CN210340502U - Processing system of natural pond liquid behind lees anaerobic fermentation - Google Patents
Processing system of natural pond liquid behind lees anaerobic fermentation Download PDFInfo
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Abstract
The utility model provides a processing system of natural pond liquid behind lees anaerobic fermentation, including consecutive centrifugal separation unit, filter-pressing unit, medium filter unit, membrane filter unit, receive filter unit and reverse osmosis unit. The utility model relates to a processing system of lees anaerobic fermentation back natural pond liquid can retrieve organic and inorganic nutrient substance, water etc. in the natural pond liquid respectively, has realized the resourceful treatment of lees anaerobic fermentation back natural pond liquid.
Description
Technical Field
The utility model relates to a waste water treatment specifically is a processing system of natural pond liquid behind lees anaerobic fermentation.
Background
A large amount of vinasse can be produced in a winery in the production process, the vinasse is treated by anaerobic fermentation at present, the vinasse forms biogas slurry after the anaerobic fermentation, the COD concentration in the biogas slurry usually reaches tens of thousands of milligrams per liter, the main components of the biogas slurry are organic matters, humic acid and protein, ammonia nitrogen of thousands of milligrams per liter, potassium and phosphorus of hundreds of milligrams per liter, a small amount of sulfate, calcium and magnesium and the like, and the biogas slurry is a very good organic fertilizer, but the biogas slurry is difficult to use. The main points are as follows:
1. the biogas slurry has large volume and low fertility content, is uneconomical for long-distance transportation, and is difficult to treat when applied to returning to fields nearby.
2. If the waste water is discharged after reaching the standard after being treated, the investment and the operation cost are very high, and the waste of resources is also very large.
Therefore, biogas slurry needs to be concentrated by fully utilizing the biogas slurry, and common concentration treatment ideas include low-temperature evaporation concentration, membrane concentration and the like, but because the solid content in the biogas slurry reaches about 2%, the turbidity is high, a large amount of colloid substances exist, the biogas slurry foams, adheres to walls, is thick, scales and other sites along with the evaporation of water in the evaporation process, and the evaporation is difficult to continue. In addition, ammonium salt in the biogas slurry is decomposed and enters a gas phase, the ammonium salt can be discharged only by treatment, and evaporation condensate water contains a large amount of organic matters and ammonia and cannot be directly utilized, so that evaporation concentration is not economically feasible. Similarly, as the biogas slurry contains more impurities and more colloidal substances, the membrane is polluted and blocked, and the direct membrane concentration is not feasible.
SUMMERY OF THE UTILITY MODEL
In order to solve the technical problem, the utility model provides a processing system of natural pond liquid behind lees anaerobic fermentation, including consecutive centrifugal separation unit, filter-pressing unit, medium filter unit, membrane filter unit, receive filter unit and reverse osmosis unit.
According to an embodiment of the invention, the centrifugal separation unit comprises a centrifuge for one-stage or multi-stage separation.
According to the utility model discloses an embodiment, the centrifugation unit includes horizontal screw centrifuge and filtration formula or disk centrifuge, horizontal screw centrifuge is used for one-level centrifugal processing, filtration formula or disk centrifuge are used for second grade centrifugal processing.
According to an embodiment of the present invention, the filter pressing unit comprises a filter press.
According to an embodiment of the invention, the media filter unit comprises one or more stages of media filters.
According to the utility model discloses an embodiment, the media filter unit includes two-stage media filter, media filter is vertical, the individual layer is horizontal or the double-deck horizontal.
According to an embodiment of the present invention, the nanofiltration unit comprises a nanofiltration membrane module, and/or the membrane filtration unit comprises an ultrafiltration membrane module or a microfiltration membrane module.
According to an embodiment of the invention, the reverse osmosis unit comprises a reverse osmosis membrane module.
According to an embodiment of the present invention, the reverse osmosis membrane module comprises one or more stages of reverse osmosis membranes.
According to an embodiment of the present invention, the reverse osmosis membrane module comprises a two-stage reverse osmosis membrane.
The utility model relates to a processing system of lees anaerobic fermentation back natural pond liquid can retrieve organic and inorganic nutrient substance, water etc. in the natural pond liquid respectively, has realized the resourceful treatment of lees anaerobic fermentation back natural pond liquid.
Drawings
The various objects, features and advantages of the present invention will become more apparent from the following detailed description of the preferred embodiments of the invention, when considered in conjunction with the accompanying drawings. The drawings are merely exemplary of the invention and are not necessarily drawn to scale. In the drawings, like reference characters designate the same or similar parts throughout the different views. Wherein:
FIG. 1 is a schematic view of biogas slurry treatment performed by a treatment system for biogas slurry after anaerobic fermentation of distiller's grains according to an embodiment of the present invention;
wherein the reference numerals are as follows:
1. a centrifugal separation unit; 2. a filter pressing unit; 3. a media filtration unit; 4. a membrane filtration unit; 5. a nanofiltration unit; 6. a reverse osmosis unit;
A. biogas slurry; B. a solid filter aid; C. centrifuging the filter cake; D. filter pressing a filter cake; E. ultrafiltration backwashing water; F. ultrafiltering the permeate; G. nano-filtering the concentrated solution; H. nanofiltration of the permeate; I. reverse osmosis permeated water; J. and (4) reverse osmosis concentrated water.
Detailed Description
Exemplary embodiments that embody features and advantages of the invention are described in detail below. It is to be understood that the invention is capable of other and different embodiments and its several details are capable of modification without departing from the scope of the invention, and that the description and drawings are to be regarded as illustrative in nature and not as restrictive.
The utility model relates to an embodiment provides a processing system of natural pond liquid behind lees anaerobic fermentation, can be used to handle lees anaerobic fermentation back natural pond liquid, retrieves organic and inorganic nutrient substance and water.
The utility model relates to an embodiment's processing system of lees anaerobic fermentation back natural pond liquid can carry out the concentration of big multiple with natural pond liquid, and all kinds of nutrients can obtain recycle, and water also all obtains the resourceful treatment of retrieval and utilization, and the simultaneous processing expense is low, the system can long-term steady operation.
As shown in the combined figure 1, the system for treating the biogas slurry after the anaerobic fermentation of the distillers' grains of the utility model comprises a centrifugal separation unit 1, a filter pressing unit 2, a medium filtering unit 3, a membrane filtering unit 4, a nanofiltration unit 5 and a reverse osmosis unit 6 which are connected in sequence.
The centrifugal separation unit 1 is used for performing centrifugal separation treatment on the biogas slurry A after the anaerobic fermentation of the vinasse, and the centrifugal separation treatment can comprise one-stage or multi-stage centrifugal separation so as to separate out solid substances as much as possible. Preferably, the centrifugation process comprises two-stage centrifugation. The centrifugal separation unit 1 comprises at least one centrifuge for performing a centrifugal separation process. The utility model discloses do not have special limited to centrifuge, can adopt the centrifuge that this field is common.
In one embodiment, the centrifugal separation unit 1 includes a horizontal screw centrifuge and a filter type (or disc type) centrifuge, and preferably, the first-stage centrifugal separation is performed by using the horizontal screw centrifuge and the second-stage centrifugal separation is performed by using the filter type (or disc type) centrifuge.
In one embodiment, the rotation speed of the horizontal screw type and filter type centrifuges may be 1000 to 4000rpm (revolutions per minute), and more preferably 2500 to 3500rpm, so as to separate as much solid matters in the biogas slurry from the solution as possible.
In the centrifugal separation treatment of an embodiment of the utility model, solid biogas residues such as rice hulls in biogas slurry A are separated under the centrifugal force action of a centrifugal machine due to the difference of specific gravity between the solid biogas residues and water, so as to obtain two logistics, namely a centrifugal filter cake C and a centrifugal separation liquid; wherein, the solid matter with large specific gravity and capable of being centrifugally separated forms a filter cake, and the centrifugally separated liquid contains organic matters, colloid, inorganic salt, water and solid particles which can not be centrifugally separated. The centrifugal filter cake C can be directly used as a solid organic fertilizer, and the centrifugal separation liquid enters a subsequent filter pressing unit 2 for filter pressing treatment.
The filter pressing unit 2 is connected with the centrifugal separation unit 1 and is used for carrying out pressure filtration treatment on the centrifugal separation liquid separated by the centrifugal separation unit 1. The centrifugal separation liquid is separated into a filter pressing filter cake D and filter pressing effluent through pressure filtration treatment, the filter pressing filter cake D can be used for directly using solid organic fertilizer, and the filter pressing effluent enters a subsequent medium filtering unit 3 for medium filtration treatment.
The filter press unit 2 comprises a filter press for performing a pressure filtration process. The utility model discloses there is not special limited to the pressure filter that uses, can adopt the filter pressing device that this field is commonly used, and the preferred pressure filter that has air drying is so that control filter cake moisture content as required.
In one embodiment, the filter press may use a non-woven fabric as the filter cloth.
In one embodiment, since the centrifuged solution contains a large amount of colloids and fine suspended solids, which can rapidly block the filter cloth during filtration and thus prevent the filtration process from being performed, a solid filter aid B, such as diatomaceous earth, can be added to the centrifuged solution to prevent the blockage and increase the filtration flux. The solid filter aid B can effectively solve the problem of pollution and blockage of suspended matters and colloidal substances in the biogas slurry to the filtering device, thereby ensuring that the biogas slurry treatment system can run stably and reliably for a long time.
In one embodiment, the amount (by mass) of the solid filter aid B may be 10 to 100 wt%, preferably 50 to 100 wt%, of the suspended matter content in the centrifuged liquid. The particle size range of the solid filter aid B can be 0.5-5 micrometers, and preferably 1-3 micrometers.
The medium filtering unit 3 is connected with the filter pressing unit 2 and is used for performing medium filtering treatment on the effluent of the filter pressing unit 2. The media filtration treatment may comprise filtering in the presence of one or more filter media to further reduce the content of suspended matter in the press filtered water to obtain media filtered effluent, which is discharged from the media filtration unit 3 and then enters the subsequent membrane filtration unit 4 for membrane filtration treatment.
The media filter unit 3 includes a media filter for performing a media filtering process. The utility model discloses do not have special restriction to media filter's form, can adopt the media filter that uses usually in the field, media filter can adopt vertical, the horizontal or double-deck horizontal of individual layer, does to adopt the filtering pond.
In one embodiment, the media filter unit 3 comprises one or more, preferably two, stages of media filters.
The filter media of the present invention is not particularly limited in kind, and one or more kinds of filter media commonly used in the art, such as quartz sand, anthracite, etc., may be used. In one embodiment, a dual-media filter is used, the filter media can be selected from quartz sand and anthracite, and preferably, the particle size of the filter media can be: quartz sand 0.4 ~ 0.6mm, anthracite 0.8 ~ 1.2mm, and the filter bed thickness can be: the quartz sand is 800mm, the anthracite is 400mm, and the thickness can be properly adjusted according to the water quality.
The membrane filtering unit 4 is connected with the medium filtering unit 3 and is used for performing membrane filtration treatment on the effluent of the medium filtering unit 3. The residual suspended matters and colloids in the wastewater can be removed through the filtering treatment of the membrane filtering unit 4, so that the SDI value of the wastewater is less than 3, and the water inlet requirement of the subsequent nanofiltration membrane filtering treatment is met. The medium filtered effluent is separated into ultrafiltration backwash water E (or microfiltration backwash water) and ultrafiltration permeate F (or microfiltration permeate) through membrane filtration treatment, the ultrafiltration backwash water E can be used for sewage farm treatment, and the ultrafiltration permeate F enters a subsequent nanofiltration unit 5 for nanofiltration membrane filtration treatment.
The medium filtration belongs to the traditional deep filtration, the membrane filtration belongs to the absolute filtration, the filtration precision is high, and the turbidity removal and colloid removal effects are better. The utility model discloses an among the processing system, membrane filtration and medium filtration cooperation are used, can show the dirty stifled tendency of colloid in improving follow-up nanofiltration membrane system.
In one embodiment, the membrane filtration unit 4 comprises a membrane module, which may be an ultrafiltration membrane or a microfiltration membrane, to perform membrane filtration treatment on the effluent of the media filtration unit 3.
In one embodiment, the membrane filtration unit 4 employs an ultrafiltration membrane module, and the ultrafiltration membrane module may employ any known ultrafiltration membrane module in the art, and more preferably employs a cross-flow filtration or immersion type ultrafiltration membrane module to satisfy a large pollutant holding capacity, or a microfiltration membrane module having the same treatment effect may be selected.
The nanofiltration unit 5 is connected with the membrane filtration unit 4 and is used for carrying out nanofiltration treatment on the ultrafiltration permeating liquid F of the membrane filtration unit 4, and the nanofiltration trapped liquid is directly utilized.
The nanofiltration unit 5 includes a nanofiltration membrane module to perform nanofiltration treatment. Ammonium bicarbonate, sodium (potassium) chloride, sodium (potassium) nitrate and water can penetrate the nanofiltration membrane, and most organic matters and SO4 2-、Ca2+、Mg2+、PO4 3-Is impermeable to nanofiltration membranes. Therefore, the nanofiltration membrane component divides the ultrafiltration permeate F into two streams, namely a nanofiltration permeate H rich in ammonium bicarbonate, sodium chloride and sodium nitrate and a nanofiltration permeate H rich in organic matters and SO4 2-、Ca2+、Mg2+、PO4 3-Nanofiltration concentrate G. The nanofiltration concentrated solution G can be directly used as organic fertilizer or high-value substances in the organic fertilizer can be continuously extracted, and nanofiltration permeating liquid H is sent to a reverse osmosis unit 6 for treatment.
The utility model discloses there is not special limited to receiving the filter membrane subassembly, can include the common filter membrane of receiving in this field. In one embodiment, the organic and SO may optionally be treated4 2-And the nanofiltration membrane has high removal rate.
In one embodiment, the inlet water temperature of the nanofiltration membrane may be 5 to 40 ℃, preferably 10 to 35 ℃, and more preferably 25 to 30 ℃, so that the concentration of the nanofiltration concentrate G can be concentrated to an ideal value as much as possible with less energy consumption.
In one embodiment, the ratio of the permeate to the nanofiltration water inflow of the nanofiltration membrane is 50 to 90% (by volume), preferably 70 to 85%.
The reverse osmosis unit 6 is connected with the nanofiltration unit 5 and is used for performing reverse osmosis treatment on nanofiltration permeate H of the nanofiltration unit 5.
The reverse osmosis unit 6 includes a reverse osmosis membrane module to perform reverse osmosis desalination treatment on the nanofiltration permeate H. Since most of the salts and all the organic substances cannot permeate the reverse osmosis membrane module, the reverse osmosis membrane module divides the nanofiltration permeate H into two streams, i.e., reverse osmosis permeate I containing less salts and reverse osmosis concentrate J rich in salts and organic substances. The reverse osmosis permeate water I can be directly recycled, and the reverse osmosis concentrate water J can be used as fertilizer.
In one embodiment, the reverse osmosis membrane module of the reverse osmosis unit 6 may be in multiple stages, such as two stages, and various reverse osmosis membrane modules of different types may be used to form the final treatment unit, so as to improve the desalination effect.
The nanofiltration permeate H mainly contains monovalent inorganic ions and has low content of organic matters, so that the nanofiltration permeate H can be concentrated in the reverse osmosis unit 6 by a high multiple and is not easy to be polluted and blocked.
In one embodiment, the reverse osmosis unit 6 includes one or more reverse osmosis membranes, preferably two reverse osmosis membranes, in order to recover as much water as possible and reduce the amount of reverse osmosis concentrate.
In one embodiment, the ratio of the permeate to the water inflow of the reverse osmosis membrane may be 50 to 95% (by volume), preferably 75 to 90%.
The utility model discloses a processing system of lees anaerobic fermentation after natural pond liquid, during the operation, send lees anaerobic fermentation after natural pond liquid A into centrifugal separation unit 1 at first and carry out the step of centrifugal separation processing, obtain centrifugal filter cake C and centrifugal separation liquid; then, sending the centrifugal separation liquid into a filter pressing unit 2 for filter pressing treatment to obtain a filter pressing filter cake D and filter pressing effluent; then, sending the filter-pressed effluent into a medium filtering unit 3 for a medium filtering treatment step to obtain medium-filtered effluent; then, sending the medium filtered water into a membrane filtration unit 4 for membrane filtration treatment to obtain ultrafiltration backwashing water E and ultrafiltration permeate F; then, the ultrafiltration permeating liquid F is sent to a nanofiltration unit 5 for nanofiltration treatment to obtain nanofiltration concentrated liquid G and nanofiltration permeating liquid H; and finally, sending the nanofiltration permeating liquid H into a reverse osmosis unit 6 for reverse osmosis treatment.
The system for treating the biogas slurry after the anaerobic fermentation of the vinasse, which is provided by the embodiment of the utility model, can separate organic matters, inorganic salts and water in the biogas slurry, recycle organic and inorganic nutrient substances in the biogas slurry and obtain high-quality water; realizes the recycling treatment of the biogas slurry after the anaerobic fermentation of the vinasse, and has remarkable economic benefit and environmental benefit.
The following will further explain the system for treating biogas slurry after anaerobic fermentation of distiller's grains according to an embodiment of the present invention with reference to the accompanying drawings and specific examples.
Examples
Treating the biogas slurry after the anaerobic fermentation of the vinasse according to the following steps, wherein the relevant parameters of the biogas slurry to be treated are as follows:
the pH value is 8.5; the concentration of the organic matter is: CODcr23000 mg/L; TDS: 19000 mg/L; hardness (as CaCO)3Meter) 688 mg/L; alkalinity (as CaCO)3Meter) 11400 mg/L; 1% of suspended matters; HCO3 -13900mg/L；Ca2+259mg/L；Mg2+9.1mg/L；K+1140 mg/L; total phosphorus 310 mg/L; NH (NH)4 +3625mg/L；Cl-313mg/L；SO4 2-73mg/L。
a. Feeding the biogas slurry into a horizontal screw centrifuge of the centrifugal separation unit 1 and a subsequent filter centrifuge for centrifugal separation treatment, wherein the rotation speed of the horizontal screw centrifuge is 3000 rpm; the rotation speed of the filter type centrifuge is 2500rpm, the filtration precision is 10 microns, the content of suspended substances in the effluent (centrifugate) of the centrifuge is 366mg/L, and the COD is 18750 mg/L.
b. And (3) feeding the effluent of the centrifuge into a filter-pressing feeding tank of a filter-pressing unit 2, and adding kieselguhr into the filter-pressing feeding tank, wherein the adding amount of the kieselguhr is 10 kg/ton of water, and the granularity of the kieselguhr is 3 micrometers. Then the material in the filter pressing feeding tank is lifted by a pump and is sent into a filter press for filter pressing treatment, and the content of suspended substances in the outlet water of the filter press is 122mg/L, and the COD is 16300 mg/L.
c. The outlet water of the filter press is lifted by a pump and is sent into a medium filter of the medium unit 3 for medium filtration treatment, quartz sand and anthracite are filled in the medium filter, wherein the filling height of the quartz sand is 800mm, the filling height of the anthracite is 400mm, and the filtering speed is 7.0 m/h. The medium filter is not connected in series in two stages, and the effluent turbidity of the medium filter is 617NTU, CODcr14308 mg/L.
d. Sending the effluent of the medium filter into an ultrafiltration membrane treatment system of a membrane filtration unit 4 for ultrafiltration membrane filtration treatment, wherein the ultrafiltration membrane adopts an Asahi chemical conversion UHS-620A submerged ultrafiltration membrane, and the filtration flux is 15Lmh/m2. At the moment, the water recovery rate is 95%, the effluent suspended matter is approximately equal to 0mg/L, the effluent turbidity is less than 0.1NTU, the effluent CODcr4980mg/L and the effluent SDI value is less than 3.
e. The ultrafiltration water enters an ultrafiltration water tank, is lifted by a pump and enters a nanofiltration membrane component system of a nanofiltration unit 5 for nanofiltration treatment, and the nanofiltration membrane component adopts a GE DK8040 type nanofiltration membrane component. The nanofiltration permeate liquid CODcr 440mg/L enters a reverse osmosis unit 6; CODcr23100mg/L in nanofiltration membrane trapped fluid.
f. The nanofiltration permeate enters a reverse osmosis membrane device of a reverse osmosis unit 6 for reverse osmosis treatment, the reverse osmosis membrane device is of two stages, wherein one stage of reverse osmosis adopts a Claw XC series resistant reverse osmosis membrane element to reach 13Lmh/m2The designed flux of (1) is used for reverse osmosis treatment, and water of first-stage reverse osmosisThe recovery rate was 75%. The TDS of the reverse osmosis produced water is less than 350mg/L, the TDS of the first-level reverse osmosis concentrated water is about 80000mg/L, and the CODcr 1760mg/L of the first-level reverse osmosis concentrated water. The secondary reverse osmosis membrane component adopts a Dow XUS180808 ultrahigh pressure reverse osmosis membrane element, the operating pressure is 10.5MPa, and the design flux is 7Lmh/m2The water recovery rate of reverse osmosis was 35%. The TDS of reverse osmosis produced water is less than 1000mg/L, the TDS of concentrated water is about 117000mg/L, and CODcr 2700 mg/L.
According to the embodiment, most of solid suspended matters in the biogas slurry are removed and recovered through centrifugal separation treatment and filter pressing treatment, residual suspended matters and colloids in the biogas slurry are removed through medium filtration treatment and ultrafiltration membrane filtration treatment, soluble organic matters in the biogas slurry are recovered through nanofiltration treatment, divalent ions are intercepted, most of water is recovered through reverse osmosis treatment, and monovalent inorganic ions such as ammonium bicarbonate and potassium salt in the biogas slurry are concentrated.
Unless otherwise defined, all terms used in the present invention have the meanings commonly understood by those skilled in the art.
The described embodiments are for illustrative purposes only and are not intended to limit the scope of the present invention, and various other substitutions, changes and modifications may be made by those skilled in the art within the scope of the present invention.
Claims (10)
1. The system for treating biogas slurry after anaerobic fermentation of vinasse is characterized by comprising a centrifugal separation unit, a filter pressing unit, a medium filtering unit, a membrane filtering unit, a nanofiltration unit and a reverse osmosis unit which are sequentially connected.
2. The system of claim 1, wherein the centrifugal separation unit comprises a centrifuge for one or more stages of separation.
3. The system of claim 2, wherein the centrifugal separation unit comprises a horizontal screw centrifuge for primary centrifugation and a filter or disc centrifuge for secondary centrifugation.
4. The system of claim 1, wherein the pressure filtration unit comprises a filter press.
5. The system of claim 1, wherein the media filtration unit comprises one or more stages of media filters.
6. The system of claim 5, wherein the media filtration unit comprises a two-stage media filter, the media filter being vertical, single-layer horizontal, or double-layer horizontal.
7. The system of claim 1, wherein the nanofiltration unit comprises a nanofiltration membrane module, and/or wherein the membrane filtration unit comprises an ultrafiltration membrane module or a microfiltration membrane module.
8. The system of claim 1, wherein the reverse osmosis unit comprises a reverse osmosis membrane module.
9. The system of claim 8, wherein the reverse osmosis membrane module comprises one or more stages of reverse osmosis membranes.
10. The system of claim 9, wherein the reverse osmosis membrane module comprises a two-stage reverse osmosis membrane.
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| CN110078241A (en) * | 2019-05-29 | 2019-08-02 | 美景（北京）环保科技有限公司 | The processing system and method for biogas slurry after a kind of vinasse anaerobic fermentation |
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| CN110078241A (en) * | 2019-05-29 | 2019-08-02 | 美景（北京）环保科技有限公司 | The processing system and method for biogas slurry after a kind of vinasse anaerobic fermentation |
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