CN220736214U - Beer lees filtrate evaporation concentration system - Google Patents
Beer lees filtrate evaporation concentration system Download PDFInfo
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- CN220736214U CN220736214U CN202322495589.4U CN202322495589U CN220736214U CN 220736214 U CN220736214 U CN 220736214U CN 202322495589 U CN202322495589 U CN 202322495589U CN 220736214 U CN220736214 U CN 220736214U
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- 239000000706 filtrate Substances 0.000 title claims abstract description 41
- 238000001704 evaporation Methods 0.000 title claims abstract description 25
- 230000008020 evaporation Effects 0.000 title claims abstract description 25
- 235000013405 beer Nutrition 0.000 title claims abstract description 14
- 239000007788 liquid Substances 0.000 claims abstract description 52
- 238000001035 drying Methods 0.000 claims abstract description 20
- 239000002002 slurry Substances 0.000 claims abstract description 10
- 238000005406 washing Methods 0.000 claims abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 31
- 239000003513 alkali Substances 0.000 claims description 22
- 239000010865 sewage Substances 0.000 claims description 10
- 238000004140 cleaning Methods 0.000 claims description 7
- 238000000605 extraction Methods 0.000 claims description 4
- 238000011010 flushing procedure Methods 0.000 claims description 4
- 239000007789 gas Substances 0.000 abstract description 10
- 230000000694 effects Effects 0.000 abstract description 9
- 235000015097 nutrients Nutrition 0.000 abstract description 5
- 239000002918 waste heat Substances 0.000 abstract description 5
- 239000000126 substance Substances 0.000 abstract description 4
- 238000003912 environmental pollution Methods 0.000 abstract description 2
- 235000013339 cereals Nutrition 0.000 description 10
- 239000000243 solution Substances 0.000 description 10
- 240000008042 Zea mays Species 0.000 description 3
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 3
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 3
- 235000005822 corn Nutrition 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000000855 fermentation Methods 0.000 description 2
- 230000004151 fermentation Effects 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 230000009291 secondary effect Effects 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- 240000005979 Hordeum vulgare Species 0.000 description 1
- 235000007340 Hordeum vulgare Nutrition 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 150000001413 amino acids Chemical class 0.000 description 1
- 239000003674 animal food additive Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 235000014633 carbohydrates Nutrition 0.000 description 1
- 150000001720 carbohydrates Chemical class 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000000050 nutritive effect Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses a beer lees filtrate evaporation concentration system, which comprises one-effect to four-effect heat exchangers, wherein each effect is matched with a separator, and each two-effect heat exchanger comprises a first two-effect heat exchanger and a second two-effect heat exchanger; the outlet of the filtrate pump is connected with the tube side inlet of the four-effect heat exchanger, the four-effect liquid outlet tube is connected with the three-effect circulating tube, the three-effect liquid outlet tube is connected with the second two-effect circulating tube, the second two-effect liquid outlet tube is connected with the first two-effect circulating tube, the first two-effect liquid outlet tube is connected with the one-effect circulating tube, and the one-effect liquid outlet tube is connected with the inlet of the thick slurry tank; the tube bundle drying secondary steam is connected to the shell side of the first-effect heat exchanger, the flash steam outlet of the first-effect separator is connected to the shell side inlet of the first-effect heat exchanger, the tube bundle drying washing tail gas pipe is connected to the shell side of the second-effect heat exchanger, the flash steam outlet of the second-effect separator is connected to the shell side of the three-effect heat exchanger, and the three-effect flash steam is connected to the shell side of the four-effect heat exchanger. The utility model adopts waste heat evaporation to recycle the nutrient substances in the filtrate, and reduces environmental pollution.
Description
Technical Field
The utility model relates to a beer lees filtrate evaporation concentration system, and belongs to the technical field of evaporation concentration systems.
Background
Beer lees are a main byproduct of the beer industry, and are residues obtained by taking barley as a raw material and extracting soluble carbohydrates in seeds through fermentation. About 1/4 ton of brewer's grains are produced per 1 ton of beer produced, the annual yield of brewer's grains in our country has reached 1000 more than ten thousand tons, and is increasing. The brewery grain contains abundant proteins, amino acids and microelements, is widely used in cultivation and is also utilized in other aspects.
The beer grains have high water content (80 percent of water content) and high fluidity, and cannot be piled up and stored on the ground. Extrusion dewatering is necessary prior to fermentation, however dewatering produces a filtrate that contains a variety of soluble nutrients. Because the concentration of the organic matters is high (concentration: 5-7%), the direct discharge of the filtrate can pollute the environment. If the sewage is treated in a sewage plant, the sewage treatment cost is increased, and 5-7% of nutrient substances are wasted.
The Chinese patent publication No. CN 106509946B discloses a production system of corn pulp fiber, which utilizes waste heat to evaporate and concentrate corn pulp. The system has the following problems: 1. tail gas of the tube bundle dryer after purification is mixed with secondary steam generated by condensate water of the tube bundle dryer and then enters an evaporator, and the pure steam and the mixture of air and steam cannot be independently supplied to the evaporator for heating, so that the utilization rate of the pure steam is reduced;
2. tail gas of the tube bundle dryer after purification is not subjected to cascade utilization;
3. the corn steep liquor evaporator has high feeding concentration, low concentration after concentration and small concentration multiple, and is not suitable for concentration of brewery grain filtrate.
Disclosure of Invention
The utility model aims to overcome the problems in the prior art and provide a beer residue filtrate evaporation and concentration system which can be used as a feed additive after concentrating filtrate by using waste heat of beer residue drying, thereby avoiding environmental pollution and completely recovering all nutrient substances in the beer residue filtrate.
In order to solve the technical problems, the utility model relates to a brewery grain filtrate evaporation concentration system which comprises a filtrate tank, a first-effect heat exchanger, a second-effect heat exchanger, a third-effect heat exchanger and a fourth-effect heat exchanger, wherein the bottoms of the first-to-fourth-effect heat exchangers are correspondingly connected with first-to-fourth-effect separators, and the outlets of the bottoms of tube passes of the first-to-fourth-effect heat exchangers are respectively connected with the inlets of the tops of tube passes of the first-to-fourth-effect heat exchangers through first-effect circulating pumps and first-effect circulating pipes; the second-effect heat exchanger comprises a first second-effect heat exchanger and a second-effect heat exchanger;
the bottom outlet of the filtrate tank is connected with the inlet of the filtrate pump, the outlet of the filtrate pump is connected with the tube side inlet of the four-effect heat exchanger, the outlet of the four-effect circulating pump is connected with the three-effect circulating tube through the four-effect liquid outlet tube, the outlet of the three-effect circulating pump is connected with the second two-effect circulating tube through the three-effect liquid outlet tube, the outlet of the second two-effect circulating pump is connected with the first two-effect circulating tube through the second two-effect liquid outlet tube, the outlet of the first two-effect circulating pump is connected with the first two-effect circulating tube through the first two-effect liquid outlet tube, and the outlet of the first two-effect circulating pump is connected with the inlet of the thick slurry tank through the first two-effect liquid outlet tube G1;
the tube bundle drying secondary steam pipe is connected with the shell side inlet of the first-effect heat exchanger, the flash steam outlet of the first-effect separator is connected with the shell side inlet of the first-effect heat exchanger, the tube bundle drying washing tail gas pipe is connected with the shell side inlet of the second-effect heat exchanger, the flash steam outlets of the first-effect separator and the second-effect separator are connected with the shell side inlet of the three-effect heat exchanger, and the flash steam outlet of the three-effect separator is connected with the shell side inlet of the four-effect heat exchanger.
As an improvement of the utility model, the shell-side condensed water outlet of the first-effect heat exchanger is connected with the lower part of the shell side of the first-effect heat exchanger, the shell-side condensed water outlet of the first-effect heat exchanger is connected with the lower part of the shell side of the three-effect heat exchanger, the shell-side condensed water outlet of the three-effect heat exchanger is connected with the lower part of the shell side of the four-effect heat exchanger, and the shell-side condensed water outlet of the four-effect heat exchanger is connected with the inlet of the sewage condensed water tank.
As a further development of the utility model, the shell side condensate outlet of the second secondary heat exchanger is connected to the inlet of the flushing water tank.
As a further development of the utility model, a tube bundle drying condensate is connected to the lower shell side of the first two-effect heat exchanger.
As a further improvement of the utility model, shell side extraction openings of the first-effect heat exchanger, the second-effect heat exchanger, the three-effect heat exchanger and the four-effect heat exchanger are all connected with a shell side inlet of a condenser through an extraction tube, and a shell side outlet of the condenser is connected with a vacuum pump.
As a further improvement of the utility model, the flash vapor outlet of the four-effect separator is connected to the shell side inlet of the condenser.
As a further improvement of the utility model, the outlet of the alkali liquid tank is connected with the inlet of the alkali liquid pump, the outlet of the alkali liquid pump is connected with the cleaning ports of the various-effect separators and the thick slurry tank through alkali liquid cleaning pipes, and the one-effect circulating pipe is connected with the inlet of the alkali liquid tank through an alkali liquid return pipe.
Compared with the prior art, the utility model has the following beneficial effects: 1. the water content of the wet vinasse is extruded by adopting a wringing machine, so that the energy consumption of a drying system is reduced; taking secondary steam generated by tube bundle condensed water as one effect, wherein the secondary steam of the one effect is used for the first two effects; the purified tail gas of the tube bundle dryer is used for the second effect; secondary steam generated by the first secondary effect and the second secondary effect is used for three effects, so that the utilization rate of the secondary steam of the condensate water of the tube bundle dryer after flash evaporation is improved;
2. the tail gas of the purified tube bundle dryer firstly enters a preheater of a product dryer, the tail gas temperature of the tube bundle dryer after the preheater is used is 75 ℃, the relative humidity is 100%, and the higher latent heat is used as a second-effect heat source, so that the cascade utilization of waste heat is realized, and the waste heat utilization rate is improved;
3. the evaporation four-effect feeding, countercurrent circulation, one-effect discharging and one-effect forced circulation are adopted, so that the discharging viscosity is reduced, the flow speed of the heat exchange tube is improved, the scaling opportunity of the heat exchange tube is reduced, and high-multiple concentration and high-concentration discharging can be realized. The concentration of the brewery grain filtrate is about 5%, the brewery grain filtrate can be concentrated to 50% through four-effect evaporation, and the brewery grain filtrate is added into the fermented feed, so that not only is all nutrient substances in the filtrate recovered, but also the nutritive value of the fermented feed is improved.
Drawings
The utility model will now be described in further detail with reference to the drawings and the detailed description, which are provided for reference and illustration only and are not intended to limit the utility model.
FIG. 1 is a flow chart of a beer filtrate evaporative concentration system of the present utility model;
in the figure: r1, drying a secondary steam pipe by a pipe bundle; r2, drying a condensation water pipe by the pipe bundle; r3, drying and washing a tail gas pipe by the pipe bundle;
H1. a first-effect heat exchanger; h2a first two-effect heat exchanger; h2b a second-effect heat exchanger; H3. a three-effect heat exchanger; H4. a four-effect heat exchanger; H5. a condenser; p5. vacuum pump; C1. a water cooling tower;
s1, a first-effect separator; s2a, a first two-effect separator; s2b, a second-effect separator; s3, a three-effect separator; s4, a four-effect separator;
p1. a first-effect circulating pump; p2. a first two-way circulation pump; p2b a second-effect circulation pump; p3. a triple-effect circulating pump; p4. a four-effect circulation pump;
G1. a first-effect liquid outlet pipe; g2a first two-effect liquid outlet pipe; g2b. A second effect liquid outlet pipe; G3. a three-effect liquid outlet pipe; G4. a four-effect liquid outlet pipe;
t1, a filtrate tank; t1a. filtrate pump; t2, an alkali solution tank; t2a alkaline solution pump; t2b washing the tube with alkali solution; t2c alkali liquor return pipe; t3, concentrating the slurry tank; t3a thick stock pump; t4, a dirty condensate water tank; t4a sewage delivery pump; and T5, flushing the water tank.
Description of the embodiments
In the following description of the present utility model, the terms "upper", "lower", "front", "rear", "left", "right", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are merely for convenience in describing the present utility model and simplifying the description, and do not mean that the device must have a specific orientation.
The utility model is further described with reference to the following detailed drawings in order to make the technical means, the creation characteristics, the achievement of the purpose and the effect of the implementation of the utility model easy to understand.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this utility model belongs. The terminology used herein in the description of the utility model is for the purpose of describing particular embodiments only and is not intended to be limiting of the utility model.
As shown in fig. 1, the beer lees filtrate evaporation concentration system of the utility model comprises a filtrate tank T1, a first-effect heat exchanger H1, a second-effect heat exchanger, a third-effect heat exchanger H3 and a fourth-effect heat exchanger H4, wherein the second-effect heat exchanger comprises a first second-effect heat exchanger H2a and a second-effect heat exchanger H2b.
The bottom of the effective heat exchanger H1 is connected with an effective separator S1, and the outlet of the bottom of the tube side of the effective heat exchanger H1 is connected with the inlet of the top of the tube side of the effective heat exchanger H1 through an effective circulating pump P1 and an effective circulating tube.
The bottom of the first two-effect heat exchanger H2a is connected with a first two-effect separator S2a, and the outlet of the bottom of the tube side of the first two-effect heat exchanger H2a is connected with the inlet of the top of the tube side of the first two-effect heat exchanger H2a through a first two-effect circulating pump P2a and a first two-effect circulating tube.
The bottom of the second-effect heat exchanger H2b is connected with a second-effect separator S2b, the outlet at the bottom of the tube side of the second-effect heat exchanger H2b is connected with the inlet at the top of the tube side of the second-effect heat exchanger H2b through a second-effect circulating pump P2b and a second-effect circulating tube.
The bottom of the three-effect heat exchanger H3 is connected with a three-effect separator S3, and the outlet of the bottom of the tube side of the three-effect heat exchanger H3 is connected with the inlet of the top of the tube side of the three-effect heat exchanger H3 through a three-effect circulating pump P3 and a three-effect circulating tube.
The bottom of the four-effect heat exchanger H4 is connected with a four-effect separator S4, and the outlet of the bottom of the tube side of the four-effect heat exchanger H4 is connected with the inlet of the top of the tube side of the four-effect heat exchanger H4 through a four-effect circulating pump P4 and a four-effect circulating tube.
The bottom outlet of the filtrate tank T1 is connected with the inlet of a filtrate pump T1a, the outlet of the filtrate pump T1a is connected with the tube side inlet of a four-effect heat exchanger H4, the outlet of the four-effect circulating pump P4 is connected with a three-effect circulating tube through a four-effect liquid outlet tube G4, the outlet of the three-effect circulating pump P3 is connected with a second two-effect circulating tube through a three-effect liquid outlet tube G3, the outlet of the second two-effect circulating pump P2b is connected with a first two-effect circulating tube through a second two-effect liquid outlet tube G2b, the outlet of the first two-effect circulating pump P2a is connected with a first two-effect circulating tube through a first two-effect liquid outlet tube G2a, the outlet of the first two-effect circulating pump P1 is connected with the inlet of a thick slurry tank T3 through a first two-effect liquid outlet tube G1, and the outlet of the thick slurry tank T3 is connected with the inlet of the thick slurry pump T3a.
The 5%wt brewery grain filtrate enters the tube side of a four-effect heat exchanger H4, the four-effect circulation is maintained by a four-effect circulation pump P4, the four-effect concentrated solution enters a three-effect circulation system through a four-effect liquid outlet pipe G4, the three-effect circulation is maintained by a three-effect circulation pump P3, the three-effect concentrated solution enters a second two-effect circulation system through a three-effect liquid outlet pipe G3, the circulation is maintained by a second two-effect circulation pump P2b, the second two-effect concentrated solution enters a first two-effect circulation system through a second two-effect liquid outlet pipe G2b, the circulation is maintained by a first two-effect circulation pump P2a, the first two-effect concentrated solution enters a first-effect circulation system through a first two-effect liquid outlet pipe G2a, the concentration of the first-effect concentrated solution is increased to 45-50%, the first-effect concentrated solution is sent into a thick slurry tank T3 through a first-effect liquid outlet pipe G1, and the first-effect concentrated solution is sent out to feed for addition.
The tube bundle drying secondary steam tube R1 is connected with a shell side inlet of the first-effect heat exchanger H1, and a flash steam outlet of the first-effect separator S1 is connected with a shell side inlet of the first-effect heat exchanger H2 a; the tube bundle drying condensate pipe R2 is connected with the lower part of the shell side of the first two-effect heat exchanger H2a, and the shell side condensate outlet of the second two-effect heat exchanger H2b is connected with the inlet of the flushing water tank T5.
The temperature of secondary steam generated after flash evaporation of the steam condensate water discharged by tube bundle drying is up to 100 ℃, and the secondary steam enters a shell pass of a primary heat exchanger H1 through a tube bundle drying secondary steam tube R1 to carry out evaporation concentration on the primary concentrated solution with highest concentration; the flash steam with the temperature of 65 ℃ generated by the first-effect separator S1 enters a tube pass of the first two-effect heat exchanger H2a to carry out evaporation concentration on the first two-effect circulating liquid. The high-temperature condensate water at 100 ℃ after the tube bundle secondary steam flash evaporation enters the shell pass of the first two-effect heat exchanger H2a through the tube bundle drying condensate water pipe R2 to be subjected to flash evaporation, and the first two-effect circulating liquid is also subjected to evaporation concentration.
The tube bundle drying and washing tail gas tube R3 is connected with the shell side inlet of the second two-effect heat exchanger H2b, and flash steam outlets of the first two-effect separator S2a and the second two-effect separator S2b are connected with the shell side inlet of the three-effect heat exchanger H3. The tail gas of 75 ℃ after tube bundle drying enters the shell side of the second-effect heat exchanger H2b as a heat source, and flash steam of 55 ℃ of the first-effect separator S2a and the second-effect separator S2b are jointly used as the shell side heat source of the three-effect heat exchanger H3.
The flash steam outlet of the three-effect separator S3 is connected with the shell side inlet of the four-effect heat exchanger H4, and the flash steam at 50 ℃ of the three-effect separator S3 is used as a shell side heat source of the four-effect heat exchanger H4. The flash steam outlet of the four-effect separator S4 is also connected with the shell side inlet of the condenser H5, and the flash steam at 45 ℃ discharged by the four-effect separator S4 enters the condenser H5 for condensation.
The shell-side condensed water of the first-effect heat exchanger H1 enters the shell side of the first-effect heat exchanger H2a, the shell-side condensed water of the first-effect heat exchanger H2a enters the lower part of the shell side of the three-effect heat exchanger H3, the shell-side condensed water of the three-effect heat exchanger H3 enters the lower part of the shell side of the four-effect heat exchanger H4, the shell-side condensed water of the four-effect heat exchanger H4 enters the sewage condensate tank T4, and the sewage is sent to a sewage treatment station for treatment by the sewage delivery pump T4a.
The shell side extraction openings of the first-effect heat exchanger H1, the first-effect heat exchanger H2a, the second-effect heat exchanger H2b, the three-effect heat exchanger H3 and the four-effect heat exchanger H4 are connected with the shell side inlet of the condenser H5 through vacuumizing pipes, the shell side outlet of the condenser H5 is connected with the vacuum pump P5, and the tube side of the condenser H5 is provided with circulating cooling water by the cooling tower C1.
The outlet of the alkali liquid tank T2 is connected with the inlet of the alkali liquid pump T2a, the alkali liquid pump T2a sends alkali liquid for on-line cleaning into each effect separator through an alkali liquid cleaning pipe T2b and is connected with the cleaning port of the thick liquid tank T3, and the one-effect circulating pipe returns to the alkali liquid tank T2 through an alkali liquid return pipe T2c for circulation.
The foregoing description of the preferred embodiments of the present utility model illustrates and describes the basic principles, main features and advantages of the present utility model, and is not intended to limit the scope of the present utility model, as it should be understood by those skilled in the art that the present utility model is not limited to the above-described embodiments. In addition to the embodiments described above, other embodiments of the utility model are possible without departing from the spirit and scope of the utility model. The utility model also has various changes and improvements, and all technical schemes formed by adopting equivalent substitution or equivalent transformation fall within the protection scope of the utility model. The scope of the utility model is defined by the appended claims and equivalents thereof. The technical features of the present utility model that are not described may be implemented by or using the prior art, and are not described herein.
Claims (7)
1. A beer vinasse filtrate evaporation concentration system, includes the filtrate jar, its characterized in that: the device comprises a first-effect heat exchanger, a second-effect heat exchanger, a third-effect heat exchanger and a fourth-effect heat exchanger, wherein the bottoms of the first-to-fourth-effect heat exchangers are correspondingly connected with a first-to-fourth-effect separator, and the outlets of the bottoms of tube passes of the first-to-fourth-effect heat exchangers are respectively connected with the inlets of the tops of the tube passes of the first-to-fourth-effect heat exchangers through a first-to-fourth-effect circulating pump and a first-effect circulating tube; the second-effect heat exchanger comprises a first second-effect heat exchanger and a second-effect heat exchanger;
the bottom outlet of the filtrate tank is connected with the inlet of the filtrate pump, the outlet of the filtrate pump is connected with the tube side inlet of the four-effect heat exchanger, the outlet of the four-effect circulating pump is connected with the three-effect circulating tube through a four-effect liquid outlet tube, the outlet of the three-effect circulating pump is connected with the second two-effect circulating tube through a three-effect liquid outlet tube, the outlet of the second two-effect circulating pump is connected with the first two-effect circulating tube through the second two-effect liquid outlet tube, the outlet of the first two-effect circulating pump is connected with the first two-effect circulating tube through the first two-effect liquid outlet tube, and the outlet of the first two-effect circulating pump is connected with the inlet of the thick slurry tank through the first two-effect liquid outlet tube;
the tube bundle drying secondary steam pipe is connected with the shell side inlet of the first-effect heat exchanger, the flash steam outlet of the first-effect separator is connected with the shell side inlet of the first-effect heat exchanger, the tube bundle drying washing tail gas pipe is connected with the shell side inlet of the second-effect heat exchanger, the flash steam outlets of the first-effect separator and the second-effect separator are connected with the shell side inlet of the three-effect heat exchanger, and the flash steam outlet of the three-effect separator is connected with the shell side inlet of the four-effect heat exchanger.
2. The brewery grain filtrate evaporation and concentration system according to claim 1, wherein: the shell side condensate water outlet of the first-effect heat exchanger is connected with the lower part of the shell side of the first-effect heat exchanger, the shell side condensate water outlet of the first-effect heat exchanger is connected with the lower part of the shell side of the three-effect heat exchanger, the shell side condensate water outlet of the three-effect heat exchanger is connected with the lower part of the shell side of the four-effect heat exchanger, and the shell side condensate water outlet of the four-effect heat exchanger is connected with the inlet of the sewage condensate water tank.
3. The brewery grain filtrate evaporation and concentration system according to claim 2, wherein: and a shell side condensed water outlet of the second-effect heat exchanger is connected with an inlet of the flushing water tank.
4. The brewery grain filtrate evaporation and concentration system according to claim 2, wherein: the tube bundle drying condensate pipe is connected with the lower part of the shell side of the first two-effect heat exchanger.
5. The brewery grain filtrate evaporation and concentration system according to claim 1, wherein: the shell side extraction openings of the first-effect heat exchanger, the second-effect heat exchanger, the three-effect heat exchanger and the four-effect heat exchanger are all connected with the shell side inlet of the condenser through the vacuum pipe, and the shell side outlet of the condenser is connected with the vacuum pump.
6. The brewery grain filtrate evaporation and concentration system according to claim 5, wherein: the flash vapor outlet of the four-effect separator is connected with the shell side inlet of the condenser.
7. The brewery grain filtrate evaporation and concentration system according to claim 1, wherein: the outlet of the alkali liquid tank is connected with the inlet of the alkali liquid pump, the outlet of the alkali liquid pump is connected with the cleaning ports of the various-effect separators and the thick slurry tank through alkali liquid cleaning pipes, and the one-effect circulating pipe is connected with the inlet of the alkali liquid tank through an alkali liquid return pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322495589.4U CN220736214U (en) | 2023-09-13 | 2023-09-13 | Beer lees filtrate evaporation concentration system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322495589.4U CN220736214U (en) | 2023-09-13 | 2023-09-13 | Beer lees filtrate evaporation concentration system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220736214U true CN220736214U (en) | 2024-04-09 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322495589.4U Active CN220736214U (en) | 2023-09-13 | 2023-09-13 | Beer lees filtrate evaporation concentration system |
Country Status (1)
| Country | Link |
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| CN (1) | CN220736214U (en) |
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2023
- 2023-09-13 CN CN202322495589.4U patent/CN220736214U/en active Active
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