CN214270726U - Stearic acid recycling treatment device - Google Patents
Stearic acid recycling treatment device Download PDFInfo
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- CN214270726U CN214270726U CN202022470947.2U CN202022470947U CN214270726U CN 214270726 U CN214270726 U CN 214270726U CN 202022470947 U CN202022470947 U CN 202022470947U CN 214270726 U CN214270726 U CN 214270726U
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- stearic acid
- distillation tower
- oil furnace
- oleic acid
- heat conduction
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A stearic acid recycling treatment device comprises a preheater, a primary distillation tower, a heat conduction oil furnace, a secondary distillation tower and a seal tank. Wherein, the pre-heater the one-level distillation column the heat conduction oil furnace the second grade distillation column with be equipped with material transfer mechanism between the seal pot, compare in prior art, the utility model discloses can effectively balance the productivity difference between stearic acid and the oleic acid, when solving the stearic acid productivity surplus, provide fuel gain effect to the oleic acid production operation, make and carry out complementally between surplus resource and the scarce resource, form the virtuous circle of oleic acid production industry.
Description
Technical Field
The utility model belongs to the technical field of chemical industry equipment, concretely relates to stearic acid processing apparatus that recycles.
Background
In the rectification and purification production process of the oleic acid raw material, the oleic acid raw material is separated by a crystallization filter pressing method or a rectification method, and then stearic acid and a high-purity oleic acid product are obtained through multiple filter pressing or distillation operations. Therefore, when high-purity oleic acid is produced every time, a large amount of stearic acid byproducts are inevitably obtained, and when the byproducts are utilized, the byproducts are often sold at low price as cosmetic raw materials due to high impurity content, and for oleic acid production enterprises, the industrial span of the cosmetic field is large, the market demand is single, the stearic acid is not fully utilized, and the condition of excess stearic acid capacity is caused; and the domestic stearic acid market is always in a competitive and over-demand environment, the high-purity oleic acid is in a state of insufficient capacity, and the oleic acid purification process is accompanied by the production accumulation of a large amount of stearic acid, so that the production operation of the high-purity oleic acid is inhibited in turn, and the negative effects on the yield of scarce resources and the virtuous cycle of the market are caused. Therefore, a technical scheme for reasonably utilizing stearic acid is needed in the existing oleic acid purification process.
SUMMERY OF THE UTILITY MODEL
In order to solve the problem that exists among the above-mentioned prior art, the utility model provides a stearic acid processing apparatus that recycles, including pre-heater, one-level distillation column, heat conduction oil furnace, second grade distillation column, seal pot. Wherein a material transfer mechanism is arranged between the preheater, the primary distillation tower, the heat-conducting oil furnace, the secondary distillation tower and the seal tank, the material transfer mechanism is connected to the combustion position of the heat-conducting oil furnace, and
further, the heat-conducting oil furnace is heated by burning natural gas.
Further, the working temperature of the primary distillation tower is 220-240 ℃.
Further, the working temperature of the secondary distillation tower is 240-260 ℃.
The utility model has the advantages that:
1. the utility model discloses a pre-heater, heat conduction oil furnace, a plurality of distillation columns and between them material transfer mechanism form the cyclic utilization mode, utilize the flammability of stearic acid directly to the distillation columns at different levels of oleic acid refining operation, the pre-heater provides the heat, when fully consuming unnecessary stearic acid by-product, has practiced thrift a large amount of fuel costs for the distillation operation, compares in prior art, the utility model discloses can effectively balance the productivity gap between stearic acid and the oleic acid, when solving the stearic acid productivity surplus, provide fuel gain effect to oleic acid production operation, make and carry out complementally between surplus resource and the scarce resource, form the virtuous circle of oleic acid production industry.
2. The utility model discloses when practicing thrift the natural gas cost, the result that carries out the burning as fuel to stearic acid only is carbon dioxide and water to can break away from the natural gas supply completely in the production later stage, implement self-loopa heating with the stearic acid burning of isolation result, be a novel technical scheme of clean environmental protection, energy-conservation province material, have better marketing meaning.
Drawings
Fig. 1 is a schematic structural diagram of the present invention;
FIG. 2 is a flow chart of the present invention;
fig. 3 is a schematic view of the process of recycling stearic acid in the present invention.
Detailed Description
The present invention will be described in further detail with reference to the drawings and examples.
As shown in the figure 1-2, the stearic acid recycling treatment device comprises a preheater 1, a primary distillation tower 2, a heat conduction oil furnace 3, a secondary distillation tower 4 and a seal tank 5. Wherein, a material transfer mechanism is arranged between the preheater 1, the primary distillation tower 2, the heat-conducting oil furnace 3, the secondary distillation tower 4 and the seal pot 5, the material transfer mechanism is connected to the combustion position of the heat-conducting oil furnace, the heat-conducting oil furnace 3 is heated by the combustion of natural gas, the working temperature of the primary distillation tower 2 is 220-260 ℃, and the working temperature of the secondary distillation tower 4 is 240-260 ℃.
The utility model discloses a concrete function is implemented to following step:
(1) preheating and dehydrating: adding mixed fatty acid into a preheater 1 for preheating, heating a heat conduction oil furnace 3 by taking natural gas as fuel, raising the temperature of the connected preheater 1 to 80 ℃, controlling the system vacuum degree in the preheater 1, evaporating and removing gas, water and volatile components in the mixed fatty acid, and simultaneously obtaining dehydrated mixed liquid in the preheater 1.
(2) Primary distillation: and (2) adding the dehydrated mixed solution in the step (1) into a primary distillation tower 2 through a material transfer mechanism, heating the heat-conducting oil furnace 3 by taking natural gas as fuel, raising the temperature of the connected primary distillation tower 2 to the range of 220-240 ℃, controlling the vacuum degree in the primary distillation tower 2, condensing and collecting to obtain a stearic acid mixture with a lower boiling point, and simultaneously obtaining a heavy-phase mixed solution in the primary distillation tower 2.
(3) And (3) combustion of stearic acid: and (3) taking out the stearic acid mixture in the step (2), heating, controlling the temperature to be 70-80 ℃ to inject the stearic acid mixture into the heat-conducting oil furnace 3 in a liquid phase form, igniting to burn, and conducting heat to the secondary distillation tower 4 by taking the heat-conducting oil as a medium.
(4) Secondary distillation: and (3) adding the heavy phase mixed solution in the step (2) into a secondary distillation tower 4 through a material transfer mechanism, burning and heating the heat-conducting oil furnace 3 by taking stearic acid as fuel in the step (3), raising the temperature of the connected secondary distillation tower 4 to 240-260 ℃, controlling the vacuum degree in the secondary distillation tower 4, and condensing and collecting to obtain a light component, namely the high-purity oleic acid.
(5) And (3) recovering stearic acid: after the combustion heating operation in the step (4) is finished, taking out the residual part of the stearic acid, placing the residual part into a container, controlling the temperature to be less than or equal to 60 ℃, condensing the residual part to form solid-phase fuel, and storing the solid-phase fuel in a sealed tank 5 at a cool and dry place; before preheating operation is carried out on the next batch of mixed fatty acid, the solid phase fuel is taken out and heated, the temperature is controlled to be 70-80 ℃ to form a liquid phase, the liquid phase is injected into a heat conduction oil furnace for ignition and combustion, then stearic acid is used as a main fuel, heat is carried out on the preheater 1 in the step (1), the primary distillation tower 2 in the step (2) and the secondary distillation tower 4 in the step (4) by taking heat conduction oil as a medium, and the operation is repeatedly carried out in the same way of the step (1), the step (2) and the step (4), so that the stearic acid completely replaces natural gas for combustion and heating (as shown in figure 3), and continuous production operation is carried out.
The above-mentioned embodiments are merely preferred embodiments of the present invention, and are not intended to limit the present invention in any form, so that any person skilled in the art can make modifications and equivalent changes within the scope of the claims of the present invention.
Claims (4)
1. A stearic acid recycling treatment device comprises a preheater, a primary distillation tower, a heat conduction oil furnace, a secondary distillation tower and a seal tank, and is characterized in that a material transfer mechanism is arranged among the preheater, the primary distillation tower, the heat conduction oil furnace, the secondary distillation tower and the seal tank, and the material transfer mechanism is connected to the combustion position of the heat conduction oil furnace.
2. The apparatus of claim 1, wherein the heat-conducting oil furnace is heated by combustion of natural gas.
3. The apparatus for recycling stearic acid according to claim 1, wherein the primary distillation column is operated at 220-240 ℃.
4. The apparatus for recycling stearic acid according to claim 1, wherein the secondary distillation column is operated at 240-260 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022470947.2U CN214270726U (en) | 2020-10-30 | 2020-10-30 | Stearic acid recycling treatment device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022470947.2U CN214270726U (en) | 2020-10-30 | 2020-10-30 | Stearic acid recycling treatment device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214270726U true CN214270726U (en) | 2021-09-24 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022470947.2U Active CN214270726U (en) | 2020-10-30 | 2020-10-30 | Stearic acid recycling treatment device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214270726U (en) |
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2020
- 2020-10-30 CN CN202022470947.2U patent/CN214270726U/en active Active
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Address after: 332500 high tech chemical park, Hukou County, Jiujiang City, Jiangxi Province Patentee after: Jiangxi Runda New Material Co.,Ltd. Address before: 332500 high tech chemical park, Hukou County, Jiujiang City, Jiangxi Province Patentee before: Jiujiang Kerun New Material Co.,Ltd. |