CN111375218B - Molasses concentrating device and using method and process thereof - Google Patents
Molasses concentrating device and using method and process thereof Download PDFInfo
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- CN111375218B CN111375218B CN202010238060.2A CN202010238060A CN111375218B CN 111375218 B CN111375218 B CN 111375218B CN 202010238060 A CN202010238060 A CN 202010238060A CN 111375218 B CN111375218 B CN 111375218B
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- 235000013379 molasses Nutrition 0.000 title claims abstract description 158
- 238000000034 method Methods 0.000 title claims abstract description 56
- 238000001704 evaporation Methods 0.000 claims abstract description 249
- 230000008020 evaporation Effects 0.000 claims abstract description 244
- 108090000623 proteins and genes Proteins 0.000 claims abstract description 34
- 102000004169 proteins and genes Human genes 0.000 claims abstract description 34
- 238000001035 drying Methods 0.000 claims abstract description 17
- 239000011552 falling film Substances 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims description 85
- 238000000926 separation method Methods 0.000 claims description 24
- 238000003860 storage Methods 0.000 claims description 15
- 239000000203 mixture Substances 0.000 claims description 13
- 238000010992 reflux Methods 0.000 claims description 12
- 238000002156 mixing Methods 0.000 claims description 8
- 230000007774 longterm Effects 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 abstract description 15
- 235000018102 proteins Nutrition 0.000 description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 25
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 23
- 238000004140 cleaning Methods 0.000 description 14
- 108010073771 Soybean Proteins Proteins 0.000 description 9
- 239000012141 concentrate Substances 0.000 description 9
- 235000019710 soybean protein Nutrition 0.000 description 9
- 238000009826 distribution Methods 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
- 230000002035 prolonged effect Effects 0.000 description 4
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000004088 simulation Methods 0.000 description 3
- 235000010469 Glycine max Nutrition 0.000 description 2
- 244000068988 Glycine max Species 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 235000019764 Soybean Meal Nutrition 0.000 description 1
- 230000001934 delay Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 239000004455 soybean meal Substances 0.000 description 1
- 210000003437 trachea Anatomy 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/26—Multiple-effect evaporating
-
- 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
- A23L29/00—Foods or foodstuffs containing additives; Preparation or treatment thereof
- A23L29/30—Foods or foodstuffs containing additives; Preparation or treatment thereof containing carbohydrate syrups; containing sugars; containing sugar alcohols, e.g. xylitol; containing starch hydrolysates, e.g. dextrin
-
- 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
- A23L5/00—Preparation or treatment of foods or foodstuffs, in general; Food or foodstuffs obtained thereby; Materials therefor
- A23L5/51—Concentration
-
- 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
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
- A23V2002/00—Food compositions, function of food ingredients or processes for food or foodstuffs
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- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Nutrition Science (AREA)
- Engineering & Computer Science (AREA)
- Food Science & Technology (AREA)
- Polymers & Plastics (AREA)
- Molecular Biology (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a molasses evaporation and concentration device and a using method and a process thereof, wherein the molasses evaporation and concentration device comprises a first evaporation unit, a second evaporation unit, a third evaporation unit and a fourth evaporation unit; the first evaporation unit takes the secondary steam generated by the second evaporation unit as a heat source, the second evaporation unit takes the secondary steam generated by the third evaporation unit as a heat source, the third evaporation unit takes the secondary steam generated by the fourth evaporation unit as a heat source, and the fourth evaporation unit takes the secondary steam generated in the wet protein drying process as a heat source; the evaporators of the first evaporation unit, the second evaporation unit, the third evaporation unit and the fourth evaporation unit are all tubular falling film evaporators; the molasses gelatinization wall-hanging phenomenon is obviously reduced, the equipment utilization rate is improved, the production cost of an enterprise is greatly reduced, and greater economic benefit is brought to the enterprise.
Description
Technical Field
The invention relates to the technical field of molasses evaporative concentration, in particular to a molasses evaporative concentration process for preparing soybean protein concentrate by an alcohol method, and specifically relates to a molasses concentration device and a use method and a process thereof.
Background
In the process for preparing the soybean protein concentrate by the mainstream alcohol method, five working procedures of soybean meal leaching, wet protein drying, molasses evaporation concentration, secondary steam condensation, tail gas recovery and the like are involved, wherein: the wet protein drying process and the molasses evaporating and concentrating process are two high energy consumption processes. The wet protein drying process adopts a dryer dividing wall heating mode to dry and remove ethanol and water contained in solid materials, and secondary steam generated by drying is directly sent to a condenser for condensation; the molasses evaporation and concentration process adopts a single-effect evaporation process at present, generally, three tube-array evaporators are adopted firstly for gradual concentration, a stripping tower is used for recovering ethanol in the molasses, four evaporation units are heated by water vapor, and secondary steam generated by evaporation is directly sent to a condenser for condensation; the total water vapor consumption of the process for preparing the soybean protein concentrate by the main alcohol method is about 2500kg/t protein, wherein the water vapor consumption of a wet protein drying procedure is about 700kg/t protein, and the water vapor consumption of molasses evaporation concentration is about 1600kg/t protein; the steam consumption of molasses evaporation concentration is 64% of the total steam consumption of soybean protein concentrate.
In the process of molasses evaporative concentration, molasses has high viscosity and is very easy to stick to the inner wall of an evaporation tube, and simultaneously, the molasses is very easy to gelatinize and hang on the wall due to the fact that steam is adopted for heating, the temperature difference between the inside and the outside of the evaporation tube wall is 70-90 ℃, the effective surface area of mass transfer and heat transfer of the evaporation tube is reduced, the evaporation tube needs to be shut down at intervals of 1-2 months for cleaning, and the shut down is needed for at least 48 hours for one-time cleaning; the shutdown cleaning not only increases various consumption, but also delays production and increases the production cost of enterprises.
The molasses evaporation process in the production process for preparing the concentrated protein by the mainstream alcohol method has high energy consumption, and the machine is stopped for 48 hours for cleaning an evaporation pipe within 1-2 months, thereby wasting precious energy, increasing the production cost of enterprises, increasing the burden of upstream and downstream enterprises and influencing the popularization and application of the alcohol method concentrated protein. In the research of preparing the soybean protein concentrate by the alcohol method, the water vapor consumption is reduced, the shutdown time caused by cleaning is reduced, and the production cost is further reduced, thus the method becomes a common pursuit target of researchers.
Disclosure of Invention
In order to overcome the problems in the prior art, the invention provides a molasses concentrating device for a molasses evaporating and concentrating process in a process for preparing soybean protein concentrate by an alcohol method, and a using method and a process thereof.
The invention is realized by the following three technical schemes.
The invention provides a molasses concentrating device, which comprises a first evaporation unit and a second evaporation unit and is realized by the following three technical schemes.
The first aspect of the invention provides a molasses evaporative concentration device, which comprises a first evaporation unit, a second evaporation unit, a third evaporation unit and a fourth evaporation unit; the first evaporation unit takes the secondary steam generated by the second evaporation unit as a heat source, the second evaporation unit takes the secondary steam generated by the third evaporation unit as a heat source, the third evaporation unit takes the secondary steam generated by the fourth evaporation unit as a heat source, and the fourth evaporation unit takes the secondary steam generated in the wet protein drying process as a heat source; the evaporators of the first evaporation unit, the second evaporation unit, the third evaporation unit and the fourth evaporation unit are all tube type falling film evaporators.
As a further improvement of the technical scheme, the tubular falling film evaporator comprises a shell, and a liquid inlet pipe, an air inlet pipe, an evaporation pipe, a lower tube plate, a lower box body, an upper box body, a liquid distributor, an upper tube plate, a baffle plate, a non-condensable gas pipe and a gas-liquid mixing pipe which are arranged on the shell; the liquid inlet pipe is arranged on one side of the upper part of the shell and is communicated with the upper box body, and the liquid distributor is arranged on the lower part of the upper box body and is positioned on the upper part of the upper tube plate; the gas inlet pipe is arranged on one side of the shell and positioned at the lower part of the upper tube plate, the lower tube plate is arranged at the lower part of the shell, the lower box body is arranged at the bottom of the shell and positioned at the lower part of the lower tube plate, the baffle plates are provided with a plurality of baffle plates, the baffle plates are uniformly distributed between the upper tube plate and the lower tube plate, the non-condensable gas pipe is arranged on one side of the shell and positioned at the upper part of the lower tube plate, the gas-liquid mixing pipe is arranged on one side of the shell and connected with the lower box body, the upper part of the evaporation pipe is connected with the upper tube plate, and the lower part of the evaporation pipe is connected with the lower tube plate; the top of the shell is also provided with a circulating pipe, and the circulating pipe is connected with the upper tank body.
As a further improvement of the above technical solution, the first evaporation unit comprises a feeding pump, a first evaporator a, a first evaporator B, a first flash tank and a first circulating pump; the feed pump is connected with the first evaporator A, a shell of the first evaporator A is communicated with a shell of the first evaporator B through an intermediate connecting pipe to form a series structure, and a tube side of the first evaporator A is communicated with a tube side of the first evaporator B through an intermediate connecting pipe to form a series structure; in order to achieve the purpose that the first evaporator A and the second evaporator B share the first flash tank and make the layout of the first flash tank more compact, the tube pass of the first evaporator B is communicated with the first flash tank through a middle connecting pipe to form a series structure; one side of the first circulating pump is communicated with the first evaporator B, and the other side of the first circulating pump is connected with the first evaporator A and the second evaporation unit respectively.
As a further improvement of the above technical solution, the second evaporation unit comprises a second evaporator a, a second evaporator B, a flash tank ii and a circulation pump ii; the second evaporator A is connected with the first circulating pump, a shell of the second evaporator A is communicated with a shell of the second evaporator B through a middle connecting pipe to form a series structure, and a tube side of the second evaporator A is communicated with a tube side of the second evaporator B through the middle connecting pipe to form a series structure; in order to realize the purpose that two evaporators of the second evaporator A and the second evaporator B share one flash box II and make the layout of the flash box II more compact, the tube pass of the second evaporator B is communicated with the flash box II through a middle connecting pipe to form a series structure; one side of the second circulating pump is communicated with the second evaporator B, and the other side of the second circulating pump is connected with the second evaporator A and the third evaporation unit respectively.
As a further improvement of the above technical solution, the third evaporation unit includes a third evaporator a, a third evaporator B, a third flash tank and a third circulation pump; the third evaporator A is connected with the second circulating pump, a shell of the third evaporator A is communicated with a shell of the third evaporator B through a middle connecting pipe to form a series structure, and a tube side of the third evaporator A is communicated with a tube side of the third evaporator B through the middle connecting pipe to form a series structure; in order to achieve the purpose that the third evaporator A, the third evaporator B and the two evaporators share one flash box III and enable the layout of the flash box III to be more compact, the tube pass of the third evaporator B is communicated with the flash box III through a middle connecting pipe and forms a series structure; one side of the third circulating pump is communicated with the third evaporator B, and the other side of the third circulating pump is connected with the third evaporator A and the fourth evaporation unit respectively.
As a further improvement of the above technical solution, the fourth evaporation unit comprises a fourth evaporator a, a fourth evaporator B, a flash tank four and a circulation pump four; the fourth evaporator A is connected with the third circulating pump, a shell of the fourth evaporator A is communicated with a shell of the fourth evaporator B through a middle connecting pipe to form a series structure, and a tube side of the fourth evaporator A is communicated with a tube side of the fourth evaporator B through the middle connecting pipe to form a series structure; in order to achieve the purpose that the fourth evaporator A, the fourth evaporator B and the two evaporators share one flash box IV and enable the layout of the flash box IV to be more compact, the tube pass of the fourth evaporator B is communicated with the flash box IV through a middle connecting pipe to form a series structure; one side of the fourth circulating pump is communicated with the fourth evaporator B, and the other side of the fourth circulating pump is connected with the fourth evaporator A and the storage tank respectively.
The second aspect of the invention provides a molasses evaporative concentration device using method, molasses enters a first evaporator from a feeding pump for evaporative concentration, the evaporative heat source of the first evaporator is secondary steam generated by a second evaporator, molasses gas-liquid after being evaporated by the first evaporator is subjected to gas-liquid separation through a flash tank I, the generated secondary steam is condensed by a condenser, one part of molasses is subjected to forced circulation by a circulating pump I, and the other part of molasses enters the second evaporator for evaporative concentration; the second evaporator evaporation heat source is secondary steam generated by a third evaporator, gas-liquid separation is carried out on molasses gas-liquid evaporated by the second evaporator through a flash tank II, the generated secondary steam is used as a heat source of the first evaporator, one part of molasses is forcibly circulated by a circulating pump II, and the other part of liquid enters the third evaporator for evaporation and concentration; the heat source of the third evaporator is secondary steam generated by the fourth evaporator. The gas-liquid separation of the molasses gas-liquid after the evaporation of the third evaporator is carried out through the flash tank III, the generated secondary steam is used as the heat source of the second evaporator, one part of the molasses gas-liquid is forcibly circulated by the circulating pump III, and the other part of the molasses gas-liquid enters the fourth evaporator for evaporation and concentration; the heat source of the fourth evaporator is secondary steam generated in the wet protein drying process. The molasses gas-liquid after the evaporation of the fourth evaporator is subjected to gas-liquid separation through the flash tank IV, the generated secondary steam is used as a heat source of the third evaporator, one part of the molasses is subjected to forced circulation through the circulating pump IV, and the other part of the molasses enters the storage tank for long-term storage.
The third aspect of the invention provides a molasses evaporation and concentration energy-saving process, which comprises the following steps:
s1, conveying the molasses with the concentration of 8-12% and the temperature of 45-55 ℃ into a first evaporation unit through a feeding pump;
s2, feeding the molasses with the concentration of 12-15% and the temperature of 55-65 ℃ into a second evaporation unit through a first circulating pump;
s3, feeding the molasses with the concentration of 20-30% and the temperature of 65-75 ℃ into a third evaporation unit through a second circulating pump;
s4, feeding the molasses with the concentration of 35-45% and the temperature of 75-85 ℃ into a fourth evaporation unit through a third circulating pump.
As a further improvement of the technical scheme, in step S1, the molasses firstly enters a first evaporator for evaporation concentration, an evaporation heat source is secondary steam with the temperature of 65-75 ℃ generated by a second evaporator, the evaporation temperature is 55-65 ℃, the vacuum degree is-0.08-0.10 MPa, and a gas-liquid mixture generated by evaporation enters a first flash tank for gas-liquid separation; secondary steam generated by the evaporation of the first evaporator is condensed in a condenser; forcibly refluxing 70-80% of the concentrated molasses to the first evaporator by using a first circulating pump for circulating evaporation, and allowing the remaining 20-30% of the molasses with the concentration of 12-15% to enter a second evaporation unit for continuous concentration;
s2, feeding the molasses with the concentration of 12-15% and the temperature of 55-65 ℃ into a second evaporation unit through a first circulating pump; the molasses enters a second evaporator for evaporation and concentration, and an evaporation heat source is secondary steam of 75-85 ℃ generated by evaporation of a third evaporator; the evaporation temperature is 65-75 ℃, the vacuum degree is-0.70-0.09 MPa, and a gas-liquid mixture generated by evaporation enters a flash tank II for gas-liquid separation; secondary steam generated by evaporation of the second evaporator is used as a heat source of the first evaporator and enters the shell side of the first evaporator; forcibly refluxing 70-80% of the concentrated molasses to a second evaporator by a second circulating pump for circulating evaporation, and allowing the remaining 20-30% of the molasses with the concentration of 20-30% to enter a third evaporation unit for continuous concentration;
as a further improvement of the technical scheme, in step S3, the molasses with the temperature of 65-75 ℃ and the concentration of 20-30% is sent to a third evaporation unit by a second circulating pump; the molasses enters a third evaporator for evaporation and concentration, and an evaporation heat source is secondary steam of 85-95 ℃ generated by evaporation of a fourth evaporator; the evaporation temperature is 75-85 ℃, the vacuum degree is-0.06-0.08 MPa, and a gas-liquid mixture generated by evaporation enters a flash tank III for gas-liquid separation; the secondary steam generated by the third evaporator is used as a heat source of the second evaporator and enters the shell side of the second evaporator; forcibly refluxing 70-80% of the concentrated molasses to a third evaporator by a third circulating pump for circulating evaporation, and allowing the remaining 20-30% of the molasses with the concentration of 35-45% to enter a fourth evaporation unit to adjust the concentration of the molasses;
in step S4, feeding the molasses with the concentration of 35-45% and the temperature of 75-85 ℃ into a fourth evaporation unit through a third circulating pump; the molasses enters a fourth evaporator for evaporation concentration, the heat source of evaporation is secondary steam at 90-110 ℃ generated in the wet protein drying process, the evaporation temperature is 85-95 ℃, the vacuum degree is-0.05-0.07 MPa, and a gas-liquid mixture generated by evaporation enters a flash tank IV for gas-liquid separation; secondary steam generated by the fourth evaporator is used as a heat source of the third evaporator and enters the shell side of the third evaporator; and forcibly refluxing 40-60% of the concentrated molasses to the fourth evaporator by a circulating pump for circulating evaporation, and conveying the residual 40-60% of molasses with the concentration of 55-60% to a molasses storage tank by a conveying pump for long-term storage.
The method has the advantages that the water vapor consumption is greatly reduced, the water vapor consumption of molasses evaporation concentration is about 90-110 kg/t protein, and the total water vapor consumption of alcohol method concentration protein is about 900-1100 kg/t protein. Compared with the main stream alcohol method for preparing the soybean protein concentrate, the total water vapor consumption is reduced by 60 percent; meanwhile, as the evaporator adopts a tubular falling film evaporator, each section adopts a combined liquid distributor, and each evaporator adopts a forced external circulation process, the molasses gelatinization wall-hanging phenomenon is obviously reduced, the cleaning time interval is prolonged to 6 months, and the shutdown time of each time is not more than 24 hours; the energy consumption is greatly reduced, the downtime is reduced, the equipment utilization rate is improved, the production cost of an enterprise is greatly reduced, and greater economic benefits are brought to the enterprise.
According to the technical scheme, the invention has the following advantages:
the high-temperature heat source of the evaporator shell is discharged from the non-condensable gas pipe after fully exchanging heat with molasses in the evaporating pipe through the plurality of baffle plates in the shell, and the gas enters the next procedure, so that the uniform liquid distribution of the evaporating pipe can be ensured, the molasses and the high-temperature heat source fully exchange heat, the heat efficiency is improved, and the molasses is not easy to be pasted and hung on the wall.
By adjusting the heat distribution of each process, secondary steam generated in the wet protein drying process is used as a molasses evaporative concentration heat source, and a four-effect evaporation technology is adopted, so that molasses evaporative concentration can be carried out without water vapor, the problem of high water vapor consumption in the preparation of the soybean concentrated protein by the alcohol method is solved, the total water vapor consumption of the alcohol method concentrated protein is greatly reduced, the cleaning time interval of an evaporation pipe is prolonged, the cleaning time is shortened, the downtime caused by cleaning the evaporation pipe is reduced, and the production cost is reduced.
The method has the advantages that the water vapor consumption is greatly reduced, the water vapor consumption of molasses evaporation concentration is about 90-110 kg/t protein, and the total water vapor consumption of alcohol method concentration protein is about 900-1100 kg/t protein. Compared with the main stream alcohol method for preparing the soybean protein concentrate, the total water vapor consumption is reduced by 60 percent; meanwhile, as the evaporator adopts a tubular falling film evaporator, each section adopts a combined liquid distributor, and each evaporator adopts a forced external circulation process, the molasses gelatinization wall-hanging phenomenon is obviously reduced, the cleaning time interval is prolonged to 6 months, and the shutdown time of each time is not more than 24 hours; the energy consumption is greatly reduced, the downtime is reduced, the equipment utilization rate is improved, the production cost of an enterprise is greatly reduced, and greater economic benefits are brought to the enterprise.
Drawings
In order to more clearly illustrate the technical solution of the present invention, the drawings used in the description will be briefly introduced, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained based on these drawings without creative efforts.
FIG. 1 is a schematic view of the evaporator of the present invention;
FIG. 2 is a three-dimensional simulation of the evaporator of the present invention;
FIG. 3 is a three-dimensional view of the upper tube box of the evaporator of the present invention;
FIG. 4 is a three-dimensional simulation of an overflow weir-type distributor of the present invention;
FIG. 5 is a three-dimensional simulation of a porous flow pattern distributor according to the present invention;
FIG. 6 is a schematic diagram of the molasses evaporation and concentration energy-saving process of the invention.
In the attached drawings, 1, a fourth evaporator A; 2. a fourth evaporator B; 3. a flash tank IV; 4. a fourth circulating pump; 5. a third evaporator A; 6. a third evaporator B; 7. a third flash tank; 8. a third circulating pump; 9. a second evaporator A; 10. a second evaporator B; 11. a second flash tank; 12. a second circulating pump; 13. a first evaporator A; 14. a first evaporator B; 15. a first flash box; 16. a first circulating pump; 17. a feed pump; 18. a gas-liquid mixing pipe; 19. a circulation pipe; 20. a liquid inlet pipe; 21. a steam inlet pipe; 22. an evaporation tube; 23. a housing; 24. a lower tube plate; 25. a lower box body; 26. an upper box body; 27. an overflow weir-type distributor; 28. a porous flow pattern distributor; 29. an upper tube sheet; 30. a baffle plate; 31. does not condense the trachea.
Detailed Description
In order to make the objects, features and advantages of the present invention more obvious and understandable, the technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings in the present embodiment, and it is apparent that the embodiments described below are only a part of embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the scope of protection of this patent.
Referring to fig. 1 to 5, an aspect of the present invention provides a tubular falling film evaporator, which comprises a shell 23, and a liquid inlet pipe 20, an air inlet pipe 21, an evaporation pipe 22, a lower pipe plate 24, a lower box 25, an upper box 26, a liquid distributor, an upper pipe plate 29, a baffle plate 30, a noncondensable air pipe 31 and a gas-liquid mixing pipe 18 which are arranged on the shell 23; the liquid inlet pipe 20 is arranged on one side of the upper part of the shell 23 and is communicated with the upper box body 26, and the liquid distributor is arranged on the lower part of the upper box body 26 and is positioned on the upper part of the upper tube plate 29; the gas inlet pipe 21 is arranged on one side of the shell 23 and is positioned at the lower part of the upper tube plate 29, the lower tube plate 24 is arranged at the lower part of the shell 23, the lower box body 25 is arranged at the bottom of the shell 23 and is positioned at the lower part of the lower tube plate 24, the baffle plates 30 are provided with a plurality of baffle plates 30, the baffle plates 30 are uniformly distributed between the upper tube plate 29 and the lower tube plate 24, the noncondensable gas pipe 31 is arranged on one side of the shell 23 and is positioned at the upper part of the lower tube plate 24, the gas-liquid mixing pipe 18 is arranged on one side of the shell 23 and is connected with the lower box body 25, the upper part of the evaporation pipe 22 is connected with the upper tube plate 29, and the lower part of the evaporation pipe 22 is connected with the lower tube plate 24; the top of the shell 23 is also provided with a circulating pipe 19, and the circulating pipe 19 is connected with the upper tank 26.
In the above embodiment, the liquid distributor includes the weir-type distributor 27 and the porous flow-type distributor 28; the overflow weir type distributor 27 is disposed at a lower portion of the upper tank 26, the perforated flow type distributor 28 is disposed at a lower portion of the overflow weir type distributor 27, and the upper tube plate 29 is disposed at a lower portion of the perforated flow type distributor 28.
When the tubular falling-film evaporator is used, molasses serving as a raw material enters an upper box body 26 of the evaporator from a liquid inlet pipe 20, is distributed by an overflow weir-type distributor 27, falls into a porous flow-type distributor 28, is distributed again, finally falls onto an upper tube plate 29 of the evaporation tube, and uniformly flows into the inner surface of the evaporation tube 22 to be evaporated; the molasses on the inner surface of the evaporation tube 22 and the high-temperature heat source entering the evaporator shell 23 from the steam inlet tube 21 of the evaporator carry out partition wall heat exchange, and the ethanol and the water in the molasses absorb heat and are vaporized to form steam; the vapor-liquid mixture formed by evaporation enters the next process from the vapor-liquid mixing pipe 18 of the evaporator lower box 25; the lower box body 25 can also temporarily store part of molasses, and part of molasses is sent to the upper box body 26 of the evaporator through the circulating pump 6 through the circulating pipe 19 to be forcibly circulated and evaporated; the high-temperature heat source entering the evaporator shell 23 is discharged from the non-condensable gas pipe 31 after fully exchanging heat with molasses in the evaporation pipe 22 through the plurality of baffle plates 30 in the shell 23, and the gas enters the next procedure, so that the uniform liquid distribution of the evaporation pipe 22 can be ensured, the molasses and the high-temperature heat source fully exchange heat, the heat efficiency is improved, and the molasses is not easy to gelatinize and is not easy to hang on the wall.
Referring to fig. 6, a second aspect of the present invention provides a molasses evaporative concentration apparatus, comprising a first evaporation unit, a second evaporation unit, a third evaporation unit and a fourth evaporation unit; the first evaporation unit takes the secondary steam generated by the second evaporation unit as a heat source, the second evaporation unit takes the secondary steam generated by the third evaporation unit as a heat source, the third evaporation unit takes the secondary steam generated by the fourth evaporation unit as a heat source, and the fourth evaporation unit takes the secondary steam generated in the wet protein drying process as a heat source; the evaporators of the first evaporation unit, the second evaporation unit, the third evaporation unit and the fourth evaporation unit are all tube type falling film evaporators.
The first evaporation unit comprises a feed pump 17, a first evaporator A13, a first evaporator B14, a first flash tank 15 and a first circulating pump 16; the feed pump 17 is connected with the first evaporator A13, the shell of the first evaporator A13 is communicated with the shell of the first evaporator B14 through an intermediate connecting pipe and forms a series structure, and the tube side of the first evaporator A13 is communicated with the tube side of the first evaporator B14 through an intermediate connecting pipe and forms a series structure; in order to realize the purpose that the first evaporator A13 and the first evaporator B14 share one flash box I15 and make the layout more compact, the tube side of the first evaporator B14 is communicated with the flash box I15 through an intermediate connecting pipe to form a series structure; one side of the first circulation pump 16 is communicated with the first evaporator B14, and the other side of the first circulation pump 16 is connected with the first evaporator a13 and the second evaporation unit, respectively.
The second evaporation unit comprises a second evaporator A9, a second evaporator B10, a second flash tank 11 and a second circulating pump 12; the second evaporator A9 is connected with the first circulation pump 16, the shell of the second evaporator A9 is communicated with the shell of the second evaporator B10 through an intermediate connecting pipe and forms a series structure, and the tube side of the second evaporator A9 is communicated with the tube side of the second evaporator B10 through an intermediate connecting pipe and forms a series structure; in order to realize the purpose that two evaporators of the second evaporator A9 and the second evaporator B10 share the second flash box 11, the layout of the second flash box is more compact, and the tube side of the second evaporator B10 is communicated with the second flash box 11 through an intermediate connecting pipe to form a series structure; one side of the second circulation pump 12 is communicated with the second evaporator B9, and the other side of the second circulation pump 12 is connected with the second evaporator a9 and the third evaporation unit, respectively.
The third evaporation unit comprises a third evaporator A5, a third evaporator B6, a flash tank III 7 and a circulating pump III 8; the third evaporator A5 is connected with the second circulating pump 12, the shell of the third evaporator A5 is communicated with the shell of the third evaporator B6 through an intermediate connecting pipe to form a series structure, and the tube side of the third evaporator A5 is communicated with the tube side of the third evaporator B6 through an intermediate connecting pipe to form a series structure; in order to realize the purpose that the third evaporator A5, the third evaporator B6 and the two evaporators share one flash box III 7 and make the layout more compact, the tube side of the third evaporator B6 is communicated with the flash box III 7 through an intermediate connecting pipe and forms a series structure; one side of the circulating pump III 8 is communicated with the third evaporator B6, and the other side of the circulating pump III 8 is respectively connected with the third evaporator A5 and the fourth evaporation unit.
The fourth evaporation unit comprises a fourth evaporator A1, a fourth evaporator B2, a flash tank four 3 and a circulation pump four 4; the four evaporator A1 is connected with the circulating pump III 8, the shell of the fourth evaporator A1 is communicated with the shell of the fourth evaporator B2 through an intermediate connecting pipe and forms a series structure, and the tube side of the fourth evaporator A1 is communicated with the tube side of the fourth evaporator B2 through an intermediate connecting pipe and forms a series structure; in order to realize the purpose that the fourth evaporator A1, the fourth evaporator B2 and the two evaporators share one flash box four 3, the layout of the flash box four 3 is more compact, and the tube side of the fourth evaporator B2 is communicated with the flash box four 3 through an intermediate connecting pipe to form a series structure; one side of the circulation pump four 4 is communicated with the fourth evaporator B2, and the other side of the circulation pump four 4 is respectively connected with the fourth evaporator A1 and the storage tank.
The molasses evaporating and concentrating device ensures that the molasses and a high-temperature heat source fully exchange heat, and improves the heat efficiency; the temperature difference between the high-temperature heat source and the molasses is small, the liquid distribution of the evaporation tube is uniform, and the molasses is not easy to be pasted and hung on the wall.
The third aspect of the invention provides a molasses evaporative concentration device using method, molasses enters a first evaporator from a feeding pump 17 for evaporative concentration, the evaporative heat source of the first evaporator is secondary steam generated by a second evaporator, molasses gas-liquid after being evaporated by the first evaporator is subjected to gas-liquid separation through a flash tank I15, the generated secondary steam is condensed by a condenser, one part of molasses is subjected to forced circulation by a circulating pump I16, and the other part of molasses enters the second evaporator for evaporative concentration; the evaporation heat source of the second evaporator is secondary steam generated by the third evaporator, gas-liquid separation is carried out on molasses gas-liquid evaporated by the second evaporator through a flash tank II 11, the generated secondary steam is used as a heat source of the first evaporator, one part of molasses is forcibly circulated by a circulating pump II 12, and the other part of liquid enters the third evaporator for evaporation and concentration; the heat source of the third evaporator is secondary steam generated by the fourth evaporator. The molasses gas-liquid after the evaporation of the third evaporator is subjected to gas-liquid separation through a flash tank III 7, the generated secondary steam is used as a heat source of the second evaporator, one part of the molasses is subjected to forced circulation through a circulating pump III 8, and the other part of the molasses enters a fourth evaporator for evaporation and concentration; the heat source of the fourth evaporator is secondary steam generated in the wet protein drying process. The gas-liquid separation is carried out on the molasses gas-liquid after the evaporation of the fourth evaporator through the flash tank IV 3, the generated secondary steam is used as a heat source of the third evaporator, one part of the molasses is forcibly circulated by the circulating pump IV 4, and the other part of the molasses enters the storage tank for long-term storage.
The molasses evaporative concentration device using method adjusts the heat distribution of each process, utilizes the secondary steam generated in the wet protein drying process as the molasses evaporative concentration heat source, adopts the four-effect evaporation technology, can carry out molasses evaporative concentration without water vapor, solves the problem of high water vapor consumption of the alcohol method prepared soybean concentrated protein, greatly reduces the total water vapor consumption of the alcohol method concentrated protein, prolongs the cleaning time interval of an evaporation pipe, reduces the cleaning time, further reduces the shutdown time caused by cleaning the evaporation pipe, and reduces the production cost.
The fourth aspect of the invention provides a molasses evaporation and concentration energy-saving process, which comprises the following steps:
s1, conveying the molasses with the concentration of 8-12% and the temperature of 45-55 ℃ into a first evaporation unit through a feeding pump; the molasses firstly enters a first evaporator for evaporation concentration, an evaporation heat source is secondary steam at 65-75 ℃ generated by a second evaporator, the evaporation temperature is 55-65 ℃, the vacuum degree is-0.08-0.10 MPa, and a gas-liquid mixture generated by evaporation enters a flash tank I for gas-liquid separation; secondary steam generated by the evaporation of the first evaporator is condensed in a condenser; forcibly refluxing 70-80% of the concentrated molasses to the first evaporator by using a first circulating pump for circulating evaporation, and allowing the remaining 20-30% of the molasses with the concentration of 12-15% to enter a second evaporation unit for continuous concentration;
s2, feeding the molasses with the concentration of 12-15% and the temperature of 55-65 ℃ into a second evaporation unit through a first circulating pump; the molasses enters a second evaporator for evaporation and concentration, and an evaporation heat source is secondary steam of 75-85 ℃ generated by evaporation of a third evaporator; the evaporation temperature is 65-75 ℃, the vacuum degree is-0.70-0.09 MPa, and a gas-liquid mixture generated by evaporation enters a flash tank II for gas-liquid separation; secondary steam generated by evaporation of the second evaporator is used as a heat source of the first evaporator and enters the shell side of the first evaporator; forcibly refluxing 70-80% of the concentrated molasses to a second evaporator by a second circulating pump for circulating evaporation, and allowing the remaining 20-30% of the molasses with the concentration of 20-30% to enter a third evaporation unit for continuous concentration;
s3, feeding the molasses with the concentration of 20-30% and the temperature of 65-75 ℃ into a third evaporation unit through a second circulating pump; the molasses enters a third evaporator for evaporation and concentration, and an evaporation heat source is secondary steam of 85-95 ℃ generated by evaporation of a fourth evaporator; the evaporation temperature is 75-85 ℃, the vacuum degree is-0.06-0.08 MPa, and a gas-liquid mixture generated by evaporation enters a flash tank III for gas-liquid separation; the secondary steam generated by the third evaporator is used as a heat source of the second evaporator and enters the shell side of the second evaporator; forcibly refluxing 70-80% of the concentrated molasses to a third evaporator by a third circulating pump for circulating evaporation, and allowing the remaining 20-30% of the molasses with the concentration of 35-45% to enter a fourth evaporation unit to adjust the concentration of the molasses;
s4, feeding the molasses with the concentration of 35-45% and the temperature of 75-85 ℃ into a fourth evaporation unit through a third circulating pump; the molasses enters a fourth evaporator for evaporation concentration, the heat source of evaporation is secondary steam at 90-110 ℃ generated in the wet protein drying process, the evaporation temperature is 85-95 ℃, the vacuum degree is-0.05-0.07 MPa, and a gas-liquid mixture generated by evaporation enters a flash tank IV for gas-liquid separation; secondary steam generated by the fourth evaporator is used as a heat source of the third evaporator and enters the shell side of the third evaporator; and forcibly refluxing 40-60% of the concentrated molasses to the fourth evaporator by a circulating pump for circulating evaporation, and conveying the residual 40-60% of molasses with the concentration of 55-60% to a molasses storage tank by a conveying pump for long-term storage.
The method has the advantages that the water vapor consumption is greatly reduced, the water vapor consumption of molasses evaporation concentration is about 90-110 kg/t protein, and the total water vapor consumption of alcohol method concentration protein is about 900-1100 kg/t protein. Compared with the main stream alcohol method for preparing the soybean protein concentrate, the total water vapor consumption is reduced by 60 percent; meanwhile, as the evaporator adopts a tubular falling film evaporator, each section adopts a combined liquid distributor, and each evaporator adopts a forced external circulation process, the molasses gelatinization wall-hanging phenomenon is obviously reduced, the cleaning time interval is prolonged to 6 months, and the shutdown time of each time is not more than 24 hours; the energy consumption is greatly reduced, the downtime is reduced, the equipment utilization rate is improved, the production cost of an enterprise is greatly reduced, and greater economic benefits are brought to the enterprise.
The embodiments in the present description are described in a progressive manner, each embodiment focuses on differences from other embodiments, and the same and similar parts among the embodiments are referred to each other.
The terms "first," "second," "third," "fourth," and the like in the description and in the claims, as well as in the drawings, if any, are used for distinguishing between similar elements and not necessarily for describing a particular sequential or chronological order. It is to be understood that the data so used is interchangeable under appropriate circumstances such that the embodiments of the invention described herein are capable of operation in sequences other than those illustrated or described herein. Furthermore, the terms "comprising" and "having," as well as any variations thereof, are intended to cover non-exclusive inclusions.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (8)
1. The molasses evaporation and concentration device is characterized by comprising a first evaporation unit, a second evaporation unit, a third evaporation unit and a fourth evaporation unit; the first evaporation unit takes the secondary steam generated by the second evaporation unit as a heat source, the second evaporation unit takes the secondary steam generated by the third evaporation unit as a heat source, the third evaporation unit takes the secondary steam generated by the fourth evaporation unit as a heat source, and the fourth evaporation unit takes the secondary steam generated in the wet protein drying process as a heat source; the evaporators of the first evaporation unit, the second evaporation unit, the third evaporation unit and the fourth evaporation unit are all tubular falling film evaporators; the first evaporation unit comprises a feeding pump, a first evaporator A, a first evaporator B, a first flash tank and a first circulating pump; the feed pump is connected with the first evaporator A, a shell of the first evaporator A is communicated with a shell of the first evaporator B through an intermediate connecting pipe to form a series structure, and a tube side of the first evaporator A is communicated with a tube side of the first evaporator B through an intermediate connecting pipe to form a series structure; in order to achieve the purpose that the first evaporator A and the second evaporator B share the first flash tank and make the layout of the first flash tank more compact, the tube pass of the first evaporator B is communicated with the first flash tank through a middle connecting pipe to form a series structure; one side of the first circulating pump is communicated with the first evaporator B, and the other side of the first circulating pump is connected with the first evaporator A and the second evaporation unit respectively.
2. The molasses evaporative concentration device according to claim 1, wherein the tubular falling-film evaporator comprises a shell, and a liquid inlet pipe, a gas inlet pipe, an evaporation pipe, a lower pipe plate, a lower box body, an upper box body, a liquid distributor, an upper pipe plate, a baffle plate, a non-condensable gas pipe and a gas-liquid mixing pipe which are arranged on the shell; the liquid inlet pipe is arranged on one side of the upper part of the shell and is communicated with the upper box body, and the liquid distributor is arranged on the lower part of the upper box body and is positioned on the upper part of the upper tube plate; the gas inlet pipe is arranged on one side of the shell and positioned at the lower part of the upper tube plate, the lower tube plate is arranged at the lower part of the shell, the lower box body is arranged at the bottom of the shell and positioned at the lower part of the lower tube plate, the baffle plates are provided with a plurality of baffle plates, the baffle plates are uniformly distributed between the upper tube plate and the lower tube plate, the non-condensable gas pipe is arranged on one side of the shell and positioned at the upper part of the lower tube plate, the gas-liquid mixing pipe is arranged on one side of the shell and connected with the lower box body, the upper part of the evaporation pipe is connected with the upper tube plate, and the lower part of the evaporation pipe is connected with the lower tube plate; the top of the shell is also provided with a circulating pipe, and the circulating pipe is connected with the upper tank body.
3. The molasses evaporative concentration device according to claim 1, wherein the second evaporation unit comprises a second evaporator A, a second evaporator B, a second flash tank and a second circulating pump; the second evaporator A is connected with the first circulating pump, a shell of the second evaporator A is communicated with a shell of the second evaporator B through a middle connecting pipe to form a series structure, and a tube side of the second evaporator A is communicated with a tube side of the second evaporator B through the middle connecting pipe to form a series structure; in order to realize the purpose that two evaporators of the second evaporator A and the second evaporator B share one flash box II and make the layout of the flash box II more compact, the tube pass of the second evaporator B is communicated with the flash box II through a middle connecting pipe to form a series structure; one side of the second circulating pump is communicated with the second evaporator B, and the other side of the second circulating pump is connected with the second evaporator A and the third evaporation unit respectively.
4. The molasses evaporative concentration device according to claim 1, wherein the third evaporation unit comprises a third evaporator A, a third evaporator B, a flash tank III and a circulating pump III; the third evaporator A is connected with the second circulating pump, a shell of the third evaporator A is communicated with a shell of the third evaporator B through a middle connecting pipe to form a series structure, and a tube side of the third evaporator A is communicated with a tube side of the third evaporator B through the middle connecting pipe to form a series structure; in order to achieve the purpose that the third evaporator A, the third evaporator B and the two evaporators share one flash box III and enable the layout of the flash box III to be more compact, the tube pass of the third evaporator B is communicated with the flash box III through a middle connecting pipe and forms a series structure; one side of the third circulating pump is communicated with the third evaporator B, and the other side of the third circulating pump is connected with the third evaporator A and the fourth evaporation unit respectively.
5. The molasses evaporative concentration device according to claim 1, wherein the fourth evaporation unit comprises a fourth evaporator A, a fourth evaporator B, a flash tank IV and a circulating pump IV; the fourth evaporator A is connected with the third circulating pump, a shell of the fourth evaporator A is communicated with a shell of the fourth evaporator B through a middle connecting pipe to form a series structure, and a tube side of the fourth evaporator A is communicated with a tube side of the fourth evaporator B through the middle connecting pipe to form a series structure; in order to achieve the purpose that the fourth evaporator A, the fourth evaporator B and the two evaporators share one flash box IV and enable the layout of the flash box IV to be more compact, the tube pass of the fourth evaporator B is communicated with the flash box IV through a middle connecting pipe to form a series structure; one side of the fourth circulating pump is communicated with the fourth evaporator B, and the other side of the fourth circulating pump is connected with the fourth evaporator A and the storage tank respectively.
6. A method for using the molasses evaporative concentration device according to any one of claims 1-5, characterized in that molasses enters a first evaporator for evaporative concentration by a feed pump, the evaporative heat source of the first evaporator is secondary steam generated by a second evaporator, the molasses gas-liquid after evaporation in the first evaporator is subjected to gas-liquid separation by a flash tank I, the generated secondary steam is condensed in a condenser, one part of the molasses is subjected to forced circulation by a circulating pump I, and the other part of the molasses enters the second evaporator for evaporative concentration; the second evaporator evaporation heat source is secondary steam generated by a third evaporator, gas-liquid separation is carried out on molasses gas-liquid evaporated by the second evaporator through a flash tank II, the generated secondary steam is used as a heat source of the first evaporator, one part of molasses is forcibly circulated by a circulating pump II, and the other part of liquid enters the third evaporator for evaporation and concentration; the heat source of the third evaporator is secondary steam generated by the fourth evaporator; the gas-liquid separation of the molasses gas-liquid after the evaporation of the third evaporator is carried out through the flash tank III, the generated secondary steam is used as the heat source of the second evaporator, one part of the molasses gas-liquid is forcibly circulated by the circulating pump III, and the other part of the molasses gas-liquid enters the fourth evaporator for evaporation and concentration; the heat source of the fourth evaporator is secondary steam generated in the wet protein drying process; the molasses gas-liquid after the evaporation of the fourth evaporator is subjected to gas-liquid separation through the flash tank IV, the generated secondary steam is used as a heat source of the third evaporator, one part of the molasses is subjected to forced circulation through the circulating pump IV, and the other part of the molasses enters the storage tank for long-term storage.
7. An energy-saving process for molasses evaporation and concentration is characterized by comprising the following steps:
s1: conveying the molasses with the concentration of 8-12% and the temperature of 45-55 ℃ into a first evaporation unit through a feed pump;
s2: feeding the molasses with the concentration of 12-15% and the temperature of 55-65 ℃ into a second evaporation unit through a first circulating pump;
s3: feeding the molasses with the concentration of 20-30% and the temperature of 65-75 ℃ into a third evaporation unit through a second circulating pump;
s4: feeding the molasses with the concentration of 35-45% and the temperature of 75-85 ℃ into a fourth evaporation unit through a third circulating pump;
in step S1, the molasses firstly enters a first evaporator for evaporation concentration, an evaporation heat source is secondary steam at 65-75 ℃ generated by a second evaporator, the evaporation temperature is 55-65 ℃, the vacuum degree is-0.08-0.10 MPa, and a gas-liquid mixture generated by evaporation enters a first flash tank for gas-liquid separation; secondary steam generated by the evaporation of the first evaporator is condensed in a condenser; forcibly refluxing 70-80% of the concentrated molasses to the first evaporator by using a first circulating pump for circulating evaporation, and allowing the remaining 20-30% of the molasses with the concentration of 12-15% to enter a second evaporation unit for continuous concentration;
s2: feeding the molasses with the concentration of 12-15% and the temperature of 55-65 ℃ into a second evaporation unit through a first circulating pump; the molasses enters a second evaporator for evaporation and concentration, and an evaporation heat source is secondary steam of 75-85 ℃ generated by evaporation of a third evaporator; the evaporation temperature is 65-75 ℃, the vacuum degree is-0.70-0.09 MPa, and a gas-liquid mixture generated by evaporation enters a flash tank II for gas-liquid separation; secondary steam generated by evaporation of the second evaporator is used as a heat source of the first evaporator and enters the shell side of the first evaporator; and forcibly refluxing 70-80% of the concentrated molasses by a second circulating pump to a second evaporator for circulating evaporation, and allowing the remaining 20-30% of the molasses with the concentration of 20-30% to enter a third evaporation unit for continuous concentration.
8. The molasses evaporative concentration energy-saving process according to claim 7, characterized in that in step S3, molasses with the concentration of 20-30% and the temperature of 65-75 ℃ is sent to a third evaporation unit through a second circulating pump; the molasses enters a third evaporator for evaporation and concentration, and an evaporation heat source is secondary steam of 85-95 ℃ generated by evaporation of a fourth evaporator; the evaporation temperature is 75-85 ℃, the vacuum degree is-0.06-0.08 MPa, and a gas-liquid mixture generated by evaporation enters a flash tank III for gas-liquid separation; the secondary steam generated by the third evaporator is used as a heat source of the second evaporator and enters the shell side of the second evaporator; forcibly refluxing 70-80% of the concentrated molasses to a third evaporator by a third circulating pump for circulating evaporation, and allowing the remaining 20-30% of the molasses with the concentration of 35-45% to enter a fourth evaporation unit to adjust the concentration of the molasses;
in step S4, feeding the molasses with the concentration of 35-45% and the temperature of 75-85 ℃ into a fourth evaporation unit through a third circulating pump; the molasses enters a fourth evaporator for evaporation concentration, the heat source of evaporation is secondary steam at 90-110 ℃ generated in the wet protein drying process, the evaporation temperature is 85-95 ℃, the vacuum degree is-0.05-0.07 MPa, and a gas-liquid mixture generated by evaporation enters a flash tank IV for gas-liquid separation; secondary steam generated by the fourth evaporator is used as a heat source of the third evaporator and enters the shell side of the third evaporator; and forcibly refluxing 40-60% of the concentrated molasses to the fourth evaporator by a circulating pump for circulating evaporation, and conveying the residual 40-60% of molasses with the concentration of 55-60% to a molasses storage tank by a conveying pump for long-term storage.
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| CN102641603A (en) * | 2012-03-11 | 2012-08-22 | 甘肃蓝科石化高新装备股份有限公司 | Plate-type evaporator device with mechanical vapor compressor |
| CN104645645A (en) * | 2013-11-25 | 2015-05-27 | 武汉市金德戈糖业有限公司 | High fructose syrup quadruple-effect concentration evaporator |
| CN205740829U (en) * | 2016-02-05 | 2016-11-30 | 山东华鲁恒升化工股份有限公司 | Extend methylamine catalyst and use the catalyst application apparatus in cycle |
| CN206198721U (en) * | 2016-08-11 | 2017-05-31 | 兆光生物工程(邹平)有限公司 | Multiple-effect falling film evaporator |
| CN206045444U (en) * | 2016-08-31 | 2017-03-29 | 苏州乔发环保科技股份有限公司 | Multi-effect evaporator based on MVR |
| CN206304378U (en) * | 2016-10-26 | 2017-07-07 | 山东百盛生物科技有限公司 | The energy-conservation MVR evaporators that a kind of vapor recompression is utilized |
| CN207347439U (en) * | 2017-09-29 | 2018-05-11 | 湖北瑞邦生物科技有限公司 | A kind of collagen peptide enrichment facility |
| CN110237554A (en) * | 2019-07-08 | 2019-09-17 | 中国科学院理化技术研究所 | A kind of falling film evaporation system and method |
| CN111359240A (en) * | 2020-03-30 | 2020-07-03 | 山东凯斯达机械制造有限公司 | Tubular falling film evaporator, concentration device and using method and process of concentration device |
| CN211885427U (en) * | 2020-03-30 | 2020-11-10 | 山东凯斯达机械制造有限公司 | Tubular falling film evaporator and tubular falling film evaporation device |
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