CN217173354U - Device for recovering lactic acid evaporation condensate water - Google Patents
Device for recovering lactic acid evaporation condensate water Download PDFInfo
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- CN217173354U CN217173354U CN202221066746.9U CN202221066746U CN217173354U CN 217173354 U CN217173354 U CN 217173354U CN 202221066746 U CN202221066746 U CN 202221066746U CN 217173354 U CN217173354 U CN 217173354U
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- lactic acid
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy
Abstract
The utility model discloses a device that lactic acid evaporation comdenstion water was retrieved has solved the recovery unit inefficiency of lactic acid evaporation comdenstion water among the prior art, cycle length, process complicacy, the big technical problem of investment. The lactic acid membrane dialysis system comprises a lactic acid membrane concentration system (2) and a membrane purification system (3), wherein the membrane purification system (3) is provided with a dialysis water inlet pipe for receiving dialysis water after superior treatment, a recycling pipe (7) for recycling low-concentration lactic acid solution and a dialysis water pipe II (6) for outputting the dialysis water. The utility model separates lactic acid in the lactic acid evaporation condensed water from components such as formic acid, acetic acid, water and the like, and simultaneously enriches and concentrates the lactic acid, thereby realizing the recycling of the lactic acid, improving the yield of the lactic acid in the production line and improving the economic value of the product; through the technology, COD in the effluent is greatly reduced, the effluent index is improved, water resources are continuously reused for water supplement of a production line, cyclic utilization of the water resources is realized, and the sewage treatment load and treatment cost of a factory are reduced.
Description
Technical Field
The utility model relates to a recovery unit of evaporation comdenstion water, concretely relates to device that lactic acid evaporation comdenstion water was retrieved.
Background
Lactic acid (IUPAC, scientific name: 2-hydroxypropionic acid) is a compound and an important industrial raw material, and is widely used in various industries such as chemical industry, medicine, food, printing and dyeing, textile, leather and the like. Lactic acid is a carboxylic acid of formula C 3 H 6 O 3 When a plurality of lactic acid molecules are brought together, the-OH groups and-COOH groups between adjacent molecules are subjected to dehydration condensation to form polylactic acid. Polylactic acid is also called polylactide, belongs to a polyester family, has sufficient and renewable raw material lactic acid sources, has no pollution in the production process, can be biodegraded, realizes the circulation in nature, and is an ideal green high polymer material.
Under the drive of environment-friendly bio-based materials, domestic and foreign enterprises continue to enter the field of lactic acid production, and in the production process of lactic acid, evaporation condensate water with high COD and low pH is generated in the evaporation concentration link, and the lactic acid content is usually more than 3 g/L. The wastewater is characterized by high organic matter content, easy decay, acidity and high salt content, and the high COD, low ph, lactic acid and the like can cause adverse effects on the sewage treatment environment, and the discharge into rivers or underground water systems can seriously destroy the ecological balance, so that the eutrophication of the water body can cause the oxygen deficiency of the water body, the deterioration of the water quality and the environmental pollution.
At present, no more popularization and application or external publication treatment schemes exist, enterprises still adopt the traditional biochemical, anaerobic and aeration treatment methods, and although the biochemical method is low in cost and simple to operate, the biochemical method occupies a large area, the wastewater treatment efficiency is low, the operation cost is high, and byproducts with additional values are less generated; in combination with the current national 'double-carbon' target background, the traditional water treatment process does not completely eliminate or fully utilize carbon sources, nitrogen sources and the like in a true sense, but converts the carbon sources, the nitrogen sources and the like into carbon dioxide, nitrogen oxides and the like which are discharged into the air from water through treatment modes such as biochemical oxidation and the like, and does not achieve the true-sense emission reduction. Therefore, the problem of carbon and nitrogen emission commonly existing in the lactic acid industry, the fermentation industry and the traditional water treatment field is urgently needed to be solved, and a new process technology capable of solving the resource utilization in the production process and the problem of waste water is formed.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a device that lactic acid evaporation comdenstion water was retrieved to solve the recovery unit inefficiency of lactic acid evaporation comdenstion water among the prior art, cycle length, process complicacy, the big technical problem of investment.
In order to achieve the above purpose, the utility model provides a following technical scheme:
the utility model provides a device for recovering lactic acid evaporation condensate water, which comprises a lactic acid membrane concentration system and a membrane purification system;
the lactic acid membrane concentration system is provided with a condensate water inlet pipe connected with a lactic acid evaporation condensate water pipe, a lactic acid outlet pipe used for outputting concentrated lactic acid and a dialysis water pipe I used for outputting dialysis water;
the membrane purification system is provided with a dialysis water inlet pipe for receiving dialysis water after superior treatment, a recycling pipe for recycling low-concentration lactic acid solution and a dialysis water pipe II for outputting the dialysis water;
the first dialysis water pipe is connected with the dialysis water inlet pipe, and one end, far away from the membrane purification system, of the reuse pipe is connected to the condensate water inlet pipe.
Optionally or preferably, a condensate water inlet pipe of the lactic acid membrane concentration system is further provided with a pretreatment system for controlling the inlet liquid temperature and flow rate of the condensate water.
Optionally or preferably, the system further comprises a control system, and the pretreatment system, the lactic acid membrane concentration system and the membrane purification system are respectively electrically connected with the control system.
Alternatively or preferably, the lactic acid membrane concentration system and the membrane purification system respectively adopt a continuous flow-through membrane filtration device.
Optionally or preferably, membrane elements in the lactic acid membrane concentration system and the membrane purification system are high-pollution-resistance roll type acid-resistant sanitary reverse osmosis membrane elements, and the NaCl rejection rate of the membrane elements is more than or equal to 99.5%.
Based on the technical scheme, the embodiment of the utility model provides a can produce following technological effect at least:
(1) the device for recovering the lactic acid evaporation condensed water separates the lactic acid in the lactic acid evaporation condensed water from components such as formic acid, acetic acid, water and the like, and simultaneously enriches and concentrates the lactic acid, thereby realizing the recovery and utilization of the lactic acid, improving the yield of the lactic acid in the production line and improving the economic value of the product; by the technology, COD in the discharged water is greatly reduced, the water discharge index is improved, water resources are continuously reused for water supplement of a production line, cyclic utilization of the water resources is realized, and the treatment load and treatment cost of the factory sewage are reduced; the resource utilization of the lactic acid evaporation condensate water and zero discharge of wastewater are comprehensively realized, and the project creates economic benefits for enterprises while solving problems. Concentrating lactic acid in the evaporated condensate from 4g/l to more than 200g/l, enabling the content of the lactic acid in the purified water to be below 0.05g/l, returning the concentrated lactic acid to a production line to be continuously processed into a lactic acid product, returning the membrane concentrated water to the production line to be used as production water or make up water by circulating water, recycling lactic acid resources, recycling water resources, and realizing zero emission.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the structures shown in the drawings without creative efforts.
Fig. 1 is a schematic structural diagram of embodiment 1 of the present invention;
fig. 2 is a schematic structural diagram of embodiment 2 of the present invention;
fig. 3 is a schematic flow chart of an embodiment of the present invention.
In the figure: 1. a pre-treatment system; 2. a lactic acid membrane concentration system; 3. a membrane purification system; 4. feeding condensed water into the pipe; 5. a lactic acid outlet pipe; 6. a second dialysis water pipe; 7. and (7) a recycling pipe.
Detailed Description
It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention. And it should be noted that like reference numerals and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, not all of the embodiments, and features in the following embodiments and examples may be combined with each other without conflict. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the following examples, both the lactic acid membrane concentration system and the membrane purification system employ an acid-resistant sanitary reverse osmosis membrane element having a NaCl rejection rate of not less than 99.5%, which is provided by fluid separation technologies ltd, and the specific parameters of the reverse osmosis membrane element are shown in table 1 below:
TABLE 1 reverse osmosis membrane element parameters
Example 1
As shown in fig. 1:
the utility model provides a device for recovering lactic acid evaporation condensate water, which comprises a lactic acid membrane concentration system 2 and a membrane purification system 3;
the lactic acid membrane concentration system 2 is provided with a condensed water inlet pipe 4 connected with a lactic acid evaporation condensed water pipeline, a lactic acid outlet pipe 5 used for outputting concentrated lactic acid and a dialysis water pipe I used for outputting dialysis water;
the membrane purification system 3 is provided with a dialysis water inlet pipe for receiving dialysis water after superior treatment, a recycling pipe 7 for recycling low-concentration lactic acid solution and a dialysis water pipe II 6 for outputting the dialysis water;
the first dialysis water pipe is connected with the dialysis water inlet pipe, and one end, far away from the membrane purification system 3, of the recycling pipe 7 is connected to the condensate water inlet pipe 4.
When the device is used, sewage to be treated enters the lactic acid membrane concentration system 2 through the condensate water inlet pipe 4, the sewage is divided into concentrated lactic acid solution and water after primary dialysis after treatment, the concentrated lactic acid solution is conveyed to a production line through the lactic acid outlet pipe 5 and is continuously processed into a lactic acid product, and the water after primary dialysis enters the dialysis water inlet pipe through the dialysis water inlet pipe I; and the secondary dialysis water is output by a dialysis water pipe II 6 and is used as production water or circulating water replenishing water of a production line.
More specifically, the device comprises the following processing steps:
s1, pretreatment
Sequentially carrying out temperature reduction and filtration pretreatment on S1 incoming water (lactic acid evaporation condensed water, the content of lactic acid is 4g/L) to obtain S1 effluent; the incoming water temperature of the lactic acid evaporation condensed water is 67 ℃, and the temperature is cooled to 35 ℃ through heat exchange, so that the retention rate of the concentration membrane on lactic acid is ensured, and the service life of a membrane element is ensured; the lactic acid evaporation condensate water after the temperature reduction treatment is pre-filtered by a security filter to remove suspended matter impurities, so that the water quality is clear;
s2, membrane concentration
Performing lactic acid concentration on the S1 outlet water by using an S2 lactic acid membrane concentration system 2 (a reverse osmosis membrane system, and specific data are shown in the following table 2) to obtain an S2 concentrated phase and an S2 clear phase; the operation pressure of an S2 membrane concentration system is 1.5-3.5MPa, and the membrane concentration temperature is 38 ℃; the content of lactic acid in the S2 concentrated phase is 2.64 percent, and a lactic acid product is produced by a lactic acid removing production line;
s3, membrane purification
Adjusting the pH of the S2 clear phase to 7.1 by using sodium hydroxide, and obtaining an S3 concentrated phase and a clear phase by using an S3 membrane purification system 3 (a reverse osmosis membrane purification system is adopted, and the specific data are shown in the following table 3); the operating pressure of the S3 membrane purification system is 1.5MPa, and the temperature is 32 ℃; and S3, the conductivity of the clear phase is 3us/cm, the clear phase is used as the water supplement of a production workshop, and the S3 concentrated phase is discharged into a sewage system workshop and then discharged.
The lactic acid membrane concentration system 2 and the membrane purification system 3 are operated in the device, and specific data of each liquid are shown in tables 2 and 3.
TABLE 2 reverse osmosis membrane concentration system for evaporation condensed water of lactic acid in example 1 (pressure grade < 4MPa)
TABLE 3 reverse osmosis membrane purification System for lactic acid evaporation condensate in example 1 (pressure rating < 2.5MPa)
Example 2
As shown in figure 2 of the drawings, in which,
compared to example 1, the present application also has the following differences:
as an optional embodiment, a condensed water inlet pipe 4 of the lactic acid membrane concentration system 2 is further provided with a pretreatment system 1 for controlling the inlet liquid temperature and flow rate of the condensed water.
The pretreatment system 1 is used for adjusting the liquid inlet temperature to 35-40 ℃, controlling the flow of condensed water entering the pipe 4 and matching with the treatment of the subsequent process.
As an optional embodiment, the system further comprises a control system, and the pretreatment system 1, the lactic acid membrane concentration system 2 and the membrane purification system 3 are respectively electrically connected with the control system.
The control system regulates and controls the regulation temperature of the pretreatment system 1, controls the input of condensed water, and manages the treatment process and the starting of the device of the lactic acid membrane concentration system 2 and the membrane purification system 3.
As an alternative embodiment, the lactic acid membrane concentration system 2 and the membrane purification system 3 each employ a continuous flow-through membrane filtration device.
The continuous flow-through membrane filtration device is a continuous flow-through membrane filtration device and a method which are invented by patent number ZL202010443535.1 of green and environment-friendly engineering Limited company in Sichuan, and the patent technology strictly controls the external conditions such as flow speed, temperature, pressure and the like in a membrane system, thereby realizing continuous, low-consumption, high-efficiency and long-period stable production of the membrane system.
As an optional implementation mode, the membrane elements in the lactic acid membrane concentration system 2 and the membrane purification system 3 are high-pollution-resistance roll type acid-resistant sanitary reverse osmosis membrane elements, and the NaCl rejection rate of the membrane elements is more than or equal to 99.5%.
The membrane element can tolerate more than 30% of lactic acid, the normal service life is more than 3 years, the membrane applies a high-pollution-resistance bionic structure flow channel to increase the pollution resistance of the membrane, and a support system continuously operates.
The structures, functions, and connections disclosed herein may be implemented in other ways. For example, the above described embodiments are merely illustrative, and for example, the lactic acid membrane concentration system 2 and the membrane purification system 3 may have other installation manners, for example, a plurality of components may be combined or integrated with another component; in addition, functional components in the embodiments herein may be integrated into one functional component, or each functional component may exist alone physically, or two or more functional components may be integrated into one functional component.
The above description is only for the specific embodiments of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art can easily think of the changes or substitutions within the technical scope of the present invention, and all should be covered within the protection scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (5)
1. The utility model provides a device that lactic acid evaporation comdenstion water was retrieved which characterized in that: comprises a lactic acid membrane concentration system (2) and a membrane purification system (3);
the lactic acid membrane concentration system (2) is provided with a condensed water inlet pipe (4) connected with a lactic acid evaporation condensed water pipeline, a lactic acid outlet pipe (5) used for outputting concentrated lactic acid and a dialysis water pipe I used for outputting dialysis water;
the membrane purification system (3) is provided with a dialysis water inlet pipe for receiving dialysis water after superior treatment, a recycling pipe (7) for recycling low-concentration lactic acid solution and a dialysis water pipe II (6) for outputting the dialysis water;
the first dialysis water pipe is connected with the dialysis water inlet pipe, and one end, far away from the membrane purification system (3), of the recycling pipe (7) is connected to the condensate water inlet pipe (4).
2. The apparatus for recovering lactic acid evaporation condensate as claimed in claim 1, wherein: and a condensed water inlet pipe (4) of the lactic acid membrane concentration system (2) is also provided with a pretreatment system (1) for controlling the liquid inlet temperature and flow of the condensed water.
3. The apparatus for recovering lactic acid evaporation condensate as claimed in claim 2, wherein: the device is characterized by further comprising a control system, wherein the pretreatment system (1), the lactic acid membrane concentration system (2) and the membrane purification system (3) are respectively electrically connected with the control system.
4. The apparatus for recovering lactic acid evaporation condensate as claimed in claim 1, wherein: the lactic acid membrane concentration system (2) and the membrane purification system (3) respectively adopt continuous flow-through membrane filtration devices.
5. The apparatus for recovering lactic acid evaporation condensate as claimed in claim 4, wherein: the membrane elements in the lactic acid membrane concentration system (2) and the membrane purification system (3) are high-pollution-resistance roll type acid-resistant sanitary reverse osmosis membrane elements, and the NaCl rejection rate of the membrane elements is more than or equal to 99.5%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221066746.9U CN217173354U (en) | 2022-05-06 | 2022-05-06 | Device for recovering lactic acid evaporation condensate water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221066746.9U CN217173354U (en) | 2022-05-06 | 2022-05-06 | Device for recovering lactic acid evaporation condensate water |
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| Publication Number | Publication Date |
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| CN217173354U true CN217173354U (en) | 2022-08-12 |
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| CN202221066746.9U Active CN217173354U (en) | 2022-05-06 | 2022-05-06 | Device for recovering lactic acid evaporation condensate water |
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- 2022-05-06 CN CN202221066746.9U patent/CN217173354U/en active Active
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