CN204841160U - Feed liquid enrichment facility - Google Patents
Feed liquid enrichment facility Download PDFInfo
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- CN204841160U CN204841160U CN201520440810.9U CN201520440810U CN204841160U CN 204841160 U CN204841160 U CN 204841160U CN 201520440810 U CN201520440810 U CN 201520440810U CN 204841160 U CN204841160 U CN 204841160U
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Abstract
The utility model discloses a feed liquid enrichment facility, it includes concentrated system, solvent recycling system and concentration governing system, utilize organic solvent to produce the solvent vapour at extrinsic cycle evaporation separator and carry out " vapour - gas " heating through the secondary heating ware with live steam, if the concentration of water extract, then carry out " vapour - vapour " hybrid heating principle with flash steam and live steam, as the heating heat source in fast pass to the extrinsic cycle evaporimeter, make the feed liquid maintain boiling state, part steam becomes the condensate behind the heater, feed liquid preheats the use, the liquid solvent that changes the attitude after the noncondensable gas in the steam and the heat exchange all will rationally be retrieved, its waste heat of make full use of continues to preheat for the feed liquid, it is final through the recovery cycle recycle of plate heat exchanger realization to organic solvent, the utility model discloses energy -conserving, high -efficient in concentration process and organic solvent (like ethanol etc. ) concentration process, consumption reduction, low -cost, low drop into and the concentration process in the concentration can be adjusted freely of liquid medicine.
Description
Technical field
The utility model relates to technical field of medicament, specifically relates to a kind of concentration device for material liquid.
Background technology
The concentrated of feed liquid is requisite key unit operations during preparation is produced, through heat transfer, extract is warming up to fluidized state at a certain temperature, by the material of non-volatile or difficult volatilization with have volatile separated from solvent to a certain degree, obtain the concentrate with certain density.
At present, in industrial processes, the concentrated of extract adopts single-action, economic benefits and social benefits and Multi-effect concentration device more.In recent years, MVR inspissator also to start apply by minority enterprise.Single-action or Multi-effect concentration equipment adopt steam jacket mode to heat, its remarkable defect is to conduct heat that length consuming time, temperature are high, lack of homogeneity etc., is unfavorable for thermal sensitivity and effumability composition, simultaneously, such equipment cost is high, energy consumption is large, production efficiency is low, and steam is wasted in a large number.And MVR to concentrate be utilize compressor to heat up to the indirect steam reclaimed, recirculation uses, thus reduces a technology of energy demand to external world.Relative to single-action and Multi-effect concentration equipment, MVR inspissator possesses the advantages such as efficiency is high, energy consumption is low, space is little.And MVR inspissator is expensive, noise is large, subsequent maintenance cost is high, concentrated solution density is low and can not be used for reclaiming organic solvent (as ethanol) etc.But in actual production, if feed liquid solvent is organic solvent (as alcohol), the efficiency of above-mentioned inspissator to organic solvent recycling is low, causes a large amount of loss of organic solvent and waste, thus occurs the phenomenon of resource irrational utilization.
Utility model content
The purpose of this utility model is to overcome traditional evaporation and concentration and solvent recovery exists the problem that energy resource consumption is high, waste of solvent is large, provides a kind of concentration device for material liquid.
In order to realize the purpose of this utility model, the technical solution adopted in the utility model is:
A kind of concentration device for material liquid, it comprises concentration systems, solvent recovering system and density Adjusting System, and described concentration systems comprises live steam room;
The magnetic drive pump that feed liquid pipe connects successively, feed liquid storage tank, the first plate type heat exchanger, the second plate type heat exchanger, calandria preheater and external circulation evaporation separator;
And
The external circulation heater be all communicated with feed liquid pipe and the steam pipe of external circulation evaporation separator;
The steam pipework that described external circulation evaporation separator is connected with external circulation heater is provided with after-heater, and external circulation heater and the outside of after-heater are provided with and are interconnected and the steam jacket be communicated with live steam room.
Described external circulation heater comprises gas-liquid separation chamber from top to bottom, rises the concentrated solution outlet of membrane type tube still heater and back taper, and steam jacket is located at and is risen membrane type tube still heater outside.
Described concentrated solution outlet is divided into three tunnels behind the door through liquid valve, and the first via is connected with density Adjusting System, and the second tunnel is connected with external circulation evaporation separator bottom charging aperture through pipe circle pump, and the 3rd tunnel is connected with the charging aperture of side, external circulation evaporation separator top.
Described density Adjusting System comprises heater, and heater one end is connected with concentrated solution outlet, and the other end is connected with the charging aperture of external circulation evaporation separator.
Described solvent recovering system comprises the plate-type condenser, condenser receiving slit, water-ring vacuum pump and the vacuum buffer tank that are communicated with successively, condenser receiving slit top is located at by described plate-type condenser, condenser receiving slit bottom is provided with vaccum centrifugal pump, and the delivery port of described vacuum buffer tank is communicated with again with the water inlet of water-ring vacuum pump.
Described first plate type heat exchanger is provided with waste heat import and waste heat outlet, waste heat import and the steam jacket outlet rising membrane type tube still heater, vapour preheating more than the first time of formation feed liquid, and waste heat outlet is connected with plate-type condenser.
Described plate type preheater and calandria preheater are equipped with steam preheating mouth, and the steam jacket outlet of after-heater is communicated with the second time and third time remaining vapour preheating that form feed liquid respectively respectively with plate type preheater and the steam preheating mouth of calandria preheater.
Filter is provided with between described magnetic drive pump and feed liquid storage tank.
The outside of described after-heater steam jacket is provided with heat-insulation layer.
The utility model beneficial effect:
The utility model is energy-conservation in concentration process and organic solvent (as ethanol etc.) concentration process, efficiently, consumption reduction, low cost, low input, utilize organic solvent to carry out " vapour-gas " at external circulation evaporation separator generation solvent vapour by after-heater and live steam to heat, if aqueous extract is concentrated, then indirect steam is carried out the mode that " vapour-vapour " mix to heat with live steam, finally be sent in external circulation evaporator as heat source, feed liquid is made to maintain fluidized state, condensate liquid is become after some vapor heater via, for feed liquid preheating, after fixed gas in steam and heat exchange, the liquid solvent of transition all will rationally reclaim, make full use of its waste heat and continue as feed liquid preheating, eventually pass through the recovery cycling and reutilization of plate type heat exchanger realization to organic solvent, the utility model is energy-conservation in concentration process and organic solvent (as ethanol etc.) concentration process, efficiently, consumption reduction, low cost, low input and the concentration of concentration process herb liquid can free adjustment.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model;
In figure: external circulation heater 1, external circulation evaporation separator 2, after-heater 3, calandria preheater 4, second plate type heat exchanger 5, first plate type heat exchanger 6, pipe circle pump 7, plate-type condenser 8, condenser receiving slit 9, feed liquid storage tank 10, water-ring vacuum pump 11, vacuum buffer tank 12, magnetic drive pump 13, filter 14, vaccum centrifugal pump 15, heater 16, gas-liquid separation chamber 1-1, rise membrane type tube still heater 1-2, concentrated solution outlet 1-3, steam valve 100,101.
Detailed description of the invention
The utility model is by the following examples can the utility model will be further described, but scope of the present utility model is not limited to following embodiment, can carry out various change in the scope not departing from purport of the present utility model.
Embodiment 1: shown in Figure 1.
A kind of concentration device for material liquid, it comprises concentration systems, solvent recovering system and density Adjusting System, and described concentration systems comprises live steam room;
The magnetic drive pump 13 that feed liquid pipe connects successively, feed liquid storage tank 10, first plate type heat exchanger 6, second plate type heat exchanger 5, calandria preheater 4 and external circulation evaporation separator 2;
And
The external circulation heater 1 be all communicated with feed liquid pipe and the steam pipe of external circulation evaporation separator 2;
The steam pipework that described external circulation evaporation separator 2 is connected with external circulation heater 1 is provided with after-heater 3, and external circulation heater 1 and the outside of after-heater 3 are provided with and are interconnected and the steam jacket be communicated with live steam room.
Described external circulation heater 1 comprises gas-liquid separation chamber 1-1 from top to bottom, rises the concentrated solution outlet 1-3 of membrane type tube still heater 1-2 and back taper, and steam jacket is located at and is risen membrane type tube still heater 1-2 outside.
Described concentrated solution outlet 1-3 is divided into three tunnels behind the door through liquid valve, the first via is connected with density Adjusting System, second tunnel is connected with external circulation evaporation separator 2 bottom feed mouth through pipe circle pump 7, and the 3rd tunnel is connected with the charging aperture of side, external circulation evaporation separator 2 top.
Described density Adjusting System comprises heater 16, and heater 16 one end is connected with concentrated solution outlet 1-3, and the other end is connected with the charging aperture of external circulation evaporation separator 2.
Described solvent recovering system comprises the plate-type condenser 8, condenser receiving slit 9, water-ring vacuum pump 11 and the vacuum buffer tank 12 that are communicated with successively, condenser receiving slit 9 top is located at by described plate-type condenser 8, condenser receiving slit 9 bottom is provided with vaccum centrifugal pump 15, and the delivery port of described vacuum buffer tank 12 is communicated with again with the water inlet of water-ring vacuum pump 11.
Described first plate type heat exchanger 6 is provided with waste heat import and waste heat outlet, waste heat import and the steam jacket outlet rising membrane type tube still heater 1-2, vapour preheating more than the first time of formation feed liquid, and waste heat outlet is connected with plate-type condenser 8.
Described second plate type heat exchanger 5 and calandria preheater 4 are equipped with steam preheating mouth, and the steam jacket outlet of after-heater 3 is communicated with the second time and third time remaining vapour preheating that form feed liquid respectively respectively with the second plate type heat exchanger 5 and the steam preheating mouth of calandria preheater 4.
Filter 14 is provided with between described magnetic drive pump 13 and feed liquid storage tank 10.
The outside of described after-heater 3 steam jacket is provided with heat-insulation layer.
Feed liquid concentration process: feed liquid is squeezed in filter 14 by magnetic drive pump 13 and filtered, filtrate enters in feed liquid storage tank 10 and lays in, deposit feed liquid carries out first time preheating through the first plate type heat exchanger 6, again to the second plate type heat exchanger 5 carries out second time preheating, carry out third time preheating to calandria preheater 4 again, finally enter into external circulation evaporation separator 2, now ON cycle pump 7 feed liquid is driven in external circulation heater 1.
When feed liquid solvent is water, close the steam valve 101 of after-heater 3 steam jacket, open the steam valve 100 rising membrane type tube still heater 1-2 steam jacket, in external circulation evaporation separator 2, indirect steam out mixes with live steam at 1-21 place, external circulation heater 1 steam inlet and carries out supplementary heating, mixed vapor (steam) temperature raises, heat content increases, and enters in external circulation heater 1 and heats liquid.
When feed liquid solvent is ethanol, steam off valve 100, opens steam valve 101, makes live steam carry out indirect type " vapour-gas " heating to solvent vapour out in external circulation evaporation separator 2 in after-heater 3.Steam after heating passes in external circulation heater 1 and heats the concentrated feed liquid in tubulation.
The waste heat import that condensed water in external circulation heater 1 interlayer enters the first plate type heat exchanger 6 carries out first time remaining vapour preheating to feed liquid, waste heat outlet is then reclaimed by solvent recovering system, and the incoagulable gas in external circulation heater 1 interlayer is then extracted out by water-ring vacuum pump 11.
After-heater 3 remaining vapour out reclaims the steam preheating mouth passed into the second plate type heat exchanger 5 and calandria preheater 4 respectively and carries out second time and third time remaining vapour preheating to feed liquid.In external circulation heater 1, the final concentrate of feed liquid is released by the fluid valve of its lower end.
Solvent recovery process: when feed liquid solvent needs to reclaim, open water ring vacuum pumps vacuumizes external circulation heater 1, be evacuated to by steam in plate-type condenser 8 and flow into after condensation in condensate liquid receiving slit 9, steam passes to the first plate type heat exchanger 6 and realizes reclaiming for flowing to after feed liquid preheating condensate liquid receiving slit 9 again rising in membrane type tube still heater 1-2 interlayer from the condensate outlet of bottom after condensation.
Concentration adjustment process: when concentration of liquid medicine is to higher concentration, heater 16 can be started, concentrate enters heater 16 from external circulation heater 1, vapor-liquid separation is carried out through external circulation evaporation separator 2, return in external circulation heater 16 and heat, circulation, directly releases after requiring concentration to concentration of liquid medicine.
Claims (9)
1. a concentration device for material liquid, it comprises concentration systems, solvent recovering system and density Adjusting System, it is characterized in that,
Described concentration systems comprises live steam room;
The magnetic drive pump (13) that feed liquid pipe connects successively, feed liquid storage tank (10), the first plate type heat exchanger (6), the second plate type heat exchanger (5), calandria preheater (4) and external circulation evaporation separator (2);
And
The external circulation heater (1) be all communicated with feed liquid pipe and the steam pipe of external circulation evaporation separator (2);
The steam pipework that described external circulation evaporation separator (2) is connected with external circulation heater (1) is provided with after-heater (3), and external circulation heater (1) and the outside of after-heater (3) are provided with and are interconnected and the steam jacket be communicated with live steam room.
2. a kind of concentration device for material liquid according to claim 1, it is characterized in that, described external circulation heater (1) comprises gas-liquid separation chamber (1-1) from top to bottom, rise the concentrated solution outlet (1-3) of membrane type tube still heater (1-2) and back taper, steam jacket is located at and is risen membrane type tube still heater (1-2) outside.
3. a kind of concentration device for material liquid according to claim 2, it is characterized in that, described concentrated solution outlet (1-3) is divided into three tunnels behind the door through liquid valve, the first via is connected with density Adjusting System, second tunnel is connected with external circulation evaporation separator (2) bottom feed mouth through pipe circle pump (7), and the 3rd tunnel is connected with the charging aperture of external circulation evaporation separator (2) side, top.
4. a kind of concentration device for material liquid according to claim 3, it is characterized in that, described density Adjusting System comprises heater (16), heater (16) one end is connected with concentrated solution outlet (1-3), and the other end is connected with the charging aperture of external circulation evaporation separator (2).
5. a kind of concentration device for material liquid according to claim 2, it is characterized in that, described solvent recovering system comprises the plate-type condenser (8), condenser receiving slit (9), water-ring vacuum pump (11) and the vacuum buffer tank (12) that are communicated with successively, condenser receiving slit (9) top is located at by described plate-type condenser (8), condenser receiving slit (9) bottom is provided with vaccum centrifugal pump (15), and the delivery port of described vacuum buffer tank (12) is communicated with again with the water inlet of water-ring vacuum pump (11).
6. a kind of concentration device for material liquid according to claim 5, it is characterized in that, described first plate type heat exchanger (6) is provided with waste heat import and waste heat outlet, waste heat import and the steam jacket outlet rising membrane type tube still heater (1-2), vapour preheating more than the first time of formation feed liquid, waste heat outlet is connected with plate-type condenser (8).
7. a kind of concentration device for material liquid according to claim 1, it is characterized in that, described second plate type heat exchanger (5) and calandria preheater (4) are equipped with steam preheating mouth, and the steam jacket outlet of after-heater (3) is communicated with the second time and third time remaining vapour preheating that form feed liquid respectively respectively with the second plate type heat exchanger (5) and the steam preheating mouth of calandria preheater (4).
8. a kind of concentration device for material liquid according to claim 1, is characterized in that, be provided with filter (14) between described magnetic drive pump (13) and feed liquid storage tank (10).
9. a kind of concentration device for material liquid according to claim 1, is characterized in that, the outside of described after-heater (3) steam jacket is provided with heat-insulation layer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520440810.9U CN204841160U (en) | 2015-06-25 | 2015-06-25 | Feed liquid enrichment facility |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520440810.9U CN204841160U (en) | 2015-06-25 | 2015-06-25 | Feed liquid enrichment facility |
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| CN204841160U true CN204841160U (en) | 2015-12-09 |
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| CN201520440810.9U Active CN204841160U (en) | 2015-06-25 | 2015-06-25 | Feed liquid enrichment facility |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104922974A (en) * | 2015-06-25 | 2015-09-23 | 江西中医药大学 | Extracting liquid concentrating device |
| CN106512459A (en) * | 2016-12-16 | 2017-03-22 | 江西中医药大学 | Concentrator based on vapor thermal gain technology |
| CN107858535A (en) * | 2017-11-07 | 2018-03-30 | 赣州科源甬致科技有限公司 | A kind of high-speed temperature adjusting apparatus for rare earth feed liquid |
| CN109095535A (en) * | 2018-10-16 | 2018-12-28 | 江苏必领能源科技有限公司 | Sewage evaporation enrichment facility and its operating method |
-
2015
- 2015-06-25 CN CN201520440810.9U patent/CN204841160U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104922974A (en) * | 2015-06-25 | 2015-09-23 | 江西中医药大学 | Extracting liquid concentrating device |
| CN106512459A (en) * | 2016-12-16 | 2017-03-22 | 江西中医药大学 | Concentrator based on vapor thermal gain technology |
| CN107858535A (en) * | 2017-11-07 | 2018-03-30 | 赣州科源甬致科技有限公司 | A kind of high-speed temperature adjusting apparatus for rare earth feed liquid |
| CN109095535A (en) * | 2018-10-16 | 2018-12-28 | 江苏必领能源科技有限公司 | Sewage evaporation enrichment facility and its operating method |
| CN109095535B (en) * | 2018-10-16 | 2024-03-19 | 江苏必领能源科技有限公司 | Sewage evaporation concentration device and operation method thereof |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20170420 Address after: 330000 Nanchang high tech Industrial Development Zone, Nanchang, AI Bei Sihu Road, No. 688, building No. 8 Patentee after: Jiangxi Hebai Hong Wah Pharmaceutical Equipment Co. Ltd. Address before: 330004 Jiangxi city of Nanchang province Wanli District Hing Wan Road No. 818 Patentee before: JIANGXI UNIVERSITY OF TRADITIONAL CHINESE MEDICINE |
|
| TR01 | Transfer of patent right |