CN211871715U - Fermentation production wastewater treatment system - Google Patents
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Abstract
The utility model discloses a treatment system for fermentation production wastewater, which comprises a flocculation device, a solid-liquid separation device and a membrane separation device; the fermentation production wastewater is communicated with a liquid inlet of the solid-liquid separation device through a flocculation device; the clear phase liquid outlet of the solid-liquid separation device is communicated with the liquid inlet of the membrane separation device. The system reasonably performs grading treatment on the fermentation production wastewater, and is suitable for treating large-batch wastewater in real time.
Description
Technical Field
The utility model particularly relates to a processing system of fermentation waste water belongs to the sewage treatment field.
Background
At present, the wastewater treatment process mainly removes salt and thallus residues in wastewater by multi-effect evaporation, the distilled wastewater is subjected to biochemical treatment, the original treatment of the evaporated residues is landfill, but the evaporated residues cannot be treated along with the emergence of an increasingly strict environmental protection method, so that the development of a new wastewater treatment process is particularly important.
CN202881044U discloses a vitamin B2 production wastewater treatment system, which comprises a water distribution adjusting tank, an HAF anaerobic reaction tank, an FSBBR flow biological reaction tank, an ozone oxidation tank, a TBF secondary biochemical treatment tank, a sedimentation tank and a water outlet, wherein the system mainly adopts a biochemical method to treat wastewater to reach the standard and discharge, but does not recover vitamin B2 in the wastewater.
CN 109081478A relates to a processing apparatus of zymotic fluid waste water, includes: the neutralizing tank is used for carrying out a neutralization reaction on the fermented acidic wastewater; the NaOH adding tank is connected with the neutralizing tank and is used for adding NaOH into the neutralizing tank; the electrodialyzer is connected with the neutralization tank and is used for performing electrodialytic desalination on the wastewater after the neutralization reaction; a divalent salt adding tank connected to the dilute liquid side of the electrodialyzer and used for adding divalent salt into the desalted wastewater; the first flocculation tank is connected to the dilute liquid side of the electrodialyzer and is used for flocculating the electrodialyzer dilute liquid; the first solid-liquid separation device is connected with the first flocculation tank and is used for performing solid-liquid separation treatment on the feed liquid subjected to flocculation treatment in the first flocculation tank; the second flocculation tank is connected with the first solid-liquid separation device and is used for flocculating the clear liquid obtained by the first solid-liquid separation device; the second solid-liquid separation device is connected with the second flocculation tank and is used for performing solid-liquid separation treatment on the feed liquid subjected to flocculation treatment in the second flocculation tank; the first dryer is connected with the first solid-liquid separation device and/or the second solid-liquid separation device and is used for drying the solid obtained by solid-liquid separation; the nanofiltration membrane is connected to the second solid-liquid separation device and is used for concentrating and filtering the clear liquid obtained by the second solid-liquid separation device; the first adsorption tower is connected to the concentrated solution side of the nanofiltration membrane, is filled with a first adsorbent and is used for carrying out first adsorption treatment on the nanofiltration concentrated solution; the second adsorption tower is connected with the water producing port of the first adsorption tower, is filled with a second adsorbent and is used for carrying out second adsorption treatment on the produced water of the first adsorption tower; the second dryer is connected with the water production port of the second adsorption tower and is used for drying the filtrate obtained in the second adsorption tower; further comprising: and the biochemical treatment system is connected with the nanofiltration membrane and is used for performing biochemical treatment on the clear liquid obtained by the nanofiltration membrane. However, the above system has the following disadvantages: firstly, because the prior art mainly adopts a multi-effect concentration process to treat vitamin B2 fermentation production wastewater, high-salinity concentrated slurry can be generated, the wastewater is firstly neutralized and then subjected to electrodialysis desalination in the technology, but when the wastewater is measured by tons every day in actual production, electrodialysis on ton-level wastewater is not well realized, so that the system is not well applied; secondly, the vitamin B2 fermentation wastewater is acidic, wherein the first flocculation treatment is also carried out under the pH condition of 3-6, but in the technology, after the neutralization and the electrodialysis are carried out firstly, the subsequent first flocculation treatment needs to be carried out and needs to add a large amount of acid to reduce the pH, so that the advantage condition that the vitamin B2 fermentation wastewater is acidic cannot be utilized firstly, and the process complexity and the resource waste are also caused; thirdly, the nanofiltration membrane filtrate needs to be subjected to two-stage adsorption towers, and the process system is complex.
SUMMERY OF THE UTILITY MODEL
The utility model discloses the technical problem that will solve is: aiming at the defects of the prior art, the treatment system for the fermentation production wastewater is provided. The system can treat mass production wastewater in real time.
The utility model discloses a solve the technical scheme that the problem that the aforesaid provided adopted and be:
a treatment system for fermentation production wastewater comprises a flocculation device, a solid-liquid separation device and a membrane separation device; the fermentation production wastewater is communicated with a liquid inlet of the solid-liquid separation device through a flocculation device; the clear phase liquid outlet of the solid-liquid separation device is communicated with the liquid inlet of the membrane separation device.
According to the scheme, the device also comprises a biochemical treatment device, and a clear phase liquid outlet of the membrane separation device is communicated with a liquid inlet of the biochemical treatment device.
According to the scheme, the device also comprises an ion air flotation machine, wherein a clear phase liquid outlet of the solid-liquid separation device is communicated with a liquid inlet of the ion air flotation machine, and a clear phase liquid outlet of the ion air flotation machine is communicated with a liquid inlet of the membrane separation device.
According to the scheme, the device further comprises a first drying device, and the solid phase outlet of the solid-liquid separation device and the solid phase outlet of the ion air flotation machine are connected with the first drying device.
According to the scheme, the flocculation device and the solid-liquid separation device are two-stage, a storage tank of the fermentation production wastewater is communicated with a liquid inlet of the first-stage solid-liquid separation device through the first-stage flocculation device, and a clear phase liquid outlet of the first-stage solid-liquid separation device is communicated with a liquid inlet of the second-stage solid-liquid separation device through the second-stage flocculation device; the clear phase liquid outlet of the second stage solid-liquid separation device is communicated with the liquid inlet of the membrane separation device.
According to the scheme, the first flocculation device comprises a first mixing device and a first buffer tank which are sequentially connected, wherein the iron salt tank and the PAM storage tank are respectively communicated with the first mixing device, and the first mixing device is connected with a storage tank for fermentation production wastewater; the second flocculation device comprises a second mixing device and a second buffer tank which are sequentially connected, the iron salt tank, the lye tank and the PAM storage tank are communicated with the second mixing device, the second buffer tank is connected with the first solid-liquid separation device, and an outlet of the first buffer tank is connected with the second mixing device.
According to the scheme, the second-stage flocculation device is divided into two sections, a buffer tank is arranged between the two sections of flocculation devices, a clear phase liquid outlet of the first-stage solid-liquid separation device is communicated with a liquid inlet of the first-stage flocculation device, a liquid outlet of the first-stage flocculation device is communicated with the buffer tank, the buffer tank is communicated with a liquid inlet of the second-stage flocculation device, and a liquid outlet of the second-stage flocculation device is communicated with a liquid inlet of the second-stage solid-liquid separation device.
According to the scheme, the device further comprises a third mixing device positioned between the second buffer tank and the second solid-liquid separation device, and the iron salt tank, the lye tank and the PAM storage tank are communicated with the third mixing device.
According to the scheme, the first mixing device, the second mixing device, the third mixing device and the pH pre-adjusting device all adopt a plurality of pipeline mixers; the first mixing device adopts two pipeline mixers, and the iron salt tank and the PAM storage tank are respectively connected with the two pipeline mixers; the second mixing device adopts four pipeline mixers which are sequentially connected with an alkali liquor storage tank, an iron salt tank, an alkali liquor tank and a PAM storage tank; the third mixing device adopts a pipeline mixer and is connected with the acid tank; the pH pre-adjusting device is a pipeline mixer, and the hydrochloric acid storage tank is connected with the pipeline mixer.
According to the scheme, the membrane separation device comprises a pH pre-adjusting device and a nanofiltration membrane machine, and a clear phase liquid outlet of the solid-liquid separation device is connected with the pH pre-adjusting device; the clear liquid outlet of the nanofiltration membrane machine is connected with the biochemical treatment device, the concentrated liquid outlet of the nanofiltration membrane machine is connected with the inlet of the centrifugal separation device, the clear liquid outlet of the centrifugal separation device is connected with the biochemical treatment device, and the solid phase outlet of the centrifugal separation device is connected with the second drying device.
According to the scheme, the biochemical treatment device comprises an anaerobic activation tank, an anaerobic ammonia oxidation tank, an aerobic tank and a sedimentation tank which are connected in sequence, a clear liquid outlet of the nanofiltration membrane machine is connected with the anaerobic activation tank, and a clear liquid outlet of the centrifugal separation device is connected with the aerobic tank.
According to the scheme, the outlet of the first drying device is sequentially connected with a first dust remover, a protein feed collecting device and a tail gas absorbing device; the outlet of the second drying device is sequentially connected with a second dust remover, a vitamin B2 crude product collector and a tail gas absorption device.
According to the scheme, the centrifugal separation device adopts a disc type centrifugal machine.
According to the scheme, the outlet ends of the second drying device and the first drying device are connected with the same tail gas absorption device. The tail gas absorption device comprises a hydrocyclone separator, an ammonia removal tower, an H2 removal 2s tower and a plasma purifier which are sequentially connected.
According to the scheme, the first solid-liquid separation device and the second solid-liquid separation device both adopt horizontal spiral centrifuges; the first drying device and the second drying device both adopt cyclone flash dryers.
According to the scheme, the storage tank is used for storing the vitamin B2 fermentation production wastewater; and the iron salt tank and the PAM storage tank are respectively used for storing the iron salt solution and the PAM solution.
Compared with the prior art, the beneficial effects of the utility model are that:
firstly, for the processing system of the fermentation waste water that CN 109081478A relates to, the utility model discloses abandoned the thought that reduces NaCl concentration in the waste water so that the nano-filtration membrane withholds vitamin B2 through the electrodialysis, but in order to part protein bacteria mud product and vitamin B2 product, directly flocculate, keep the concentration of NaCl in the waste water, do benefit to and guarantee vitamin B2 higher solubility in clear phase before the nano-filtration membrane filters, follow-up again combines centrifugal separation to retrieve vitamin B2 crude through the nano-filtration membrane; and simultaneously ensures that the effluent meets the environmental protection requirement. Therefore, on one hand, the method is beneficial to rapid and large-batch treatment of wastewater in actual production, on the other hand, the concentrated phase generated in membrane separation can be dried and used as low-content VB2, and the problem of high-salinity concentrated slurry which is difficult to treat does not exist in the whole system process; and the steps of adsorption, impurity removal and the like are not needed, so that the method is simple and easy to implement.
Secondly, in the flocculation process, the utility model firstly carries out acid flocculation and then alkaline flocculation, thus fully utilizing the acidity of the vitamin B2 fermentation wastewater and reducing the cost; in addition, an ion air flotation device can be added before the flocculated clear phase enters the nanofiltration membrane, the service life of the nanofiltration membrane is ensured, and the yield of the protein bacterial sludge is further improved.
Thirdly, a large amount of organic matters and SO in the vitamin B2 wastewater4 2-The interception is obtained at the flocculation centrifugation and membrane separation stages, and the clear liquid effluent index after the nanofiltration membrane treatment can reach COD<10000mg/L, B/C value can reach 0.75, COD is obtained after subsequent anaerobic biochemical treatment<700 mg/L; after the anaerobic ammonia oxidation process, the COD of the effluent is less than or equal to 150mg/L, the ammonia nitrogen is less than or equal to 100mg/L, and the total nitrogen is less than or equal to 150 mg/L; after the aerobic biochemical process, the COD of the final effluent can be ensured to be less than or equal to 70mg/L, the ammonia nitrogen is ensured to be less than or equal to 5mg/L, and the total nitrogen is ensured to be less than or equal to 20 mg/L.
Therefore, process systems can realize online real-time rapid processing big batch vitamin B2 waste water at the waste water treatment in-process, has not only extracted mycoprotein feed and partially remain VB2, and all tail gases and waste water discharge after the centralized processing in addition, can guarantee to reach emission standard.
Drawings
Fig. 1 is a schematic view of a treatment system according to the present invention.
Wherein, 1-a storage tank, 2-a first pipeline mixer, 3-a first buffer tank, 4-a first horizontal spiral centrifuge, 5-an iron salt tank, 6-a PAM storage tank, 7-an albumen bacteria mud tank, 8-a second pipeline mixer, 9-a second buffer tank, 10-a third pipeline mixer, 11-a second horizontal spiral centrifuge, 12-a first alkali liquor tank, 13-a second alkali liquor tank, 14-an ion air flotation machine, 15-a fourth pipeline mixer, 16-a nano membrane filtering machine, 17-a hydrochloric acid storage tank, 18-a disk centrifuge, 19-an anaerobic activation tank, 20-an anaerobic ammonia oxidation tank, 21-an aerobic tank, 22-a sedimentation tank, 23-a first cyclone flash dryer, 24-a first cyclone dust collector and 25-a first cloth dust collector, 26-vitamin B2 crude product collector, 27-second cyclone flash evaporation dryer, 28-second cyclone dust collector, 29-second cloth dust collector, 30-protein feed collector, 31-atomization condenser, 32-hydrocyclone, 33-ammonia removal tower and 34-H removal tower2The system comprises an S tower, a 35-dilute sulfuric acid pump, a 36-dilute lye pump, a 37-plasma purifier, a 38-induced draft fan, a 39-chimney and a 40-gas hot-blast stove.
FIG. 2 is a main process flow diagram of the treatment system according to the present invention.
Detailed Description
For a better understanding of the present invention, the contents of the present invention will be further illustrated below with reference to examples, but the present invention is not limited to only the following examples.
The VB2 fermentation wastewater adopted in the following examples mainly comprises four parts, namely double cone water, plate frame water, equipment washing water, domestic water, demineralized water or clear water in the VB2 production process of certain pharmaceutical industry fermentation, and the specific water quality is shown in Table 1. The above waste water was mixed to have a pH of about 5.6.
In the following examples, the ferric chloride solution had a ferric chloride concentration of 10% and a pH of 1.2 to 1.5.
Example 1
A treatment system for vitamin B2 fermentation production wastewater comprises a first flocculation device, a first horizontal spiral centrifuge, a second flocculation device, a second horizontal spiral centrifuge, an ion air floatation machine, a membrane separation device and a biochemical treatment device, wherein,
the first flocculation device comprises two pipeline mixers 2 and a first buffer tank 3 which are connected in sequence; the storage tank 1 is connected with an inlet of a first buffer tank 3 through two pipeline mixers 2 which are connected in sequence, and an outlet of the first buffer tank 3 is connected with a first horizontal spiral centrifuge 4; the iron salt tank 5 and the PAM storage tank 6 are respectively communicated with the two pipeline mixers 2 and are respectively used for introducing an iron salt solution and a PAM solution; the solid phase outlet of the first horizontal spiral centrifuge 4 is connected with the protein bacterial sludge pool 7;
the second flocculation device comprises four pipeline mixers 8, a second buffer tank 9 and four pipeline mixers 10 which are connected in sequence; a liquid phase outlet of the first horizontal spiral centrifuge 4 is connected with an inlet of a second buffer tank 9 through four pipeline mixers 8 which are connected in sequence, and an outlet of the second buffer tank 9 is connected with a second horizontal spiral centrifuge 11 through four pipeline mixers 10 which are connected in sequence; the lye tank 12, the iron salt tank 5, the lye tank 13 and the PAM storage tank 6 are respectively communicated with one of the two groups of four pipeline mixers 8 and 10 and used for introducing an iron salt solution and a PAM solution and controlling the mixed pH; the solid phase outlet of the second horizontal spiral centrifugal machine 11 is connected with the protein bacterial sludge pool 7; the liquid phase outlet of the second horizontal spiral centrifugal machine 11 is connected with the inlet of the ion air flotation machine 14;
a liquid phase outlet of the ion air flotation machine 14 is connected with the membrane separation device, and a solid phase outlet of the ion air flotation machine 14 is connected with the protein bacterial sludge tank 7;
the membrane separation device comprises a pipeline mixer 15 and a nanofiltration membrane machine 16 which are connected in sequence, wherein a liquid phase outlet of the ion air flotation machine 14 is connected with the pipeline mixer 15, and the pipeline mixer 15 is communicated with a hydrochloric acid storage tank 17 and is used for controlling the pH value of wastewater entering the nanofiltration membrane machine 16; a clear liquid outlet of the nanofiltration membrane machine 16 is connected with a biochemical treatment device; a concentrated solution outlet of the nanofiltration membrane machine 16 is connected with a disk centrifuge 18;
the biochemical treatment device comprises an anaerobic activation tank 19, an anaerobic ammonia oxidation tank 20 and an aerobic tank 21 in sequence, wherein the aerobic tank 21 is communicated with the outside through a sedimentation tank 22; a clear liquid outlet of the nanofiltration membrane machine 16 is connected with an anaerobic activation tank 19; the clear liquid outlet of the disk centrifuge 18 is connected with the aerobic tank 21.
The solid phase outlet of the disc centrifuge 18 is connected with a crude vitamin B2 product collector 26 sequentially through a cyclone flash dryer 23, a cyclone dust collector 24 and/or a cloth dust collector 25. The protein bacterium mud pool 7 is connected with a protein feed collector 30 through a cyclone flash dryer 27, a cyclone dust collector 28 and/or a cloth dust collector 29 in sequence. In addition, the outlets of the dust collectors are connected with a tail gas absorption device, wherein the tail gas absorption device comprises an atomization condenser 31, a hydrocyclone 32, an ammonia removal tower 33 and an H removal tower which are sequentially connected2S tower 34, plasma purifier 37 is connected with chimney 39 through draught fan 38.
The process for producing the vitamin B2 wastewater by adopting the system to treat the fermentation method comprises the following specific steps:
the first step is as follows: VB2 fermented waste water is added with medicine and mixed with acid for flocculation through a pipeline. The initial pH value of VB2 fermentation wastewater is about 5.6, firstly, ferric chloride solution is added through a pipeline mixer to adjust the pH value to 4.3-4.5, then, polyacrylamide PAM solution (the mass concentration of the PAM solution is 0.1%, after the PAM solution is added into a pipeline, the concentration of PAM in the wastewater is 0.0025%, which is equivalent to 40 times dilution.) is added through the pipeline mixer, and then, the wastewater enters a horizontal spiral centrifuge after passing through a buffer tank to separate out first protein bacterial sludge I and obtain a first clear phase I;
the second step is that: and (3) feeding the first clear phase I obtained by the horizontal spiral centrifuge in the first step into a second pipeline, adding chemicals, mixing and carrying out acid flocculation. Adding ferric chloride solution into the first clear phase I through a pipeline mixer to adjust the pH value to 4.3-4.5 (since the pH value of the commercially available ferric chloride solution is 1.2-1.5, NaOH solution is introduced before the ferric chloride solution is added, so that the pH value of a solution system mixed by the pipeline mixer is about 4.8-5.0), and then adding polyacrylamide PAM solution through the pipeline mixer (the concentration and the addition amount of the PAM solution are the same as those in the first step);
and thirdly, carrying out third pipeline dosing, mixing and flocculation on the pipeline effluent treated in the second step. After passing the effluent of the pipeline treated in the second step through a buffer tank, adding NaOH solution through a pipeline mixer again to adjust the pH value in the pipeline to 8.8-9.0, then adding ferric chloride solution to adjust the pH value to be kept at 8.4-8.5 for carrying out third flocculation, then adding PAM solution for flocculation, wherein the concentration and the adding amount of the PAM solution are the same as those of the first step, and then entering a secondary horizontal spiral centrifuge to separate out a first protein bacterial sludge II and a first clear phase II again;
fourthly, the first clear phase II enters an ion air flotation machine, and first protein bacterial sludge III and a first clear phase III are separated;
the fifth step: the pH value of the first clear phase III is adjusted to about 6.0 by hydrochloric acid in a pipeline mixer, and then the first clear phase III enters a nanofiltration membrane machine, the molecular weight is intercepted by 250, and the first clear phase III is divided into a second clear phase and a second concentrated phase; the second clear phase directly enters an anaerobic biochemical section of a biochemical system, and the second concentrated phase is separated by a disk centrifuge to obtain a third clear phase and a third concentrated phase; the third clear phase directly enters an aerobic biochemical section of the biochemical system;
and a sixth step: the drying process comprises two parts, specifically as follows: a first part: mixing and stirring first protein bacterial sludge I, II and III obtained by a two-stage horizontal spiral centrifuge, sending the mixture into a cyclone flash evaporation dryer, and then passing through a dust remover to obtain a bacterial protein feed finished product (indexes are shown in table 1), wherein generated tail gas is discharged after passing through a tail gas treatment device; a second part: sending the third concentrated phase obtained by the disc centrifuge into a cyclone flash dryer, and then passing through a dust remover to obtain a VB2 finished product (the index is shown in Table 2), wherein the purity is about 30 percent, and the generated tail gas is discharged after passing through a tail gas treatment device;
the seventh step: and (4) performing biochemical treatment. Directly feeding the second clear phase (with the indexes of cod being approximately 10000mg/L and total nitrogen being approximately 900mg/L after detection) obtained by the treatment of the nanofiltration membrane system into an anaerobic biochemical section of the biochemical treatment system; after the wastewater is treated by the anaerobic biochemical section, the index of the effluent is detected to be about 800mg/L cod and 900mg/L total nitrogen, and then the effluent enters the anaerobic ammonia oxidation biochemical section for treatment, and the index of the effluent is detected to be about 300mg/L cod and 150mg/L total nitrogen; then, the effluent of the anaerobic ammonia oxidation biochemical section (the section adopts anaerobic ammonia oxidation bacteria, which is called as red bacteria for short) enters an aerobic biochemical section;
meanwhile, the third clear phase obtained by the disc centrifuge contains higher SO4 2-The concentration is about 20000mg/L (the total amount is about 50T/d), in order to avoid the influence on the anaerobic biochemical part, the mixture directly enters the aerobic biochemical system at the later stage (the mixture is injected into the aerobic biochemical section to be just used as the supplement of the carbon source of the aerobic biochemical section after being mixed with the effluent of the anaerobic ammonia oxidation section entering the aerobic biochemical section at the earlier stage, and the diluted SO is4 2-The concentration is 1000mg/L, and the operation of the aerobic biochemical section is not influenced. ) And finally, the final effluent is detected to have indexes of cod about 150mg/L and total nitrogen about 50mg/L, and reaches the discharge standard.
The physicochemical indexes of the obtained mycoprotein feed finished product are shown in Table 1.
TABLE 1
| Item | Index (I) |
| Crude protein,% greater than or equal to | 60.0 |
| Water content is less than or equal to% | 10.0 |
| Coarse ash content not more than% | 15.0 |
| The total amount of amino acids is ≥ h | 50.0 |
| Lead (calculated by Pb) is less than or equal to mg/kg | 10.0 |
| Arsenic (calculated by As) is less than or equal to mg/kg | 2.0 |
| Mercury (calculated by Hg) is less than or equal to mg/kg | 0.1 |
| Total bacterial count allowance (bacteria per gram of product) Total bacterial count 105< | 2 |
| Salmonella | Cannot be detected |
| Coliform group, WPN/100g | 100 |
| The allowable amount of aflatoxin B1 (per kilogram of product) is less than or equal to mu g | 10 |
The above obtained VB2 finished product was tested by the national feed quality supervision and inspection center (Wuhan), and the inspection report is shown in Table 2.
TABLE 2
| Serial number | Detecting items | The result of the detection | Detection method |
| 1 | Vitamin B2 content (fluorescence spectrophotometry) | 3.04×105mg/kg | GB/T14701-2002 |
| 2 | Crude protein content (arbitration method) | 63.73％ | GB/T6432-1994 |
Example 2
The difference from example 1 is that: the second flocculation device only comprises four pipeline mixers and a second buffer tank which are connected in sequence, a liquid phase outlet of the first horizontal spiral centrifuge is connected with an inlet of the second buffer tank through the four pipeline mixers which are connected in sequence, and an outlet of the second buffer tank is connected with the second horizontal spiral centrifuge; the alkali liquor tank, the iron salt tank, the alkali liquor tank and the PAM storage tank are respectively communicated with one of the four pipeline mixers and are used for introducing an iron salt solution and a PAM solution and controlling the mixed pH; the solid phase outlet of the second horizontal spiral centrifuge is connected with the protein bacterial sludge pool; the liquid phase outlet of the second horizontal spiral centrifugal machine is connected with the inlet of the ion air flotation machine.
Example 3
The difference from example 1 is that: the liquid phase outlet of the second horizontal spiral centrifugal machine is connected with the inlet of the ion air flotation machine through a pipeline mixer. The pipeline mixer is connected with the aluminum chloride tank and is used for introducing aluminum chloride solution.
Example 4
The difference from example 1 is that: the first horizontal screw centrifuge is omitted.
Example 5
The difference from example 1 is that: the ion floatation machine is omitted.
Example 6
The difference from example 1 is that: the first horizontal screw centrifugal machine and the ion floatation machine are omitted.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, many modifications and changes can be made without departing from the inventive concept, and these modifications and changes all belong to the protection scope of the present invention.
Claims (14)
1. A treatment system for fermentation production wastewater is characterized by comprising a flocculation device, a solid-liquid separation device and a membrane separation device; the fermentation production wastewater is communicated with a liquid inlet of the solid-liquid separation device through a flocculation device; the clear phase liquid outlet of the solid-liquid separation device is communicated with the liquid inlet of the membrane separation device.
2. The treatment system of claim 1, further comprising a biochemical treatment unit, wherein the clear phase liquid outlet of the membrane separation unit is in communication with the liquid inlet of the biochemical treatment unit.
3. The treatment system of claim 2, wherein the membrane separation device comprises a PH pre-adjusting device and a nanofiltration membrane machine, and a clear phase liquid outlet of the solid-liquid separation device is connected with the PH pre-adjusting device; and a clear liquid outlet of the nanofiltration membrane machine is connected with a biochemical treatment device.
4. The treatment system according to claim 3, further comprising a centrifugal separation device and a first drying device, wherein the concentrated solution outlet of the nanofiltration membrane machine is connected with the inlet of the centrifugal separation device, the clear solution outlet of the centrifugal separation device is connected with the biochemical treatment device, and the solid phase outlet of the centrifugal separation device is connected with the first drying device.
5. The system for treating wastewater from fermentation production according to claim 4, wherein the biochemical treatment device comprises an anaerobic activation tank, an anaerobic ammonia oxidation tank, an aerobic tank and a sedimentation tank which are connected in sequence, the clear liquid outlet of the nanofiltration membrane machine is connected with the anaerobic activation tank, and the clear liquid outlet of the centrifugal separation device is connected with the aerobic tank.
6. The treatment system as claimed in claim 1, further comprising an ion flotation machine, wherein the clear phase liquid outlet of the solid-liquid separation device is communicated with the liquid inlet of the ion flotation machine, and the clear phase liquid outlet of the ion flotation machine is communicated with the liquid inlet of the membrane separation device.
7. The treatment system according to claim 6, further comprising a second drying device, wherein the solid phase outlet of the solid-liquid separation device and the solid phase outlet of the ion flotation machine are connected with the second drying device.
8. The fermentation production wastewater treatment system according to claim 7, wherein the outlet of the second drying device is sequentially connected with a first dust remover, a protein feed collecting device and a tail gas absorbing device; the outlet of the first drying device is sequentially connected with a second dust remover, a vitamin B2 crude product collector and a tail gas absorption device.
9. The system for treating wastewater from fermentation production according to claim 7, wherein the outlet ends of the first drying device and the second drying device are connected to the same tail gas absorption device.
10. The treatment system according to claim 1, wherein the flocculation device and the solid-liquid separation device are two-stage, a storage tank of the fermentation production wastewater is communicated with a liquid inlet of the first-stage solid-liquid separation device through the first-stage flocculation device, and a clear phase liquid outlet of the first-stage solid-liquid separation device is communicated with a liquid inlet of the second-stage solid-liquid separation device through the second-stage flocculation device; the clear phase liquid outlet of the second stage solid-liquid separation device is communicated with the liquid inlet of the membrane separation device.
11. The treatment system of claim 10, wherein the first flocculation device comprises a first mixing device and a first buffer tank which are sequentially connected, the iron salt tank and the PAM storage tank are respectively communicated with the first mixing device, and the first mixing device is connected with a storage tank of the fermentation production wastewater; the second flocculation device comprises a second mixing device and a second buffer tank which are sequentially connected, the iron salt tank, the lye tank and the PAM storage tank are communicated with the second mixing device, the second buffer tank is connected with the first solid-liquid separation device, and an outlet of the first buffer tank is connected with the second mixing device.
12. The treatment system according to claim 10, wherein the second stage flocculation device is provided in two sections, a buffer tank is provided between the two sections of flocculation devices, the clear phase liquid outlet of the first stage solid-liquid separation device is communicated with the liquid inlet of the first stage flocculation device, the liquid outlet of the first stage flocculation device is communicated with the buffer tank, the buffer tank is communicated with the liquid inlet of the second stage flocculation device, and the liquid outlet of the second stage flocculation device is communicated with the liquid inlet of the second stage solid-liquid separation device.
13. The treatment system of claim 11, further comprising a third mixing device positioned between the second buffer tank and the second solid-liquid separation device, wherein the iron salt tank, the lye tank, the PAM tank are in communication with the third mixing device.
14. The system for treating wastewater from fermentation production according to claim 13, wherein the first mixing device, the second mixing device, the third mixing device and the pre-pH adjusting device are provided with a plurality of pipeline mixers; the first mixing device adopts two pipeline mixers, and the iron salt tank and the PAM storage tank are respectively connected with the two pipeline mixers; the second mixing device adopts four pipeline mixers which are sequentially connected with an alkali liquor storage tank, an iron salt tank, an alkali liquor tank and a PAM storage tank; the third mixing device adopts a pipeline mixer and is connected with the acid tank; the pH pre-adjusting device is a pipeline mixer, and the hydrochloric acid storage tank is connected with the pipeline mixer.
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| CN110713319A (en) * | 2019-11-04 | 2020-01-21 | 武汉纪源环保科技有限公司 | Fermentation production wastewater treatment system |
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