CN101874938A - Forced circulation continuous crystallization system with mechanical vapor recompression function - Google Patents
Forced circulation continuous crystallization system with mechanical vapor recompression function Download PDFInfo
- Publication number
- CN101874938A CN101874938A CN2009102586026A CN200910258602A CN101874938A CN 101874938 A CN101874938 A CN 101874938A CN 2009102586026 A CN2009102586026 A CN 2009102586026A CN 200910258602 A CN200910258602 A CN 200910258602A CN 101874938 A CN101874938 A CN 101874938A
- Authority
- CN
- China
- Prior art keywords
- pipe
- crystallizer
- compressor
- pump
- connects
- 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.)
- Pending
Links
- 238000002425 crystallisation Methods 0.000 title claims abstract description 19
- 230000005712 crystallization Effects 0.000 title claims abstract description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000007599 discharging Methods 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 239000002994 raw material Substances 0.000 abstract description 2
- 239000007788 liquid Substances 0.000 description 4
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 238000004134 energy conservation Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000009835 boiling Methods 0.000 description 1
- 230000001112 coagulant Effects 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000035945 sensitivity Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000002207 thermal evaporation Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Abstract
The invention discloses a forced circulation continuous crystallization system with a mechanical vapor recompression function and relates to a continuous crystallization system which comprises a crystallizer, a compressor and a heater. The bottom of the crystallizer is connected with a circulation pipe; the other end of the circulation pipe is connected with a feed inlet of a circulation pump; the feed outlet of the circulation pump is connected with a discharge pipe; the other end of the discharge pipe is connected with the feed inlet of a discharge pump; the feed outlet of the discharge pump is connected with a finished product tank; the top of the crystallizer is connected with the inlet of the compressor through a pipe; a lower seal head is connected with the circulation pipe; one side of the lower seal head is connected with a feeding pipe which is provided with a ball valve and a feeding pump; the other end of the feeding pipe is connected with a raw material tank; an upper seal head is connected with the crystallizer through a pipe; a shell side is arranged outside the heater and is communicated with the outlet of the compressor through a pipe; the heater is connected with a vacuumizing pipe; and the shell side is also connected with a condensed water discharge pipe. The forced circulation continuous crystallization system with the mechanical vapor recompression function can meet the crystallization production requirement on continuous feeding and charging; and the compressor is used to collect secondary vapor, thereby saving energy sources.
Description
Technical field
The present invention relates to a kind of continuous crystallisation system, be specially a kind of energy-conservation continuous crystalizer, promptly with the forced circulation continuous crystallisation system of mechanical vapour recompression.
Background technology
Traditional crystallizer is the crystallizer of earlier solution to be crystallized being packed into, after making equipment operation a period of time then, when the solution circulation concentrates when reaching certain crystallization content, discharge magma opening discharging pump, Deng opening the inlet valve stoste of packing into after the magma emptying once more, repeat said process.This just makes the production gap carry out and can't produce continuously.In addition, the indirect steam that normally crystallizer produced of traditional crystallizer is directly discharged or is drained after the condensing plant condensation.So not only waste the latent heat of indirect steam, wasted the energy, must be that the condensation indirect steam increases by a cover condensing plant, not only increased investment but also not environmental protection and economy.Also have traditional crystallizer generally to evaporate under normal pressure, this needs the big material of thermal sensitivity of low-temperature evaporation to some is disadvantageous.For this reason, can produce continuously and can be energy-conservation but also crystallizer that can low-temperature evaporation becomes the focus of a research.
Summary of the invention
The objective of the invention is: provide a kind of can continuous feed, discharging and can energy savings and the continuous crystalizer that can evaporate at a lower temperature.
The object of the present invention is achieved like this: the forced circulation continuous crystallisation system of band mechanical vapour recompression, comprise crystallizer, also comprise compressor, be provided with the heater of low head (28) and upper cover (29), described crystallizer (1) bottom connects circulation pipe (16), the other end of described circulation pipe connects the charging aperture of circulating pump (11), the discharging opening of described circulating pump connects discharge nozzle (17), the other end of discharge nozzle (17) connects the charging aperture of discharging pump (10), the discharging opening of discharging pump (10) connects finished product jar (9), the crystallizer top is connected with compressor inlet by pipeline (27), the low head of heater (28) links to each other with circulation pipe (16), the first side of lower seal connects feed pipe (30), feed pipe is provided with ball valve (31) and feed pump (12), and the feed pipe other end links to each other with head tank; The upper cover of heater links to each other with crystallizer by pipeline (18), and heater is provided with shell side outward, and described shell side is communicated with compressor (2) outlet by pipeline (19), and described heater connects the pipeline (20) of finding time, and described shell side connects condensed water discharge pipe (21).
Equipment provided by the present invention can satisfy the crystallization production requirement of continuous feed and discharge, adopt compressor to collect indirect steam, reused the latent heat of indirect steam, save the energy, save condensing plant, reduced the consumption of cooling water, reduced the cost of enterprise, increase enterprise income, adopted water circulating vacuum pump to extract incoagulable gas out and keep intrasystem vacuum, guaranteed solution explosive evaporation under lower saturation temperature.
In order to keep the vacuum of system, be provided with balance pipe (22), ball valve (5) and vavuum pump (6) on the described pipeline of finding time successively, ball valve (23) is set on the described balance pipe, balance pipe is terminal to link to each other with drainer (24).
For the condensed condensed water of steam is discharged, be provided with successively on the described condensed water discharge pipe and look pipe (7) and ball valve (25), the condensed water discharge pipe end links to each other with drainer, and the drainer bottom is provided with evacuated tube, is provided with ball valve (26) and drain pump (8) on the evacuated tube successively.
For the balance that keep-ups pressure, described compressor is the roots-type compressor, and the import and export of compressor is provided with bypass pipe (32), and bypass pipe is provided with ball valve (3).
As a further improvement on the present invention, baffle plate (36) is arranged at described crystallizer top, the pipeline (18) that advances crystallizer in crystallizer, be provided with a bend pipe (33) deeply to the crystallizer center line and along center line to the preceding paragraph, be provided with a conical hopper (37) endways, this structure can the crystallization control particle size, satisfy production requirement.
For raw material is preheated, be provided with heat exchanger (15) in the described head tank.
Description of drawings
Fig. 1 is a kind of structural representation of the present invention.
Wherein, 1-crystallizer, 2-compressor, 3-ball valve, 4-heater, 5-ball valve, 6-vavuum pump, 7-look find time pipeline, 21-of pipe, 8-drain pump, 9-finished product jar, 10-discharge pump, 11-circulating pump, 12-feed pump, 13-flowmeter, 14-head tank, 15-heat exchanger, 16-circulation pipe, 17-discharge nozzle, 18-pipeline, 19-pipeline, 20-and coagulate water discharge pipe, 22-balance pipe, 23-ball valve, 24-drainer, 25-ball valve, 26-ball valve, 27-pipeline, 28-low head, 29-upper cover, 30-feed pipe, 31-ball valve, 32-bypass pipe, 33-shell side.
The specific embodiment
As shown in Figure 1, the forced circulation continuous crystalizer of band mechanical vapour recompression, comprise crystallizer 1, compressor 2, heater 4, crystallizer 1 bottom is provided with circulation pipe 16, circulating pump 11 is set on the circulation pipe 16, be provided with discharge nozzle 17 behind the circulating pump 11, discharge nozzle 17 back are provided with discharging pump 10, discharge nozzle 17 ends are provided with finished product jar 9, crystallizer 1 top links to each other with compressor 2 imports by pipeline 27, heater 4 bottoms are provided with low head 28 tops upper cover 29 are set, low head 28 bottoms link to each other with circulation pipe 16, low head 28 1 sides have feed pipe 30, feed pipe 30 is provided with flowmeter 13, ball valve 31 and feed pump 12, feed pipe 30 ends link to each other with head tank 14, upper cover 29 links to each other with crystallizer 1 by pipeline 18, the shell side 33 of heater 4 links to each other with compressor 2 outlets by pipeline 19, shell side 33 bottoms of heater 4 are provided with find time pipeline 20 and condensed water discharge pipe 21, the pipeline 20 of finding time is provided with balance pipe 22, ball valve 5 and vavuum pump 6, balance pipe 22 is provided with ball valve 23, balance pipe 22 ends link to each other with drainer 24, condensed water discharge pipe 21 is provided with looks pipe 7 and ball valve 25, condensed water discharge pipe 21 ends link to each other with drainer 24, drainer 24 bottoms are provided with evacuated tube, and ball valve (26) and drain pump (8) are arranged on the evacuated tube.
Feed liquid in the head tank 14 continuous heater 4 that enters after heat exchanger 15 heating are preheating to boiling point is subjected to thermal evaporation, after heated feed liquid is sent into crystallizer 1 separation, magma is formed on the bottom that the feed liquid that has concentrated drops to crystallizer 1, magma by a circulation pipe 16 and circulating pump 11 parts enter discharge nozzle 17 through discharge pump 10 with magma continuous be discharged to finished product jar 9, another part continues to participate in circulation.Isolated indirect steam is delivered to compressor 2 through pipeline 27 in the crystallizer 1, delivers to the heater tube side after compressed machine 2 compressions heat up, boost and emits solution in the latent heat heating heat exchanger tube 35.The water that coagulates that condensation is got off is discharged to drainer 24 through coagulating water discharge pipe 21, coagulates the water pipe bottom evacuated tube is housed, and evacuated tube is provided with ball valve 26 and drain pump 8, can will coagulate water by drain pump when drainer is full and discharge.The import and export of compressor has a bypass pipe 32 to link to each other, and bypass pipe is provided with a ball valve 3, can protect like this compressor when starting and stopping not because of too high overload of loading.Evaporate at low temperatures for making feed liquid, the vacuum of system is kept with the discharge of incoagulable gas and is finished by the vavuum pump on the evacuation tube 20 6, be provided with ball valve 5 on the evacuation tube before vavuum pump and be used for the vacuum of control system, be provided with a balance pipe 22 that connects drainer before the evacuation tube ball valve, balance pipe is provided with ball valve 23.
Claims (7)
1. be with the forced circulation continuous crystallisation system of mechanical vapour recompression, comprise crystallizer, it is characterized in that: also comprise compressor, be provided with the heater of low head (28) and upper cover (29), described crystallizer (1) bottom connects circulation pipe (16), the other end of described circulation pipe connects the charging aperture of circulating pump (11), the discharging opening of described circulating pump connects discharge nozzle (17), the other end of discharge nozzle (17) connects the charging aperture of discharging pump (10), the discharging opening of discharging pump (10) connects finished product jar (9), the crystallizer top is connected with compressor inlet by pipeline (27), the low head of heater (28) links to each other with circulation pipe (16), the first side of lower seal connects feed pipe (30), feed pipe is provided with ball valve (31) and feed pump (12), and the feed pipe other end links to each other with head tank; The upper cover of heater links to each other with crystallizer by pipeline (18), and heater is provided with shell side outward, and described shell side is communicated with compressor (2) outlet by pipeline (19), and described heater connects the pipeline (20) of finding time, and described shell side connects condensed water discharge pipe (21).
2. the forced circulation continuous crystallisation system of band mechanical vapour recompression according to claim 1, it is characterized in that: be provided with balance pipe (22), ball valve (5) and vavuum pump (6) on the described pipeline of finding time successively, ball valve (23) is set on the described balance pipe, and balance pipe is terminal to link to each other with drainer (24).
3. the forced circulation continuous crystallisation system of band mechanical vapour recompression according to claim 1, it is characterized in that: be provided with successively on the described condensed water discharge pipe and look pipe (7) and ball valve (25), the condensed water discharge pipe end links to each other with drainer, the drainer bottom is provided with evacuated tube, is provided with ball valve (26) and drain pump (8) on the evacuated tube successively.
4. the forced circulation continuous crystallisation system of band mechanical vapour recompression according to claim 1, it is characterized in that: described compressor is the roots-type compressor, and the import and export of compressor is provided with bypass pipe (32), and bypass pipe is provided with ball valve (3).
5. the forced circulation continuous crystallisation system of band mechanical vapour recompression according to claim 1, it is characterized in that: the crystallizer inner top has baffle plate (36).
6. the forced circulation continuous crystallisation system of band mechanical vapour recompression according to claim 1, it is characterized in that: pipeline (18) is arranged in the inner of crystallizer on the axis of crystallizer, and the end of pipeline (18) connects the conical hopper (37) that an opening makes progress.
7. the forced circulation continuous crystallisation system of band mechanical vapour recompression according to claim 1 is characterized in that: be provided with heat exchanger (15) in the head tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009102586026A CN101874938A (en) | 2009-12-07 | 2009-12-07 | Forced circulation continuous crystallization system with mechanical vapor recompression function |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009102586026A CN101874938A (en) | 2009-12-07 | 2009-12-07 | Forced circulation continuous crystallization system with mechanical vapor recompression function |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101874938A true CN101874938A (en) | 2010-11-03 |
Family
ID=43017682
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009102586026A Pending CN101874938A (en) | 2009-12-07 | 2009-12-07 | Forced circulation continuous crystallization system with mechanical vapor recompression function |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101874938A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102060408A (en) * | 2010-12-07 | 2011-05-18 | 华电水处理技术工程有限公司 | Wastewater evaporating process and device system |
| CN102070272A (en) * | 2010-12-07 | 2011-05-25 | 华电水处理技术工程有限公司 | Wastewater evaporation concentration process and device system |
| CN102343162A (en) * | 2011-07-20 | 2012-02-08 | 常州大学 | Energy-saving evaporating process and equipment for L-phenylalanine brine solution |
| CN102407029A (en) * | 2011-10-17 | 2012-04-11 | 宜兴市格兰特干燥浓缩设备有限公司 | Evaporated crystallization device |
| CN102772907A (en) * | 2012-06-29 | 2012-11-14 | 常州环生科创石墨设备有限公司 | Continuous extracting, crystalizing and evaporating equipment |
| CN103908788A (en) * | 2012-12-31 | 2014-07-09 | 中国科学院理化技术研究所 | MVR heat pump evaporation system |
| CN103768808B (en) * | 2014-01-23 | 2015-09-09 | 南京航空航天大学 | Some vapor recompression evaporation concentration system and method |
| CN106693414A (en) * | 2017-01-06 | 2017-05-24 | 南京航空航天大学 | Heat-mass co-transfer evaporation and crystallization system and working method thereof |
-
2009
- 2009-12-07 CN CN2009102586026A patent/CN101874938A/en active Pending
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102060408A (en) * | 2010-12-07 | 2011-05-18 | 华电水处理技术工程有限公司 | Wastewater evaporating process and device system |
| CN102070272A (en) * | 2010-12-07 | 2011-05-25 | 华电水处理技术工程有限公司 | Wastewater evaporation concentration process and device system |
| CN102060408B (en) * | 2010-12-07 | 2012-06-06 | 华电水处理技术工程有限公司 | Wastewater evaporating process and device system |
| CN102343162A (en) * | 2011-07-20 | 2012-02-08 | 常州大学 | Energy-saving evaporating process and equipment for L-phenylalanine brine solution |
| CN102343162B (en) * | 2011-07-20 | 2014-04-09 | 常州大学 | Energy-saving evaporating process and equipment for L-phenylalanine brine solution |
| CN102407029A (en) * | 2011-10-17 | 2012-04-11 | 宜兴市格兰特干燥浓缩设备有限公司 | Evaporated crystallization device |
| CN102772907A (en) * | 2012-06-29 | 2012-11-14 | 常州环生科创石墨设备有限公司 | Continuous extracting, crystalizing and evaporating equipment |
| CN103908788A (en) * | 2012-12-31 | 2014-07-09 | 中国科学院理化技术研究所 | MVR heat pump evaporation system |
| CN103908788B (en) * | 2012-12-31 | 2015-12-23 | 中国科学院理化技术研究所 | A kind of MVR thermo-compression evaporation system |
| CN103768808B (en) * | 2014-01-23 | 2015-09-09 | 南京航空航天大学 | Some vapor recompression evaporation concentration system and method |
| CN106693414A (en) * | 2017-01-06 | 2017-05-24 | 南京航空航天大学 | Heat-mass co-transfer evaporation and crystallization system and working method thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101874938A (en) | Forced circulation continuous crystallization system with mechanical vapor recompression function | |
| CN104759108B (en) | Three grades of continuous falling liquid film circulating and evaporating concentration systems with function of mechanical steam recompression | |
| CN101966997B (en) | Process and device for producing pyrotechnite from sodium sulfate decahydrate | |
| CN103768808A (en) | Partial steam recompression, evaporation and concentration system and method | |
| CN204522328U (en) | Three grades with function of mechanical steam recompression continuous falling liquid film circulating and evaporating concentration systems | |
| CN103951005B (en) | The more technology coupling seawater desalination plants of zero-emission and its method | |
| CN106115804A (en) | A kind of for cobaltous sulfate efficient concentration with the apparatus system of continuous crystallisation | |
| CN107008026A (en) | Nickel sulfate evaporative crystallization technique | |
| CN102320575A (en) | The method of low-temperature evaporation Sodium Persulfate | |
| CN206508573U (en) | A kind of function of mechanical steam recompression evaporation and crystallization system of high-salt wastewater | |
| CN210278295U (en) | Sulfate process titanium dioxide titanium liquid concentration system | |
| CN201643771U (en) | Forced circulation continuous crystallizing system with function of mechanical steam recompression | |
| CN207371123U (en) | A kind of soda manufacture MVR vaporising devices | |
| CN205627127U (en) | MVR triple -effect evaporator | |
| CN102336419B (en) | Equipment special for producing bulk wet salt by using sodium sulfate type brine | |
| CN105056565B (en) | Device and method for evaporation and crystallization of sodium gluconate solution | |
| CN101982450A (en) | Method for recovering butanol-butyl acetate from waste acid water generated during antibiotic production through reduced pressure distillation | |
| CN102221191A (en) | Secondary steam generator | |
| CN201534891U (en) | Vacuum evaporation system for recycling electrotinplate liquid | |
| CN107867709A (en) | A kind of processing technology for being concentrated by evaporation aqueous sodium persulfate solution crystallization | |
| CN212293347U (en) | Resource production equipment for organic calcium protein liquid fertilizer | |
| CN204824178U (en) | Monoammonium phosphate solution evaporation crystallization equipment | |
| CN108786169A (en) | A kind of crystal system and its method of liquid | |
| CN208302233U (en) | A kind of novel thin film concentration evaporator | |
| CN209204718U (en) | The multiple tank group continuous production system of grease in a kind of leaching aggregate |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20101103 |
|
| WD01 | Invention patent application deemed withdrawn after publication |