Device for recovering solvent in reverse extraction acid
By combining a high-shear reactor with a membrane filter, tributyl phosphate is extracted from sulfonated kerosene at low temperatures, solving the problem of solvent residue in phosphoric acid production, achieving efficient and safe solvent recovery, and reducing energy consumption and costs.
Patent Information
- Application Number
- CN202421008804.1
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-05-10
- Publication Date
- 2025-01-07
- Estimated Expiration
- 2034-05-10
AI Technical Summary
Existing technologies for phosphoric acid production suffer from the problem of residual organic solvents such as tributyl phosphate, leading to high processing costs, quality issues, and safety risks. Traditional methods are energy-intensive and require expensive equipment investment.
The device, which combines a high-shear reactor and a membrane filter, mixes phosphoric acid and sulfonated kerosene under low-temperature conditions using a high-shear stirrer. It utilizes the non-polar properties of sulfonated kerosene to extract organic matter, and combines reflux and membrane filtration technology to achieve efficient solvent recovery.
Under low temperature conditions, the extraction time is significantly shortened, energy consumption is reduced, raw material consumption is reduced, and the TOC content is reduced from 800ppm to below 20ppm, thereby improving safety and product quality.
Smart Images
Figure CN222304838U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the field of phosphoric acid purification industry, in particular to a device for recovering solvent in acid stripping. Background Art
[0002] In modern phosphoric acid production, especially wet phosphoric acid production, organic solvent extraction is often used to improve the purity of phosphoric acid, which enables phosphoric acid to meet industrial and even food grade standards. However, a common problem in this process is the residue of organic solvents such as tributyl phosphate, which not only increases the processing cost, but may also affect the quality of the final product.
[0003] At present, traditional methods such as increasing the residence time of the stripping section or using distillation to remove the solvent are not only energy-intensive, but also expensive in equipment investment and operating costs. More importantly, these methods have potential safety risks in operation, especially when dealing with solvent recovery under high temperature and high pressure conditions. Utility Model Content
[0004] In view of the deficiencies in the prior art, the purpose of the utility model is to provide a solvent recovery device in stripping acid, which can effectively remove organic solvents in stripping acid at a relatively low temperature, thereby reducing energy consumption, reducing operating costs, and improving safety.
[0005] A device for recovering solvent in stripping acid comprises a high shear reactor, wherein a high shear agitator is arranged inside the high shear reactor; the high shear reactor is connected to a phase separation tank through a mixing outlet pipe, a circulation reflux pipeline is connected above the phase separation tank, the end of the circulation reflux pipeline is connected to the front end of a sulfonated kerosene pipeline, the lower part of the phase separation tank is connected to a membrane filter through a stripping acid output pipeline, and the upper part of the membrane filter is connected to the phase separation tank through an organic concentrated phase pipeline.
[0006] A stripping acid inlet pipe is connected above the high shear reactor.
[0007] The high shear stirrer is connected to the end of the sulfonated kerosene pipe.
[0008] An extraction solvent output pipeline is also connected above the phase separation tank.
[0009] A high-purity stripping acid outlet is also connected below the membrane filter.
[0010] The beneficial effects of the utility model are as follows:
[0011] The high shear reactor ensures that phosphoric acid and sulphonated kerosene are fully mixed, reducing the time required to reach extraction equilibrium from 30-40 minutes to 3-5 minutes.
[0012] The circulation reflux pipeline allows part of the sulfonated kerosene to be circulated back to the reactor to participate in the extraction again, thus reducing the consumption of raw materials.
[0013] This device is specially designed to operate under low temperature conditions of 30-40℃ through a high shear reactor, using sulfonated kerosene to fully mix with stripping acid to effectively extract and remove organic matter such as tributyl phosphate dissolved in the stripping acid, so that the total organic carbon (TOC) content in phosphoric acid is reduced from more than 800ppm to less than 20ppm. BRIEF DESCRIPTION OF THE DRAWINGS
[0014] Figure 1 : Schematic diagram of the structure of this device.
[0015] Explanations in the figure: 1. High shear reactor; 2. Phase separation tank; 3. High shear agitator; 4. Stripping acid inlet pipe; 5. Sulfonated kerosene pipe; 6. Mixing outlet pipe; 7. Circulation reflux pipe; 8. Extraction solvent output pipe; 9. Stripping acid output pipe; 10. Membrane filter; 11. Organic concentrated phase pipe. DETAILED DESCRIPTION
[0016] The implementation scheme of the utility model will be described in detail below in conjunction with examples. The following examples are only used to illustrate the utility model and should not be regarded as limiting the scope of the utility model.
[0017] Example 1
[0018] A device for recovering solvent in stripping acid comprises a high shear reactor 1, wherein a high shear stirrer 3 is arranged inside the high shear reactor 1; the high shear reactor 1 is connected to a phase separation tank 2 via a mixing outlet pipe 6, a circulation reflux pipeline 7 is connected above the phase separation tank 2, the end of the circulation reflux pipeline 7 is connected to the front end of a sulfonated kerosene pipe 5, the lower part of the phase separation tank 2 is connected to a membrane filter 10 via a stripping acid output pipeline 9, and the upper part of the membrane filter 10 is connected to the phase separation tank 2 via an organic dense phase pipeline 11.
[0019] The high shear reactor 1 is connected with a stripping acid inlet pipe 4 above.
[0020] The high shear stirrer 3 is connected to the end of the sulfonated kerosene pipe 5 .
[0021] An extraction solvent output pipeline 8 is also connected above the phase separation tank 2 .
[0022] The membrane filter 10 is also connected to a high-purity stripping acid outlet below.
[0023] Example 2
[0024] Using the device of Example 1, the stripping acid (phosphoric acid) with a TOC greater than 800 ppm enters the high shear reactor 1 through the stripping acid inlet pipe 4, and the sulfonated kerosene enters the high shear agitator 3 through the sulfonated kerosene pipe 5. Under the low temperature condition of 30-40°C, the stripping acid and the sulfonated kerosene are fully mixed by the strong shear force of the high shear agitator 3. This process utilizes the non-polar characteristics of the sulfonated kerosene to effectively extract organic substances such as tributyl phosphate from phosphoric acid.
[0025] The mixture is transported from the high shear reactor 1 to the phase separation tank 2 through the mixing outlet pipe 6 and allowed to stand for stratification. During this process, the heavier stripping phosphoric acid is deposited at the bottom, while the lighter organic phase rich in sulfonated kerosene floats on the upper layer. The circulation reflux pipe 7 recycles part of the upper organic phase of the phase separation tank 2 back to the high shear reactor 1 to participate in the extraction process again, thereby optimizing the use efficiency of the sulfonated kerosene. The extraction solvent output pipe 8 is drawn out from the upper layer of the phase separation tank 2, and part of the solvent rich in sulfonated kerosene is sent to an external process for further phosphoric acid treatment. The stripping acid output pipe 9 is drawn out from the bottom of the phase separation tank 2 and enters the membrane filter 10 to obtain high-purity stripping acid with a TOC of less than 20 ppm for further processing and utilization. The organic-rich concentrated phase obtained by membrane separation is returned to the phase separation tank 2 through the organic concentrated phase pipe 11.
Claims
1. A device for recovering solvent in stripping acid, characterized in that: The invention comprises a high shear reactor (1), wherein a high shear stirrer (3) is installed inside the high shear reactor (1); the high shear reactor (1) is connected to a phase separation tank (2) via a mixing outlet pipe (6); a circulation reflux pipeline (7) is connected above the phase separation tank (2); the end of the circulation reflux pipeline (7) is connected to the front end of a sulfonated kerosene pipe (5); the lower part of the phase separation tank (2) is connected to a membrane filter (10) via a stripping acid output pipeline (9); and the upper part of the membrane filter (10) is connected to the phase separation tank (2) via an organic concentrated phase pipeline (11).
2. The device for recovering solvent in stripping acid according to claim 1, characterized in that: The high shear reactor (1) is connected to a stripping acid inlet pipe (4) above.
3. The device for recovering solvent in stripping acid according to claim 1, characterized in that: The high shear stirrer (3) is connected to the end of the sulfonated kerosene pipe (5).
4. The device for recovering solvent in stripping acid according to claim 1, characterized in that: An extraction solvent output pipeline (8) is also connected above the phase separation tank (2).
5. The device for recovering solvent in stripping acid according to claim 1, characterized in that: A high-purity stripping acid outlet is also connected below the membrane filter (10).