CN218686389U - Sodium gulonate MVR concentration system - Google Patents
Sodium gulonate MVR concentration system Download PDFInfo
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- CN218686389U CN218686389U CN202223143439.9U CN202223143439U CN218686389U CN 218686389 U CN218686389 U CN 218686389U CN 202223143439 U CN202223143439 U CN 202223143439U CN 218686389 U CN218686389 U CN 218686389U
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- evaporator
- mvr
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- RGHNJXZEOKUKBD-QTBDOELSSA-N L-gulonic acid Chemical compound OC[C@H](O)[C@@H](O)[C@H](O)[C@H](O)C(O)=O RGHNJXZEOKUKBD-QTBDOELSSA-N 0.000 title claims abstract description 30
- 239000011734 sodium Substances 0.000 title claims abstract description 20
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 title claims abstract description 18
- 229910052708 sodium Inorganic materials 0.000 title claims abstract description 18
- 239000007788 liquid Substances 0.000 claims abstract description 38
- 239000011552 falling film Substances 0.000 claims abstract description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000013078 crystal Substances 0.000 claims description 7
- 239000002002 slurry Substances 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 2
- 239000000463 material Substances 0.000 abstract description 9
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 238000001704 evaporation Methods 0.000 description 11
- 230000008020 evaporation Effects 0.000 description 8
- 239000012452 mother liquor Substances 0.000 description 8
- 238000000034 method Methods 0.000 description 7
- 230000008569 process Effects 0.000 description 6
- 230000006835 compression Effects 0.000 description 4
- 238000007906 compression Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005886 esterification reaction Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000011347 resin Substances 0.000 description 3
- 229920005989 resin Polymers 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000032050 esterification Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 229940088594 vitamin Drugs 0.000 description 2
- 229930003231 vitamin Natural products 0.000 description 2
- 235000013343 vitamin Nutrition 0.000 description 2
- 239000011782 vitamin Substances 0.000 description 2
- 150000003722 vitamin derivatives Chemical class 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000004925 denaturation Methods 0.000 description 1
- 230000036425 denaturation Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000010408 film Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
Images
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses a concentrated system of gulonic acid sodium MVR, include: a plate heat exchanger; the feed inlet of the first-stage falling-film evaporator is connected with the outlet of the plate heat exchanger, and the first-stage falling-film evaporator is connected with the gas-liquid separator; the material inlet of the second-stage forced circulation evaporator is connected with the material outlet of the gas-liquid separator, and the second-stage forced circulation evaporator is connected with the crystallizer; an inlet of the MVR vapor compressor is respectively connected with vapor outlets of the gas-liquid separator and the crystallizer, and an outlet of the MVR vapor compressor is connected with vapor inlets of the first-stage falling-film evaporator and the second-stage forced circulation evaporator; the inlet of the condenser is connected with the non-condensable gas outlets of the first-stage falling film evaporator and the second-stage forced circulation evaporator; and the inlet of the condensed water tank is connected with condensed water outlets of the first-stage falling-film evaporator and the second-stage forced circulation evaporator, the inlet of the condensed water tank is also connected with an outlet of the condenser, and the outlet of the condensed water tank is connected with a condensed water inlet of the plate heat exchanger. The utility model discloses the system has effectively improved the utilization ratio of steam, energy-conservation subtracts consumption, reduce cost.
Description
Technical Field
The utility model relates to an evaporative concentration technical field especially relates to a sodium gulonate MVR concentration system.
Background
The traditional process for preparing the sodium gulonate solution is as follows: the gulonic acid sodium mash produced by fermentation generates gulonic acid resin exchange liquid after resin exchange, and the gulonic acid resin exchange liquid is separated and dehydrated to generate gulonic acid crystals through decompression concentration, crystallization and a centrifuge (simultaneously, gulonic acid mother liquor is generated, the gulonic acid mother liquor is concentrated and then centrifugally separated to generate a dry gulonic acid mother liquor, and then the dry gulonic acid mother liquor is intensively fed into a reaction tank for esterification and conversion reaction when the accumulated amount is enough for esterification reaction for one batch, so that an intermediate vitamin C-Na is obtained, and the yield of the normal gulonic acid is supplemented). The gulonic acid crystal is put into a reaction tank and dissolved by methanol for esterification and conversion reaction to obtain an intermediate vitamin C-Na.
The traditional production method has long period, high cost and more processes. A large amount of gulonic acid mother liquor is generated in the production process, and the gulonic acid mother liquor is concentrated, cooled, crystallized and centrifugally separated to obtain a dry gulonic acid mother liquor and a gulonic acid multi-mother liquor. Gulonic acid solution is usually concentrated by a film evaporation method, so that the energy consumption is high, the cost is high, and effective components can be damaged by heating and concentrating.
SUMMERY OF THE UTILITY MODEL
For overcoming the partial defect that prior art exists at least, the utility model provides a concentrated system of gulonic sodium MVR has effectively improved the utilization ratio of steam, energy-conservation subtracts consumption, reduce cost.
The utility model adopts the technical proposal that:
a sodium gulonate MVR concentration system, comprising:
a plate heat exchanger;
the feed inlet of the first-stage falling-film evaporator is connected with the outlet of the plate heat exchanger, and the first-stage falling-film evaporator is connected with the gas-liquid separator;
the feeding port of the second-stage forced circulation evaporator is connected with the discharging port of the gas-liquid separator, and the second-stage forced circulation evaporator is connected with the crystallizer;
an inlet of the MVR vapor compressor is respectively connected with vapor outlets of the gas-liquid separator and the crystallizer, and an outlet of the MVR vapor compressor is connected with vapor inlets of the first-stage falling-film evaporator and the second-stage forced circulation evaporator;
the inlet of the condenser is connected with the non-condensable gas outlets of the first-stage falling-film evaporator and the second-stage forced circulation evaporator;
and the inlet of the condensed water tank is connected with the condensed water outlet of the first-stage falling-film evaporator and the condensed water outlet of the second-stage forced circulation evaporator, the inlet of the condensed water tank is also connected with the outlet of the condenser, and the outlet of the condensed water tank is connected with the condensed water inlet of the plate heat exchanger.
As a further improvement of the present invention, the inlet of the plate heat exchanger is connected to the feed tank by a feed pump.
As a further improvement of the utility model, the outlet of the crystallizer is connected with the crystal slurry tank.
The beneficial effects of the utility model reside in that:
MVR evaporator system adopts and forces falling film and MVR mechanical compression evaporative concentration's mode to carry out evaporative concentration to gulonic sodium sediment liquid, owing to adopt MVR vapor compressor to provide the heat source, compares the difference in temperature less with traditional evaporimeter, can reach the effect of gentle evaporation, improves the output quality volume, reduces the equipment scale deposit.
Drawings
Other features, objects and advantages of the present application will become more apparent upon reading of the following detailed description of non-limiting embodiments thereof, made with reference to the accompanying drawings.
Fig. 1 is a schematic diagram of the sodium gulonate MVR concentration system of the embodiment of the present invention.
The numbers in the figure are compared as follows:
1-a plate heat exchanger; 2-a feed tank; 3-first-stage falling film evaporator; 4-a gas-liquid separator; 5-a second-stage forced circulation evaporator; 6-a crystallizer; 7-MVR vapor compressor; 8-crystal slurry tank; 9-a condenser; 10-condensation water tank.
Detailed Description
The present application will be described in further detail with reference to the following drawings and examples. It is to be understood that the specific embodiments described herein are merely illustrative of the relevant invention and are not limiting of the invention. It should be noted that, for convenience of description, only the portions related to the present invention are shown in the drawings.
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present application will be described in detail below with reference to the accompanying drawings in conjunction with embodiments.
Referring to fig. 1, the utility model discloses a sodium gulonate MVR system of concentrating, it mainly includes plate heat exchanger 1, one-level falling film evaporator 3, vapour and liquid separator 4, second grade forced circulation evaporimeter 5, crystallizer 6, MVR vapor compressor 7, condenser 9 and condensate tank 10. Further may include a feed tank 2 and a slurry tank 8.
The inlet of the plate heat exchanger 1 is connected to the feed tank 2 by means of a feed pump. The plate heat exchanger is a high-efficiency heat exchanger formed by stacking a series of metal sheets with certain corrugated shapes. Thin rectangular channels are formed between the various plates through which heat is exchanged. The plate heat exchanger is an ideal device for liquid-liquid and liquid-steam heat exchange. The heat exchanger has the characteristics of high heat exchange efficiency, small heat loss, compact and light structure, small occupied area, wide application, long service life and the like. Under the condition of the same pressure loss, the heat transfer coefficient of the heat exchanger is 3-5 times higher than that of the tubular heat exchanger, the occupied area of the heat exchanger is one third of that of the tubular heat exchanger, and the heat recovery rate can reach more than 90 percent.
The outlet of the plate heat exchanger 1 is connected with the feed inlet of the first-stage falling-film evaporator 3, the first-stage falling-film evaporator 3 is connected with the gas-liquid separator 4 through a circulating pump, the secondary steam outlet of the gas-liquid separator 4 is connected with the steam inlet of the MVR steam compressor 7, the feed liquid outlet of the gas-liquid separator 4 is connected with the feed inlet of the second-stage forced circulation evaporator 5, the second-stage forced circulation evaporator 5 is connected with the crystallizer 6 through a circulating pump, the steam outlet of the crystallizer 6 is connected with the steam inlet of the MVR steam compressor 7, and the discharge port of the crystallizer 6 is connected with the inlet of the crystal slurry tank 8.
And a steam outlet of the MVR steam compressor is respectively connected with steam inlets of the first-stage falling-film evaporator 3 and the second-stage forced circulation evaporator 5, so that a heat source is provided for evaporation and concentration of the first-stage falling-film evaporator 3 and the second-stage forced circulation evaporator 5. Compare with traditional evaporimeter, provide the heat source by MVR vapor compressor, the difference in temperature is less, can reach the effect of gentle evaporation to improve the output quality volume, reduce the equipment scale deposit.
The non-condensable gas outlets of the first-stage falling-film evaporator 3 and the second-stage forced circulation evaporator 5 are respectively connected with the inlet of a condenser 9, the condensed water outlet of the condenser 9 is further connected with a condensed water tank 10, and the condensed water outlet of the condensed water tank 10 is connected with the condensed water inlet of the plate heat exchanger 1 and is supplied to the plate heat exchanger 1 for preheating the feed liquid.
The utility model discloses a sodium gulonate MVR concentrated system adopts forced falling film and MVR mechanical compression evaporative concentration's mode to carry out evaporative concentration to sodium gulonate sediment liquid.
The sodium gulonate slag liquid is continuously pumped by a feed pump, passes through a primary plate heat exchanger 1 and enters a primary falling film evaporator 3; the raw steam (or the secondary steam after mechanical compression) is used as a heat source, the feed liquid is heated to 40-45 ℃, the temperature of the heated solution is maintained under a specific pressure, the water is evaporated to generate the secondary steam, and the sodium gulonate slag liquid is concentrated. Boiling and evaporating the material in the tube of the first-stage falling-film evaporator 3, separating gas and liquid in the gas-liquid separator 4, and heating, evaporating and concentrating the feed liquid separated by the gas-liquid separator in the second-stage forced circulation evaporator 5 and the crystallizer 6; after the concentration is detected to be qualified on line through the mass flow meter, the material is sent out by a discharge pump and enters the next procedure. Wherein, the mass flow meter can be arranged at the outlet of the crystallizer 6, and the outlet of the crystallizer 6 can be further connected with the crystal slurry tank 8.
The secondary steam generated by the first-stage falling-film evaporator 3 is subjected to gas-liquid separation through a gas-liquid separator 4, the separated secondary steam enters an MVR steam compressor 7, the feed liquid separated by the gas-liquid separator 4 enters a second-stage forced circulation evaporator 5 for reheating evaporation, the secondary steam generated by the second-stage forced circulation evaporator 5 is subjected to gas-liquid separation through a separator, the separator is in an Oslo continuous crystallizer, and the secondary steam separated by the crystallizer 6 can enter a cyclone separator (not shown in the figure) for gas-liquid separation again. A cyclone separator is used for separating a gas-solid system or a liquid-solid system, and the working principle of the cyclone separator is that solid particles or liquid drops with larger inertial centrifugal force are thrown to an outer wall surface to be separated by virtue of rotary motion caused by tangential introduction of airflow. The secondary steam separated by the cyclone separator enters an MVR steam compressor 7, meanwhile, the secondary steam separated by the gas-liquid separator 4 of the first-stage falling-film evaporator 3 also enters the MVR steam compressor 7, an air suction port of a compression fan of the MVR steam compressor 7 is arranged at an outlet of the cyclone separator, and an air exhaust port is arranged at an inlet of the first-stage falling-film evaporator 3. The secondary steam is compressed from about 35 c to about 49 c by the MVR steam compressor 7 compressor fan temperature. The vapor compressed by the MVR vapor compressor 7 enters the first-stage falling-film evaporator 3 and the second-stage forced circulation evaporator 5 to be used as a heat source again, and the low-pressure vapor is subjected to pressure reduction and temperature reduction and then is used for supplementing vapor for two-stage evaporation.
The non-condensable gas of the first-stage falling-film evaporator 3 and the second-stage forced circulation evaporator 5 enters a condenser 9, is cooled by cooling water and then is discharged out of the system, or enters a condensate water tank 10, and the condensate water in the condensate water tank 10 is preheated in the plate heat exchanger 1. Meanwhile, the sewage condensate water discharged by the first-stage falling-film evaporator 3 and the second-stage forced circulation evaporator 5 is also collected into the condensate water tank 10, and is sent to the plate heat exchanger 1 for preheating after being flashed.
Compared with the traditional concentration process, the process has the advantages that:
1. the process has short route and less effect bodies.
2. The process reduces the probability of pipe blockage, most of the traditional evaporation systems are multi-effect evaporation systems, the front-back temperature span is large, the retention time of feed liquid in a pipeline of an MVR evaporator system is long, and the pipe blockage is easily caused; the MVR evaporator has compact system structure, short material flow, low heating temperature and greatly reduced probability of pipe blockage.
3. The MVR evaporator system is a good evaporator technology at present, needs less raw steam (a small amount of raw steam is needed when the evaporator system is started, and the raw steam is almost not needed in normal operation), reduces the operation cost of enterprises, and reduces the environmental pollution.
4. Because the compressor is adopted to provide a heat source, the temperature difference is much smaller compared with the traditional evaporator, mild evaporation can be achieved, the yield and quality are improved, and scaling is reduced.
5. The MVR evaporator system enables the materials to be evaporated at low temperature, the material liquid is uniform, the materials do not run, coking is not easy to occur, and the material heating denaturation is small.
6. The process has low operation cost and high energy utilization rate.
The above description is only a preferred embodiment of the application and is illustrative of the principles of the technology employed. It will be understood by those skilled in the art that the scope of the present invention is not limited to the specific combination of the above-mentioned features, but also covers other embodiments formed by any combination of the above-mentioned features or their equivalents without departing from the spirit of the present invention. For example, the above features may be replaced with (but not limited to) features having similar functions disclosed in the present application.
Claims (3)
1. A sodium gulonate MVR concentrated system which characterized in that includes:
a plate heat exchanger;
the feed inlet of the first-stage falling-film evaporator is connected with the outlet of the plate heat exchanger, and the first-stage falling-film evaporator is connected with the gas-liquid separator;
the feeding port of the second-stage forced circulation evaporator is connected with the discharging port of the gas-liquid separator, and the second-stage forced circulation evaporator is connected with the crystallizer;
an inlet of the MVR vapor compressor is respectively connected with vapor outlets of the gas-liquid separator and the crystallizer, and an outlet of the MVR vapor compressor is connected with vapor inlets of the first-stage falling-film evaporator and the second-stage forced circulation evaporator;
the inlet of the condenser is connected with the non-condensable gas outlets of the first-stage falling-film evaporator and the second-stage forced circulation evaporator;
and the inlet of the condensed water tank is connected with the condensed water outlets of the primary falling-film evaporator and the secondary forced circulation evaporator, the inlet of the condensed water tank is also connected with the outlet of the condenser, and the outlet of the condensed water tank is connected with the condensed water inlet of the plate heat exchanger.
2. The sodium gulonate MVR concentration system according to claim 1, wherein the inlet of the plate heat exchanger is connected to the feed tank by a feed pump.
3. The sodium gulonate MVR concentration system according to claim 1, wherein the outlet of the crystallizer is connected with a crystal slurry tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223143439.9U CN218686389U (en) | 2022-11-25 | 2022-11-25 | Sodium gulonate MVR concentration system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223143439.9U CN218686389U (en) | 2022-11-25 | 2022-11-25 | Sodium gulonate MVR concentration system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN218686389U true CN218686389U (en) | 2023-03-24 |
Family
ID=85625082
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202223143439.9U Active CN218686389U (en) | 2022-11-25 | 2022-11-25 | Sodium gulonate MVR concentration system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN218686389U (en) |
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- 2022-11-25 CN CN202223143439.9U patent/CN218686389U/en active Active
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| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20231219 Address after: 201306 Room A205, Building 1, No. 336, Tianjiao Road, Lingang New Area, China (Shanghai) Pilot Free Trade Zone, Pudong New Area, Shanghai Patentee after: SHANGHAI SENON Co.,Ltd. Patentee after: Qidong Shennong Machinery Co.,Ltd. Address before: 201306 Room A205, Building 1, No. 336, Tianjiao Road, Lingang New Area, China (Shanghai) Pilot Free Trade Zone, Pudong New Area, Shanghai Patentee before: SHANGHAI SENON Co.,Ltd. |