CN204569785U - A kind of device reclaiming DMSO from the DMSO aqueous solution - Google Patents
A kind of device reclaiming DMSO from the DMSO aqueous solution Download PDFInfo
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- CN204569785U CN204569785U CN201520144499.3U CN201520144499U CN204569785U CN 204569785 U CN204569785 U CN 204569785U CN 201520144499 U CN201520144499 U CN 201520144499U CN 204569785 U CN204569785 U CN 204569785U
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Abstract
The utility model relates to a kind of device reclaiming DMSO from the DMSO aqueous solution, comprise one-level dehydration tower, secondary dehydration tower, three grades of dehydration towers, product tower and recovery vapo(u)rization system, be connected with secondary dehydration tower by the forced circulation system before secondary dehydration tower bottom one-level dehydration tower, be connected with three grades of dehydration towers bottom secondary dehydration tower, be connected with product tower at the bottom of three grades of dehydration tower towers, be connected with recovery vapo(u)rization system at the bottom of product tower tower, a product tower preheater is provided with between one-level dehydration tower and described forced circulation system, described one-level dehydration tower is connected with described forced circulation system by described product tower preheater, described product tower preheater is also connected with described product top of tower.This device is negative-pressure operation, and device operation easier is low, and safety coefficient is high, and adopt economic benefits and social benefits to be coupled four tower rectification process, take full advantage of low grade heat energy, reduce production cost, reach the object of economical and energy saving, economic benefit and social benefit significantly improve.
Description
Technical field
The utility model relates to a kind of device reclaiming DMSO from the DMSO aqueous solution, belongs to chemical materials purification field.
Background technology
Dimethyl sulfoxide (DMSO) is a kind of not only water-soluble but also is dissolved in the very important aprotic polar solvent of organic solvent, is used as solvent and reaction reagent widely, has very high selection extracting ability.The dimethyl sulfoxide (DMSO) process water environmental pollution produced in chemical process is very large, and dimethyl sulfoxide (DMSO) is reclaimed not only economy but also environmental protection, but the extraction difficulty of current DMSO is large, and purity is low, and energy consumption is high, and wastes time and energy.
Utility model content
The deficiency that the utility model exists for prior art, provides a kind of processing method reclaiming DMSO from the mixture of process waste liquor DMSO and water, obtains highly purified DMSO, make full use of heat and cold, economical and energy saving simultaneously.
The technical scheme that the utility model solves the problems of the technologies described above is as follows: a kind of device reclaiming DMSO from the DMSO aqueous solution, this device comprises one-level dehydration tower, secondary dehydration tower, three grades of dehydration towers, product tower and recovery vapo(u)rization system, be connected with described secondary dehydration tower by the forced circulation system before secondary dehydration tower bottom described one-level dehydration tower, be connected with described three grades of dehydration towers bottom described secondary dehydration tower, be connected with described product tower at the bottom of described three grades of dehydration tower towers, be connected with described recovery vapo(u)rization system at the bottom of described product tower tower, a product tower preheater is provided with between described one-level dehydration tower and described forced circulation system, described one-level dehydration tower is connected with described forced circulation system by described product tower preheater, described product tower preheater is also connected with described product top of tower.
As further optimization of the present utility model, described forced circulation evaporation system comprises evaporating pot, is connected with evaporating pot and forms the evaporating pot well heater of circulation loop and the forced circulation pump for the formation of pump circulation, and described evaporating pot top is provided with a circulating and evaporating treatment agent entrance.
As further optimization of the present utility model, the tower top of described one-level dehydration tower, secondary dehydration tower, three grades of dehydration towers and product tower being respectively provided with one for the condenser of cooling exhaust and the return tank for storing discharge technology water, being respectively one-level dehydration tower condenser, one-level dehydration tower return tank, secondary dehydration tower condenser, secondary dehydration tower return tank, three grades of dehydration tower condensers, three grades of dehydration tower return tanks, product tower condenser, product tower return tanks.
As further optimization of the present utility model, the bottom of described one-level dehydration tower, secondary dehydration tower, three grades of dehydration towers and product tower be respectively provided with one with the reboiler in formation loop, bottom, be respectively one-level dehydration column reboiler, secondary dehydration column reboiler, three grades of dehydration column reboilers and product tower reboiler.
As further optimization of the present utility model, described secondary dehydration tower top is connected with one-level dehydration column reboiler and forms economic benefits and social benefits coupling circuit.
As further optimization of the present utility model, between described product tower and described recovery vapo(u)rization system, be connected with a high transfer tank that boils.
As further optimization of the present utility model, described recovery vapo(u)rization system is scraper evaporator, described scraper evaporator top is provided with a scraper evaporator gaseous phase outlet, described scraper evaporator gaseous phase outlet is connected with a scraper evaporator condenser and a scraper evaporator receiving tank, is provided with a scraper evaporator liquid-phase outlet bottom described scraper evaporator.
As further optimization of the present utility model, described recovery vapo(u)rization system is evaporating kettle, described evaporating kettle top is provided with one and reclaims evaporation process agent entrance and evaporating kettle gaseous phase outlet, described evaporating kettle gaseous phase outlet is connected with an evaporating kettle condenser and an evaporating kettle receiving tank, an evaporating kettle liquid-phase outlet is provided with, in order to discharge the thing that heavily boils bottom described evaporating kettle.
As further optimization of the present utility model, described recovery vapo(u)rization system comprises scraper evaporator and evaporating kettle, described scraper evaporator top is provided with a scraper evaporator gaseous phase outlet, described scraper evaporator gaseous phase outlet is connected with a scraper evaporator condenser and a scraper evaporator receiving tank, a scraper evaporator liquid-phase outlet is provided with bottom described scraper evaporator, described evaporating kettle top is provided with one and reclaims evaporation process agent entrance and evaporating kettle gaseous phase outlet, described evaporating kettle gaseous phase outlet is connected with an evaporating kettle condenser and an evaporating kettle receiving tank, an evaporating kettle liquid-phase outlet is provided with bottom described evaporating kettle, in order to discharge the thing that heavily boils, described scraper evaporator liquid-phase outlet is connected with described evaporating kettle top.
The beneficial effects of the utility model are: the utility model can reclaim qualified DMSO from the DMSO aqueous solution, four towers and vapo(u)rization system are negative-pressure operation, reduce service temperature, improve the safety performance of plant running, reduce production cost, one-level dehydration tower and secondary dehydration tower adopt the scheme of economic benefits and social benefits thermal coupling, secondary dehydration column overhead steam is utilized to heat to one-level dehydration tower, complete the utilization of tow taste heat, reach and make full use of heat and cold, the object of economical and energy saving, economic benefit and social benefit significantly improve.
Accompanying drawing explanation
Fig. 1 is the Structure and Process schematic diagram of the utility model embodiment one;
Fig. 2 is the Structure and Process schematic diagram of the utility model embodiment two;
Fig. 3 is the Structure and Process schematic diagram of the utility model embodiment three;
Fig. 4 is the Structure and Process schematic diagram of the utility model embodiment four;
Fig. 5 is the Structure and Process schematic diagram of the utility model embodiment five;
Fig. 6 is the Structure and Process schematic diagram of the utility model embodiment six;
Wherein, 1, one-level dehydration tower; 2, secondary dehydration tower; 3, three grades of dehydration towers; 4, product tower; 5, evaporating pot; 6, evaporating kettle; 7, scraper evaporator; 8, one-level dehydration tower condenser; 9, one-level dehydration tower return tank; 10, three grades of dehydration tower condensers; 11, evaporating pot well heater; 12, secondary dehydration tower condenser; 13, secondary dehydration tower return tank; 14, one-level dehydration column reboiler; 15, three grades of dehydration tower return tanks; 16, product tower condenser; 17, product tower return tank; 18, height boils transfer tank; 19, scraper condenser; 20, scraper evaporator receiving tank; 21, evaporating kettle condenser; 22, evaporating kettle receiving tank; 23, head tank; 24, scraper evaporator gaseous phase outlet; 25, scraper evaporator liquid-phase outlet; 26, evaporating kettle liquid-phase outlet; 27, evaporating kettle gaseous phase outlet; 28, treatment agent import; 29, secondary dehydration column reboiler; 30, three grades of dehydration column reboilers; 31, product tower reboiler; 32, product tower preheater; 33, forced circulation pump.
Embodiment
Be described principle of the present utility model and feature below in conjunction with accompanying drawing, example, only for explaining the utility model, is not intended to limit scope of the present utility model.
In the utility model, what adopt is a kind of device reclaiming DMSO from the DMSO aqueous solution, this device comprises one-level dehydration tower 1, secondary dehydration tower 2, three grades of dehydration towers 3, product tower 4 and evaporating kettle 6, product tower preheater 32 by being connected with product tower 4 tower top bottom described one-level dehydration tower 1 is connected with described secondary dehydration tower 2 tower reactor, be connected with described three grades of dehydration tower 3 tower reactors bottom described secondary dehydration tower 2, be connected with described product tower 4 tower reactor at the bottom of described three grades of dehydration tower 3 towers, at the bottom of described product tower 4 tower and be provided with a scraper evaporator 7 between described evaporating kettle 6, be connected with described evaporating kettle 6 by described scraper evaporator 7 at the bottom of described product tower 4 tower.
Described evaporating kettle 6 top is provided with a treatment agent import 28 and an evaporating kettle gaseous phase outlet 27, and bottom is provided with an evaporating kettle liquid-phase outlet 26, and described evaporating kettle gaseous phase outlet 27 place is connected with an evaporating kettle condenser 21 and an evaporating kettle receiving tank 22 in turn.
Described scraper evaporator 7 top is provided with a scraper evaporator gaseous phase outlet 24, and bottom is provided with a scraper evaporator liquid-phase outlet 25, and described scraper evaporator gaseous phase outlet 24 place is connected with a scraper condenser 19 and a scraper plate receiving tank 20 in turn.
The tower top of described one-level dehydration tower 1 tower top and three grades of dehydration towers 3 is respectively provided with one for the condenser of cooling exhaust and the return tank for storing discharge technology water, is respectively one-level dehydration tower condenser 8, one-level dehydration tower return tank 9 and secondary dehydration tower condenser 12, secondary dehydration tower return tank 13.
The pipeline that described three grades of dehydration tower condensers 10 are connected with described secondary dehydration tower 2 is communicated with an evaporating pot 5, described evaporating pot 5 is connected with an evaporating pot well heater 11.
The bottom of described one-level dehydration tower 1, secondary dehydration tower 2, three grades of dehydration towers 3 and product tower 4 be respectively provided with one with the reboiler in formation loop, bottom, be respectively one-level dehydration column reboiler 14, secondary dehydration column reboiler 29, three grades of dehydration column reboilers 30 and product tower reboiler 31.
Described secondary dehydration tower 2 top is connected with one-level dehydration column reboiler 14 and forms loop.
The backflow branch road that described secondary dehydration tower 2 top is connected with described secondary dehydration column reboiler 29 is communicated with successively a secondary dehydration tower condenser 12 and a secondary dehydration tower return tank 13.
Embodiment one:
As shown in Figure 1, present embodiment one is under condition of negative pressure, the mixture of DMSO and water is added one-level dehydration tower 1, feed composition is DMSO45% (wt%) and water 55% (wt%), feeding temperature is 60 DEG C, the working pressure of one-level dehydration tower 1 is 10-15KPa (A), service temperature is 45-55 DEG C, one-level dehydration tower 1 trim the top of column is than being 0.1-0.8, process steam is from one-level dehydration tower 1 overhead extraction, by collecting in one-level dehydration tower return tank 9 after the condensation of one-level dehydration tower condenser 8, then a part of cooled process water is discharged to process water system, another part is back to one-level dehydration tower 1 tower top and completes reflux operation, kettle material enters into product tower preheater 32, product tower preheater 32 is connected with the tower top of product tower 4 simultaneously, material carries out thermal exchange in the steam discharging of product tower preheater 32 neutralized product tower 4 tower top, material is after preheating, enter into the evaporating pot 5 before secondary dehydration tower 2, pump circulation treatment agent is added in evaporating pot 5, by the effect of forced circulation pump 33 and evaporating pot well heater 11, one-level dehydration tower 1 still material pump circulation is heated, thus make one-level dehydration tower 1 still material become steam to enter secondary dehydration tower.
Working pressure in evaporating pot 5 is 25-37KPa (A), service temperature 100-127 DEG C.
Secondary dehydration tower 2 working pressure is 25-35KPa (A), service temperature is 60-125 DEG C, trim the top of column is than being 0.2-1.0, material process steam after secondary dehydration tower 2 rectifying carries out condensation by secondary dehydration tower 2 overhead extraction to secondary dehydration tower condenser 12, after entering secondary dehydration tower return tank 13, the cooled process water of a part is discharged to process water system, another part is back to secondary dehydration tower 2 tower top and completes reflux operation, secondary dehydration tower 2 still material enters three grades of dehydration towers 3, the process steam of secondary dehydration tower 2 tower top can enter one-level dehydration column reboiler 14 provides heat to one-level dehydration tower 1, enter the condensation of secondary dehydration tower condenser 12 again to discharge.
Three grades of dehydration tower 3 working pressures are 10-15KPa (A), service temperature is 45-125 DEG C, trim the top of column is than being 3-6, material process steam after the rectifying of three grades of dehydration towers 3 all enters into the condensation of three grades of dehydration tower condensers 10 from three grades of dehydration tower 3 tower tops, then after entering three grades of dehydration tower return tanks 15, the cooled process water of a part is discharged to process water system, another part is back to three grades of dehydration tower 3 tower tops and circulates, material component is now DMSO and a small amount of high boiling material, and three grades of dehydration tower 3 still material enter product tower 4.
Product tower 4 working pressure is 5-12KPa (A), service temperature is 110-127 DEG C, trim the top of column is than being 0.5-1.5, material in product tower 4 after rectifying DMSO from tower top by product tower condenser 16 collect after, enter into product tower return tank 17, product composition DMSO >=99.95% (wt%) now obtained, heavily boil thing and a small amount of DMSO in tower reactor boil after transfer tank 18 and scraper evaporator 7 by height, from the scraper evaporator liquid-phase outlet 25 be positioned at bottom scraper evaporator 7, enter into evaporating kettle 6.
Described scraper evaporator 7 top is provided with a scraper evaporator gaseous phase outlet 24, and scraper evaporator gaseous phase outlet 24 place is communicated with a scraper condenser 19 and a scraper plate receiving tank 20 successively, discharges for the vapor condensation of being discharged by scraper evaporator 7.
Add the agent of a certain amount of recovery evaporation process in evaporating kettle 6, by DMSO and water evaporation, flow to after evaporating kettle condenser 21 condensation from the evaporating kettle gaseous phase outlet 27 being arranged in evaporating kettle 6 top and enter evaporating kettle receiving tank 22, then can select to enter into head tank 23 or evaporating pot 5 circulates, evaporating kettle liquid-phase outlet 26 extraction of thing from evaporating kettle 6 end of heavily boiling.
Embodiment two:
As shown in Figure 2, present embodiment two is under condition of negative pressure, the mixture of DMSO and water is added one-level dehydration tower 1, feed composition is DMSO15% (wt%) and water 85% (wt%), feeding temperature is 60 DEG C, the working pressure of one-level dehydration tower 1 is 10-15KPa (A), service temperature is 45-55 DEG C, one-level dehydration tower 1 trim the top of column is than being 0.1-0.8, process steam is from one-level dehydration tower 1 overhead extraction, by collecting in one-level dehydration tower return tank 9 after the condensation of one-level dehydration tower condenser 8, then a part of cooled process water is discharged to process water system, another part is back to one-level dehydration tower 1 tower top and circulates, material enters into product tower preheater 32, product tower preheater 32 is connected with the tower top of product tower 4 simultaneously, material carries out thermal exchange in the steam discharging of product tower preheater 32 neutralized product tower 4 tower top, material is after preheating, enter into the evaporating pot 5 before secondary dehydration tower 2, pump circulation treatment agent is added in evaporating pot 5, by the effect of forced circulation pump 33 and evaporating pot well heater 11, one-level dehydration tower 1 still material pump circulation is heated, thus make one-level dehydration tower 1 still material become steam to enter secondary dehydration tower.
Working pressure in evaporating pot 5 is 25-37KPa (A), service temperature 100-127 DEG C.
Secondary dehydration tower 2 working pressure is 25-35KPa (A), service temperature is 60-125 DEG C, trim the top of column is than being 0.2-1.0, material process steam after secondary dehydration tower 2 rectifying carries out condensation by secondary dehydration tower 2 overhead extraction to secondary dehydration tower condenser 12, after entering secondary dehydration tower return tank 13, the cooled process water of a part is discharged to process water system, another part is back to secondary dehydration tower 2 tower top and completes backflow, secondary dehydration tower 2 still material enters three grades of dehydration towers 3, the process steam of secondary dehydration tower 2 tower top can enter one-level dehydration column reboiler 14 provides heat to one-level dehydration tower 1, enter the condensation of secondary dehydration tower condenser 12 again to discharge.
Three grades of dehydration tower 3 working pressures are 10-15KPa (A), service temperature is 45-125 DEG C, trim the top of column is than being 3-6, material process steam after the rectifying of three grades of dehydration towers 3 all enters into the condensation of three grades of dehydration tower condensers 10 from three grades of dehydration tower 3 tower tops, then after entering three grades of dehydration tower return tanks 15, the cooled process water of a part is discharged to process water system, another part is back to three grades of dehydration tower 3 tower tops and completes reflux operation, material component is now DMSO and a small amount of high boiling material, and three grades of dehydration tower 3 still material enter product tower 4.
Product tower 4 working pressure is 5-12KPa (A), service temperature is 110-127 DEG C, trim the top of column is than being 0.5-1.5, material in product tower 4 after rectifying DMSO from tower top by product tower condenser 16 collect after, enter into product tower return tank 17, product composition DMSO >=99.95% (wt%) now obtained, heavily boil thing and a small amount of DMSO in tower reactor enter into scraper evaporator 7 by the height transfer tank 18 that boils.
Described scraper evaporator 7 top is provided with a scraper evaporator gaseous phase outlet 24, scraper evaporator gaseous phase outlet 24 place is communicated with a scraper condenser 19 and a scraper plate receiving tank 20 successively, DMSO condensation for being discharged by scraper evaporator 7 is discharged, be provided with a scraper evaporator liquid-phase outlet 25 bottom described scraper evaporator 19, the thing that heavily boils is from scraper evaporator liquid-phase outlet 25 extraction.
Embodiment three:
As shown in Figure 3, present embodiment three is under condition of negative pressure, the mixture of DMSO and water is added one-level dehydration tower 1, feed composition is DMSO80% (wt%) and water 20% (wt%), feeding temperature is 60 DEG C, the working pressure of one-level dehydration tower 1 is 10-15KPa (A), service temperature is 45-55 DEG C, one-level dehydration tower 1 trim the top of column is than being 0.1-0.8, process steam is from one-level dehydration tower 1 overhead extraction, by collecting in one-level dehydration tower return tank 9 after the condensation of one-level dehydration tower condenser 8, then a part of cooled process water is discharged to process water system, another part is back to one-level dehydration tower 1 tower top and completes backflow, material enters into product tower preheater 32, product tower preheater 32 is connected with the tower top of product tower 4 simultaneously, material carries out thermal exchange in the steam discharging of product tower preheater 32 neutralized product tower 4 tower top, material is after preheating, enter into the evaporating pot 5 before secondary dehydration tower 2, pump circulation treatment agent is added in evaporating pot 5, by the effect of forced circulation pump 33 and evaporating pot well heater 11, one-level dehydration tower 1 still material pump circulation is heated, thus make one-level dehydration tower 1 still material become steam to enter secondary dehydration tower.After the discharging of one-level dehydration tower 1 still material, at product tower preheater 32 neutralized product tower 4 overhead vapours discharging heat-shift, after preheating, enter the evaporating pot 5 before secondary dehydration tower 2.
Working pressure in evaporating pot 5 is 25-37KPa (A), service temperature 100-127 DEG C.
Secondary dehydration tower 2 working pressure is 25-35KPa (A), service temperature is 60-125 DEG C, trim the top of column is than being 0.2-1.0, material process steam after secondary dehydration tower 2 rectifying carries out condensation by secondary dehydration tower 2 overhead extraction to secondary dehydration tower condenser 12, after entering secondary dehydration tower return tank 13, the cooled process water of a part is discharged to process water system, another part is back to secondary dehydration tower 2 tower top and completes reflux operation, secondary dehydration tower 2 still material enters three grades of dehydration towers 3, the process steam of secondary dehydration tower 2 tower top can enter one-level dehydration column reboiler 14 provides heat to one-level dehydration tower 1, enter the condensation of secondary dehydration tower condenser 12 again to discharge.
Three grades of dehydration tower 3 working pressures are 10-15KPa (A), service temperature is 45-125 DEG C, trim the top of column is than being 3-6, material process steam after the rectifying of three grades of dehydration towers 3 all enters into the condensation of three grades of dehydration tower condensers 10 from three grades of dehydration tower 3 tower tops, then after entering three grades of dehydration tower return tanks 15, the cooled process water of a part is discharged to process water system, another part is back to three grades of dehydration tower 3 tower tops and circulates, material component is now DMSO and a small amount of high boiling material, and three grades of dehydration tower 3 still material enter product tower 4.
Product tower 4 working pressure is 5-12KPa (A), service temperature is 110-127 DEG C, trim the top of column is than being 0.5-1.5, material in product tower 4 after rectifying DMSO from tower top by product tower condenser 16 collect after, enter into product tower return tank 17, product composition DMSO >=99.95% (wt%) now obtained, heavily boil thing and a small amount of DMSO in tower reactor enter into evaporating kettle 6 by the height transfer tank 18 that boils.
Add the agent of a certain amount of recovery evaporation process in evaporating kettle 6, by DMSO and water evaporation, flow to after evaporating kettle condenser 21 condensation from the evaporating kettle gaseous phase outlet 27 being arranged in evaporating kettle 6 top and enter evaporating kettle receiving tank 22, then can select to enter into head tank 23 or evaporating pot 5 circulates, evaporating kettle liquid-phase outlet 26 extraction of thing from evaporating kettle 6 end of heavily boiling.
Embodiment four:
As shown in Figure 4, present embodiment four, on the basis of embodiment one, cancels the high transfer tank 18 that boils, that is: be directly connected with described scraper evaporator 24 at the bottom of the tower of product tower 4.
Embodiment five:
As shown in Figure 5, present embodiment five, on the basis of embodiment two, cancels the high transfer tank 18 that boils, that is: be directly connected with described scraper evaporator 24 at the bottom of the tower of product tower 4.
Embodiment six:
As shown in Figure 6, present embodiment six, on the basis of embodiment three, cancels the high transfer tank 18 that boils, that is: be directly connected with described evaporating kettle 6 at the bottom of the tower of product tower 4.
The foregoing is only preferred embodiment of the present utility model, not in order to limit the utility model, all within spirit of the present utility model and principle, any amendment done, equivalent replacement, improvement etc., all should be included within protection domain of the present utility model.
Claims (9)
1. one kind is reclaimed the device of DMSO from the DMSO aqueous solution, comprise one-level dehydration tower, secondary dehydration tower, three grades of dehydration towers, product tower and recovery vapo(u)rization system, it is characterized in that: be connected with described secondary dehydration tower by the forced circulation system before secondary dehydration tower bottom described one-level dehydration tower, be connected with described three grades of dehydration towers bottom described secondary dehydration tower, be connected with described product tower at the bottom of described three grades of dehydration tower towers, be connected with described recovery vapo(u)rization system at the bottom of described product tower tower, a product tower preheater is provided with between described one-level dehydration tower and described forced circulation system, described one-level dehydration tower is connected with described forced circulation system by described product tower preheater, described product tower preheater is also connected with described product top of tower.
2. a kind of device reclaiming DMSO from the DMSO aqueous solution according to claim 1, it is characterized in that, described forced circulation evaporation system comprises evaporating pot, is connected with evaporating pot and forms the evaporating pot well heater of circulation loop and the forced circulation pump for the formation of pump circulation, and described evaporating pot top is provided with a circulating and evaporating treatment agent entrance.
3. a kind of device reclaiming DMSO from the DMSO aqueous solution according to claim 1, it is characterized in that, the tower top of described one-level dehydration tower, secondary dehydration tower, three grades of dehydration towers and product tower being respectively provided with one for the condenser of cooling exhaust and the return tank for storing discharge technology water, being respectively one-level dehydration tower condenser, one-level dehydration tower return tank, secondary dehydration tower condenser, secondary dehydration tower return tank, three grades of dehydration tower condensers, three grades of dehydration tower return tanks, product tower condenser, product tower return tanks.
4. a kind of device reclaiming DMSO from the DMSO aqueous solution according to claim 1 or 3, it is characterized in that, the bottom of described one-level dehydration tower, secondary dehydration tower, three grades of dehydration towers and product tower be respectively provided with one with the reboiler in formation loop, bottom, be respectively one-level dehydration column reboiler, secondary dehydration column reboiler, three grades of dehydration column reboilers and product tower reboiler.
5. a kind of device reclaiming DMSO from the DMSO aqueous solution according to claim 4, is characterized in that, described secondary dehydration tower top is connected with one-level dehydration column reboiler and forms economic benefits and social benefits coupling circuit.
6. a kind of device reclaiming DMSO from the DMSO aqueous solution according to claim 5, is characterized in that, is connected with a high transfer tank that boils between described product tower and described recovery vapo(u)rization system.
7. a kind of device reclaiming DMSO from the DMSO aqueous solution according to claim 1 or 6, it is characterized in that, described recovery vapo(u)rization system is scraper evaporator, described scraper evaporator top is provided with a scraper evaporator gaseous phase outlet, described scraper evaporator gaseous phase outlet is connected with a scraper evaporator condenser and scraper evaporator receiving tank, is provided with a scraper evaporator liquid-phase outlet bottom described scraper evaporator.
8. a kind of device reclaiming DMSO from the DMSO aqueous solution according to claim 1 or 6, it is characterized in that, described recovery vapo(u)rization system is evaporating kettle, described evaporating kettle top is provided with one and reclaims evaporation process agent entrance and evaporating kettle gaseous phase outlet, described evaporating kettle gaseous phase outlet is connected with an evaporating kettle condenser and an evaporating kettle receiving tank, an evaporating kettle liquid-phase outlet is provided with, in order to discharge the thing that heavily boils bottom described evaporating kettle.
9. a kind of device reclaiming DMSO from the DMSO aqueous solution according to claim 1 or 6, it is characterized in that, described recovery vapo(u)rization system comprises scraper evaporator and evaporating kettle, described recovery vapo(u)rization system is scraper evaporator, described scraper evaporator top is provided with a scraper evaporator gaseous phase outlet, described scraper evaporator gaseous phase outlet is connected with a scraper evaporator condenser and a scraper evaporator receiving tank, a scraper evaporator liquid-phase outlet is provided with bottom described scraper evaporator, described evaporating kettle top is provided with one and reclaims evaporation process agent entrance and evaporating kettle gaseous phase outlet, described evaporating kettle gaseous phase outlet is connected with an evaporating kettle condenser and an evaporating kettle receiving tank, an evaporating kettle liquid-phase outlet is provided with bottom described evaporating kettle, in order to discharge the thing that heavily boils, described scraper evaporator liquid-phase outlet is connected with described evaporating kettle top.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520144499.3U CN204569785U (en) | 2015-03-13 | 2015-03-13 | A kind of device reclaiming DMSO from the DMSO aqueous solution |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201520144499.3U CN204569785U (en) | 2015-03-13 | 2015-03-13 | A kind of device reclaiming DMSO from the DMSO aqueous solution |
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| CN204569785U true CN204569785U (en) | 2015-08-19 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113559542A (en) * | 2021-07-19 | 2021-10-29 | 常州乐研分离技术有限公司 | Device and method for DMSO (dimethyl sulfoxide) concentration process |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113559542A (en) * | 2021-07-19 | 2021-10-29 | 常州乐研分离技术有限公司 | Device and method for DMSO (dimethyl sulfoxide) concentration process |
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