Separation and purification system
By combining the dehydration vaporization unit and purification unit of the separation and purification system with concentration treatment, the problems of low efficiency and high energy consumption in the separation of organic matter and water in traditional methods are solved, and high-purity organic compounds are purified efficiently and produced at low cost.
Patent Information
- Application Number
- CN202520515852.8
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2025-03-21
- Publication Date
- 2026-03-06
- Estimated Expiration
- 2035-03-21
AI Technical Summary
Existing technologies suffer from low separation efficiency, high energy consumption, or secondary pollution in the separation of organic matter and water, especially in microemulsions or high-viscosity systems where permeability is poor, and traditional methods are also costly.
A separation and purification system is adopted, including a dehydration vaporization unit, a purification unit, and a concentration unit. Organic compounds are vaporized through heating and stirring and purified by a distillation column. Combined with a dehydration agent supply unit, the separation efficiency is improved and the cost is reduced.
It achieves efficient separation and purification, resulting in high purity organic compound products, reduced energy consumption and secondary pollution, and improved process economy.
Smart Images
Figure CN223969515U_ABST
Abstract
Description
Technical Field
[0001] This invention relates to separation systems, and more particularly to a system for separating and purifying mixed solutions of organic compounds and water. Background Technology
[0002] In fields such as chemical synthesis, biomass extraction, and petrochemicals, the efficient separation of organic matter from water is a core element in ensuring product purity and improving process economics. Traditional dehydration technologies generally suffer from low separation efficiency, high energy consumption, or secondary pollution, making it difficult to meet increasingly stringent industrial demands.
[0003] A common dehydration method in existing technologies is to adsorb water using porous materials such as molecular sieves and silica gel. However, these materials have limited adsorption capacity (typically <30% of their own weight), requiring frequent regeneration, and have poor permeability to microemulsions or high-viscosity systems, easily leading to the loss of organic phase. Another method is to introduce azeotropic agents such as toluene and cyclohexane to carry water away during evaporation. This method requires secondary treatment of azeotropic agent residues, increasing energy consumption and cost.
[0004] In addition, there is the method of using pervaporation membranes for water removal. Although pervaporation membranes are highly selective for low concentrations of water (<10%), the flux drops sharply (<5L / m³) when treating systems with high water content. 2 ·h), and membrane modules are expensive. Utility Model Content
[0005] To overcome at least one of the defects of the prior art, one embodiment of the present invention provides a separation and purification system, including a dehydration vaporization unit and a purification unit; the dehydration vaporization unit is used to remove at least part of the water in a first solution containing water and organic compounds, and to convert some or all of the organic compounds in the first solution into a gaseous state, to obtain a dehydrated product and a gas containing organic compounds; the purification unit is used to purify the gas containing organic compounds or to condense the gas containing organic compounds into a liquid before purification.
[0006] According to one embodiment of the present invention, the separation and purification system further includes a concentration unit, which is connected to the dehydration vaporization unit and is used to concentrate the second solution containing water and organic compounds to obtain a first solution.
[0007] According to one embodiment of the present invention, the concentration unit includes a dehydration device.
[0008] According to one embodiment of the present invention, the dehydration device is a distillation column, and the concentration unit further includes a first cooling device connected to the distillation column.
[0009] According to one embodiment of the present invention, the system includes a dehydrating agent supply unit for supplying a dehydrating agent to the dehydration vaporization unit to remove at least a portion of the water in the first solution; and / or,
[0010] The dewatering vaporization unit includes a containment chamber, a heating component, and a stirring component.
[0011] According to one embodiment of the present invention, the dewatering vaporization unit includes a dryer.
[0012] According to one embodiment of the present invention, the dryer is a single cone dryer, a spiral dryer, a paddle dryer, a vacuum disc dryer, a vacuum rotary flash dryer, a vacuum rake dryer, or a vacuum belt dryer.
[0013] According to one embodiment of the present invention, the purification unit includes a distillation column, which is connected to the dewatering vaporization unit.
[0014] According to one embodiment of the present invention, the purification unit further includes a second cooling device and a condensate storage device. The second cooling device is used to cool the gas containing the organic compound to obtain a condensate containing the organic compound. The condensate storage device is used to store the condensate containing the organic compound and is connected to the second cooling device and the distillation column respectively.
[0015] The separation and purification system of this utility model, through processing a solution containing water and organic compounds, can obtain a high concentration of organic compound products. Attached Figure Description
[0016] The accompanying drawings are for illustrative purposes only and are not intended to limit the scope of this invention.
[0017] in:
[0018] Figure 1 This is a schematic diagram of the separation and purification system according to one embodiment of the present invention;
[0019] Figure 2 This is a schematic diagram of the separation and purification system according to another embodiment of the present invention;
[0020] The annotations in the attached figures are explained as follows:
[0021] 11. Dehydration device; 12. First cooling device; 21. Dryer; 31. Distillation column; 32. Second cooling device; 33. Condensate storage device; 40. Dehydrating agent supply unit. Detailed Implementation
[0022] Typical embodiments embodying the features and advantages of this utility model will be described in detail in the following description. It should be understood that this utility model can have various variations in different embodiments, all of which do not depart from the scope of this utility model, and the description herein is for illustrative purposes only and not intended to limit this utility model.
[0023] One embodiment of this utility model provides a separation and purification system for separating and purifying a first solution containing water and organic compounds (i.e., an aqueous solution of organic compounds). The system includes a dehydration vaporization unit and a purification unit. The dehydration vaporization unit is used to remove at least part of the water in the first solution and convert some or all of the organic compounds in the first solution into a gaseous state (vaporization treatment) to separate them from most of the water, obtaining a dehydrated product and a gas containing organic compounds. The purification unit is used to purify the gas containing organic compounds (or the gas enriched with organic compounds) or to condense the gas containing organic compounds into a liquid before purification.
[0024] In one embodiment, the separation and purification system further includes a concentration unit connected to the dehydration vaporization unit, used to concentrate a second solution containing low concentrations of water and organic compounds to obtain a first solution. The first solution is then passed into the dehydration vaporization unit for further processing.
[0025] In one embodiment, the content of organic compounds in the first solution is higher than that in the second solution. The first solution can be a concentrate of the second solution, meaning that the two solutions contain the same types of organic compounds but at different concentrations (or different contents of organic compounds). Further, the content of organic compounds in the first solution can be above 40 wt%, and the content of organic compounds in the second solution can be below 30 wt%. The lower concentration of the second solution can be adjusted to a suitable concentration of the first solution through a concentration unit, followed by dehydration and vaporization treatment to facilitate the related processes.
[0026] In one embodiment, the organic compound may be pentanediamine, butanediamine, piperidine, pyridine, acetic acid, acetone, isobutanol, or ethanol, etc. The structure and operation of the separation and purification system will be further described below using an aqueous solution of the above-mentioned organic compound as the first solution or the second solution.
[0027] Reference Figure 1 , 2 As shown, in one embodiment, the concentration unit includes a dehydration device 11, which can be an existing device for removing water.
[0028] In one embodiment, the dehydration device 11 is a distillation column for dehydration. Further, the concentration unit includes a first cooling device 12, which may be a heat exchanger. The first cooling device 12 is connected to the dehydration device 11, and can first pass the second solution through the dehydration device 11 to obtain a mixed gas containing organic compounds and water vapor, and then pass the mixed gas through the first cooling device 12 for cooling to obtain the first solution.
[0029] In one embodiment, the concentration unit is connected to the dehydration vaporization unit so that the first solution from the concentration unit is passed into the dehydration vaporization unit for separation of organic compounds from water (e.g., pentanediamine, butanediamine, piperidine, pyridine, acetic acid, acetone, isobutanol, or ethanol and water).
[0030] In one embodiment, in the dehydration vaporization unit, a dehydrating agent can be added to the first solution for dehydration treatment to reduce the water content in the system. The dehydrating agent can be a physical dehydrating agent that absorbs water through physical action, or a chemical dehydrating agent that removes water through chemical reaction.
[0031] In one embodiment, the water removal treatment can be carried out under the action of stirring and heating.
[0032] In one embodiment, in the dewatering vaporization unit, most of the organic compounds in the system can be converted into gaseous substances and enriched in the gas phase by heating, thus obtaining a gas enriched with organic compounds (i.e., a gas containing organic compounds).
[0033] In one embodiment, the dehydration and vaporization unit includes a containment chamber, a heating element, and a stirring element. A first solution can be placed in the containment chamber and subjected to dehydration and vaporization treatment, optionally using the heating element and / or the stirring element.
[0034] In one embodiment, the dewatering vaporization unit includes a dryer 21. The dryer 21 may be, for example, a single cone dryer, a spiral dryer, a paddle dryer, a vacuum disc dryer, a vacuum rotary flash dryer, a vacuum rake dryer, or a vacuum belt dryer.
[0035] In one embodiment, the purification unit is connected to the dehydration vaporization unit and is used to purify the gas enriched with organic compounds discharged from the dehydration vaporization unit or to condense the gas enriched with organic compounds into a liquid before purification.
[0036] In one implementation, reference Figure 1 , 2 As shown, the purification unit includes a distillation column 31, which is connected to a dehydration vaporization unit. The gas enriched with organic compounds discharged from the dehydration vaporization unit can be directly passed into the distillation column 31 for purification to obtain a high-purity organic compound product.
[0037] In one embodiment, the top of the distillation column 31 is connected to a concentration unit or a dehydration vaporization unit, so that a small amount of mixed gas of organic compounds and water discharged from the top of the column can be sent to the concentration unit, or the mixed gas can be condensed and sent to the dehydration vaporization unit for reuse, so as to further recover and purify the organic compounds therein.
[0038] In one implementation, reference Figure 2 As shown, the purification unit further includes a second cooling device 32 and a condensate storage device 33, which are disposed between the dehydration vaporization unit and the distillation column 31. The second cooling device 32 is used to cool the gas enriched with organic compounds discharged from the dehydration vaporization unit to obtain a condensate containing organic compounds; the condensate storage device 33 is used to store the condensate containing organic compounds, so that it can be sent to the distillation column 31 for purification as needed.
[0039] In one embodiment, the second cooling device 32 may be a heat exchanger, and the condensate storage device 33 may be a storage tank.
[0040] In one embodiment, the second cooling device 32 is connected to the dryer 21 of the dewatering vaporization unit, and the condensate storage device 33 is connected to the second cooling device 32 and the distillation column 31 respectively.
[0041] In one embodiment, the separation and purification system further includes a dehydrating agent supply unit 40 for supplying a dehydrating agent to the dehydration vaporization unit. Further, the dehydrating agent supply unit 40 is connected to the dehydration vaporization unit (e.g., connected to the dryer 21), and the dehydrating agent can be transported from the dehydrating agent supply unit 40 to the dehydration vaporization unit via a discharge port or a pipeline connected to the discharge port.
[0042] In one embodiment, the dehydrating agent supply unit 40 may include a silo.
[0043] In one embodiment, corresponding control valves are installed on multiple connecting pipelines of the system to control the flow and cut-off of corresponding material passages. For example, control valves are installed on the connecting pipeline between the dehydrating agent supply unit 40 and the dryer 21.
[0044] The separation and purification system of this utility model is suitable for separating and purifying solutions containing water and organic compounds, and can obtain high-purity organic compound products.
[0045] The separation and purification system of one embodiment of this utility model can improve the purification efficiency of organic compounds.
[0046] The separation and purification system of this utility model can provide dehydrating agent to the dehydration vaporization unit through a dehydrating agent supply unit. The raw materials for the dehydrating agent are widely available and low in cost. At the same time, the product after reacting with water may also generate added value.
[0047] The following description, in conjunction with the embodiments and accompanying drawings, further illustrates the use of a separation and purification system according to one embodiment of the present invention.
[0048] Example 1: Separation and purification of pentamethylenediamine
[0049] S1: A dehydrating agent is added to the dryer 21 (spiral dryer) through the dehydrating agent supply unit 40. At the same time, an 80wt% pentanediamine aqueous solution is introduced into the dryer 21, heated and stirred to continuously reduce the moisture content of the pentanediamine aqueous solution. Then, under the action of high temperature heating, pentanediamine is continuously enriched into the gas phase to obtain dehydrated products and gas enriched with pentanediamine. The dehydrated products are discharged through the outlet at the bottom of the dryer 21.
[0050] S2: The gas enriched with pentanediamine is passed into distillation column 31 for distillation to obtain pentanediamine product with a purity of 99.9%.
[0051] Example 2: Separation and purification of butanediamine
[0052] S1: A dehydrating agent is added to the dryer 21 (double cone dryer) through the dehydrating agent supply unit 40. At the same time, a 70wt% butanediamine aqueous solution is introduced into the dryer 21, heated and stirred to continuously reduce the moisture content of the butanediamine aqueous solution. Then, under the action of high temperature heating, butanediamine is continuously enriched into the gas phase to obtain dehydrated products and gas enriched with butanediamine. The dehydrated products are discharged through the outlet at the bottom of the dryer 21.
[0053] S2: The gas enriched with butanediamine is passed into distillation column 31 for distillation to obtain butanediamine product with a purity of 99.9%.
[0054] Example 3: Isolation and purification of piperidine
[0055] S1: A 25wt% piperidine aqueous solution is passed into the concentration unit and successively processed by the dehydration device 11 and the first cooling device 12 to obtain a concentrated solution with a concentration of more than 60wt%.
[0056] S2: The concentrate is fed into the dryer 21 (paddle dryer), and a dehydrating agent is added to the dryer 21 through the dehydrating agent supply unit 40. The mixture is heated and stirred to continuously reduce the moisture content of the concentrate. Then, piperidine is continuously enriched into the gas phase under high temperature heating to obtain dehydrated products and gas enriched with piperidine. The dehydrated products are discharged through the outlet at the bottom of the dryer 21.
[0057] S3: The gas enriched with piperidine is passed into distillation column 31 for distillation to obtain a piperidine product with a purity of 99.9%.
[0058] Example 4: Isolation and purification of pyridine
[0059] S1: A 10wt% pyridine aqueous solution is passed into the concentration unit and successively processed by the dehydration device 11 and the first cooling device 12 to obtain a concentrated solution with a concentration of more than 90wt%.
[0060] S2: A dehydrating agent is added to the dryer 21 (disc dryer) through the dehydrating agent supply unit 40, and the concentrate is sent into the dryer 21 at the same time. The concentrate is heated and stirred to continuously reduce the water content. Then, pyridine is continuously enriched into the gas phase under high temperature heating to obtain dehydrated products and pyridine-enriched gas. The dehydrated products are discharged through the outlet at the bottom of the dryer 21.
[0061] S3: The pyridine-enriched gas is passed into distillation column 31 for distillation to obtain a pyridine product with a purity of 99.9%.
[0062] Example 5: Separation and purification of ethanol
[0063] S1: A dehydrating agent is added to the dryer 21 (vacuum rake dryer) through the dehydrating agent supply unit 40. At the same time, an ethanol aqueous solution with a concentration of 90wt% is introduced into the dryer 21, heated and stirred to continuously reduce the water content of the ethanol aqueous solution. Then, under the action of high temperature heating, ethanol is continuously enriched into the gas phase to obtain dehydrated product and gas enriched with ethanol. The dehydrated product is discharged through the outlet at the bottom of the dryer 21.
[0064] S2: The gas enriched with ethanol is passed into distillation column 31 for distillation to obtain an ethanol product with a purity of 99.9%.
[0065] Example 6: Separation and purification of isobutanol
[0066] S1: A 60wt% isobutanol aqueous solution is introduced into dryer 21 (paddle dryer), and simultaneously a dehydrating agent is added to dryer 21 through dehydrating agent supply unit 40. The mixture is heated and stirred to continuously reduce the water content of the isobutanol aqueous solution. Subsequently, isobutanol is continuously enriched into the gas phase under high temperature heating to obtain dehydrated product and gas enriched with isobutanol. The dehydrated product is discharged through the outlet at the bottom of dryer 21.
[0067] S2: The gas enriched with isobutanol is passed into distillation column 31 for distillation to obtain isobutanol product with a purity of 99.8%.
[0068] Example 7: Separation and purification of acetic acid
[0069] S1: An aqueous solution of acetic acid with a concentration of 2wt% is passed into the concentration unit and successively processed by the dehydration device 11 and the first cooling device 12 to obtain a concentrated solution with a concentration of more than 40wt%.
[0070] S2: After adding dehydrating agent to dryer 21 (spiral dryer) through dehydrating agent supply unit 40, the concentrate is simultaneously sent into dryer 21, heated and stirred to continuously reduce the water content of the concentrate; then, acetic acid is continuously enriched into the gas phase under high temperature heating to obtain dehydrated product and gas enriched with acetic acid; the dehydrated product is discharged through the outlet at the bottom of dryer 21.
[0071] S3: The gas enriched with acetic acid is passed into distillation column 31 for distillation to obtain acetic acid product with a purity of 99.7%.
[0072] Example 8: Separation and purification of acetone
[0073] S1: A dehydrating agent is added to the dryer 21 (double cone dryer) through the dehydrating agent supply unit 40. At the same time, an acetone aqueous solution with a concentration of 80wt% is introduced into the dryer 21, heated and stirred to continuously reduce the water content of the acetone aqueous solution. Then, under the action of high temperature heating, acetone is continuously enriched into the gas phase to obtain dehydrated products and acetone-enriched gas. The dehydrated products are discharged through the outlet at the bottom of the dryer 21.
[0074] S2: The acetone-enriched gas is passed into distillation column 31 for distillation to obtain acetone product with a purity of 99.9%.
[0075] Unless otherwise specified, the terms used in this utility model have the meanings commonly understood by those skilled in the art.
[0076] The embodiments described in this utility model are for illustrative purposes only and are not intended to limit the scope of protection of this utility model. Those skilled in the art can make various other substitutions, changes and improvements within the scope of this utility model. Therefore, this utility model is not limited to the above embodiments, but is only defined by the claims.
Claims
1. A separation purification system characterized by, The separation and purification system comprises: a water removal vaporization unit for removing at least part of water in a first solution containing water and organic compounds and converting part or all of the organic compounds in the first solution into a gas state to obtain a water removal product and a gas containing organic compounds; and a purification unit for purifying the gas containing organic compounds or condensing the gas containing organic compounds into a liquid and then purifying the liquid. The separation and purification system further comprises a concentration unit connected to the water removal vaporization unit for concentrating a second solution containing water and organic compounds to obtain the first solution.
2. The system of claim 1, wherein, The concentration unit comprises a dehydration device.
3. The system of claim 2, wherein, The dehydration device is a rectifying tower, and the concentration unit further comprises a first cooling device connected to the rectifying tower.
4. The system of claim 3, wherein, The separation and purification system comprises a water removal agent supply unit for supplying a water removal agent to the water removal vaporization unit to remove at least part of water in the first solution; and / or 5. The system of claim 1, wherein, The water removal vaporization unit comprises a containing cavity, a heating component and a stirring component. The water removal vaporization unit comprises a dryer.
6. The system of claim 1, wherein, The dryer is a single-cone dryer, a spiral dryer, a paddle dryer, a vacuum disc dryer, a vacuum rotary flash dryer, a vacuum rake dryer or a vacuum belt dryer.
7. The system of claim 6, wherein, The purification unit comprises a rectifying tower connected to the water removal vaporization unit.
8. The system of claim 1, wherein, The purification unit further comprises a second cooling device for cooling the gas containing organic compounds to obtain a condensed liquid containing organic compounds, and a condensed liquid storage device for storing the condensed liquid containing organic compounds, the condensed liquid storage device being connected to the second cooling device and the rectifying tower, respectively.
9. The system of claim 8, wherein,