CN109276898B - Integrated system for concentrating fruit juice and recovering essence - Google Patents
Integrated system for concentrating fruit juice and recovering essence Download PDFInfo
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- CN109276898B CN109276898B CN201710590845.4A CN201710590845A CN109276898B CN 109276898 B CN109276898 B CN 109276898B CN 201710590845 A CN201710590845 A CN 201710590845A CN 109276898 B CN109276898 B CN 109276898B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0011—Heating features
- B01D1/0041—Use of fluids
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- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
- A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Their preparation
- A23L2/02—Non-alcoholic beverages; Dry compositions or concentrates therefor; Their preparation containing fruit or vegetable juices
- A23L2/08—Concentrating or drying of juices
- A23L2/10—Concentrating or drying of juices by heating or contact with dry gases
- A23L2/107—Electric or wave heating
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/30—Accessories for evaporators ; Constructional details thereof
- B01D1/305—Demister (vapour-liquid separation)
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/148—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step in combination with at least one evaporator
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
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- Nutrition Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Food Science & Technology (AREA)
- Polymers & Plastics (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to the technical field of evaporation and rectification, in particular to a juice concentration and essence recovery integrated system. The system comprises an evaporator, a first rectifying tower, a second rectifying tower, a first steam compressor, a second steam compressor, a gas-liquid separator, a first reboiler, a second reboiler, a first preheater and a second preheater, wherein the evaporator is connected with the gas-liquid separator, the gas-liquid separator is connected with the first rectifying tower, the first rectifying tower is connected with the second steam compressor, the second steam compressor is connected with the second reboiler, the second reboiler is connected with the first preheater, and the first preheater is respectively correspondingly connected with a reflux inlet and a juice storage tank of the first rectifying tower through a first branch pipeline and a second branch pipeline. The invention combines the heat pump evaporation and the rectification, fully utilizes the condensate at the bottom of the evaporator and the steam at the top of the tower, fully utilizes the latent heat of the secondary steam, recovers the latent heat and improves the heat efficiency.
Description
Technical Field
The invention relates to the technical field of evaporation and rectification, in particular to a juice concentration and essence recovery integrated system.
Background
The evaporation distillation is widely applied to various industries such as water treatment, chemical industry, pharmacy, food, seawater desalination, salt manufacturing and the like. The evaporation distillation is a high-energy-consumption process, and the evaporation process is an energy-consuming large household in the industries, so the main production consumption of the industries is the energy consumption cost.
At present, the prior domestic various industries related to the evaporation process generally adopt a multi-effect evaporation technology for evaporation and concentration, a large amount of raw steam needs to be provided in the working process, and a coal-fired boiler and a cooling system need to be configured. The problems of the existing system are as follows: the whole structure is complex and the volume is huge; high energy consumption, rapid rise of operation cost and environmental pollution caused by coal burning.
Disclosure of Invention
Technical problem to be solved
The invention aims to provide a juice concentration and essence recovery integrated system, which solves the problems of complex structure, high energy consumption and high operation cost in the prior art.
(II) technical scheme
In order to solve the technical problems, the invention provides a juice concentration and essence recovery integrated system, which comprises an evaporator, a first rectifying tower, a second rectifying tower, a first steam compressor, a second steam compressor, a gas-liquid separator, a first reboiler, a second reboiler, a first preheater and a second preheater, wherein the evaporator is connected with the first rectifying tower;
the bottom discharge hole of the evaporator is connected with the gas-liquid separator, and the bottom discharge hole of the gas-liquid separator is connected with the first rectifying tower;
a top steam outlet of the first rectifying tower is connected with an inlet of the second steam compressor, an outlet of the second steam compressor is connected with a hot material flow inlet of the second reboiler, a hot material flow outlet of the second reboiler is connected with a hot material flow inlet of the first preheater, and the hot material flow outlet of the first preheater is correspondingly connected with a reflux inlet of the first rectifying tower and a juice storage tank through a first branch pipeline and a second branch pipeline respectively;
the top secondary steam outlet of the evaporator is connected with the inlet of the first steam compressor, the outlet of the first steam compressor is connected with the hot substance inlet of the first reboiler, the hot substance outlet of the first reboiler is connected with the feed inlet of the second rectifying tower, the top steam outlet of the second rectifying tower is connected with the steam inlet of the evaporator, and the condensate outlet of the evaporator is correspondingly connected with the reflux inlet of the second rectifying tower and the rectifying storage tank through a third branch pipeline and a fourth branch pipeline respectively.
Further, still include the inlet pipe and set up raw materials charge pump on the inlet pipe, wherein the inlet pipe is connected the cold commodity circulation entry of first pre-heater, the cold commodity circulation exit linkage of first pre-heater the cold commodity circulation entry of second pre-heater, the cold commodity circulation exit linkage of second pre-heater the evaporimeter the second pre-heater with be equipped with the feeding choke valve on the connecting pipeline between the evaporimeter.
Furthermore, a hot material inlet of the second preheater is connected with the fourth branch pipeline, and an essence product pump is arranged on the fourth branch pipeline; the hot material outflow port of the second preheater is connected with the essence storage tank, and an essence solution throttle valve is arranged on a connecting pipeline between the second preheater and the essence storage tank.
And the third branch pipeline is provided with an essence backflow throttling valve, and the fourth branch pipeline is provided with an essence product throttling valve.
Further, the bottom outlet of the first rectifying tower is connected with the cold fluid inlet of the first reboiler, and the cold fluid outlet of the first reboiler is connected with the bottom inlet of the first rectifying tower; and the outlet of the tower bottom of the second rectifying tower is connected with the cold fluid inlet of the second reboiler, and the outlet of the cold fluid of the second reboiler is connected with the inlet of the tower bottom of the second rectifying tower.
Specifically, a juice feeding pump and a juice feeding throttle valve are arranged on a connecting pipeline between a bottom discharge hole of the gas-liquid separator and the first rectifying tower.
Furthermore, a hot substance outlet of the first preheater is connected with a fruit juice product pipeline, and the fruit juice product pipeline is respectively connected with the first branch pipeline and the second branch pipeline; the fruit juice pump is arranged on the fruit juice product pipeline, the fruit juice backflow throttling valve is arranged on the first branch pipeline, and the fruit juice throttling valve is arranged on the second branch pipeline.
Further, the top gas outlet of the gas-liquid separator is connected with the evaporator.
Specifically, the first preheater and the second preheater both adopt plate preheaters; the first rectifying tower and the second rectifying tower adopt a packing rectifying tower, a plate rectifying tower or a mixed rectifying tower; the first vapor compressor and the second vapor compressor both adopt single-screw compressors or centrifugal compressors.
Specifically, the evaporator, the first rectifying tower and the second rectifying tower are respectively provided with an electric heater inside.
(III) advantageous effects
The technical scheme of the invention has the following advantages:
according to the integrated system for fruit juice concentration and essence recovery, the evaporator, the first rectifying tower, the second rectifying tower, the first steam compressor, the second steam compressor, the gas-liquid separator, the first reboiler, the second reboiler, the first preheater and the second preheater are arranged, heat pump evaporation and rectification are combined, condensate at the bottom of the evaporator and steam at the top of the tower are fully utilized, latent heat of secondary steam is fully utilized, latent heat is recovered, and heat efficiency is improved.
The integrated system for concentrating the fruit juice and recovering the essence, disclosed by the invention, has the advantages of simple structure and reasonable design, retains the original advantages of a heat pump system, does not need a boiler or raw steam, and obtains the essence with high concentration by combining evaporation and rectification, so that the cost is greatly saved, and the energy-saving economy, integrity, rationality and flexibility of the technology for concentrating the fruit juice and recovering the essence are further improved.
Drawings
FIG. 1 is a schematic diagram of an integrated system for concentrating fruit juice and recovering essence according to an embodiment of the present invention.
In the figure: 1: an evaporator; 2: a first rectification column; 3: a second rectification column; 4: a first vapor compressor; 5: a second vapor compressor; 6: a gas-liquid separator; 7: a first reboiler; 8: a second reboiler; 9: a feed pipe; 10: a raw material feed pump; 11: a first preheater; 12: a second preheater; 13: a feed throttle valve; 14: a condensate pump; 15: an essence backflow throttling valve; 16: an essence product throttling valve; 17: an essence product pump; 18: an essence solution throttle valve; 19: an essence storage tank; 20: a juice feed throttle valve; 21: a fruit juice hot stream throttling valve; 22: a juice product pump; 23: a fruit juice reflux throttle valve; 24: a fruit juice product throttling valve; 26: a fruit juice storage tank; 27: a juice feed pump.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. All other embodiments, which can be obtained by a person skilled in the art without any inventive step based on the embodiments of the present invention, are within the scope of the present invention.
As shown in fig. 1, the integrated system for fruit juice concentration and essence recovery provided by the embodiment of the present invention includes an evaporator 1, a first rectifying tower 2, a second rectifying tower 3, a first vapor compressor 4, a second vapor compressor 5, a gas-liquid separator 6, a first reboiler 7, a second reboiler 8, a first preheater 11, and a second preheater 12.
The bottom discharge hole of the evaporator 1 is connected with the gas-liquid separator 6, and the bottom discharge hole of the gas-liquid separator 6 is connected with the first rectifying tower 2.
The top steam outlet of the first rectifying tower 2 is connected to the inlet of the second steam compressor 5, the outlet of the second steam compressor 5 is connected to the hot material inlet of the second reboiler 8, the hot material outlet of the second reboiler 8 is connected to the hot material inlet of the first preheater 11, and the hot material outlet of the first preheater 11 is correspondingly connected to the reflux inlet of the first rectifying tower 2 and the juice storage tank 26 through a first branch pipeline and a second branch pipeline, respectively.
The top secondary steam outlet of the evaporator 1 is connected with the inlet of the first steam compressor 4, the outlet of the first steam compressor 4 is connected with the hot substance inlet of the first reboiler 7, the hot substance outlet of the first reboiler 7 is connected with the feed inlet of the second rectifying tower 3, the top steam outlet of the second rectifying tower 3 is connected with the steam inlet of the evaporator 1, and the condensate outlet of the evaporator 1 is correspondingly connected with the reflux inlet of the second rectifying tower 3 and the essence storage tank 19 through a third branch pipeline and a fourth branch pipeline respectively.
In the present invention, after the top steam of the evaporator 1 is heated and pressurized by the first steam compressor 4, the enthalpy of the steam is increased, and the steam with increased enthalpy enters the first reboiler 7 to heat the tower bottom liquid of the first rectifying tower 2, so as to recycle the potential energy of the top steam of the evaporator 1. Meanwhile, after the temperature and the pressure of the top steam of the first rectifying tower 2 are raised and pressurized by the second steam compressor 5, the enthalpy of the steam is improved, the steam with the improved enthalpy enters the second reboiler 8 and is used for heating the tower bottoms of the second rectifying tower 3, and therefore the potential energy of the top steam of the first rectifying tower 2 is recycled. The tower top steam of the second rectifying tower 3 is introduced into the evaporator 1 and used for heating and evaporating the feed liquid in the evaporator 1, so that the purposes of evaporation and rectification are realized by means of system self-circulation without external steam generation.
Further, the system of the present invention further includes a feeding pipe 9 and a raw material feeding pump 10 disposed on the feeding pipe 9, wherein the feeding pipe 9 is connected to a cold stream inlet of the first preheater 11, a cold stream outlet of the first preheater 11 is connected to a cold stream inlet of the second preheater 12, a cold stream outlet of the second preheater 12 is connected to the evaporator 1, and a feeding throttle valve 13 is disposed on a connecting pipeline between the second preheater 12 and the evaporator 1.
Further, the hot inflow port of the second preheater 12 is connected to the fourth branch pipeline, and the essence product pump 17 is disposed on the fourth branch pipeline. The hot material outflow port of the second preheater 12 is connected with the essence storage tank 19, and a essence solution throttle valve 18 is arranged on a connecting pipeline between the second preheater 12 and the essence storage tank 19.
The condensate outlet of the evaporator 1 is respectively connected with the third branch pipeline and the fourth branch pipeline through condensate pipelines, wherein a condensate pump 14 is arranged on the condensate pipeline, an essence backflow throttling valve 15 is arranged on the third branch pipeline, and an essence product throttling valve 16 is arranged on the fourth branch pipeline.
Further, the bottom outlet of the first rectification column 2 is connected to the cold stream inlet of the first reboiler 7, and the cold stream outlet of the first reboiler 7 is connected to the bottom inlet of the first rectification column 2. The outlet of the tower bottom of the second rectifying tower 3 is connected with the cold fluid inlet of the second reboiler 8, and the outlet of the cold fluid of the second reboiler 8 is connected with the inlet of the tower bottom of the second rectifying tower 3.
Specifically, a juice feed pump 27 and a juice feed throttle valve 20 are provided on a connection line between the bottom discharge port of the gas-liquid separator 6 and the first rectifying tower 2.
Specifically, the hot material outlet of the second reboiler 8 is connected to the hot material inlet of the first preheater 11 through a hot material flow line, and a syrup hot material flow throttle valve 21 is provided in the hot material flow line. The hot material outflow port of the first preheater 11 is connected with a fruit juice product pipeline, and the fruit juice product pipeline is respectively connected with the first branch pipeline and the second branch pipeline. Wherein be equipped with juice product pump 22 on the juice product pipeline, be equipped with juice backward flow choke valve 23 on the first branch pipeline, be equipped with juice product choke valve 24 on the second branch pipeline.
Specifically, the top gas outlet of the gas-liquid separator 6 is connected to the evaporator 1.
More specifically, the first preheater 11 and the second preheater 12 may employ a plate preheater. The first rectifying tower 2 and the second rectifying tower 3 can adopt a packing rectifying tower, a plate rectifying tower or a mixed rectifying tower. The first vapor compressor 4 and the second vapor compressor 5 may employ a single screw compressor or a centrifugal compressor.
More specifically, the evaporator 1, the first rectifying tower 2 and the second rectifying tower 3 are respectively provided with an electric heater inside to supplement heat to the system, but the heat can also be supplemented by directly adding supplementary steam.
In addition, the system of the invention can adopt an industrial personal computer and a PLC to form an MVR series real-time monitoring center, and collects the state signals of various sensors in real time through software programming, thereby automatically controlling the rotating speed of a motor, closing and adjusting a valve, controlling and adjusting the flow rate and the flow of liquid, temperature and pressure and the like, and leading the system to work to reach a dynamic balance state. Meanwhile, the system of the invention also has the functions of automatic alarm, automatic parameter recording and report providing.
The fruit juice concentration and essence recovery integrated system provided by the embodiment of the invention has the following working principle:
through the raw material liquid of inlet pipe 9 input, pass through earlier first preheater 11 heats back reentrant heating in the second preheater 12, raw material liquid preheats twice and then gets into carry out evaporation treatment in the evaporimeter 1, the warp steam after evaporimeter 1 evaporation passes through top steam outlet and gets into first steam compressor 4, steam is in behind the intensification pressurization in the first steam compressor 4, improved the enthalpy of steam, the steam that is improved the enthalpy gets into in the first reboiler 7 in with the tower cauldron liquid of first rectifying column 2 output carries out the heat transfer, get into after the heat transfer carry out the rectification in the second rectifying column 3.
The concentrated solution after the steam treatment in the evaporator 1 is fed into the gas-liquid separator 6 together with the feed material for gas-liquid separation, the concentrated solution output from the bottom outlet of the gas-liquid separator 6 is fed into the first rectifying tower 2 for rectification, the steam generated by the rectification in the first rectifying tower 2 is fed into the second steam compressor 5 through the top steam outlet of the first rectifying tower 2, the steam is heated and pressurized in the second steam compressor 5, the enthalpy of the steam is increased, the steam with the increased enthalpy enters the second reboiler 8, the steam exchanges heat with the tower bottom liquid output from the second rectifying tower 3 in the second reboiler 8, the steam enters the first preheater 11 after the heat exchange and is used as a heat source for heating the raw material liquid, and a part of the cooled condensate flows back into the first rectifying tower 2 through the first branch pipeline, another portion flows through the second branch line as product to the juice tank 26 for collection.
And the top steam outlet of the second rectifying tower 3 enters the evaporator 1 to be used as an evaporation heat source during the evaporation treatment of the feed liquid, one part of the cooled condensate liquid flows back to the second rectifying tower 3 through the first branch pipeline, the other part of the cooled condensate liquid is used as a product and then is injected into the second preheater 12 through the second branch pipeline to preheat the feed, and then the product flows into the essence storage tank 19 to be collected.
In conclusion, the juice concentration and essence recovery integrated system disclosed by the invention combines the heat pump evaporation and rectification, so that the condensate at the bottom of the evaporator and the steam at the top of the tower are fully utilized, the latent heat of the secondary steam is fully utilized, the latent heat is recovered, and the heat efficiency is improved.
The integrated system for concentrating the fruit juice and recovering the essence has the advantages of simple structure and reasonable design, does not need a boiler or raw steam while keeping the original advantages of a heat pump system, can obtain the essence with high concentration by combining evaporation and rectification, greatly saves the cost, and further improves the energy-saving economy, integrity, rationality and flexibility of the technology for concentrating the fruit juice and recovering the essence.
Finally, it should be noted that: the above examples are only intended to illustrate the technical solution of the present invention, but not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.
Claims (10)
1. The utility model provides a concentrated and essence recovery integration system of fruit juice which characterized in that: the system comprises an evaporator (1), a first rectifying tower (2), a second rectifying tower (3), a first steam compressor (4), a second steam compressor (5), a gas-liquid separator (6), a first reboiler (7), a second reboiler (8), a first preheater (11) and a second preheater (12);
a bottom discharge hole of the evaporator (1) is connected with the gas-liquid separator (6), and a bottom discharge hole of the gas-liquid separator (6) is connected with the first rectifying tower (2);
the top steam outlet of the first rectifying tower (2) is connected with the inlet of the second steam compressor (5), the outlet of the second steam compressor (5) is connected with the hot material flow inlet of the second reboiler (8), the hot material flow outlet of the second reboiler (8) is connected with the hot material flow inlet of the first preheater (11), and the hot material flow outlet of the first preheater (11) is correspondingly connected with the reflux inlet of the first rectifying tower (2) and the juice storage tank (26) through a first branch pipeline and a second branch pipeline respectively;
the top secondary steam outlet of the evaporator (1) is connected with the inlet of the first steam compressor (4), the outlet of the first steam compressor (4) is connected with the hot substance inflow port of the first reboiler (7), the hot substance outflow port of the first reboiler (7) is connected with the feeding port of the second rectifying tower (3), the top steam outlet of the second rectifying tower (3) is connected with the steam inlet of the evaporator (1), and the condensate outlet of the evaporator (1) is correspondingly connected with the reflux inlet and the condensate storage tank (19) of the second rectifying tower (3) through a third branch pipeline and a fourth branch pipeline respectively.
2. The integrated juice concentration and flavor recovery system according to claim 1, wherein: still include inlet pipe (9) and set up raw materials charge pump (10) on inlet pipe (9), wherein inlet pipe (9) are connected the cold commodity circulation entry of first preheater (11), the cold commodity circulation exit linkage of first preheater (11) the cold commodity circulation entry of second preheater (12), the cold commodity circulation exit linkage of second preheater (12) evaporimeter (1) second preheater (12) with be equipped with on the connecting line between evaporimeter (1) and feed throttle valve (13).
3. The integrated juice concentration and flavor recovery system according to claim 1, wherein: a hot material inlet of the second preheater (12) is connected with the fourth branch pipeline, and an essence product pump (17) is arranged on the fourth branch pipeline; the hot material outflow port of the second preheater (12) is connected with the essence storage tank (19), and an essence solution throttle valve (18) is arranged on a connecting pipeline between the second preheater (12) and the essence storage tank (19).
4. The integrated juice concentration and flavor recovery system according to claim 1, wherein: and an essence backflow throttling valve (15) is arranged on the third branch pipeline, and an essence product throttling valve (16) is arranged on the fourth branch pipeline.
5. The integrated juice concentration and flavor recovery system according to claim 1, wherein: the bottom outlet of the first rectifying tower (2) is connected with the cold fluid inlet of the first reboiler (7), and the cold fluid outlet of the first reboiler (7) is connected with the bottom inlet of the first rectifying tower (2); the bottom outlet of the second rectifying tower (3) is connected with the cold fluid inlet of the second reboiler (8), and the cold fluid outlet of the second reboiler (8) is connected with the bottom inlet of the second rectifying tower (3).
6. The integrated juice concentration and flavor recovery system according to claim 1, wherein: a fruit juice feeding pump (27) and a fruit juice feeding throttle valve (20) are arranged on a connecting pipeline between a bottom discharge hole of the gas-liquid separator (6) and the first rectifying tower (2).
7. The integrated juice concentration and flavor recovery system according to claim 1, wherein: the hot substance outlet of the first preheater (11) is connected with a fruit juice product pipeline, and the fruit juice product pipeline is respectively connected with the first branch pipeline and the second branch pipeline; the fruit juice pump is characterized in that a fruit juice pump (22) is arranged on the fruit juice product pipeline, a fruit juice backflow throttling valve (23) is arranged on the first branch pipeline, and a fruit juice throttling valve (24) is arranged on the second branch pipeline.
8. The integrated juice concentration and flavor recovery system according to claim 1, wherein: and a top gas outlet of the gas-liquid separator (6) is connected with the evaporator (1).
9. The integrated juice concentration and flavor recovery system according to any one of claims 1 to 8, wherein: the first preheater (11) and the second preheater (12) both adopt plate preheaters; the first rectifying tower (2) and the second rectifying tower (3) both adopt a packing rectifying tower, a plate rectifying tower or a mixed rectifying tower; the first vapor compressor (4) and the second vapor compressor (5) both adopt single-screw compressors or centrifugal compressors.
10. The integrated juice concentration and flavor recovery system according to any one of claims 1 to 8, wherein: the evaporator (1), the first rectifying tower (2) and the second rectifying tower (3) are respectively internally provided with an electric heater.
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| CN201710590845.4A CN109276898B (en) | 2017-07-19 | 2017-07-19 | Integrated system for concentrating fruit juice and recovering essence |
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| CN201710590845.4A CN109276898B (en) | 2017-07-19 | 2017-07-19 | Integrated system for concentrating fruit juice and recovering essence |
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| CN109276898B true CN109276898B (en) | 2020-10-16 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110564440A (en) * | 2019-10-24 | 2019-12-13 | 重庆建峰工业集团有限公司 | BDO tar recovery system and BDO tar recovery process |
| CN112870746B (en) * | 2019-11-29 | 2022-07-22 | 中国科学院理化技术研究所 | MVR heat pump system for realizing integration of concentration, steam stripping and rectification |
| CN115364499A (en) * | 2022-08-16 | 2022-11-22 | 重庆上甲电子股份有限公司 | Hydroquinone production system and process capable of recycling steam |
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| US4783242A (en) * | 1986-05-22 | 1988-11-08 | The Dow Chemical Company | Distillation system and process |
| CN105363227A (en) * | 2015-12-02 | 2016-03-02 | 中国科学院理化技术研究所 | Mechanical vapor recompression system and mechanical vapor recompression method based on system |
| CN106237642A (en) * | 2015-06-04 | 2016-12-21 | 河北化大科技有限公司 | A kind of industrial process saves the technology of energy consumption |
| CN206081667U (en) * | 2016-09-06 | 2017-04-12 | 甘肃蓝科石化高新装备股份有限公司 | MVR distillation plant |
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| US4783242A (en) * | 1986-05-22 | 1988-11-08 | The Dow Chemical Company | Distillation system and process |
| CN106237642A (en) * | 2015-06-04 | 2016-12-21 | 河北化大科技有限公司 | A kind of industrial process saves the technology of energy consumption |
| CN105363227A (en) * | 2015-12-02 | 2016-03-02 | 中国科学院理化技术研究所 | Mechanical vapor recompression system and mechanical vapor recompression method based on system |
| CN206081667U (en) * | 2016-09-06 | 2017-04-12 | 甘肃蓝科石化高新装备股份有限公司 | MVR distillation plant |
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