CN215947022U - Gelatin effluent disposal system - Google Patents
Gelatin effluent disposal system Download PDFInfo
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- CN215947022U CN215947022U CN202121313256.XU CN202121313256U CN215947022U CN 215947022 U CN215947022 U CN 215947022U CN 202121313256 U CN202121313256 U CN 202121313256U CN 215947022 U CN215947022 U CN 215947022U
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Abstract
The application discloses gelatin effluent disposal system includes: a pretreatment section, a membrane treatment section and an evaporation concentration crystallization section; the pretreatment section comprises a dosing tank and a flocculation precipitation tank, wherein the upstream of the dosing tank is communicated with a discharge port of the gelatin wastewater, and the downstream of the dosing tank is communicated with the flocculation precipitation tank; the membrane treatment section comprises an ultrafiltration device, a nanofiltration device and a reverse osmosis device which are sequentially communicated, the upstream of the ultrafiltration device is communicated with a clarified liquid outlet of the flocculation precipitation tank, and the reverse osmosis device comprises a concentrated water outlet and a clear water outlet; the evaporation concentration crystallization section comprises an MVR evaporation device, a three-effect evaporation device, a single-effect evaporation device and a cooling slicing device which are sequentially communicated, wherein the upstream of the MVR evaporation device is communicated with a concentrated water outlet of a reverse osmosis device; wherein, the clear water outlet of the reverse osmosis device, the MVR evaporation plant, the triple-effect evaporation plant and the single-effect evaporation plant are respectively communicated with the medicine feeding groove. The application effectively realizes zero emission and recycling of the gelatin wastewater through the treatment of the wastewater containing the salt and the organic matters.
Description
Technical Field
The utility model relates to the technical field of treatment of wastewater containing salt and organic matters, in particular to a gelatin wastewater treatment system.
Background
Gelatin is a partially hydrolyzed product of collagen, belongs to the category of protein macromolecules, has similar characteristics to protein macromolecules, and has wide application in the fields of food, medicines and other industries. The raw materials for producing the gelatin mainly comprise skins and bones of animals, leather-making waste materials and the like, the gelatin is obtained by moderate hydrolysis and thermal denaturation of collagen, common gelatin on the market is mostly prepared by taking cow cattle bones or pig skins as raw materials, and at present, the production method of the gelatin mainly comprises an alkaline method, an acid method, an enzymatic method and the like.
Gelatin produces a lot of waste water in the production process, and the gelatin waste water is waste water containing a large amount of high salt and high Chemical Oxygen Demand (COD). After most of phosphate is recovered by the traditional process, a large amount of waste water containing calcium chloride, protein and amino acid is still generated, the waste water with high salt and high COD cannot be biochemically treated, the environment is influenced by direct discharge, more and more waste water can be accumulated for recycling, the use is influenced, and the normal production activity of enterprises is influenced at present.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a gelatin wastewater treatment system, which aims to solve the problems in the technical background, and the treated product can be recycled, so that the recycling and zero discharge of wastewater are realized.
In order to achieve the purpose, the utility model adopts the following technical scheme:
the application provides a gelatin effluent disposal system, includes: a pretreatment section, a membrane treatment section and an evaporation concentration crystallization section;
the pretreatment section comprises: the device comprises a dosing tank and a flocculation precipitation tank, wherein the upstream of the dosing tank is communicated with a discharge port of gelatin wastewater, the downstream of the dosing tank is communicated with the flocculation precipitation tank, and the flocculation precipitation tank comprises a discharge port of precipitated slurry and a clear liquid outlet;
the membrane treatment stage comprises: the device comprises an ultrafiltration device, a nanofiltration device and a reverse osmosis device which are sequentially communicated, wherein the upstream of the ultrafiltration device is communicated with a clear liquid water outlet of a flocculation precipitation tank, the ultrafiltration device also comprises a discharge port for concentrating slurry, the nanofiltration device also comprises a concentrated water outlet, and the reverse osmosis device comprises a concentrated water outlet and a clear water outlet;
the evaporation concentration crystallization section comprises: the MVR evaporation device, the triple-effect evaporation device, the single-effect evaporation device and the cooling slicing device are sequentially communicated, and the upstream of the MVR evaporation device is communicated with a concentrated water outlet of the reverse osmosis device;
wherein, the clear water outlet of the reverse osmosis device, the MVR evaporation plant, the triple-effect evaporation plant and the single-effect evaporation plant are also respectively communicated with the medicine feeding groove.
Preferably, the flocculating agent added into the flocculation precipitation tank comprises one or more of polyaluminium chloride (PAC), polyferric sulfate (PFS), Polyacrylamide (PAM) and barium chloride.
Preferably, the ultrafiltration device adopts an ultrafiltration membrane with the aperture of 1-200 nm.
Preferably, the pressure of the ultrafiltration device is 0.1-1 MPa.
Preferably, the nanofiltration device adopts a nanofiltration membrane with the aperture of 1-5 nm.
Preferably, the pressure of the nanofiltration device is 1-4 MPa, and the membrane flux is 10-35L/m2·h。
Preferably, the reverse osmosis device is a reverse osmosis membrane with the aperture of 0.5-10 nm.
Preferably, the pressure of the reverse osmosis device is 4-8 MPa, and the membrane flux is 30-60L/m2·h。
Preferably, the processing conditions of the MVR evaporation device include: the temperature is 0-60 ℃, the pressure is 0.1-0.3 MPa, and the solid content is 3-12%.
Preferably, the processing conditions of the triple effect evaporation device comprise: the temperature is 60-120 ℃, the pressure is 0.1-0.5 MPa, and the solid content is 20-30%.
Preferably, the processing conditions of the single-effect evaporation device include: the temperature is 80-170 ℃, the pressure is 0.1-0.8 MPa, and the solid content is 60-70%.
Preferably, the gelatin wastewater treatment system further comprises: and the granulating device is connected with the cooling slicing device and is used for carrying out dry granulation on the calcium chloride dihydrate output by the cooling slicing device, and the granulation diameter range is 1-5 mm.
More preferably, the gelatin wastewater treatment system further comprises: and the packaging and stacking device is connected with the granulating device and is used for packaging and stacking the solid output by the granulating device to prepare a snow melting agent or other calcium chloride products for sale.
Preferably, the gelatin wastewater treatment system further comprises: and the inlet of the lime milk generator is respectively connected with the clean water outlet of the reverse osmosis device, the MVR evaporation device, the three-effect evaporation device and the single-effect evaporation device and is communicated, and the outlet of the lime milk generator is communicated with the chemical feeding groove.
Preferably, the gelatin wastewater treatment system further comprises: and the slurry recovery device is respectively communicated with the discharge port of the slurry of the flocculation precipitation tank, the discharge port of the concentrated slurry of the ultrafiltration device and the concentrated water outlet of the nanofiltration device.
More preferably, the mud recovery device further comprises a filter press, a mud outlet is formed in the filter press, and mud in the mud recovery device is subjected to filter pressing by the filter press to form a filter cake, and then is discharged from the mud outlet and transported outwards.
Further, the filter press also comprises a wastewater outlet which is communicated with the dosing tank and used for refluxing filtrate generated in the filter pressing process of the filter press into the dosing tank.
The application also provides a gelatin wastewater treatment method, which is realized by adopting the gelatin wastewater treatment system, and the method comprises the following steps:
introducing the gelatin wastewater into a pretreatment area, and removing macromolecular organic matters by flocculation precipitation treatment, ultrafiltration treatment, nanofiltration treatment and reverse osmosis treatment in sequence;
carrying out MVR evaporation treatment, triple-effect evaporation treatment and single-effect evaporation treatment on the concentrated water formed after the reverse osmosis treatment in sequence to obtain concentrated solution, cooling and slicing the concentrated solution, and drying the concentrated solution by hot air to prepare calcium chloride dihydrate or anhydrous calcium chloride;
part or all of clear water generated in the reverse osmosis treatment, the MVR evaporation treatment, the three-effect evaporation treatment and the single-effect evaporation treatment is returned to the pretreatment area for recycling; and concentrated water generated in the flocculation precipitation treatment, the ultrafiltration treatment and the nanofiltration treatment is used as organic fertilizer or used for preparing organic fertilizer.
In a preferred embodiment, the macromolecular organic substance is any one or more of a peptide, a protein or an amino acid.
Preferably, the settling time of the flocculation precipitation treatment is 1-4 h.
Preferably, the flocculation precipitation treatment comprises:
putting a flocculating agent to a specified dosing point;
sending supernatant liquor obtained after precipitation to ultrafiltration treatment;
and directly discharging the precipitated slurry or automatically flowing to a filter press to be filter-pressed into a filter cake and then discharging, wherein the filtrate generated in the filter pressing process of the filter press returns to the pretreatment area to be recycled.
More preferably, the flocculant comprises one or more of polyaluminium chloride (PAC), polyferric sulfate (PFS), Polyacrylamide (PAM), barium chloride.
More preferably, the mass ratio of the flocculating agent to the gelatin wastewater is 1: 100-1: 10000.
More preferably, the mud or filter cake after flocculation precipitation treatment separation is used as organic fertilizer production raw material.
Preferably, an ultrafiltration membrane with the aperture of 1-200 nm is selected in the ultrafiltration treatment.
Preferably, the pressure of the ultrafiltration treatment is 0.1-1 MPa.
Preferably, ultrafiltration product water and concentrated slurry are obtained after the ultrafiltration treatment, the ultrafiltration product water is sent to nanofiltration treatment, and the concentrated slurry is directly discharged or automatically flows to a filter press to be filter-pressed into a filter cake.
More preferably, the concentrated slurry or filter cake after ultrafiltration treatment separation is used as an organic fertilizer production raw material.
Preferably, a nanofiltration membrane with the aperture of 1-5 nm is selected in the nanofiltration treatment.
Preferably, the pH value of the inlet water subjected to nanofiltration treatment is 6.5-11.0.
Preferably, the pressure of nanofiltration treatment is 1-4 MPa, and the membrane flux is 10-35L/m2·h。
Preferably, nanofiltration water and nanofiltration concentrated water are obtained after the nanofiltration treatment, the nanofiltration water is sent to reverse osmosis treatment, and the nanofiltration concentrated water is used as an organic fertilizer production raw material.
Preferably, a reverse osmosis membrane with the aperture of 0.5-10 nm is selected in the reverse osmosis treatment.
Preferably, the pH value of the inlet water of the reverse osmosis treatment is 5.0-10.0.
Preferably, the pressure of the reverse osmosis treatment is 4-8 MPa, and the membrane flux is 30-60L/m2·h。
Preferably, the conditions of the MVR evaporation treatment include: the temperature is 0-60 ℃, the pressure is 0.1-0.3 MPa, and the solid content is 3-12%.
Preferably, the conditions of the triple effect evaporation process include: the temperature is 60-120 ℃, the pressure is 0.1-0.4 MPa, and the solid content is 20-30%.
Preferably, the conditions of the single-effect evaporation treatment include: the temperature is 80-170 ℃, the pressure is 0.1-0.4 MPa, and the solid content is 60-70%.
Preferably, the cooling slicing process includes: and (3) carrying out cooling crystallization on the concentrated solution obtained after single-effect evaporation treatment through indirect heat exchange of cooling water, and slicing to obtain calcium chloride dihydrate crystals.
Preferably, the product after the cooling and slicing treatment is dried by a hot air drying system to prepare calcium chloride dihydrate and anhydrous calcium chloride.
More preferably, the hot air temperature of the hot air drying system is 200-300 ℃, the heat source adopts steam or natural gas, and the tail gas is directly introduced into the MVR evaporation storage tank at the front section to recover heat.
Preferably, the calcium chloride dihydrate or the anhydrous calcium chloride prepared after the cooling slicing treatment is sold as a snow melting agent or other calcium chloride products.
More preferably, after the cooling slice treatment is performed to prepare calcium chloride dihydrate, the wastewater treatment method further comprises the following steps: and (3) performing dry granulation on the prepared calcium chloride dihydrate or anhydrous calcium chloride, wherein the granulation diameter range is 1-5 mm, and then packaging and stacking the granules to prepare the snow-melting agent for sale.
Preferably, the wastewater treatment method further comprises: and lime milk is added into part or all of the clear water generated in the reverse osmosis treatment, the MVR evaporation treatment, the three-effect evaporation treatment and the single-effect evaporation treatment, and the filtered supernatant is returned to the pretreatment area for recycling after standing and precipitating.
More preferably, the lime milk is directly prepared from saturated lime milk or industrial quick lime.
Compared with the prior art, the technical scheme of the utility model has the following beneficial effects:
the application will contain gelatin waste water of high COD, high salt and get rid of macromolecular organic matters such as most protein, amino acid through flocculation and precipitation, ultrafiltration, receive and strain, reverse osmosis treatment, retrieve partly clear water through reverse osmosis, reverse osmosis dense water passes through MVR evaporation, triple effect evaporation, single effect evaporation, cooling section and prepares calcium chloride dihydrate. Wherein clear water recovered by nanofiltration and reverse osmosis is used as process water for producing gelatin, nanofiltration concentrated water, ultrafiltration concentrated water, flocculation precipitation concentrated slurry or filter cakes are used as raw materials for producing organic fertilizer, and calcium chloride dihydrate or anhydrous calcium chloride prepared by slicing is used as a snow melting agent or other calcium chloride products for sale. The method effectively realizes zero discharge and recycling of the gelatin wastewater and realizes win-win of environmental protection benefit and economic benefit for treating the wastewater containing salt and organic matters.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the application and, together with the description, serve to explain the application and are not intended to limit the application. In the drawings:
FIG. 1 is a process flow diagram of a gelatin wastewater treatment process of the present application.
Detailed Description
In order to make the objects, technical solutions and effects of the present invention clearer and clearer, the present invention is further described in detail below with reference to the accompanying drawings and examples. It should be understood that the specific embodiments described herein are merely illustrative of the utility model and are not intended to limit the utility model.
Please refer to fig. 1. It should be noted that the drawings provided in the present embodiment are only for schematically illustrating the basic idea of the present invention, and the drawings only show the components related to the present invention and are not drawn according to the number, shape and size of the components in actual implementation.
Example (b):
the combined process flow of the attached figure 1 of the application is adopted to treat certain gelatin wastewater, wherein the gelatin wastewater is obtained by the preparation method of acid gelatin.
The quality of the wastewater is as follows: pH 5, COD 2000mg/L, Ca2+Is 400mol/L, Cl-Is 300mol/L, PO4 3+200mol/L, total salt content of 15000mg/L and wastewater treatment water amount of 200m3/h。
In this embodiment, a wastewater treatment system is used which comprises: a pretreatment section, a membrane treatment section and an evaporation concentration crystallization section.
Wherein the pre-processing section comprises: the device comprises a dosing tank and a flocculation precipitation tank, wherein the upstream of the dosing tank is communicated with a discharge port of gelatin wastewater, the downstream of the dosing tank is communicated with the flocculation precipitation tank, and the flocculation precipitation tank comprises a discharge port of precipitated slurry and a clear liquid outlet. In the drug adding tank, barium chloride is required to be added besides the gelatin wastewater. The flocculant is prepared in a dosing tank, and then is pumped into a flocculation precipitation tank in a liquid state by a dosing pump after preparation.
Wherein the membrane treatment stage comprises: the device comprises an ultrafiltration device, a nanofiltration device and a reverse osmosis device which are sequentially communicated, wherein the upstream of the ultrafiltration device is communicated with a clarified liquid outlet of a flocculation precipitation tank, the ultrafiltration device further comprises a discharge outlet of concentrated slurry, the nanofiltration device further comprises a concentrated water outlet, and the reverse osmosis device comprises a concentrated water outlet and a clear water outlet.
Wherein, the evaporation concentration crystallization section comprises: MVR evaporation plant, triple effect evaporation plant, single effect evaporation plant and the cooling section device that communicate in proper order, MVR evaporation plant's upper reaches intercommunication reverse osmosis unit's dense water delivery port.
In the above wastewater treatment system, the clean water outlet of the reverse osmosis device, the MVR evaporation device, the triple-effect evaporation device and the single-effect evaporation device are also respectively communicated with the dosing tank.
In a preferred embodiment, the gelatin wastewater treatment system further comprises: a granulating device and a packaging and stacking device. The granulation device is connected with the cooling slicing device and is used for carrying out dry granulation on calcium chloride dihydrate output by the cooling slicing device, and the granulation diameter range is 1-5 mm; and the packaging and stacking device is connected with the granulating device and is used for packaging and stacking the solid output by the granulating device to prepare the sold snow-melting agent.
In a preferred embodiment, the gelatin wastewater treatment system further comprises: and the inlet of the lime milk generator is respectively connected with the clean water outlet of the reverse osmosis device, the MVR evaporation device, the three-effect evaporation device and the single-effect evaporation device and is communicated, and the outlet of the lime milk generator is communicated with the chemical feeding groove.
The treatment system is used for treating the wastewater, and the treatment steps are as follows:
1) introducing the gelatin wastewater into a dosing tank; putting a flocculating agent, wherein the mass ratio of the flocculating agent to the gelatin wastewater is 1: 100-1: 10000, and the flocculating agent comprises polyaluminium chloride (PAC), polyferric sulfate (PFS), Polyacrylamide (PAM) and barium chloride; and precipitating for 1-4 hours, directly discharging the slurry obtained after precipitation, or automatically flowing to a filter press to be filter-pressed into a filter cake and then discharging the filter cake to be used as a raw material for producing an organic fertilizer (liquid fertilizer), and sending supernatant clarified liquid obtained after precipitation to a next-stage ultrafiltration device for ultrafiltration treatment.
2) And an ultrafiltration membrane with the aperture of 1-200 nm is selected in the ultrafiltration treatment, and the pressure of the ultrafiltration treatment is 0.1-1 MPa. After the clarified liquid entering the ultrafiltration device is subjected to ultrafiltration treatment, the generated concentrated slurry is directly discharged, or automatically flows to a filter press to be filter-pressed into a filter cake to be discharged, the filter cake is used as a raw material for producing organic fertilizer (liquid fertilizer), and the generated ultrafiltration water is sent to a nanofiltration device to be subjected to nanofiltration treatment.
3) The pH value of the inlet water subjected to nanofiltration treatment is 5.0-10.0, a nanofiltration membrane with the aperture of 1-5 nm is selected in the nanofiltration treatment, the pressure of the nanofiltration treatment is 1-4 MPa, and the membrane flux is 10-35L/m2H. Nanofiltration device is used for processing to obtain nanofiltration produced water and nanofiltration concentrated water, the nanofiltration concentrated water is used as organic fertilizer (liquid fertilizer) production raw material, and the nanofiltration produced water is sent to reverse osmosis device for reverse osmosisAnd (4) performing thorough treatment.
4) The pH value of the inlet water of the reverse osmosis treatment is 5.0-10.0, the reverse osmosis membrane with the aperture of 0.5-10 nm is selected in the reverse osmosis treatment, the pressure of the reverse osmosis treatment is 4-8 MPa, and the membrane flux is 30-60L/m2·h。
After the flocculation precipitation treatment, the ultrafiltration treatment, the nanofiltration treatment and the reverse osmosis treatment, most of macromolecular organic matters such as protein, amino acid and the like in the wastewater are removed. At this time, the removal rate of protein was 98%, the removal rate of amino acid was 95%, the removal rate of sulfate was 99%, and the removal rate of phosphate was 97%.
5) The concentrated water formed after the reverse osmosis treatment is subjected to MVR evaporation treatment, triple effect evaporation treatment and single effect evaporation treatment in sequence.
Wherein the MVR evaporation treatment conditions comprise: the temperature is 0-60 ℃, the pressure is 0.1-0.3 MPa, and the solid content is 3-12%; the conditions of the triple effect evaporation treatment include: the temperature is 60-120 ℃, the pressure is 0.1-0.5 MPa, and the solid content is 20-30%; the conditions of the single-effect evaporation treatment include: the temperature is 80-150 ℃, the pressure is 0.1-0.8 MPa, and the solid content is 60-70%.
6) Cooling, crystallizing and slicing the concentrated solution obtained after single-effect evaporation treatment through indirect heat exchange of cooling water to obtain calcium chloride dihydrate crystals; and (3) carrying out dry granulation on the prepared calcium chloride dihydrate, wherein the granulation diameter range is 1-5 mm, and then packaging and stacking to prepare the snow-melting agent for sale.
7) And recovering part of clear water generated by reverse osmosis treatment, and recovering part of clear water generated in MVR evaporation treatment, triple-effect evaporation treatment and single-effect evaporation treatment. At the moment, the removal rate of protein in the recovered clear water is 99.8 percent, the removal rate of amino acid is 98 percent, the content of TDS is 500mg/L, COD is less than 200mg/L, and the standard of recycling the process water can be met.
8) And adding lime milk into part of the clear water recovered in the reverse osmosis treatment, the MVR evaporation treatment, the three-effect evaporation treatment and the single-effect evaporation treatment, wherein the lime milk is prepared by directly adopting saturated lime milk or adopting industrial quick lime. The lime milk enables phosphate, sulfate, magnesium salt and the lime milk in the recovered clear water to be chemically precipitated, and the hardness of the water is effectively reduced. And returning the filtered supernatant to the medicine adding tank for recycling after standing and precipitating.
To sum up, this application will contain gelatin waste water of high COD, high salt and get rid of macromolecular organic matters such as most protein, amino acid through flocculation and precipitation, ultrafiltration, receive and strain, reverse osmosis treatment, retrieve partly clear water through reverse osmosis, reverse osmosis dense water passes through MVR evaporation, triple effect evaporation, single effect evaporation, cooling section, hot air drying prepares calcium chloride dihydrate or anhydrous calcium chloride. Wherein clear water recovered by nanofiltration and reverse osmosis is used as process water for producing gelatin, nanofiltration concentrated water, ultrafiltration concentrated water, flocculation precipitation concentrated slurry or filter cakes are used as raw materials for producing organic fertilizer, and calcium chloride dihydrate or anhydrous calcium chloride prepared by slicing is used as a snow melting agent or other calcium chloride products for sale. The method effectively realizes zero discharge and recycling of the gelatin wastewater and realizes win-win of environmental protection benefit and economic benefit for treating the wastewater containing salt and organic matters.
The embodiments of the present invention have been described in detail, but the embodiments are merely examples, and the present invention is not limited to the embodiments described above. Any equivalent modifications and substitutions to those skilled in the art are also within the scope of the present invention. Accordingly, equivalent changes and modifications made without departing from the spirit and scope of the present invention should be covered by the present invention.
Claims (10)
1. A gelatin wastewater treatment system, comprising: a pretreatment section, a membrane treatment section and an evaporation concentration crystallization section;
the pretreatment section comprises: the device comprises a dosing tank and a flocculation precipitation tank, wherein the upstream of the dosing tank is communicated with a discharge port of gelatin wastewater, the downstream of the dosing tank is communicated with the flocculation precipitation tank, and the flocculation precipitation tank comprises a discharge port of precipitated slurry and a clear liquid outlet;
the membrane treatment stage comprises: the device comprises an ultrafiltration device, a nanofiltration device and a reverse osmosis device which are sequentially communicated, wherein the upstream of the ultrafiltration device is communicated with a clear liquid water outlet of a flocculation precipitation tank, the ultrafiltration device also comprises a discharge port for concentrating slurry, the nanofiltration device also comprises a concentrated water outlet, and the reverse osmosis device comprises a concentrated water outlet and a clear water outlet;
the evaporation concentration crystallization section comprises: the MVR evaporation device, the triple-effect evaporation device, the single-effect evaporation device and the cooling slicing device are sequentially communicated, and the upstream of the MVR evaporation device is communicated with a concentrated water outlet of the reverse osmosis device;
wherein, the clear water outlet of the reverse osmosis device, the MVR evaporation plant, the triple-effect evaporation plant and the single-effect evaporation plant are also respectively communicated with the medicine feeding groove.
2. The gelatin wastewater treatment system as claimed in claim 1, wherein the ultrafiltration device is an ultrafiltration membrane with a pore size of 1nm to 200 nm.
3. The gelatin wastewater treatment system as claimed in claim 1, wherein the nanofiltration device is a nanofiltration membrane with a pore size of 1nm to 5 nm.
4. The gelatin wastewater treatment system as claimed in claim 1, wherein the reverse osmosis device is a reverse osmosis membrane with a pore size of 0.5nm to 10 nm.
5. The gelatin wastewater treatment system as claimed in claim 1, wherein the system further comprises: and the granulating device is connected with the cooling slicing device and is used for carrying out dry granulation on the calcium chloride dihydrate output by the cooling slicing device, and the granulation diameter range is 1-5 mm.
6. The gelatin wastewater treatment system as claimed in claim 5, wherein the system further comprises: and the packaging and stacking device is connected with the granulating device and is used for packaging and stacking the solid output by the granulating device to prepare the sold snow-melting agent.
7. The gelatin wastewater treatment system as claimed in claim 1, wherein the system further comprises: and the inlet of the lime milk generator is respectively connected with the clean water outlet of the reverse osmosis device, the MVR evaporation device, the three-effect evaporation device and the single-effect evaporation device and is communicated, and the outlet of the lime milk generator is communicated with the chemical feeding groove.
8. The gelatin wastewater treatment system as claimed in claim 1, wherein the system further comprises: and the slurry recovery device is respectively communicated with the discharge port of the slurry of the flocculation precipitation tank, the discharge port of the concentrated slurry of the ultrafiltration device and the concentrated water outlet of the nanofiltration device.
9. The gelatin wastewater treatment system as claimed in claim 8, wherein the slurry recovery device further comprises a filter press, a sludge outlet is formed in the filter press, and the slurry in the slurry recovery device is subjected to pressure filtration by the filter press to form a filter cake, and then is discharged from the sludge outlet and transported outside.
10. The gelatin wastewater treatment system as claimed in claim 9, wherein the filter press further comprises a wastewater outlet, and the wastewater outlet is communicated with the chemical feeding tank and used for returning filtrate generated in the filter pressing process of the filter press to the chemical feeding tank.
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| CN202121313256.XU CN215947022U (en) | 2021-06-11 | 2021-06-11 | Gelatin effluent disposal system |
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| CN202121313256.XU CN215947022U (en) | 2021-06-11 | 2021-06-11 | Gelatin effluent disposal system |
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| CN215947022U true CN215947022U (en) | 2022-03-04 |
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Effective date of registration: 20221130 Address after: 014030 South of Fengzhi Road and west of Guangyao Road, Binhe New District, Baotou Rare Earth Development Zone, Inner Mongolia Autonomous Region Patentee after: Inner Mongolia Dongbao Datian Biotechnology Co.,Ltd. Address before: 201518 No.588, Huifeng East Street, Luxiang Town, Jinshan District, Shanghai Patentee before: SHANGHAI LANBIN PETROCHEMICAL EQUIPMENT Co.,Ltd. |
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