CN100363409C - Technique of refining solvent in process of producing synthetic rubber - Google Patents
Technique of refining solvent in process of producing synthetic rubber Download PDFInfo
- Publication number
- CN100363409C CN100363409C CNB2006100320734A CN200610032073A CN100363409C CN 100363409 C CN100363409 C CN 100363409C CN B2006100320734 A CNB2006100320734 A CN B2006100320734A CN 200610032073 A CN200610032073 A CN 200610032073A CN 100363409 C CN100363409 C CN 100363409C
- Authority
- CN
- China
- Prior art keywords
- solvent
- tower
- rectifying tower
- effect
- imitate
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
the invention discloses a solvent refining technology of rubber synthetic manufacturing course, which is characterized by the following: adopting multiple rectifying towers to replace present single rectifying tower to reduce steam by about 60-50%; adopting cooled heat of last rectifying top gas as heat source of next tower through improving operational pressure of one tower to utilize pressure difference and temperature difference of each tower; adopting two-effective paralleling combination, two-effective cascading combination or three-effective cascading combination in the course.
Description
One, technical field:
The present invention relates to a kind of synthetic rubber production process that is used for and reclaim solvent treatment technology.
Two, background technology:
In the synthetic rubber production process, as: solution styrene butadiene rubber (SSBR), solution polymerization process ethylene-propylene rubber(EPR), cis-1,4-polybutadiene rubber and styrene block copolymer SBC (SBS, SIS, SEBS) production equipment, all there are a large amount of solvents in polymerization or agglomeration phase, a large amount of solvents use at the device internal recycle, device all disposes solvent recuperation refined unit or relevant devices, all solvent treatments at present almost are to adopt to remove earlier water and light component in dehydration tower entirely, in rectifying tower, remove the single-action rectification process of heavy component again, product per ton consumes steam generally at the 2-3 ton, the energy consumption height.
Three, summary of the invention:
The object of the present invention is to provide a kind of technique of refining solvent in process of producing synthetic rubber, reclaim solvent, intend reducing the consumption of steam and heat-eliminating medium,, reduce device running cost with save energy.
This technical process is made up of rectifying tower, reboiler, condenser, return tank, solvent tank and pump.
Technical scheme of the present invention is: adopt the rectifying tower of a plurality of routines to be combined into a multiple-effect distillation system, and disposing corresponding reboiler and condenser, the solvent that cohesion process is next adopts two to imitate or three-effect rectifications through after dehydration or taking off light component, remove the impurity in the solvent, reclaim solvent; By improving a working pressure of imitating, make one to imitate the thermal source of cat head gas phase as two effect reboilers, two imitate the thermal source of cat head gas phases as the triple effect reboiler; Imitate vapor condensation heat energy by the pressure that reduces last effect in order to using one; The working pressure that one is imitated is 0.2-0.7MPa (gauge pressure), and the working pressure of last effect is 0.06MPa (vacuum tightness)-0.03MPa (gauge pressure); Its general effect tower top temperature is at 140-115 ℃, and preceding effect tower top temperature is higher than next and imitates 10-25 ℃ of tower still temperature, and last is imitated cat head gas phase and is controlled at 40-90 ℃ and 10-40 ℃ respectively in the outflow temperature of condenser and tail gas condenser.
Below two technologies of imitating rectifying and three-effect rectification are further described:
1, adopt two to imitate distillation process in parallel as shown in Figure 1, its technology is: the solvent that comes from dehydration tower is divided into the middle part that two equal stocks of flow do not enter an effect rectifying tower 1 and two effect rectifying tower 3, and cat head and tower still logistics composition that an effect, two is imitated rectifying tower all reach separation requirement.One imitates rectifying tower 1 provides heat by reboiler 2, and thermal source is steam or other heating agent; Send into a solvent of imitating in the rectifying tower 1 and separated by refining, refining qualified solvent drains into two reboiler 4 shell-sides of imitating rectifying tower 3 with gas phase from cat head, and as two thermals source of imitating rectifying tower 3, most of vapor phase solvent is condensed into liquid state and is discharged into solvent tank 5; A small amount of gas that is not condensed then drains into condenser 7, and controls this tower working pressure by the flow of this strand gas.Another strand solvent that comes from dehydration tower is sent into two and is imitated rectifying tower 3 middle and lower parts, imitates that rectifying tower 3 separate and qualified solvent enters condenser 7 from cat head with the gas phase form through two, is condensed to flow into return tank 9.
Utilize pressure reduction to be pressed into return tank 9 for refining qualified solvent in the solvent tank 5.Be refining qualified solvent in the return tank 9, a part is sent to one respectively by reflux pump 10 imitates rectifying tower 1, two and imitates rectifying tower 3 cats head and make backflow usefulness, the concrete technology of quantity of reflux root a tree name and deciding; Return tank 9 remaining solvents are sent distillation system as product by reflux pump 10.
One to imitate rectifying tower 1 tower still be the impurity that contains solvent, utilizes two to imitate pressure reduction between rectifying tower and send into two and imitate rectifying tower 3 tower stills, and solvent-laden impurity is imitated rectifying tower 3 tower stills from two and discharged distillation systems with pump 6.
2, adopt two to imitate the series connection distillation process as shown in Figure 2, its technology is: enter one of multiple-effect distillation system from the next solvent of dehydration tower and imitate rectifying tower 1, this tower provides heat by reboiler 2, and thermal source is steam or other heating agent; Solvent is imitated in the rectifying tower 1 by refining one, and refining qualified solvent drains into two reboiler 4 shell-sides of imitating rectifying tower 3 with gas phase from cat head, and as the thermal source of two effect rectifying, most of gas phase is condensed into liquid state and is discharged into solvent tank 5; A small amount of gas that is not condensed then drains into condenser 7, and controls this tower working pressure by the flow of this strand gas.One to imitate rectifying tower 1 tower still be the solvent that contains impurity, utilize two imitate between pressure reduction and deliver to two and imitate rectifying tower 3 towers.Imitate that rectifying tower 3 separate and qualified solvent enters condenser 7 from cat head with the gas phase form through two, the back that is condensed flows into return tank 9.
Utilize pressure reduction to be pressed into return tank 9 for refining qualified solvent in the solvent tank 5, qualified solvent in the return tank 9, a part is sent to one respectively by reflux pump 10 imitates rectifying tower 1, two and imitates rectifying tower 3 cats head and do to reflux and use, the concrete technology of quantity of reflux root a tree name and deciding, remaining solvent is sent distillation system as product by reflux pump 10.
Solvent-laden impurity is imitated rectifying Tata still pump 6 discharge systems from two.
3, adopt the three-effect rectification flow process as shown in Figure 3, its technology is: enter one of multiple-effect distillation system from the next solvent of dehydration tower and imitate rectifying tower 1, this tower provides heat by reboiler 2, and thermal source can be steam or other heating agent; Solvent is imitated in the rectifying tower 1 by refining one, and refining qualified solvent drains into two reboiler 4 shell-sides of imitating rectifying tower 3 with gas phase from cat head, and as the thermal source of two effect rectifying, most of gas phase is condensed into liquid state and is discharged into solvent tank 5; A small amount of gas that is not condensed then drains into condenser 7, and controls this tower working pressure by the flow of this strand gas.One to imitate rectifying tower 1 tower still be impure solvent, utilize one, two imitate between pressure reduction and deliver to two and imitate rectifying tower 3 towers.
Impure solvent is imitated in the rectifying tower 3 separated two, refining qualified solvent enters three-effect rectification tower 5 reboilers 13 shell-sides from cat head with gas phase; Flow into solvent tank 5 as thermal source at the solvent that reboiler 13 is condensed, the gas phase that is not condensed is discharged into condenser 7, and is controlled the working pressure of two effect rectifying tower 3 by the flow of this strand gas.Two to imitate rectifying tower 3 tower stills are impure solvents, utilize two, the pressure reduction between triple effect and deliver to three-effect rectification tower 12.
The solvent that the contains impurity separation that in three-effect rectification tower 12, is distillated, refining qualified solvent enters condenser 7 from cat head with the gas phase form, and the solvent after being condensed flows into return tank 9.
Be refining qualified solvent in the solvent tank 5, deliver to one respectively by solvent pump 11 and imitate rectifying tower 1 and two and imitate rectifying tower 3 cats head and reflux, each concrete technology of tower quantity of reflux root a tree name and deciding, remaining solvent is delivered to return tank 9.
Be refining qualified solvent in the return tank 9, deliver to three-effect rectification tower 12 cats head by reflux pump 10 and reflux, the concrete technology of quantity of reflux root a tree name and deciding, remaining solvent is sent distillation system through pump 10.
Solvent-laden impurity is discharged distillation system from three-effect rectification tower 12 tower stills with pump 6.
Enter after condenser 7 most of gas phases are condensed, a small amount of gas phase that contains non-condensable gas enters tail gas condenser 8 and continues cooling and condensation reclaiming solvent, and the non-condensable gas that is not condensed effluxes.The heat-eliminating medium that condenser 7 and tail gas condenser 8 are adopted is decided on solvent species and working pressure, and the most commonly used is recirculated cooling water and refrigerated water.
60-50% when steam that solvent treatment technical process of the present invention consumes only is single-tower rectifying, the 65-45% the when consumption of recirculated cooling water is about single-tower rectifying.
Four, description of drawings:
Fig. 1 is two effects distillation process figure in parallel;
Fig. 2 is two effect series connection distillation process figure;
Fig. 3 is the three-effect rectification schema.
Among the figure: 1, one imitate rectifying tower, 2, one imitates reboiler, and 3, two imitate rectifying tower, and 4, two imitate reboilers, and 5, solvent tank, 6, raffinate discharging pump, 7, condenser, 8, tail gas condenser, 9, return tank, 10, reflux pump, 11, solvent pump, 12, the three-effect rectification tower, 13, the triple effect reboiler.
Five, embodiment:
Embodiment 1:
Reclaim two of cyclohexane solvent and imitate series connection rectification process flow process, as shown in Figure 1, the hexanaphthene that the cohesion unit reclaims enters the unitary dehydration tower of solvent treatment and removes water and light component, respectively delivers to one through pump by the equal proportion amount from dehydration Tata still and imitates the middle part that rectifying tower 1 and two is imitated rectifying tower 3.One working pressure of imitating rectifying tower 1 is 0.25MPa (table), tower top temperature is 121 ℃, 128 ℃ of tower still temperature, hydrocone type reboiler 2 adopts the low-pressure steam heating, partial solvent is vaporized in tubulation, mass transfer takes place in tower solvent separates, and purity meets the requirements of solvent and imitates the shell side that rectifying tower top to two is imitated the hydrocone type reboiler 4 of rectifying tower 3 with the gas phase form from one.Solvent-laden impurity is imitated rectifying tower 1 tower still material from one and is utilized the pressure reduction between one, two effect towers and be pressed into two effect rectifying tower, 3 tower stills; One imitates the liquid level of rectifying tower 1 tower still by being located at a variable valve control of imitating on rectifying tower 1 tower still to the two effect rectifying tower 3 tower still pipelines.To the vapor phase solvent of reboiler 4, as the heating medium of reboiler 4, in reboiler 4 shell sides by most of condensation after from flowing to solvent tank 5.Two working pressures of imitating rectifying tower 3 are normal pressure, and tower top temperature is about 81 ℃, and tower still temperature is about 102 ℃.Material is after reboiler 4 heating vaporizations, and separated refining in tower, refining qualified solvent enters the shell side of condenser 7 with the gas phase form.Vapor phase solvent is cooled to about 80 ℃ by the recirculated cooling water of tube side, after being condensed, most of gas phase enters return tank 9, the gas phase that is not condensed enters tail gas condenser 8 shell-sides, be cooled to about 20 ℃ again by the tube side refrigerated water, the solvent of gas phase is almost all flow to return tank 9 after the condensation equally certainly, and non-condensable gas effluxes.
Solvent in flowing to solvent tank 5 utilizes pressure reduction and is depressed in the return tank 9.Be refining qualified solvent in the return tank 9, through reflux pump 10, a part is delivered to an effect rectifying tower 1, two effect rectifying tower, 2 cats head respectively as refluxing, and rest part is sent this distillation system as solvent.
Two effect rectifying tower, 2 tower stills are solvent-laden impurity, send this distillation system through pump 6.When steam that this solvent treatment technical process consumes only is single-tower rectifying about 60%, 65% the when consumption of recirculated cooling water is about single-tower rectifying.
Embodiment 2:
Reclaim two of cyclohexane solvent and imitate series connection rectification process flow process, as shown in Figure 2.After the hexanaphthene that the cohesion unit reclaims enters the unitary dehydration tower of solvent treatment and removes water and light component, imitate rectifying tower 1 middle part through being pumped to one.One working pressure of imitating rectifying tower 1 is 0.25Mpa (table), tower top temperature is 121 ℃, 126 ℃ of tower still temperature, hydrocone type reboiler 2 adopts the low-pressure steam heating, partial solvent is vaporized in tubulation, mass transfer takes place in tower solvent separates, and purity meets the requirements of solvent and imitates the shell side that cat head drains into the hydrocone type reboiler 4 of two effect rectifying tower 3 with the gas phase form from one.Impure solvent is imitated rectifying tower 1 tower still from one and is utilized the pressure reduction between one, two effect towers and be pressed into two effect rectifying tower, 3 middle parts; One imitates the liquid level of rectifying tower 1 tower still by being located at the two variable valve controls of imitating on rectifying tower 3 solvent line.To the vapor phase solvent of reboiler 4, as heating medium in reboiler 4 shell sides by most of condensation after from flowing to solvent tank 5.Two working pressures of imitating rectifying tower 3 are normal pressure, and tower top temperature is about 81 ℃, and tower still temperature is about 102 ℃.Material is after reboiler 4 heating vaporizations, and separated refining in tower, refining qualified solvent enters the shell side of condenser 7 with the gas phase form.Vapor phase solvent is cooled to about 80 ℃ by the recirculated cooling water of tube side, after being condensed, most of gas phase enters return tank 9, the gas phase that is not condensed enters tail gas condenser 8 shell-sides, be cooled to about 20 ℃ again by the tube side refrigerated water, the solvent of gas phase is almost all flow to return tank 9 after the condensation equally certainly, and non-condensable gas effluxes.
Solvent in flowing to solvent tank 5 utilizes pressure reduction and is depressed in the return tank 9.Be qualified solvent in the return tank 9, through reflux pump 10, a part is delivered to an effect rectifying tower 1, two effect rectifying tower, 2 cats head respectively as refluxing, and rest part is sent this distillation system as solvent.
Two effect rectifying tower, 2 tower stills are solvent-laden impurity, send this distillation system through pump 6.
When steam that this solvent treatment technical process consumes only is single-tower rectifying 60%, 65% the when consumption of recirculated cooling water is about single-tower rectifying.
Embodiment 3:
Reclaim the triple effect tandem rectification process flow process of cyclohexane solvent, as shown in Figure 3.
The hexanaphthene that the cohesion unit reclaims is imitated rectifying tower 1 middle part from dehydration Tata still through being pumped to one after entering the unitary dehydration tower dehydration of solvent treatment.One working pressure of imitating rectifying tower 1 is 0.5MPa (table), tower top temperature is 140 ℃, 144 ℃ of tower still temperature, hydrocone type reboiler 2 adopts the low-pressure steam heating, partial solvent is vaporized in tubulation, mass transfer takes place in tower solvent separates, and purity meets the requirements of solvent and imitates the shell side that tower rectifying tower 1 cat head to two is imitated the hydrocone type reboiler 4 of rectifying tower 3 with the gas phase form from one.Impure solvent is imitated rectifying tower 1 tower still from one and is utilized the pressure reduction between one, two effect towers and be pressed into two effect rectifying tower, 3 middle parts; One imitates the liquid level of rectifying tower 1 tower still by being located at the variable valve control of imitating on rectifying tower 3 solvent line to two.To the vapor phase solvent of reboiler 4, as heating medium, in reboiler 4 shell sides by most of condensation after from flowing to solvent tank 5.
Two working pressures of imitating rectifying tower 3 are about 0.25MPa (table), tower top temperature is about 121 ℃, 126 ℃ of tower still temperature, material is after reboiler 4 heating vaporizations, separated refining in tower, purity meets the requirements of solvent and pushes up to the shell side of the hydrocone type reboiler 13 of three-effect rectification tower 12 from two effect tower rectifying tower 3 with the gas phase form.Impure solvent from two imitate that rectifying tower 3 tower stills utilize two, pressure reduction between the triple effect tower and be pressed into three-effect rectification tower 12 middle parts; Two imitate the liquid level of rectifying tower 3 tower stills by being located at the variable valve control on three-effect rectification tower 12 solvent line.To the vapor phase solvent of reboiler 13, as heating medium, in reboiler 13 shell sides by most of condensation after from flowing to solvent tank 5.
Be qualified solvent in the solvent tank 5, through solvent pump 11, a part is delivered to an effect rectifying tower 1, two effect rectifying tower, 2 cats head respectively as refluxing, and rest part is delivered in the return tank 9 as solvent.
The working pressure of three-effect rectification tower 12 is a normal pressure, and tower top temperature is about 81 ℃, and tower still temperature is about 102 ℃.Material is after reboiler 13 heating vaporizations, and separated refining in tower, refining qualified solvent enters the shell side of condenser 7 with the gas phase form.Vapor phase solvent is cooled to about 80 ℃ by the recirculated cooling water of tube side, after being condensed, most of gas phase enters return tank 9, the gas phase that is not condensed enters tail gas condenser 8 shell-sides, be cooled to about 20 ℃ again by the tube side refrigerated water, the solvent of gas phase is almost all flow to return tank 9 after the condensation equally certainly, and non-condensable gas effluxes.
Be refining qualified solvent in the return tank 9, through reflux pump 10, a part is delivered to three-effect rectification tower 12 cats head as backflow, and rest part is sent this distillation system as qualified solvent.
Three-effect rectification tower 2 tower stills are solvent-laden impurity, send this distillation system through pump 6.
When steam that this solvent treatment technical process consumes only is single-tower rectifying 50%, 45% the when consumption of recirculated cooling water is about single-tower rectifying.
Claims (4)
1. technique of refining solvent in process of producing synthetic rubber, it is characterized in that: adopt the rectifying tower of a plurality of routines to be combined into a multiple-effect distillation system, and dispose corresponding reboiler and condenser, the solvent that cohesion process is next is through after dehydration or taking off light component, adopt two to imitate or three-effect rectification, remove the impurity in the solvent, reclaim solvent; By improving a working pressure of imitating, make one to imitate the thermal source of cat head gas phase as two effect reboilers, two imitate the thermal source of cat head gas phases as the triple effect reboiler; Imitate vapor condensation heat energy by the pressure that reduces last effect in order to using one; The working pressure that one is imitated is the 0.2-0.7MPa gauge pressure, and the working pressure of last effect is 0.06MPa vacuum tightness-0.03MPa gauge pressure; One is imitated tower top temperature at 140-115 ℃, and preceding effect tower top temperature is higher than next and imitates 10-25 ℃ of tower still temperature, and last is imitated the cat head gas phase and is controlled at 40-90 ℃ and 10-40 ℃ respectively in the outflow temperature of condenser and tail gas condenser.
2. technique of refining solvent in process of producing synthetic rubber according to claim 1, it is characterized in that: two effects distillation process technology in parallel is: the solvent that comes from dehydration tower is divided into the middle part that two equal stocks of flow do not enter an effect rectifying tower (1) and two effect rectifying tower (3), and cat head and tower still logistics composition that an effect, two is imitated rectifying tower all reach separation requirement; One imitates rectifying tower (1) provides heat by reboiler (2), and thermal source is steam or other heating agent; Sending into a solvent of imitating in the rectifying tower (1) is separated by refining, refining qualified solvent drains into reboiler (4) shell-side of two effect rectifying tower (3) from cat head with gas phase, as the thermal source of two effect rectifying tower (3), most of vapor phase solvent is condensed into liquid state and is discharged into solvent tank (5); A small amount of gas that is not condensed then drains into condenser (7), and controls this tower working pressure by the flow of this strand gas; Another strand solvent that comes from dehydration tower is sent into two and is imitated rectifying tower (3) middle and lower parts, imitates that rectifying tower (3) separate and qualified solvent enters condenser (7) from cat head with the gas phase form through two, is condensed to flow into return tank (9); For refining qualified solvent, utilize pressure reduction to be pressed into return tank (9) in the solvent tank (5); Be refining qualified solvent in the return tank (9), a part is sent to one respectively by reflux pump (10) imitates rectifying tower (1), two and imitates rectifying tower (3) cats head and do to reflux and use; Return tank (9) remaining solvent is sent distillation system as product by reflux pump (10); One to imitate rectifying tower (1) tower still be the impurity that contains solvent, utilizes two to imitate pressure reduction between rectifying tower and send into two and imitate rectifying tower (3) tower stills, and solvent-laden impurity is imitated rectifying tower (3) tower stills from two and discharged distillation systems with pump (6).
3. technique of refining solvent in process of producing synthetic rubber according to claim 1, it is characterized in that: two imitate series connection distillation process technology is: enter one of multiple-effect distillation system from the next solvent of dehydration tower and imitate rectifying tower (1), this tower provides heat by reboiler (2), and thermal source is steam or other heating agent; Solvent is imitated in the rectifying tower (1) by refining one, and refining qualified solvent drains into two reboiler (4) shell-sides of imitating rectifying tower (3) with gas phase from cat head, and as the thermal source of two effect rectifying, most of gas phase is condensed into liquid state and is discharged into solvent tank (5); A small amount of gas that is not condensed then drains into condenser (7), and controls this tower working pressure by the flow of this strand gas; One to imitate rectifying tower (1) tower still be the solvent that contains impurity, utilize two imitate between pressure reduction and deliver to two and imitate rectifying tower (3); Imitate that rectifying tower (3) separate and qualified solvent enters condenser (7) from cat head with the gas phase form through two, the back that is condensed flows into return tank (9); Be refining qualified solvent in the solvent tank (5), utilize pressure reduction to be pressed into return tank (9), qualified solvent in the return tank (9), a part is sent to one respectively by reflux pump (10) imitates rectifying tower (1), two and imitates rectifying tower (3) cats head and make backflow usefulness, and remaining solvent is sent distillation system as product by reflux pump (10); Solvent-laden impurity is imitated rectifying Tata still pump (6) discharge system from two.
4. technique of refining solvent in process of producing synthetic rubber according to claim 1 is characterized in that: the three-effect rectification flow process is: enter one of multiple-effect distillation system from the next solvent of dehydration tower and imitate rectifying tower (1), this tower provides heat by reboiler (2); Solvent is imitated in the rectifying tower (1) by refining one, and refining qualified solvent drains into two reboiler (4) shell-sides of imitating rectifying tower (3) with gas phase from cat head, and as the thermal source of two effect rectifying, most of gas phase is condensed into liquid state and is discharged into solvent tank (5); A small amount of gas that is not condensed then drains into condenser (7), and controls this tower working pressure by the flow of this strand gas; One to imitate rectifying tower (1) tower still be impure solvent, utilize one, two imitate between pressure reduction and deliver to two and imitate rectifying tower (3); Impure solvent is imitated in the rectifying tower (3) separated two, refining qualified solvent enters three-effect rectification tower (5) reboiler (13) shell-side from cat head with gas phase; Flow into solvent tank (5) as thermal source at the solvent that reboiler (13) is condensed, the gas phase that is not condensed is discharged into condenser (7), and is controlled the working pressure of two effect rectifying tower (3) by the flow of this strand gas; Two to imitate rectifying tower (3) tower stills are impure solvents, utilize two, the pressure reduction between triple effect and deliver to three-effect rectification tower (12); The solvent that the contains impurity separation that in three-effect rectification tower (12), is distillated, refining qualified solvent enters condenser (7) from cat head with the gas phase form, and the solvent after being condensed flows into return tank (9); Be refining qualified solvent in the solvent tank (5), deliver to one respectively by solvent pump (11) and imitate rectifying tower (1) and two effect rectifying tower (3) cats head reflux that remaining solvent is delivered to return tank (9); Be refining qualified solvent in the return tank (9), deliver to three-effect rectification tower (12) cat head by reflux pump (10) and reflux that remaining solvent is sent distillation system through pump (10); Solvent-laden impurity is discharged distillation system from three-effect rectification tower (12) tower still with pump (6); Enter after the most of gas phase of condenser (7) is condensed, a small amount of gas phase that contains non-condensable gas enters tail gas condenser (8) and continues cooling and condensation reclaiming solvent, and the non-condensable gas that is not condensed effluxes.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100320734A CN100363409C (en) | 2006-08-06 | 2006-08-06 | Technique of refining solvent in process of producing synthetic rubber |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100320734A CN100363409C (en) | 2006-08-06 | 2006-08-06 | Technique of refining solvent in process of producing synthetic rubber |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1908040A CN1908040A (en) | 2007-02-07 |
| CN100363409C true CN100363409C (en) | 2008-01-23 |
Family
ID=37699281
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2006100320734A Active CN100363409C (en) | 2006-08-06 | 2006-08-06 | Technique of refining solvent in process of producing synthetic rubber |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100363409C (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103214346A (en) * | 2013-04-12 | 2013-07-24 | 湖南百利工程科技股份有限公司 | Recovering process of solvent tertiary butanol in production process of ammoximation |
| CN104086371B (en) * | 2014-07-07 | 2015-12-30 | 湖南百利工程科技股份有限公司 | The processing method that in the cyclohexene method preparing cyclohexanone production process, hexalin is separated |
| CN104592544B (en) * | 2015-01-27 | 2017-07-21 | 湖南百利工程科技股份有限公司 | Solvent refining processes in a kind of synthetic rubber production process |
| CN106316792B (en) * | 2016-08-09 | 2019-07-05 | 天津大学 | The device and method of methanol and ethyl alcohol is recycled from stalk sugar hydrocrackates |
| KR102592983B1 (en) * | 2016-08-11 | 2023-10-23 | 베르살리스 에스.피.에이. | Method for Purifying Solvents Derived from Preparation of Elastomer Blends |
| JP7101813B2 (en) * | 2018-11-01 | 2022-07-15 | エルジー・ケム・リミテッド | Method of separating an organic solvent from a mixed solution containing an organic solvent |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1106710A (en) * | 1994-11-18 | 1995-08-16 | 天津大学 | Single-tower atmospheric intermittent extractive rectification method |
| CN1380291A (en) * | 2002-04-12 | 2002-11-20 | 岳阳昌德化工实业有限公司 | Method for separating and recovering epoxycyclohexane from cyclohexane oxidation by-product light oil |
| CN1233710C (en) * | 2002-03-20 | 2005-12-28 | 自贡鸿鹤化工股份有限公司 | Method for recycling colvent utilized in producting polyphenylene sulfide |
-
2006
- 2006-08-06 CN CNB2006100320734A patent/CN100363409C/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1106710A (en) * | 1994-11-18 | 1995-08-16 | 天津大学 | Single-tower atmospheric intermittent extractive rectification method |
| CN1233710C (en) * | 2002-03-20 | 2005-12-28 | 自贡鸿鹤化工股份有限公司 | Method for recycling colvent utilized in producting polyphenylene sulfide |
| CN1380291A (en) * | 2002-04-12 | 2002-11-20 | 岳阳昌德化工实业有限公司 | Method for separating and recovering epoxycyclohexane from cyclohexane oxidation by-product light oil |
Non-Patent Citations (1)
| Title |
|---|
| 多级精馏装置的节能研究与分析. 王以清.能源工程，第6期. 2002 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1908040A (en) | 2007-02-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100363409C (en) | Technique of refining solvent in process of producing synthetic rubber | |
| CN103214346A (en) | Recovering process of solvent tertiary butanol in production process of ammoximation | |
| CN102040676B (en) | Method for depriving solvent for cis-polybutadiene | |
| CN101602640A (en) | The energy-saving separation method of ethyl benzene/styrene | |
| CN102211992A (en) | Process for reclaiming dibasic acid from adipic acid production waste solution | |
| CN102391064B (en) | Process for recovering and refining extracting agent in production procedure of hexanolactam | |
| CN103788026A (en) | Method of purifying propylene epoxide | |
| CN101734999A (en) | Method for sequential separation and azeotropic recovery of ethyl benzene/styrene | |
| CN203483884U (en) | Device for concentrating caprolactam solution with combination of mechanical vapor recompression and multiple-effect evaporation | |
| CN105237370A (en) | Method for producing cyclohexanone by cyclohexanol dehydrogenation | |
| CN109704920B (en) | Energy-saving process and device for producing fuel ethanol from low-concentration fermentation liquor | |
| CN104629082B (en) | Method for recovering and refining solvent and monomer in industrial production of rare earth isoprene rubber | |
| CN107915580A (en) | A kind of ethylene glycol multi-effect distillation system and process | |
| CN104370697A (en) | Flexible methanol rectification method and device capable of producing both MTO-grade and AA-grade methanol | |
| CN105566030B (en) | BTX separation method | |
| CN103484154A (en) | Condensed water stripped crude oil stabilization method and special device thereof | |
| CN103910605B (en) | The technique of a kind of infiltration evaporation system and refined biological propyl carbinol thereof | |
| CN203677978U (en) | Vapor-compression type alcohol recovery tower | |
| CN105669353B (en) | Ethylbenzene styrene separation process | |
| CN101966397B (en) | Energy-saving rectifying device for integrating energy in rectifying tower sequence and method | |
| CN203878081U (en) | Device system for solvent recovery in process of purifying phenazine by using RT base byproduct | |
| CN213924578U (en) | Dichloromethane recovery device in production process of wet lithium battery diaphragm | |
| CN112174773A (en) | Dichloromethane recovery device and method in wet lithium battery diaphragm production process | |
| CN105669354B (en) | ethylbenzene dehydrogenation reaction product separation method | |
| CN208008695U (en) | Crude styrene piece-rate system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 1 No. 414007 Hunan province Yueyang City dongting Avenue Patentee after: Hunan Baili Engineering Sci & Tech Co.,Ltd. Address before: 1 No. 414007 Hunan province Yueyang City dongting Avenue Patentee before: Hunan Baili Engineering Sci-Tech Co., Ltd. |