CN218653015U - MVR processing apparatus of lysine zymotic fluid - Google Patents
MVR processing apparatus of lysine zymotic fluid Download PDFInfo
- Publication number
- CN218653015U CN218653015U CN202223151290.9U CN202223151290U CN218653015U CN 218653015 U CN218653015 U CN 218653015U CN 202223151290 U CN202223151290 U CN 202223151290U CN 218653015 U CN218653015 U CN 218653015U
- Authority
- CN
- China
- Prior art keywords
- outlet
- inlet
- falling film
- evaporator
- mvr
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- KDXKERNSBIXSRK-UHFFFAOYSA-N Lysine Natural products NCCCCC(N)C(O)=O KDXKERNSBIXSRK-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 239000004472 Lysine Substances 0.000 title claims abstract description 40
- 238000012545 processing Methods 0.000 title claims abstract description 10
- 239000012530 fluid Substances 0.000 title claims abstract description 8
- 239000011552 falling film Substances 0.000 claims abstract description 79
- 238000001704 evaporation Methods 0.000 claims abstract description 43
- 230000008020 evaporation Effects 0.000 claims abstract description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 31
- 239000000463 material Substances 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims description 22
- 238000000855 fermentation Methods 0.000 claims description 15
- 230000004151 fermentation Effects 0.000 claims description 15
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 229960003646 lysine Drugs 0.000 description 32
- 239000002351 wastewater Substances 0.000 description 10
- 238000000034 method Methods 0.000 description 7
- 230000008569 process Effects 0.000 description 7
- 230000006835 compression Effects 0.000 description 5
- 238000007906 compression Methods 0.000 description 5
- 230000006872 improvement Effects 0.000 description 5
- 239000013078 crystal Substances 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical class Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000012528 membrane Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000013589 supplement Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- BVHLGVCQOALMSV-JEDNCBNOSA-N L-lysine hydrochloride Chemical compound Cl.NCCCC[C@H](N)C(O)=O BVHLGVCQOALMSV-JEDNCBNOSA-N 0.000 description 2
- 241001465754 Metazoa Species 0.000 description 2
- 229940024606 amino acid Drugs 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000003623 enhancer Substances 0.000 description 2
- 235000020776 essential amino acid Nutrition 0.000 description 2
- 239000003797 essential amino acid Substances 0.000 description 2
- 229960005337 lysine hydrochloride Drugs 0.000 description 2
- 235000016709 nutrition Nutrition 0.000 description 2
- 230000035764 nutrition Effects 0.000 description 2
- 230000020477 pH reduction Effects 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 239000004097 EU approved flavor enhancer Substances 0.000 description 1
- AGPKZVBTJJNPAG-WHFBIAKZSA-N L-isoleucine Chemical compound CC[C@H](C)[C@H](N)C(O)=O AGPKZVBTJJNPAG-WHFBIAKZSA-N 0.000 description 1
- ROHFNLRQFUQHCH-YFKPBYRVSA-N L-leucine Chemical compound CC(C)C[C@H](N)C(O)=O ROHFNLRQFUQHCH-YFKPBYRVSA-N 0.000 description 1
- KDXKERNSBIXSRK-YFKPBYRVSA-N L-lysine Chemical compound NCCCC[C@H](N)C(O)=O KDXKERNSBIXSRK-YFKPBYRVSA-N 0.000 description 1
- FFEARJCKVFRZRR-BYPYZUCNSA-N L-methionine Chemical compound CSCC[C@H](N)C(O)=O FFEARJCKVFRZRR-BYPYZUCNSA-N 0.000 description 1
- COLNVLDHVKWLRT-QMMMGPOBSA-N L-phenylalanine Chemical compound OC(=O)[C@@H](N)CC1=CC=CC=C1 COLNVLDHVKWLRT-QMMMGPOBSA-N 0.000 description 1
- AYFVYJQAPQTCCC-GBXIJSLDSA-N L-threonine Chemical compound C[C@@H](O)[C@H](N)C(O)=O AYFVYJQAPQTCCC-GBXIJSLDSA-N 0.000 description 1
- QIVBCDIJIAJPQS-VIFPVBQESA-N L-tryptophane Chemical compound C1=CC=C2C(C[C@H](N)C(O)=O)=CNC2=C1 QIVBCDIJIAJPQS-VIFPVBQESA-N 0.000 description 1
- KZSNJWFQEVHDMF-BYPYZUCNSA-N L-valine Chemical compound CC(C)[C@H](N)C(O)=O KZSNJWFQEVHDMF-BYPYZUCNSA-N 0.000 description 1
- ROHFNLRQFUQHCH-UHFFFAOYSA-N Leucine Natural products CC(C)CC(N)C(O)=O ROHFNLRQFUQHCH-UHFFFAOYSA-N 0.000 description 1
- 241001052560 Thallis Species 0.000 description 1
- AYFVYJQAPQTCCC-UHFFFAOYSA-N Threonine Natural products CC(O)C(N)C(O)=O AYFVYJQAPQTCCC-UHFFFAOYSA-N 0.000 description 1
- 239000004473 Threonine Substances 0.000 description 1
- QIVBCDIJIAJPQS-UHFFFAOYSA-N Tryptophan Natural products C1=CC=C2C(CC(N)C(O)=O)=CNC2=C1 QIVBCDIJIAJPQS-UHFFFAOYSA-N 0.000 description 1
- KZSNJWFQEVHDMF-UHFFFAOYSA-N Valine Natural products CC(C)C(N)C(O)=O KZSNJWFQEVHDMF-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000003862 amino acid derivatives Chemical class 0.000 description 1
- -1 amino acid salts Chemical class 0.000 description 1
- 150000001413 amino acids Chemical class 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000003729 cation exchange resin Substances 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000013065 commercial product Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000003599 detergent Substances 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000010408 film Substances 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 235000019264 food flavour enhancer Nutrition 0.000 description 1
- 235000003599 food sweetener Nutrition 0.000 description 1
- 238000001802 infusion Methods 0.000 description 1
- 229960000310 isoleucine Drugs 0.000 description 1
- AGPKZVBTJJNPAG-UHFFFAOYSA-N isoleucine Natural products CCC(C)C(N)C(O)=O AGPKZVBTJJNPAG-UHFFFAOYSA-N 0.000 description 1
- 239000002649 leather substitute Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229930182817 methionine Natural products 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- COLNVLDHVKWLRT-UHFFFAOYSA-N phenylalanine Natural products OC(=O)C(N)CC1=CC=CC=C1 COLNVLDHVKWLRT-UHFFFAOYSA-N 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000003765 sweetening agent Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000004474 valine Substances 0.000 description 1
Images
Classifications
-
- 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
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses a MVR processing apparatus of lysine zymotic fluid, include: the inlet of the plate heat exchanger is connected with the feeding pump; the falling film evaporation device is characterized in that a material inlet is connected with an outlet of the plate heat exchanger; a feed inlet of the forced circulation evaporator is connected with a discharge outlet of the falling film evaporation device, and the discharge outlet is connected with the crystallizer; an inlet of the MVR vapor compressor is respectively connected with a secondary vapor outlet of the falling film evaporation device and a secondary vapor outlet of the crystallizer, and an outlet of the MVR vapor compressor is connected with vapor inlets of the falling film evaporation device and the forced circulation evaporator; the inlet of the condenser is connected with the falling film evaporation device and the non-condensable gas outlet of the forced circulation evaporator; and the inlet of the condensed water tank is connected with the condensed water outlet of the falling film evaporation device and the 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. The utility model discloses a device 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 MVR processing apparatus of lysine zymotic fluid.
Background
Lysine is one of eight essential amino acids (also called essential amino acids, which are lysine, threonine, leucine, isoleucine, methionine, valine, phenylalanine and tryptophan) essential for human body. Lysine has a high solubility in water, and readily absorbs carbon dioxide in the air, making it difficult to obtain crystals thereof. It is therefore often present as a commercial product in the form of the monohydrochloride salt. Lysine has wide application, and is mainly applied to the following industries: in the food industry, preparing nutrition enhancers, flavor enhancers and sweeteners; in the feed industry, a nutrition enhancer is prepared; in the pharmaceutical industry, amino acid infusion, amino acid derivatives, and amino acid salts are prepared; chemical industry, preparing detergents, skin care products, artificial leather; agriculture, and preparing pollution-free pesticides. At present, more than 90% of lysine products are used in the feed industry, and if a proper amount of lysine is added into feed, the synthesis of protein in an animal body can be increased, and the growth and development of the animal are promoted.
Lysine hydrochloride is generally prepared as follows: fermenting the strain to obtain a fermentation liquid, adding a large amount of concentrated sulfuric acid into the fermentation liquid to adjust the pH value to 2.0-3.0 for acidification, filtering the fermentation liquid through a metal membrane or a ceramic membrane to remove thalli after acidification, obtaining a lysine membrane filtrate, namely a lysine-containing solution, performing adsorption exchange on the lysine-containing solution by adopting strong acid type cation exchange resin, eluting the solution by using dilute ammonia water after the resin is adsorbed and saturated, concentrating the eluted lysine, adjusting the pH value by using hydrochloric acid, crystallizing, performing solid-liquid separation, and drying to obtain a lysine hydrochloride finished product.
When the existing multi-effect evaporator is used for evaporating, concentrating and crystallizing lysine fermentation liquor, a large amount of fresh steam is consumed for each effect of evaporation and concentration, and the fresh steam is preheated, so that the energy consumption is high, and the cost is high.
SUMMERY OF THE UTILITY MODEL
For overcoming the partial defect that prior art exists at least, the utility model provides a MVR processing apparatus of lysine zymotic fluid has effectively improved the utilization ratio of steam, energy-conservation subtracts and consumes, reduce cost.
The utility model adopts the technical proposal that:
an MVR processing device of lysine fermentation liquor, which comprises:
the inlet of the plate heat exchanger is connected with a feed pump;
the material inlet of the falling film evaporation device is connected with the outlet of the plate heat exchanger;
a feed inlet of the forced circulation evaporator is connected with a discharge outlet of the falling film evaporation device, and a discharge outlet of the forced circulation evaporator is connected with the crystallizer;
an inlet of the MVR vapor compressor is respectively connected with a secondary vapor outlet of the falling film evaporation device and a secondary vapor outlet of the crystallizer, and an outlet of the MVR vapor compressor is connected with vapor inlets of the falling film evaporation device and the forced circulation evaporator;
an inlet of the condenser is connected with the falling film evaporation device and a non-condensable gas outlet of the forced circulation evaporator;
the inlet of the condensed water tank is connected with the condensed water outlet of the falling film evaporation device and the 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 utility model, the falling film evaporator is a double-effect or multi-effect falling film evaporator.
As a further improvement of the utility model, the falling film evaporation device includes one-level falling film evaporator and second grade falling film evaporator, the pan feeding mouth of one-level falling film evaporator with plate heat exchanger's exit linkage, one-level falling film evaporator discharge gate with the pan feeding mouth of second grade falling film evaporator is connected, second grade falling film evaporator discharge gate with the pan feeding mouth of forced circulation evaporator is connected.
As a further improvement of the utility model, the one-level falling film evaporator with the second grade falling film evaporator is connected with vapour and liquid separator through the circulating pump respectively, the vapour and liquid separator's of one-level falling film evaporator secondary steam export with the steam inlet of second grade falling film evaporator is connected.
As a further improvement of the utility model, the secondary steam outlet of the gas-liquid separator of the two-stage falling film evaporator is connected with the inlet of the MVR steam compressor.
As a further improvement, the MVR vapor compressor has a vapor outlet connected with the one-level falling film evaporator and a vapor inlet of the forced circulation evaporator.
The beneficial effects of the utility model reside in that:
the lysine fermentation liquor is evaporated and concentrated by adopting a forced falling film and MVR mechanical compression evaporation and concentration mode, except that steam is used for preheating the device when the device is started, only electric power is needed when the whole device is in normal operation, and raw steam does not need to be supplemented. The suction end of the MVR compressor is partially evacuated, which reduces flash vapor formed when the crystal slurry enters the centrifuge. The device does not need to supplement raw steam during operation, and all high-temperature condensed water generated by the device is used for preheating the materials to be close to the boiling point; the heat energy generated when the MVR compressor compresses steam is used for preheating the residual materials, and meanwhile, the heat loss generated by the device is compensated, so that enough heat energy is provided to ensure the air and the non-condensed steam to be discharged.
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 an MVR processing apparatus for lysine fermentation broth according to an 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-first-stage gas-liquid separator; 5-a two-stage falling-film evaporator; 6-a secondary gas-liquid separator; 7-three-stage forced circulation evaporator; 8-a crystallizer; 9-MVR vapor compressor; 10-a condenser; 11-condensed 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 embodiments with reference to the attached drawings.
Referring to fig. 1, the utility model discloses a MVR processing apparatus of lysine zymotic fluid mainly includes plate heat exchanger 1, falling liquid film evaporation plant, forced circulation evaporimeter, crystallizer, MVR vapor compressor 9, condenser 10 and condensation water pitcher 11.
The inlet of the plate heat exchanger 1 is connected to the feed tank 2 by means of a feed pump. A feed inlet of the falling film evaporation device is connected with an outlet of the plate heat exchanger 1; a feed inlet of the forced circulation evaporator is connected with a discharge outlet of the falling film evaporation device, and a discharge outlet of the forced circulation evaporator is connected with the crystallizer 8; an inlet of the MVR vapor compressor 9 is respectively connected with a secondary vapor outlet of the falling film evaporation device and a secondary vapor outlet of the crystallizer 8, and an outlet of the MVR vapor compressor 9 is connected with vapor inlets of the falling film evaporation device and the forced circulation evaporator; an inlet of the condenser 10 is connected with a falling film evaporation device and a noncondensable gas outlet of the forced circulation evaporator; the inlet of the condensate water tank 11 is connected with the condensate water outlet of the falling film evaporator and the forced circulation evaporator, the inlet of the condensate water tank 11 is also connected with the outlet of the condenser 10, and the outlet of the condensate water tank 11 is connected with the condensate water inlet of the plate heat exchanger 1.
Furthermore, the falling film evaporation device in the utility model can adopt a double-effect or multi-effect falling film evaporation device. In the embodiment, the falling film evaporation device comprises a first-stage falling film evaporator 3 and a second-stage falling film evaporator 5, a feed inlet of the first-stage falling film evaporator 3 is connected with an outlet of the plate heat exchanger, a discharge outlet of the first-stage falling film evaporator 3 is connected with a feed inlet of the second-stage falling film evaporator 5, and a discharge outlet of the second-stage falling film evaporator 5 is connected with a feed inlet of a third-stage forced circulation evaporator 7.
The first-stage falling-film evaporator 3 is connected with the first-stage gas-liquid separator 4 through a circulating pump, the second-stage falling-film evaporator 5 is connected with the second-stage gas-liquid separator 6 through a circulating pump, and a secondary steam outlet of the first-stage gas-liquid separator 4 is connected with a steam inlet of the second-stage falling-film evaporator 5. And a secondary steam outlet of the secondary gas-liquid separator 6 is connected with an inlet of the MVR steam compressor 9. The vapor outlet of the MVR vapor compressor 9 is connected with the vapor inlets of the first-stage falling-film evaporator 3 and the third-stage forced circulation evaporator 7.
The utility model discloses a forced falling film and MVR mechanical compression evaporation concentration's mode carries out evaporation concentration to the lysine zymotic fluid, and concrete work flow is as follows:
the lysine fermentation liquor 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 to heat the feed liquid to 65-70 ℃, the temperature of the heated solution is kept at a specific pressure, the water is evaporated to generate the secondary steam, and the lysine fermentation liquid is concentrated. The material is boiled and evaporated in the tube of the first-stage evaporator, and then enters the second-stage falling-film evaporator 5 to be heated, evaporated and concentrated; the concentrated material enters a three-stage forced circulation evaporator 7 to be heated, evaporated and concentrated again; the three stage separator is configured as an FC crystallizer 8. The material reaches supersaturation and separates out the crystal in tertiary forced circulation evaporimeter 7, passes through mass flow meter on-line measuring concentration after qualified, is sent out by the discharge pump, gets into next process.
Wherein, the secondary steam generated by the first-stage falling-film evaporator 3 is subjected to gas-liquid separation through the first-stage gas-liquid separator 4, and the separated secondary steam enters the second-stage falling-film evaporator 3 for heat exchange; the secondary steam generated by the secondary falling-film evaporator 5 and the tertiary forced circulation evaporator 7 is respectively subjected to gas-liquid separation through separators of respective effect bodies, and the separated secondary steam is converged and then enters a fan inlet of MVR steam compression; the temperature of the secondary steam is compressed from about 55-60 ℃ to 70-75 ℃ by a compression fan, and the secondary steam after temperature rise enters the first-stage falling-film evaporator 3 and the third-stage forced circulation evaporator 7 respectively for heat exchange.
When multi-effect evaporation is adopted, secondary steam generated by the first-stage falling-film evaporator 3 is used as a heat source of a next-stage evaporator, concentrated lysine wastewater also enters a next effect, the secondary steam heats the concentrated lysine wastewater to a certain temperature under the condition of maintaining specific pressure, water is evaporated to generate secondary steam, and the lysine wastewater is further concentrated; the concentrated lysine wastewater also enters a next-stage evaporator, the concentrated lysine wastewater is heated to a certain temperature by secondary steam under the condition of maintaining a specific pressure, water is evaporated to generate secondary steam, and the lysine wastewater is further concentrated; and (3) the concentrated lysine wastewater enters a next-stage evaporator, the concentrated lysine wastewater is heated to a certain temperature by secondary steam under the condition of maintaining a specific pressure, water is evaporated to generate secondary steam, and the lysine wastewater is further concentrated.
Thus, after multiple times of evaporation and concentration, the lysine wastewater reaches the concentration and is sent out of the device; the non-condensable gas of the two-section evaporator enters a condenser 10, is cooled by cooling water and then is discharged out of the system. When MVR evaporation is adopted, secondary steam evaporated and discharged by the separator enters the heater to be used as a heat source again after being compressed by MVR. The low-pressure steam is used for supplementing steam for two-stage evaporation after being decompressed and cooled. And the sewage condensate water of each evaporator is collected into a sewage condensate water tank 11, is sent to a primary plate heat exchanger 1 for preheating after flash evaporation, and is returned to the falling film evaporator for continuously participating in the evaporation and concentration of the lysine fermentation liquor after preheating.
Compared with the traditional concentration process, the process has the advantages that:
1. the process route is short, and the number of effective bodies is small;
2. the process only needs to use electric power when the whole system normally runs and does not need to supplement raw steam except that the steam is used for preheating the system when the system is started. The suction end of the fan is in partial vacuum, so that flash steam formed when the crystal mush enters the centrifugal machine can be reduced. The system does not need to supplement raw steam during operation, and all high-temperature condensed water generated by the system is used for preheating the materials to be close to the boiling point; the heat energy generated when the fan compresses steam is used for preheating the rest materials, meanwhile, the heat loss generated by the system is compensated, and sufficient heat energy is provided to ensure the discharge of air and non-condensed steam.
3. The process has large evaporation capacity and less equipment sets; the investment cost of the equipment is low, the occupied area is small, and the maintenance and operation personnel are few;
4. 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 (6)
1. A MVR processing apparatus of lysine zymotic fluid, characterized by, includes:
the inlet of the plate heat exchanger is connected with a feed pump;
the material inlet of the falling film evaporation device is connected with the outlet of the plate heat exchanger;
a feed inlet of the forced circulation evaporator is connected with a discharge outlet of the falling film evaporation device, and a discharge outlet of the forced circulation evaporator is connected with the crystallizer;
an inlet of the MVR vapor compressor is connected with a secondary vapor outlet of the falling film evaporation device and a secondary vapor outlet of the crystallizer respectively, and an outlet of the MVR vapor compressor is connected with vapor inlets of the falling film evaporation device and the forced circulation evaporator;
an inlet of the condenser is connected with the falling film evaporation device and a non-condensable gas outlet of the forced circulation evaporator;
the inlet of the condensed water tank is connected with the condensed water outlet of the falling film evaporation device and the 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 MVR treatment device of a lysine fermentation broth according to claim 1, wherein the falling film evaporation device is a double-effect or multi-effect falling film evaporation device.
3. The MVR treatment device for lysine fermentation broth according to claim 2, wherein the falling film evaporation device comprises a primary falling film evaporator and a secondary falling film evaporator, the feed inlet of the primary falling film evaporator is connected with the outlet of the plate heat exchanger, the discharge outlet of the primary falling film evaporator is connected with the feed inlet of the secondary falling film evaporator, and the discharge outlet of the secondary falling film evaporator is connected with the feed inlet of the forced circulation evaporator.
4. The MVR treatment device for lysine fermentation broth according to claim 3, wherein the first-stage falling-film evaporator and the second-stage falling-film evaporator are respectively connected with a gas-liquid separator through a circulating pump, and a secondary steam outlet of the gas-liquid separator of the first-stage falling-film evaporator is connected with a steam inlet of the second-stage falling-film evaporator.
5. The MVR treatment device for the lysine fermentation broth according to claim 4, wherein a secondary steam outlet of a gas-liquid separator of the two-stage falling-film evaporator is connected with an inlet of the MVR steam compressor.
6. The MVR processing device of a lysine fermentation broth according to claim 5, wherein a steam outlet of the MVR steam compressor is connected with a steam inlet of the first-stage falling-film evaporator and the forced circulation evaporator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223151290.9U CN218653015U (en) | 2022-11-25 | 2022-11-25 | MVR processing apparatus of lysine zymotic fluid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223151290.9U CN218653015U (en) | 2022-11-25 | 2022-11-25 | MVR processing apparatus of lysine zymotic fluid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN218653015U true CN218653015U (en) | 2023-03-21 |
Family
ID=85540092
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202223151290.9U Active CN218653015U (en) | 2022-11-25 | 2022-11-25 | MVR processing apparatus of lysine zymotic fluid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN218653015U (en) |
-
2022
- 2022-11-25 CN CN202223151290.9U patent/CN218653015U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108159721B (en) | Tryptophan TVR evaporating, concentrating and crystallizing system and method for concentrating and crystallizing by using system | |
| CN102616972B (en) | Comprehensive recycling method and device for high-salt-content amino acid waste water | |
| US11091381B1 (en) | Method for extracting antibacterial peptides and albumin from pea whey wastewater | |
| JP4349655B2 (en) | Organic waste liquid processing apparatus and processing method | |
| CN102557970B (en) | Preparation method of anhydrous betaine | |
| CN110613951A (en) | Evaporation concentration flash evaporation cooling crystallization equipment and process thereof | |
| CN108033893A (en) | The method that continuous flow upstream ultrasonic technique extracts levodopa from cat beans | |
| CN107879940A (en) | Device and method for continuously refining pentamethylene diamine | |
| CN102167363B (en) | New energy-saving technology for producing edible potassium chloride | |
| CN218653015U (en) | MVR processing apparatus of lysine zymotic fluid | |
| CN209221515U (en) | A kind of lithium chloride evaporation concentration device | |
| CN204891247U (en) | Sodium nitrate solution evaporation crystallization equipment | |
| CN103508877A (en) | Energy-saving method and device for four-effect concentration and crystallization of itaconic acid | |
| CN210751328U (en) | Aminoacetic acid by-product ammonium chloride recovery device | |
| CN209835872U (en) | Waste incineration sprays liquid processing system | |
| CN111892498A (en) | Method for extracting L-malic acid | |
| CN218686389U (en) | Sodium gulonate MVR concentration system | |
| CN114949893B (en) | Evaporation crystallization process and device for producing lithium chloride from salt lake brine | |
| CN112079376A (en) | Zinc sulfate evaporation crystallization drying equipment and process thereof | |
| CN209081464U (en) | A kind of high-salt wastewater positive pressure evaporated crystallization device based on the driving of steam power plant's heat source | |
| CN210560178U (en) | Valine double-effect concentration and crystallization system | |
| CN103864667B (en) | L-Trp economic benefits and social benefits consecutive evaporation deamination technique | |
| CN220513430U (en) | Plate-type and tube-array combined evaporator | |
| CN110787638B (en) | Concentration system and concentration method of pentanediamine | |
| CN106350547A (en) | Preparation method of L-arginine-alpha-ketoglutaric acid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| 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. |
|
| TR01 | Transfer of patent right |