CN211302127U - Device for removing organic solvent in polyisoprene latex - Google Patents
Device for removing organic solvent in polyisoprene latex Download PDFInfo
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- CN211302127U CN211302127U CN201922216406.4U CN201922216406U CN211302127U CN 211302127 U CN211302127 U CN 211302127U CN 201922216406 U CN201922216406 U CN 201922216406U CN 211302127 U CN211302127 U CN 211302127U
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Abstract
The utility model relates to a polyisoprene latex, concretely relates to organic solvent's in desorption polyisoprene latex device. Comprises a flash evaporator, wherein the top of the flash evaporator is respectively provided with a polyisoprene latex spray head, a steam pipeline inlet, a removed solvent and a steam outlet; a baffle type demister is arranged in the flash evaporator, and a backflow material spray head is arranged above the baffle type demister; polyisoprene latex with the liquid level height lower than that of the baffle plate type demister is reserved at the bottom of the flash evaporator, and a polyisoprene latex outlet is arranged at the bottom of the flash evaporator; and a return pipeline is arranged on a pipeline connected with the polyisoprene latex outlet and is connected with a return material spray head. The utility model discloses the separation process is the continuous process, weak point consuming time, has effectively avoided producing a large amount of foams and has phenomenons such as gel breakdown of emulsion at the desorption solvent in-process.
Description
Technical Field
The utility model relates to a polyisoprene latex, concretely relates to organic solvent's in desorption polyisoprene latex device.
Background
In the prior art, a distillation device is adopted to remove the organic solvent in the polyisoprene latex. In the traditional evaporation process, latex is in a boiling state, and when the organic solvent in the micelle on the surface of the system rapidly escapes, the protective layer of the emulsifier is broken, and the unprotected micelle is easily separated out from the system to form gel. Once gels appear, they interact within the system and more gels appear. In addition, the evaporation and gasification process of the organic solvent forms a large amount of foam in a system with low surface tension.
Chinese patent CN107474587A discloses a polyisoprene latex and a preparation method thereof, the preparation method of the polyisoprene latex comprises: and continuously introducing a medium gas with the temperature of 80-180 ℃ into the oil-in-water phase polyisoprene rubber emulsion to remove the organic solvent in the emulsion. The medium gas is one or more selected from nitrogen, air and carbon dioxide. Mixing polyisoprene rubber glue solution, an emulsifier, a pH buffering agent and a colloid stabilizer to obtain a water-in-oil phase mixed glue solution; and then contacting the obtained mixed glue solution of the water-in-oil phase with deionized water to convert the glue solution from the water-in-oil phase to the oil-in-water phase. And finally, continuously introducing medium gas with the temperature of 80-180 ℃ into the emulsion of the oil-in-water phase to remove the organic solvent in the emulsion. It is required to make a mixed glue solution of water-in-oil phase, then convert the mixed glue solution into a mixed glue solution of oil-in-water phase, and finally process the mixed glue solution. The invention adds the step of preparing the water-in-oil phase from the glue solution, and also converts the water-in-oil phase into the oil-in-water phase, and further, the invention mainly adopts the method of continuously introducing medium gas into the emulsion of the oil-in-water phase to remove the organic solvent. The invention also discloses a device for removing the organic solvent, which adopts a distillation device to remove the organic solvent from the glue solution.
At present, the development of a device for removing the organic solvent from the polyisoprene latex, which has the advantages of simple process, no generation of a large amount of foams and high removal rate of the organic solvent, is urgently needed.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a device of organic solvent in desorption polyisoprene latex does not produce a large amount of foams, and organic solvent desorption rate is high, can not have the gel breakdown of emulsion phenomenon at the desorption solvent in-process.
The device for removing the organic solvent from the polyisoprene latex comprises a flash evaporator, wherein a polyisoprene latex spray head, a steam pipeline inlet, a removed solvent and a steam outlet are respectively arranged at the top of the flash evaporator; a baffle type demister is arranged in the flash evaporator, and a backflow material spray head is arranged above the baffle type demister; polyisoprene latex with the liquid level height lower than that of the baffle plate type demister is reserved at the bottom of the flash evaporator, and a polyisoprene latex outlet is arranged at the bottom of the flash evaporator; and a return pipeline is arranged on a pipeline connected with the polyisoprene latex outlet and is connected with a return material spray head.
Wherein:
the first heat exchanger and the circulating pump are sequentially arranged along the flowing direction of the backflow materials of the backflow pipeline.
The polyisoprene latex spray head is connected with a polyisoprene latex raw material tank through a reciprocating pump on a pipeline.
The removed solvent and the steam outlet are connected with a solvent recovery tank through a second heat exchanger.
And a pipeline connected with the polyisoprene latex outlet is connected with the latex concentration tank.
The backflow material spray head is a centrifugal sprayer or a pressure sprayer.
The polyisoprene latex spray head is a centrifugal sprayer or a pressure sprayer.
Utilize the device of organic solvent in desorption polyisoprene latex, the method of organic solvent in desorption polyisoprene latex includes following step:
(1) in a flash evaporator, directly contacting atomized raw material polyisoprene latex by using steam to remove the organic solvent with low boiling point;
(2) the polyisoprene latex without the organic solvent firstly falls onto a baffle plate type demister in a flash evaporator and then falls to the bottom of the flash evaporator for aggregation, the aggregated polyisoprene latex is discharged from the bottom of the flash evaporator, and a certain liquid level of the polyisoprene latex is reserved at the bottom of the flash evaporator and is lower than the baffle plate type demister;
(3) the polyisoprene latex discharged from the bottom of the flash evaporator is divided into two parts, wherein one part of the polyisoprene latex is cooled and reflows to the inside of the flash evaporator and is sprayed above a baffle type demister in the flash evaporator; and after the polyisoprene latex falling onto the baffle plate type demister in the flash evaporator is cooled and defoamed, the polyisoprene latex and the cooled and defoamed polyisoprene latex fall to the bottom of the flash evaporator together.
Wherein:
in the step (1), the raw material polyisoprene latex comprises the following substances in percentage by mass: 50-55% of n-hexane, 40-45% of water, 4-9% of polyisoprene and 0.1-0.2% of emulsifier. The emulsifier is preferably sodium dodecyl benzene sulfonate, sodium dodecyl sulfate, etc.
In the step (3), the polyisoprene latex discharged from the bottom of the flash evaporator is divided into two parts, wherein one part of the polyisoprene latex is cooled to 30-40 ℃ and reflows to the inside of the flash evaporator.
In the step (3), the flow ratio of the polyisoprene latex sprayed to the upper part of the baffle type demister in the flash evaporator to the polyisoprene latex falling onto the baffle type demister in the flash evaporator is 1: 2-5. The amount of the refluxed polyisoprene latex is small, and the better cooling and defoaming effects are achieved.
In the step (3), the polyisoprene latex discharged from the bottom of the flash evaporator is divided into two parts, wherein one part of the polyisoprene latex is cooled and reflows to the inside of the flash evaporator and is sprayed above a baffle plate type demister in the flash evaporator.
In the step (3), the other part of the polyisoprene latex discharged from the bottom of the flash evaporator is subjected to gas stripping by adopting hot nitrogen, and the polyisoprene latex is concentrated.
The more specific technical scheme in the invention is as follows:
atomizing polyisoprene latex through a polyisoprene latex sprayer, introducing steam for flash evaporation, wherein the boiling point of an organic solvent is about 68 ℃, 521kJ heat is needed for separating 1kg of the organic solvent through simple heat calculation, 2600kJ heat can be provided for 1kg of the steam with the pressure of 0.2MPa, the polyisoprene latex is sprayed out in a mist shape by the sprayer and then is in full contact with the steam, and the organic solvent absorbs the heat and is quickly separated from the polyisoprene latex. Because the contact time of the polyisoprene latex and steam is short, other components in the latex can not be separated out, and the demulsification phenomenon can not occur, thereby achieving the purpose of removing the organic solvent.
Steam is pumped around a polyisoprene latex spray head, and the used steam is at 120 ℃ and 2-4 Kg/h. Before starting feeding, steam is firstly introduced for a period of time to preheat the interior of the flash evaporator and discharge condensed water. If the steam and the polyisoprene latex are directly introduced into the flash evaporator, the steam can be greatly condensed by heating the flash evaporator due to the low temperature in the flash evaporator, and the removal effect of the organic solvent in the polyisoprene latex is greatly influenced by the existence of the condensate, which is mainly reflected in high organic solvent residue.
Conveying the polyisoprene latex to a polyisoprene latex spray head through a reciprocating pump to spray the polyisoprene latex in a mist shape, wherein the spray head is a centrifugal sprayer or a pressure sprayer, the pressure of the outlet of the reciprocating pump is not higher than 0.4MPa, the rotating speed of the centrifugal sprayer is 3000 plus 5000rpm, and the molecular weight of the polyisoprene rubber in the polyisoprene latex is 70-100 ten thousand.
And (3) extracting the polyisoprene latex without the organic solvent from the lower part of the flash evaporator, wherein the residual organic solvent is reduced to below 5000ppm, discharging water vapor and the removed organic solvent vapor from the top of the flash evaporator, and recovering the organic solvent after passing through a second heat exchanger.
The process adopts hot nitrogen as carrier gas to destroy the gas-liquid two-phase balance of latex and organic solvent in the original latex to establish a new gas-liquid balance state, so that the residual organic solvent in the latex is separated out due to the reduced partial pressure in the gas phase, the heat of the hot nitrogen is utilized to accelerate the removal of the organic solvent, and part of water is evaporated from the latex, thereby simultaneously achieving the effect of further removing the organic solvent and concentrating the latex.
The utility model has the advantages as follows:
firstly, the utility model discloses set up the solvent and the steam outlet of polyisoprene latex shower nozzle, steam line entry, desorption respectively at the flash vessel top, use the direct and atomizing raw materials polyisoprene latex contact of steam, thereby utilize the low organic solvent desorption of organic solvent boiling point to come out in the latex.
Secondly, the spray head for atomization is a centrifugal sprayer or a pressure sprayer, and the latex is atomized and then contacted with steam, so that the separation effect is greatly enhanced.
Thirdly, after the polyisoprene latex is subjected to organic solvent removal by using steam, the polyisoprene latex subjected to organic solvent removal firstly falls onto a baffle type demister in the flash evaporator and then falls to the bottom of the flash evaporator for aggregation, the aggregated polyisoprene latex is discharged from the bottom of the flash evaporator, and polyisoprene latex at a certain liquid level is reserved at the bottom of the flash evaporator and is lower than the baffle type demister; the polyisoprene latex discharged from the bottom of the flash evaporator is divided into two parts, wherein one part of the polyisoprene latex is cooled and reflows to the inside of the flash evaporator and is sprayed above a baffle type demister in the flash evaporator; and after the polyisoprene latex falling onto the flash evaporator baffle type demister is cooled and defoamed, the polyisoprene latex and the defoamed polyisoprene latex fall to the bottom of the flash evaporator together. And (3) refluxing the polyisoprene latex with a certain amount, and cooling and defoaming the polyisoprene latex without the organic solvent. The bottom of the flash evaporator keeps certain liquid level of polyisoprene latex, the liquid level is lower than the height of the baffle type demister, otherwise, part of steam is discharged from the lower part of the flash evaporator, and the removed organic solvent returns to the polyisoprene latex.
In the spray flash apparatus, there is a certain liquid level below the flash evaporator, although the temperature is not as high as that of the boiling latex in the kettle evaporator, under the condition of long time heating, the latex as liquid seal can generate a large amount of foam on the surface and emulsion breaking phenomenon on the interface with the wall of the flash evaporator, and generate rubber hanging on the wall. And the problem will be solved to the backward flow that sets up on the latex production pipeline, and the latex spray liquid seal top after the cooling can play the effect of cooling, can also break away from a large amount of foams that produce because the solvent breaks away from.
The latex is atomized by a centrifugal sprayer or a pressure sprayer, and the organic solvent is heated to separate from the latex, so that air enters the latex, and due to the existence of an emulsifier in the latex, the surface tension between water molecules is reduced, a large amount of foam is generated and accumulated, and the production is not facilitated. Consequently, set up baffling board formula defroster in the lower part of backward flow material shower nozzle, when the foam falls on the baffling board, because the baffling board blocks, a large amount of foams flow down along the space between the baffling board, under the spraying of the backward flow latex of process cooling, the foam can break open.
It is also noted that the temperature of the wall surface of the flash evaporator is very high after the steam has been introduced, and that if the polyisoprene latex runs down the wall, it is heated for a very long time, with the result that it is possible that both the water and the organic solvent in the latex are evaporated to dryness and also a gel is formed on the wall. Therefore, the baffle plate type demister is arranged at the lower part of the backflow material spray head, and the phenomenon of glue hanging on the wall of the device is avoided under the spraying of the cooled backflow latex.
The utility model discloses compare with the distilled device desorption organic solvent of traditional adoption, can not produce a large amount of foams, can not have phenomenons such as gel breakdown of emulsion at desorption solvent in-process. The utility model discloses pass through the shower nozzle atomizing with polyisoprene latex, let in steam simultaneously and carry out the flash distillation to organic solvent in the desorption polyisoprene latex. The utility model discloses the flow is succinct, and whole process is a continuous production process, and latex and steam contact time are short, and the material gets into the evaporation space in succession, has avoided influencing each other in traditional cauldron formula evaporimeter to compare in cauldron formula evaporimeter, the spraying flash distillation has bigger evaporation space. The utility model discloses the separation process is the continuous process, weak point consuming time, has effectively avoided producing a large amount of foams and has produced at phenomenons such as desorption solvent in-process gel breakdown of emulsion. In addition, the production process is changed from the intermittent process of kettle evaporation to the continuous process of spray flash evaporation, which is beneficial to reducing energy consumption and improving production efficiency.
Drawings
Fig. 1 is a schematic structural diagram of the present invention;
wherein: 1. a steam line inlet; 2. a stripped solvent and vapor outlet; 3. a second heat exchanger; 4. a solvent recovery tank; 5. a circulation pump; 6. a first heat exchanger; 7. a latex concentration tank; 8. a polyisoprene latex showerhead; 9. a material reflux nozzle; 10. a polyisoprene latex outlet; 11. a polyisoprene latex feed tank; 12. a reciprocating pump; 13. a baffle demister; 14. a flash evaporator.
Detailed Description
The present invention will be further described with reference to the following examples.
Example 1
The device for removing the organic solvent in the polyisoprene latex of the utility model is shown in figure 1 and comprises a flash evaporator 14, wherein the top of the flash evaporator 14 is respectively provided with a polyisoprene latex spray head 8, a steam pipeline inlet 1, a removed solvent and a steam outlet 2; a baffle type demister 13 is arranged in the flash evaporator 14, and a backflow material spray head 9 is arranged above the baffle type demister 13; polyisoprene latex with the liquid level height lower than that of the baffle type demister 13 is reserved at the bottom of the flash evaporator 14, and a polyisoprene latex outlet 10 is arranged at the bottom of the flash evaporator 14; and a return pipeline is arranged on a pipeline connected with the polyisoprene latex outlet 10 and is connected with a return material spray head 9.
Wherein:
along the backflow material flowing direction of the backflow pipeline, a first heat exchanger 6 and a circulating pump 5 are sequentially arranged.
The polyisoprene latex spray head 8 is connected with a polyisoprene latex raw material tank 11 through a reciprocating pump 12 on a pipeline;
the removed solvent and the steam outlet 2 are connected with a solvent recovery tank 4 through a second heat exchanger 3;
the line to which the polyisoprene latex outlet 10 is connected to the latex concentration tank 7.
The polyisoprene latex spray head 8 is a centrifugal sprayer or a pressure sprayer.
The backflow material spray head 9 is a centrifugal sprayer or a pressure sprayer.
Utilize the utility model discloses the process of organic solvent in desorption polyisoprene latex includes following step:
(1) removal of organic solvent from polyisoprene latex:
introducing steam with the flow rate of 2kg/h, the pressure of 0.2MPa and the temperature of 120 ℃ into a flash evaporator 14, preheating polyisoprene latex with the composition of 50 percent of normal hexane, 45 percent of water, 4.9 percent of polyisoprene and 0.1 percent of emulsifier into a centrifugal atomizer according to the mass percentage of each substance at the flow rate of 6L/h, wherein the rotation speed of the centrifugal atomizer is 4500rpm, and introducing the mixed steam of the removed normal hexane and the water extracted from an upper outlet of the flash evaporator 14 into a second heat exchanger 3 for condensation and recovery.
The polyisoprene latex without n-hexane firstly falls onto a baffle plate type demister 13 in a flash evaporator 14 and then falls to the bottom of the flash evaporator 14 for aggregation, after a certain liquid level is accumulated, the polyisoprene latex without n-hexane is extracted from the bottom of the flash evaporator 14, and the polyisoprene latex at a certain liquid level is always kept at the bottom of the flash evaporator 14, wherein the liquid level is lower than the height of the baffle plate type demister 13.
The polyisoprene latex collected from the bottom of the flash evaporator 14 is divided into two parts, wherein one part of the polyisoprene latex is cooled to 40 ℃ and reflows to the inside of the flash evaporator 14, and is sprayed above a baffle type demister 13 in the flash evaporator 14 by a pressure type sprayer; after the polyisoprene latex falling onto the baffle plate type demister 13 in the flash evaporator 14 is cooled and defoamed, the polyisoprene latex and the defoamed polyisoprene latex fall to the bottom of the flash evaporator 14 together. The flow ratio of the polyisoprene latex sprayed above the baffle mist eliminator 13 in the flash evaporator 14 to the polyisoprene latex falling onto the baffle mist eliminator 13 in the flash evaporator 14 was 1: 2.
Through detection, the residue of the organic solvent in the polyisoprene latex without the organic solvent is 2100 ppm. In the production process, a large amount of foam is not generated, and the phenomena of gel demulsification and the like do not occur in the polyisoprene latex.
(2) Concentration of polyisoprene latex:
another portion of the polyisoprene latex discharged from the bottom of flash evaporator 14 is then concentrated by stripping with hot nitrogen.
Claims (7)
1. An apparatus for removing organic solvent from polyisoprene latex, which comprises a flash evaporator (14), and is characterized in that: the top of the flash evaporator (14) is respectively provided with a polyisoprene latex spray head (8), a steam pipeline inlet (1), a removed solvent and a steam outlet (2); a baffle type demister (13) is arranged in the flash evaporator (14), and a backflow material spray head (9) is arranged above the baffle type demister (13); polyisoprene latex with the liquid level height lower than that of the baffle type demister (13) is reserved at the bottom of the flash evaporator (14), and a polyisoprene latex outlet (10) is arranged at the bottom of the flash evaporator (14); a return pipeline is arranged on a pipeline connected with the polyisoprene latex outlet (10), and the return pipeline is connected with a return material spray head (9).
2. The apparatus for removing organic solvent from polyisoprene latex as claimed in claim 1, wherein: along the flowing direction of the backflow materials of the backflow pipeline, a first heat exchanger (6) and a circulating pump (5) are sequentially arranged.
3. The apparatus for removing organic solvent from polyisoprene latex as claimed in claim 1, wherein: the polyisoprene latex spray head (8) is connected with a polyisoprene latex raw material tank (11) through a reciprocating pump (12) on a pipeline.
4. The apparatus for removing organic solvent from polyisoprene latex as claimed in claim 1, wherein: the removed solvent and the steam outlet (2) are connected with a solvent recovery tank (4) through a second heat exchanger (3).
5. The apparatus for removing organic solvent from polyisoprene latex as claimed in claim 1, wherein: the pipeline connected with the polyisoprene latex outlet (10) is connected with the latex concentration tank (7).
6. The apparatus for removing organic solvent from polyisoprene latex as claimed in claim 1, wherein: the polyisoprene latex spray head (8) is a centrifugal sprayer or a pressure sprayer.
7. The apparatus for removing organic solvent from polyisoprene latex as claimed in claim 1, wherein: the backflow material spray head (9) is a centrifugal sprayer or a pressure sprayer.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201922216406.4U CN211302127U (en) | 2019-12-11 | 2019-12-11 | Device for removing organic solvent in polyisoprene latex |
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| CN201922216406.4U CN211302127U (en) | 2019-12-11 | 2019-12-11 | Device for removing organic solvent in polyisoprene latex |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114674078A (en) * | 2022-03-29 | 2022-06-28 | 江西丰大新材料有限公司 | Emulsifier heating device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114674078A (en) * | 2022-03-29 | 2022-06-28 | 江西丰大新材料有限公司 | Emulsifier heating device |
| CN114674078B (en) * | 2022-03-29 | 2023-12-29 | 江西丰大新材料有限公司 | Emulsifier heating device |
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Address after: 255411 No. 3, Feng Bei Road, Zhangdian District, Shandong, Zibo Patentee after: Zibo luhuahongjin New Material Group Co.,Ltd. Address before: 255022 No. 3, Fengbei Road, Zhangdian District, Zibo City, Shandong Province Patentee before: ZIBO LUHUA HONGJIN NEW MATERIAL Co.,Ltd. |