CN212669584U - Production device for extracting sodium acetate in furfural production - Google Patents
Production device for extracting sodium acetate in furfural production Download PDFInfo
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- CN212669584U CN212669584U CN202021384267.2U CN202021384267U CN212669584U CN 212669584 U CN212669584 U CN 212669584U CN 202021384267 U CN202021384267 U CN 202021384267U CN 212669584 U CN212669584 U CN 212669584U
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- sodium acetate
- pipeline
- neutralization
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Abstract
The utility model relates to an extract apparatus for producing of sodium acetate in furfural production, include flash tank, neutralization tank, evaporating pot, decoloration jar, crystallizer, the centrifuge that communicates in order through the pipeline. The utility model is convenient for recovering sodium acetate from alkaline sodium acetate solution by arranging a flash tank, a neutralization tank, an evaporation tank, a decoloration tank, a crystallization tank and a centrifuge; through the arrangement of the condenser, the steam flashed off is cooled and then discharged into the air, so that the pollution to the air is reduced; the operation difficulty is reduced by setting the sodium acetate stock solution to enter the tube side; the steam is used as a heat transfer medium, so that the operation is convenient, and the steam cost is low.
Description
Technical Field
The utility model relates to a retrieve the field, especially relate to the technical field that sodium acetate was retrieved, specifically indicate a draw apparatus for producing of sodium acetate in furfural production.
Background
Sodium acetate is a chemical raw material, is applied to industrial departments such as printing and dyeing, medicines and the like, can be recycled from the furfural production process, and is used for preparing other chemical products. The plant material is hydrolyzed at high temperature after being added with acid, organic acid is formed while furfural steam is produced, alkali liquor is utilized to react with acetic acid in the furfural steam to produce sodium acetate, and the sodium acetate is further processed into a product. In addition, the acidity of the neutralized aldehyde liquid is reduced, so that the corrosion degree of acetic acid on equipment and pipelines can be reduced.
The traditional production process of sodium acetate is as follows: adding sodium carbonate solution into acetic acid to perform neutralization reaction to obtain sodium acetate stock solution, wherein the neutralization mainly comprises adding sodium carbonate solution into gas phase and liquid phase, uniformly stirring, mixing and neutralizing), and the obtained sodium acetate stock solution can be used for producing crystallized sodium acetate products through main processes of evaporation, decoloration, crystallization, centrifugation and the like.
In the prior production, in order to reduce the generation and emission of carbon dioxide, alkali liquor with the components of 1-10% of sodium hydroxide solution is put into an alkaline tower and is fully neutralized with aldehyde gas to generate tower kettle liquid, in order to ensure the neutralization effect of the aldehyde gas, slightly excessive alkali liquor is added into the alkaline tower, and the solution discharged from the tower kettle of the alkaline tower is alkaline, so that the technical problem of how to extract sodium acetate from the alkaline sodium acetate solution is urgently needed to be solved at present.
SUMMERY OF THE UTILITY MODEL
The utility model discloses to prior art's not enough, provide a production facility who draws sodium acetate in furfural production, retrieve sodium acetate from the sodium acetate solution of basicity.
The utility model discloses a through following technical scheme realization, an extract apparatus for producing of sodium acetate in furfural production, include flash tank, neutralization tank, evaporating pot, decoloration jar, crystallizer, the centrifuge that communicates through the pipeline in order.
The utility model discloses when using, the sodium acetate stoste carries out the flash distillation concentration in at first entering into the flash tank, in entering into the neutralization tank, carries out acid-base neutralization, then lets in the evaporating pot again and evaporates, enters into the decoloration jar after that and carries out the decoloration, then through the crystallizer crystallization precipitation crystal, the crystal that appears obtains the sodium acetate finished product after centrifuge centrifugal treatment again.
Preferably, a condenser is connected to a first gas outlet of the flash tank. According to the optimized scheme, through the arrangement of the condenser, the steam flashed off is cooled and then discharged into the air, so that the pollution to the air is reduced.
Preferably, the pipeline is communicated with a tube pass of the evaporating pot, a third air outlet which is positioned above the tube pass and connected with the tube pass is arranged on the evaporating pot, and the third air outlet is communicated with the cooler through the pipeline.
This preferred scheme enters into the setting of tube side through sodium acetate stoste, and this device reduces the operation degree of difficulty when operating under the ordinary pressure.
Preferably, the shell side of the evaporation tank is communicated with the boiler through a steam pipeline. The preferred scheme adopts the arrangement of taking the steam as a heat transfer medium, so that the operation is convenient, and the steam cost is low.
As optimization, the neutralization tank, the decoloring tank and the crystallizing tank are respectively provided with a stirrer. The preferred scheme accelerates the neutralization speed, the decolorization speed and the crystallization speed by arranging the stirrer.
Preferably, a flash pump is arranged on a pipeline between the flash tank and the neutralization tank, a neutralization pump is arranged on a pipeline between the neutralization tank and the evaporation tank, and a decoloring pump is arranged on a pipeline between the decoloring tank and the crystallizing tank. The flash evaporation pump, the neutralization pump and the decoloration pump are arranged in the optimized scheme, so that the sodium acetate stock solution can flow conveniently.
Preferably, the crystallizer is connected with a shell-side liquid inlet of the evaporation tank through a reflux pipeline. This preferred scheme is through the setting of backflow pipeline, makes the overflow liquid that produces in the crystallizer return to the evaporating pot again in, reduces extravagantly.
Preferably, valves are arranged on a pipeline between the flash tank and the neutralization tank, a pipeline between the evaporation tank and the decoloring tank, a pipeline between the decoloring tank and the crystallizing tank, and a pipeline between the crystallizing tank and the centrifuge. This preferred scheme is through the setting of valve, is convenient for control the circulation of sodium acetate stoste through the valve.
Preferably, the liquid outlet of the centrifuge is communicated with the liquid inlet of the neutralization tank through a pipeline. This preferred scheme's setting is convenient for get back to in the neutralization jar again from the centrifugate in the centrifuge, reduces extravagantly.
The utility model has the advantages that: through the arrangement of a flash tank, a neutralization tank, an evaporation tank, a decoloring tank, a crystallization tank and a centrifuge, sodium acetate is conveniently recovered from an alkaline sodium acetate solution; through the arrangement of the condenser, the steam flashed off is cooled and then discharged into the air, so that the pollution to the air is reduced; the operation difficulty is reduced by setting the sodium acetate stock solution to enter the tube side; the steam is used as a heat transfer medium, so that the operation is convenient, and the steam cost is low.
Drawings
FIG. 1 is a schematic structural view of the present invention;
shown in the figure:
1. flash tank, 2, neutralization tank, 3, evaporating tank, 4, decolorizing tank, 5, crystallizing tank, 6, centrifuge, 7, flash pump, 8, neutralization pump, 9, evaporating pump, 10, valve, 11, first gas outlet, 21, stirrer, 22, third feeding port, 31, third steam inlet, 32, third steam outlet, 51, cooling water inlet, 52, cooling water outlet, 61 and sixth liquid outlet.
Detailed Description
In order to clearly illustrate the technical features of the present solution, the present solution is explained below by way of specific embodiments.
Referring to the attached drawing 1, the utility model discloses an include flash tank 1, neutralization tank 2, evaporating pot 3, decoloration jar 4, crystallizer 5, centrifuge 6 that communicate in order through the pipeline, be equipped with flash pump 7 on the pipeline between flash tank 1 and the neutralization tank 2, be equipped with neutralization pump 8 on the pipeline between neutralization tank 2 and the evaporating pot, be equipped with the decoloration pump on the pipeline between decoloration jar 4 and the crystallizer 5, all be equipped with valve 10 on the pipeline between pipeline, the pipeline between evaporating pot 3 and the decoloration jar 4 between flash tank 1 and the neutralization tank 2, the pipeline between decoloration jar 4 and the crystallizer 5, the pipeline between crystallizer 5 and the centrifuge 6.
Set up the first inlet and the first liquid outlet of intercommunication on the flash tank 1, still set up the first gas outlet 11 that is located flash tank 1 top on the flash tank 1, first gas outlet 11 has the condenser through the pipe connection, and during sodium acetate stoste entered into flash tank 1 from first inlet to flow out from flash tank 1 from first liquid outlet.
The neutralization tank 2 is provided with a second liquid inlet and a second liquid outlet which are communicated, the neutralization tank 2 is also provided with a second feed inlet for the neutralization liquid to enter, the sodium acetate liquid which enters the flash evaporation enters the neutralization tank 2 from the second liquid inlet and flows out of the neutralization tank 2 from the second liquid outlet, and the first liquid outlet is communicated with the second liquid inlet through a pipeline.
Be equipped with tube side and shell side in the evaporating pot 3, set up the third inlet liquid mouth through pipeline and second liquid outlet intercommunication on the tube side, the third liquid outlet has been seted up to the other end of tube side, set up the third gas outlet that communicates and lie in evaporating pot 3 top with the tube side on the evaporating pot 3, the third gas outlet passes through pipeline and cooler intercommunication, set up the third steam inlet 31 and the third steam outlet 32 of intercommunication on the shell side, third steam inlet 31 passes through steam cycle pipeline and boiler intercommunication, third steam outlet 32 passes through steam cycle pipeline and boiler intercommunication, what third steam outlet 32 mainly flowed is steam condensate water.
The fourth inlet, the fourth liquid outlet of intercommunication to and be located the exhaust hole on decoloration jar top are seted up on the decoloration jar 4, and the fourth inlet passes through the pipeline and communicates with the third liquid outlet, has placed the activated carbon adsorbent in the decoloration jar 4.
The crystallization tank 5 is provided with a fifth liquid inlet, a fifth liquid outlet and a fifth crystallization opening which are communicated, the fifth liquid inlet is communicated with the fourth liquid outlet through a pipeline, the fifth liquid outlet is communicated with the third liquid inlet through a return pipeline, the crystallization tank 5 is also provided with a cooling water inlet 51 and a cooling water outlet 52 which are communicated,
the centrifuge 6 is provided with a sixth crystal inlet, a sixth crystal outlet and a sixth liquid outlet 61 which are communicated, the sixth crystal inlet is communicated with the fifth crystallization port through a pipeline, and the sixth liquid outlet 61 is communicated with the second liquid inlet through a pipeline.
Specifically, the direction indicated by the arrow in fig. 1 is the direction of the flow of the sodium acetate solution.
The utility model discloses when using, the concentration of the highly compressed sodium acetate stoste of alkaline washing tower cauldron of high temperature reaches about 35%, and during sodium acetate stoste got into flash tank 1, pressure reduction in the twinkling of an eye produced the flash distillation, is equivalent to once evaporating, and the steam that the flash distillation goes out enters into the condenser from first gas outlet 11 to condensation is arranged outward in the condenser, and the solution concentration after the flash distillation concentration reaches about 40%.
The solution after flash evaporation enters a neutralization tank 2 for acid-base neutralization, acetic acid is added from a second feeding port 22, and a stirrer 21 is arranged in the neutralization tank 2 to ensure rapid and uniform neutralization.
The concentration of the neutralized neutral sodium acetate solution reaches about 40%, then the solution is added into the tube pass of the evaporating pot 3, the tube pass of the evaporating pot 3 is operated under normal pressure, the temperature is 100 ℃, the shell pass is connected with a boiler through a steam pipeline, the saturated steam of 0.5Mpa in the boiler heats the tube pass to evaporate the sodium acetate solution, the evaporated secondary steam enters a third gas outlet and enters a condenser, and the secondary steam is discharged outside a boundary area after being condensed, and at the moment, in order to prevent the crystallization phenomenon generated after the concentration is too high, the concentration of the evaporated solution is controlled to be about 53%. .
The solution flowing out of the evaporation tank is conveyed into a decoloring tank 4, an activated carbon adsorbent is filled in the decoloring tank 4, the dosage of the activated carbon adsorbent depends on the decoloring efficiency and the decoloring quality, is generally 2-3% of the solution, the solution is stirred for half an hour for decoloring, and the solution after decoloring can enter a crystallizing tank 5.
The temperature of the sodium acetate solution before entering the crystallization tank 5 is between 80 and 90 ℃, which can ensure the maximum solubility of the solution. And (3) introducing cooling circulating water into the crystallization tank 5, cooling the solution, and separating out crystals from the solution as the solubility is reduced along with the reduction of the temperature of the solution. The separated crystals enter the centrifuge 6 through the fifth crystallization port, the overflow liquid returns to the evaporation tank 3 again through the return pipeline for evaporation, and meanwhile, the stirrer 21 in the crystallization tank 5 accelerates the cooling of the solution and the separation of the crystals.
And (3) processing the sodium acetate by a sodium acetate centrifuge 6 to obtain a sodium acetate finished product, transferring the sodium acetate finished product to a warehouse, and conveying the centrifugate to a sodium acetate neutralization tank 2 through a pipeline for circulating evaporation.
Of course, the above description is not limited to the above examples, and technical features of the present invention that are not described in the present application may be implemented by or using the prior art, and are not described herein again; the above embodiments and drawings are only used for illustrating the technical solutions of the present invention and are not intended to limit the present invention, and the present invention has been described in detail with reference to the preferred embodiments, and those skilled in the art should understand that changes, modifications, additions or substitutions made by those skilled in the art within the spirit of the present invention should also belong to the protection scope of the claims of the present invention.
Claims (9)
1. A production device for extracting sodium acetate in furfural production is characterized in that: comprises a flash tank (1), a neutralization tank (2), an evaporation tank (3), a decoloration tank (4), a crystallization tank (5) and a centrifuge (6) which are communicated in sequence through pipelines.
2. The production device for extracting sodium acetate in furfural production according to claim 1, characterized in that: and a first air outlet (11) of the flash tank (1) is connected with a condenser.
3. The production device for extracting sodium acetate in furfural production according to claim 1, characterized in that: the pipeline communicates with the tube side of the evaporating pot (3), a third gas outlet which is arranged above the tube side and connected with the tube side is arranged on the evaporating pot (3), and the third gas outlet is communicated with the cooler through the pipeline.
4. The production device for extracting sodium acetate in furfural production according to claim 3, characterized in that: and the shell pass of the evaporating pot (3) is communicated with a boiler through a circulating steam pipeline.
5. The production device for extracting sodium acetate in furfural production according to claim 1, characterized in that: the neutralization tank (2), the decoloration tank (4) and the crystallization tank (5) are all provided with a stirrer (21).
6. The production device for extracting sodium acetate in furfural production according to claim 1, characterized in that: be equipped with flash pump (7) on the pipeline between flash tank (1) and neutralization tank (2), be equipped with neutralization pump (8) on the pipeline between neutralization tank (2) and the evaporating pot, be equipped with the decoloration pump on the pipeline between decoloration jar (4) and crystallizer (5).
7. The production device for extracting sodium acetate in furfural production according to claim 1, characterized in that: the crystallizing tank is connected with a shell side liquid inlet of the evaporating tank (3) through a reflux pipeline.
8. The production device for extracting sodium acetate in furfural production according to claim 1, characterized in that: valves (10) are arranged on a pipeline between the flash tank (1) and the neutralization tank (2), a pipeline between the evaporation tank (3) and the decoloring tank (4), a pipeline between the decoloring tank (4) and the crystallizing tank (5), and a pipeline between the crystallizing tank (5) and the centrifuge (6).
9. The production device for extracting sodium acetate in furfural production according to claim 1, characterized in that: the liquid outlet of the centrifuge (6) is communicated with the liquid inlet of the neutralization tank (2) through a pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021384267.2U CN212669584U (en) | 2020-07-15 | 2020-07-15 | Production device for extracting sodium acetate in furfural production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021384267.2U CN212669584U (en) | 2020-07-15 | 2020-07-15 | Production device for extracting sodium acetate in furfural production |
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| Publication Number | Publication Date |
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| CN212669584U true CN212669584U (en) | 2021-03-09 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202021384267.2U Active CN212669584U (en) | 2020-07-15 | 2020-07-15 | Production device for extracting sodium acetate in furfural production |
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| Country | Link |
|---|---|
| CN (1) | CN212669584U (en) |
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2020
- 2020-07-15 CN CN202021384267.2U patent/CN212669584U/en active Active
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