scope of the present invention by equivalent or modified solutions and modifications within the technical scope of the present invention.
Claims (12)
1. The CNBB treatment process for wastewater in the process of alcohol extraction of effective ingredients of plants is characterized by comprising the following treatment steps:
introducing the wastewater into a tempering and homogenizing treatment unit for carrying out tempering and homogenizing treatment on the wastewater;
the effluent of the conditioning and homogenizing unit enters a mixing and coagulating unit, and wastewater generated by each process is mixed and neutralized in the process;
the effluent of the mixed coagulation treatment unit enters a biological bacterium treatment unit, and biological bacteria are added into the biological bacterium treatment unit for biochemical treatment;
the effluent of the biological bacteria treatment unit enters an anaerobic treatment unit to carry out anaerobic treatment on organic matters in the sewage;
the effluent of the anaerobic treatment unit enters a hydrolysis treatment unit for hydrolysis treatment;
the effluent of the hydrolysis treatment unit sequentially enters a first aerobic treatment unit, an advanced oxidation treatment unit and a second aerobic treatment unit, and is respectively subjected to primary aerobic treatment, advanced oxidation treatment and secondary aerobic treatment;
the effluent of the second aerobic treatment unit is discharged into a sewage outlet pipeline network;
the sludge produced by the mixed coagulation treatment unit enters a sludge acidification unit for sludge acidification treatment;
sludge generated by the biological bacteria treatment unit, the anaerobic unit, the first aerobic treatment unit and the second aerobic treatment unit enters the sludge autolysis treatment unit for sludge autolysis treatment, after the sludge autolysis treatment unit treats the sludge, the upper layer effluent enters the biological bacteria treatment unit, the lower layer sludge enters the sludge acidification unit, and the effluent of the sludge acidification treatment unit enters the biological bacteria treatment unit;
monitoring the nitrogen and phosphorus contents of the biological bacteria treatment unit, and when the contents of the nitrogen and phosphorus contents are too high, adjusting part or all of the upper layer effluent treated by the sludge autolysis treatment unit to enter a first aerobic treatment unit, or discharging part or all of the lower layer sludge treated by the sludge autolysis treatment unit out of the system, or discharging part or all of the part of sludge after dephosphorization out of the system, and feeding the rest of sludge into a sludge acidification device.
2. The CNBB process for treating wastewater during the process of extracting effective components from plants by alcohol according to claim 1, wherein: in the mixing and coagulating unit, wastewater is uniformly mixed according to the production period of each process section, and is mixed according to the water quantity, and the PH value is controlled to be 7-9.
3. The CNBB process for treating wastewater during the process of extracting effective components from plants by alcohol according to claim 1, wherein: the biological bacteria are composite microbial bacteria, the composite microbial bacteria comprise more than two of ammonifying bacteria, nitrifying bacteria, sphaerotheca, achromobacter, flavobacterium, denitrifying bacteria, phosphotropic bacteria and actinomycetes, and the adding amount of the composite microbial bacteria accounts for 0.002-0.013% of the weight of the wastewater.
4. The CNBB process for treating wastewater during the process of extracting effective components from plants by alcohol according to claim 1, wherein: in the anaerobic treatment step, an anaerobic reactor at least provided with two anaerobic zones is adopted for anaerobic treatment.
5. The CNBB process for treating wastewater during the process of extracting effective components from plants by alcohol according to claim 1, wherein: in the sludge acidification treatment process, the pH value is controlled to be 5.5-10; the temperature is controlled within the range of 10-50 ℃.
6. The CNBB process for treating wastewater during the process of extracting effective components from plants by alcohol according to claim 1, wherein: controlling the pH value of 5-9 in the sludge autolysis treatment process; 0.5-8mg/L of dissolved oxygen.
7. The CNBB process for treating wastewater during the process of extracting effective components from plants by alcohol according to claim 1, wherein: in the advanced oxidation treatment process, an electrochemical oxidation method of a three-dimensional electrode method is adopted for oxidation.
8. The CNBB process for treating wastewater during the process of extracting effective components from plants by alcohol according to claim 7, wherein: in the advanced oxidation treatment process, the electrode potential of the advanced oxidation treatment unit is measured to indicate the concentration of the hydroxyl instantaneously generated by the advanced oxidation device, when the electrode potential cannot reach a set value, the polarity of an electrode plate of the oxidation treatment unit is changed to dissolve precipitates deposited on the electrode plate, the electrode potential is restored to be greater than or equal to the set value, the effectiveness of the electrode is restored, and the polarity of the electrode plate is changed again until the electrode potential falls below the set value again.
9. The CNBB process for treating wastewater during the process of extracting effective components from plants by alcohol according to claim 7, wherein: in the advanced oxidation treatment process, the voltage range of the pole plates is controlled to be 0-50V, and the distance range of the pole plates is controlled to be 100mm-800 mm.
10. An apparatus for treating CNBB process using the waste water from alcohol extraction of plant effective ingredients according to any one of claims 1 to 9, characterized in that: comprises an adjusting homogenizing tank, a mixing coagulation tank, a biological bacteria treatment tank, an anaerobic reactor, a hydrolysis treatment tank, a first aerobic tank, an advanced oxidation treatment device and a second aerobic tank which are sequentially communicated, and further comprises a first sludge tank, a second sludge tank, a sludge acidification device and a sludge autolysis device, wherein the mixing coagulation tank is sequentially communicated with the first sludge tank and the sludge acidification device, the biological bacteria treatment tank is sequentially communicated with the second sludge tank and the sludge autolysis device, the anaerobic reactor, the first aerobic tank and the second aerobic tank are respectively communicated with the second sludge tank, the sludge acidification device is communicated with the biological bacteria treatment tank, the sludge autolysis device is respectively communicated with the sludge acidification device and the biological bacteria treatment tank, the sludge autolysis device is also communicated with the first aerobic tank, a regulating valve is arranged on a pipeline of the sludge autolysis device, the biological bacteria treatment tank comprises a screening type bioreactor and a nitrogen-phosphorus detector, the advanced oxidation treatment device comprises an electrode potential measuring device and a pole-reversing device which are respectively used for indicating and changing the concentration of the hydroxyl instantaneously generated by the oxidation treatment unit and the polarity of the electrode plate of the oxidation treatment unit.
11. The apparatus of claim 10, wherein: the anaerobic reactor is provided with at least two anaerobic reaction zones.
12. The apparatus of claim 10, wherein: the device also comprises a dephosphorization treatment device which is respectively communicated with the sludge autolysis device and the sludge acidification device.
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