CN112843761A - Lees protein production fodder is with lees filter liquor evaporation concentration system - Google Patents
Lees protein production fodder is with lees filter liquor evaporation concentration system Download PDFInfo
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- CN112843761A CN112843761A CN202110261921.3A CN202110261921A CN112843761A CN 112843761 A CN112843761 A CN 112843761A CN 202110261921 A CN202110261921 A CN 202110261921A CN 112843761 A CN112843761 A CN 112843761A
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- 238000001704 evaporation Methods 0.000 title claims abstract description 53
- 230000008020 evaporation Effects 0.000 title claims abstract description 51
- 230000014616 translation Effects 0.000 title claims description 6
- 239000002912 waste gas Substances 0.000 claims abstract description 56
- 239000000706 filtrate Substances 0.000 claims abstract description 53
- 238000004519 manufacturing process Methods 0.000 claims abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 101
- 238000009833 condensation Methods 0.000 claims description 60
- 230000005494 condensation Effects 0.000 claims description 60
- 230000000694 effects Effects 0.000 claims description 53
- 239000007788 liquid Substances 0.000 claims description 49
- 238000000926 separation method Methods 0.000 claims description 32
- 239000007789 gas Substances 0.000 claims description 26
- 238000000034 method Methods 0.000 claims description 7
- 239000010865 sewage Substances 0.000 claims description 7
- 108010073032 Grain Proteins Proteins 0.000 claims description 5
- 238000001035 drying Methods 0.000 abstract description 11
- 108090000623 proteins and genes Proteins 0.000 abstract description 6
- 102000004169 proteins and genes Human genes 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000012141 concentrate Substances 0.000 description 8
- 238000007599 discharging Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 235000015097 nutrients Nutrition 0.000 description 2
- 240000008042 Zea mays Species 0.000 description 1
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 1
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 235000005822 corn Nutrition 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 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
- A23N—MACHINES OR APPARATUS FOR TREATING HARVESTED FRUIT, VEGETABLES OR FLOWER BULBS IN BULK, NOT OTHERWISE PROVIDED FOR; PEELING VEGETABLES OR FRUIT IN BULK; APPARATUS FOR PREPARING ANIMAL FEEDING- STUFFS
- A23N17/00—Apparatus specially adapted for preparing animal feeding-stuffs
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P60/00—Technologies relating to agriculture, livestock or agroalimentary industries
- Y02P60/80—Food processing, e.g. use of renewable energies or variable speed drives in handling, conveying or stacking
- Y02P60/87—Re-use of by-products of food processing for fodder production
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Food Science & Technology (AREA)
- Polymers & Plastics (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention provides a vinasse filtrate evaporation and concentration system for producing feed by vinasse protein, which comprises a first-effect evaporator, a second-effect evaporator and a third-effect evaporator, wherein the first-effect evaporator carries out primary evaporation and concentration on vinasse filtrate by using waste gas of a filter residue tube bundle dryer, a heater B of the third-effect evaporator carries out secondary evaporation and concentration on the vinasse filtrate by using steam separated by the second-effect evaporator, a heater A of the third-effect evaporator carries out tertiary evaporation and concentration on the vinasse filtrate by using waste gas flowing out of the heater A of the second-effect evaporator, a heater B of the second-effect evaporator carries out fourth evaporation and concentration on the vinasse filtrate by using steam separated by the first-effect evaporator, and a heater A of the second-effect evaporator carries out fifth evaporation and concentration on the vinasse filtrate by using waste gas flowing. According to the invention, high-temperature waste gas generated by filter residue in the drying process of the tube bundle dryer is used as a heat source, and the filtrate is evaporated and concentrated without generating steam, so that the energy consumption is reduced, and the production cost is reduced.
Description
Technical Field
The invention relates to the technical field of vinasse protein feed production equipment, in particular to a vinasse filtrate evaporation and concentration system for producing feed by using vinasse protein, which is used for evaporating and concentrating vinasse filtrate by using waste gas generated when vinasse liquid filter residues are dried by a tube bundle.
Background
In the alcohol production process, after alcohol is distilled from fermented mash, a vinasse liquid rich in protein is left, the vinasse liquid is subjected to solid-liquid separation to form two parts, namely a filter residue and a filtrate, wherein the filter residue is vinasse, the vinasse can be used for producing whole vinasse drying feed after being dried by a tube bundle dryer, the filtrate can also be sent into the dryer for drying after being evaporated and concentrated, and the dried product can also be used for producing whole vinasse drying feed. At present, what the drying to the filter residue adopted usually is the tube bank desiccator, the tube bank desiccator is with high-temperature steam as the heat source, in high-temperature steam gets into the heat exchanger tube bank of tube bank desiccator, carry out the heat exchange with the filter residue in the casing of tube bank desiccator, the filter residue is dried, high-temperature steam cooling condensation, at this in-process, the filter residue can produce a large amount of high temperature waste gas in drying process, at present, the processing to high temperature waste gas is direct discharge through washing back usually, calorific loss in the high temperature waste gas causes a large amount of energy extravagantly.
For the reason that the filtrate separated from the vinasse liquid still contains a large amount of protein, direct discharge not only pollutes the environment, but also causes loss of nutrient substances, and therefore, technicians in the field usually carry out evaporation concentration on the filtrate to recover the nutrient substances in the filtrate, and the evaporation concentration of the filtrate necessarily requires heat.
Disclosure of Invention
In summary, in order to overcome the defects of the prior art, the invention provides a distiller's grain filtrate evaporation and concentration system for producing feed by distiller's grain protein, which is characterized in that high-temperature waste gas generated in the drying process of a tube bundle dryer from filter residue after solid-liquid separation of distiller's grain liquid is used as a heat source to evaporate and concentrate filtrate, and the filtrate absorbs heat in the high-temperature waste gas to evaporate and concentrate without generating steam, thereby achieving the purposes of reducing energy consumption and reducing production cost.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows:
a lees albumen production fodder is with lees filter liquor evaporation concentration system, wherein: including one effect evaporator, two effect evaporator, three effect evaporator, exhaust gas condenser and separation steam condenser, the waste gas collection pipeline of air inlet intercommunication lees liquid filter residue tube bank desiccator of one effect evaporator, the liquid outlet of the feed inlet intercommunication lees liquid solid-liquid separation ware of one effect evaporator, two effect evaporator and three effect evaporator all be provided with two heaters, be heater A and heater B respectively, the waste gas outlet intercommunication two effect evaporator's heater A's air inlet, two effect evaporator's heater A's air outlet intercommunication three effect evaporator's heater A's air inlet, one effect evaporator's separation steam outlet intercommunication two effect evaporator's heater B's air inlet, two effect evaporator's separation steam outlet intercommunication three effect evaporator's heater B's air inlet, three effect evaporator's separation steam outlet intercommunication separation steam condenser's air inlet, gas outlet intercommunication vacuum pump of separation steam condenser, the air inlet of gas outlet intercommunication draught fan of heater A of three-effect evaporator, the gas outlet intercommunication waste gas condenser's of draught fan air inlet, the gas outlet evacuation of waste gas condenser, the discharge gate intercommunication three-effect evaporator's of one-effect evaporator feed inlet, the discharge gate intercommunication two-effect evaporator's of three-effect evaporator feed inlet, the follow-up processing process of the concentrated lees filtrate of discharge gate intercommunication of two-effect evaporator, one-effect evaporator utilize the waste gas of filter residue tube bank desiccator to carry out evaporative concentration for the first time to lees filtrate after the evaporative concentration for the first time, heater B of three-effect evaporator utilize lees filtrate to carry out evaporative concentration for the second time to lees filtrate after the evaporative concentration when evaporative concentration in two-effect evaporator, heater A of three-effect evaporator utilize the waste gas that heater A of two-effect evaporator flowed out to lees filtrate after the evaporative concentration for the second time And carrying out third evaporation concentration on the filtered liquid, carrying out fourth evaporation concentration on the distilled grain filtered liquid subjected to the third evaporation concentration by using steam separated when the distilled grain filtered liquid is evaporated and concentrated in the first effect evaporator by using a heater B of the second effect evaporator, and carrying out fifth evaporation concentration on the distilled grain filtered liquid subjected to the fourth evaporation concentration by using waste gas flowing out of the first effect evaporator by using a heater A of the second effect evaporator.
The technical scheme of the invention can also be realized in such a way that the one-effect evaporator comprises an one-effect heater, an one-effect separator and an one-effect circulating pump, wherein an air inlet of the one-effect heater is communicated with a waste gas collecting pipeline of the distiller's grains liquid residue tube bundle dryer, a feed inlet of the one-effect heater is communicated with a liquid outlet of a solid-liquid separator of the distiller's grains liquid, a discharge outlet of the one-effect heater is communicated with a feed inlet of the one-effect separator, a discharge outlet of the one-effect separator and a circulating discharge outlet of the one-effect heater are communicated with a feed inlet of the one-effect circulating pump, and a discharge outlet of the one-effect circulating pump is communicated with.
The technical scheme of the invention can also be realized by that the two-effect evaporator and the three-effect evaporator have the same structure and respectively comprise a heater A, a heater B, a separator, a circulating pump A and a circulating pump B, the discharge hole of the heater A and the discharge hole of the heater B are respectively communicated with the feed inlet of the separator, the discharge hole of the separator and the discharge hole of the heater B are communicated with the feed inlet of the circulating pump B, the discharge hole of the circulating pump B is communicated with the circulating feed inlet of the heater B and the feed inlet of the heater A, the discharge hole of the heater A is communicated with the feed inlet of the circulating pump A, the discharge hole of the circulating pump A is communicated with the circulating feed inlet of the heater A, the feed inlet of the heater B of the three-effect evaporator is communicated with the discharge hole of the one-effect circulating pump of the one-effect evaporator, the, the discharge port of a circulating pump A of the second-effect evaporator is communicated with the subsequent treatment process of the concentrated vinasse filtrate, the air inlet of a heater A of the second-effect evaporator is communicated with the air outlet of a first-effect heater of the first-effect evaporator, the air outlet of a heater A of the second-effect evaporator is communicated with the air inlet of a heater A of the third-effect evaporator, the air inlet of a heater B of the second-effect evaporator is communicated with the air outlet of a first-effect separator of the first-effect evaporator, and the air outlet of a separator of the second-effect evaporator is communicated with the air inlet of a heater B of the.
The technical scheme of the invention can be realized in such a way that a condensation water outlet of a first-effect heater of the first-effect evaporator is communicated with a condensation water inlet of a heater A of a second-effect evaporator, a condensation water outlet of the heater A of the second-effect evaporator is communicated with a condensation water inlet of a heater A of a third-effect evaporator, the condensation water outlet of the heater A of the third-effect evaporator and the condensation water outlet of a waste gas condenser are respectively communicated with a water inlet of a condensation water tank A, a water outlet of the condensation water tank A is communicated with a water inlet of a condensation pump A, and a water outlet of the condensation pump A is.
The technical scheme of the invention can be realized in such a way that a condensation water outlet of a heater B of the double-effect evaporator is communicated with a condensation water inlet of a heater B of the triple-effect evaporator, a condensation water outlet of the heater B of the triple-effect evaporator is communicated with a condensation water inlet of the separation steam condenser, a condensation water outlet of the separation steam condenser is communicated with a water inlet of a condensation water tank B, a water outlet of the condensation water tank B is communicated with a water inlet of a condensation pump B, and a water outlet of the condensation pump B is communicated with a sewage treatment system.
The invention has the beneficial effects that:
1. the invention uses the high-temperature waste gas generated in the drying process of the tube bundle dryer from the filter residue obtained by solid-liquid separation of the distiller's grains liquid as the heat source to evaporate and concentrate the filtrate, and the filtrate absorbs the heat in the high-temperature waste gas to evaporate and concentrate without generating steam, thereby achieving the purposes of reducing energy consumption and lowering production cost.
2. The invention relates to a double-effect evaporator and a triple-effect evaporator, which adopt two heaters, namely a heater A and a heater B, wherein the two heaters share a separator, the heater A of the double-effect evaporator adopts waste gas obtained after heat exchange of the heater of a single-effect evaporator as a heat source to recycle waste heat in the waste gas, the heater B of the double-effect evaporator adopts steam heat separated by the separator of the single-effect evaporator to evaporate and concentrate corn soaking liquid, the heater A of the triple-effect evaporator of the invention adopts the waste gas obtained after heat exchange of the heater A of the double-effect evaporator as the heat source, and the heater B of the triple-effect evaporator adopts the steam separated by the separator of the double-effect evaporator as the heat source to fully utilize the heat in the waste gas in the drying process of a filter residue tube bundle of distiller's grains liquid and the heat of the steam generated by evaporating and concentrating of the distiller's, the energy is utilized to the maximum extent, the energy is saved, and the consumption and the waste are reduced.
3. The discharge port of a circulating pump A of the two-effect evaporator is communicated with a subsequent treatment process of the vinasse filtrate through a discharge pipeline, the vinasse filtrate subjected to evaporation concentration by the one-effect evaporator firstly enters the three-effect evaporator for evaporation concentration, then enters the two-effect evaporator for evaporation concentration, the waste gas firstly passes through the one-effect evaporator, then passes through the two-effect evaporator and finally enters the three-effect evaporator, and then the temperature of the waste gas of the two-effect evaporator is inevitably higher than that of the waste gas of the three-effect evaporator. Because the distilled grain filtered liquid after evaporation and concentration also needs a subsequent tube bundle drying process, the distilled grain filtered liquid is discharged by adopting a two-effect evaporator, so that the temperature of the discharged distilled grain filtered liquid is about 70 ℃, the temperature required by the subsequent tube bundle drying can be ensured, and unnecessary damage to a subsequent tube bundle dryer caused by overhigh temperature can be avoided.
4. The condensed water produced by the heater B of the double-effect evaporator, the condensed water produced by the heater B of the triple-effect evaporator, the condensed water produced by the separated steam condenser, the vacuum pump, the condensed water tank B and the condensing pump B form a set of negative pressure condensing system which needs to provide power for steam flow, so that the system needs to operate at negative pressure, and the existence of the vacuum pump enables the system to form negative pressure. And the condensed water produced by the first-effect heater of the first-effect evaporator, the condensed water produced by the heater A of the second-effect evaporator, the condensed water produced by the heater A of the third-effect evaporator, the condensed water tank A and the condensate pump A form a set of normal-pressure condensation system, and the system can be operated at normal pressure.
5. The waste gas condenser and the separation steam condenser are arranged to play a role in condensing tail gas, and the finally discharged waste gas is cooled by low-temperature circulation of cooling water, so that the temperature of the waste gas is reduced to normal temperature and is discharged, and the pollution of the waste gas to the environment is reduced.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings.
As shown in figure 1, the vinasse filtering liquid evaporation and concentration system for producing the feed by the vinasse protein comprises a first-effect evaporator 1, a second-effect evaporator 2, a third-effect evaporator 3, an exhaust gas condenser 4 and a separation steam condenser 5, the one-effect evaporator 1 comprises an effect heater 101, an effect separator 102 and an effect circulating pump 103, the air inlet of the first-effect heater 101 is communicated with a waste gas collecting pipeline 6 of the distiller's grains liquid residue tube bundle dryer, the feed inlet of the first-effect heater 101 is communicated with a liquid outlet of a solid-liquid separator of the distiller's grains liquid through a feed pipeline 7, the feeding pipeline 7 is provided with an effective feeding valve 8, a discharging hole of the effective heater 101 is communicated with a feeding hole of the effective separator 102, a discharging hole of the effective separator 102 and a circulating discharging hole of the effective heater 101 are communicated with a feeding hole of the effective circulating pump 103, and a discharging hole of the effective circulating pump 103 is communicated with a circulating feeding hole of the effective heater 101. The triple-effect evaporator 3 comprises a triple-effect heater A301, a triple-effect heater B302, a triple-effect separator 303, a triple-effect circulating pump A304 and a triple-effect circulating pump B305, a discharge port of the single-effect circulating pump 103 is communicated with a feed port of the triple-effect heater B302 through a triple-effect feed pipeline B9, a triple-effect feed valve B10 is arranged on a triple-effect feed pipeline B9, a discharge port of the triple-effect heater B302 and a discharge port of the triple-effect heater A301 are both communicated with a feed port of the triple-effect separator 303, a circulating discharge port of the triple-effect heater B302 is communicated with a feed port of the triple-effect circulating pump B305, a discharge port of the triple-effect circulating pump B305 is communicated with a circulating feed port of the triple-effect heater B302 through a triple-effect feed pipeline A11, a triple-effect feed valve A12 is arranged on the triple-effect feed pipeline A11, a circulating discharge port of the triple-effect heater A301 is communicated with a feed port, the discharge hole of the three-effect circulating pump A304 is communicated with the circulating feed hole of the three-effect heater A301, the discharge hole of the three-effect circulating pump A304 is communicated with the feed hole of the two-effect heater B202 of the two-effect evaporator 2 through a two-effect feed pipeline B13, and a two-effect feed valve B14 is arranged on the two-effect feed pipeline B13.
The double-effect evaporator 2 comprises a double-effect heater A201, a double-effect heater B202, a double-effect separator 203, a double-effect circulating pump A204 and a double-effect circulating pump B205, a discharge hole of the double-effect heater B202 and a discharge hole of the double-effect heater A201 are communicated with a feed inlet of the double-effect separator 203, a discharge hole of the double-effect separator 203 and a circulating discharge hole of the double-effect heater B202 are communicated with a feed inlet of the double-effect circulating pump B205, a discharge hole of the double-effect circulating pump B205 is communicated with a feed inlet of the double-effect heater A201 through a double-effect feed pipeline A15, a double-effect feed valve A16 is arranged on a double-effect feed pipeline A15, a circulating discharge hole of the double-effect heater A201 is communicated with a feed inlet of the double-effect circulating pump A204, a discharge hole of the double-effect circulating pump A204 is communicated with a circulating feed inlet of the double-effect heater A201, a discharge hole of the double-effect circulating pump A204 is communicated with, the discharge pipe 17 is provided with a discharge valve 18.
The waste gas collection pipeline 6 of the air inlet intercommunication lees liquid filter residue tube bank desiccator of first effect heater 101, the air inlet of two effect heater A201 of gas outlet intercommunication three effect heater A301 of gas outlet intercommunication, the air inlet of 19 of draught fan of gas outlet intercommunication three effect heater A301 of three effect heater, the air inlet of 4 of exhaust gas condenser of gas outlet intercommunication of draught fan 19, the gas outlet evacuation of exhaust gas condenser 4. The air outlet of the first-effect separator 102 is communicated with the air inlet of the second-effect heater B202, the air outlet of the second-effect separator 203 is communicated with the air inlet of the third-effect heater B302, the air outlet of the third-effect separator 303 is communicated with the air inlet of the separation steam condenser 5, the air outlet of the separation steam condenser 5 is communicated with the air inlet of the vacuum pump 20, and the air outlet of the vacuum pump 20 is emptied.
The first-effect evaporator 1 carries out first evaporation concentration on the vinasse filtrate by utilizing the waste gas of the filter residue tube bundle dryer, the three-effect heater B302 of the three-effect evaporator 3 utilizes the steam separated when the vinasse filtrate is evaporated and concentrated in the two-effect evaporator 2 to carry out the second evaporation and concentration on the vinasse filtrate after the first evaporation and concentration, the three-effect heater A301 of the three-effect evaporator 3 utilizes the waste gas flowing out of the two-effect heater A201 of the two-effect evaporator 2 to carry out the third evaporation concentration on the distiller's grains filtrate after the second evaporation concentration, the second-effect heater B202 of the second-effect evaporator 2 carries out fourth evaporation concentration on the vinasse filtrate after the third evaporation concentration by using the steam separated when the vinasse filtrate is evaporated and concentrated in the first-effect evaporator 1, and the second-effect heater A201 of the second-effect evaporator 2 carries out fifth evaporation concentration on the vinasse filtrate subjected to the fourth evaporation concentration by using the waste gas flowing out of the first-effect evaporator 1.
The condensation water outlet of the first-effect heater 101 is communicated with the condensation water inlet of the second-effect heater A201, the condensation water outlet of the second-effect heater A201 is communicated with the condensation water inlet of the third-effect heater A301, the condensation water outlet of the third-effect heater A301 and the condensation water outlet of the waste gas condenser 4 are respectively communicated with the water inlet of the condensation water tank A21, the water outlet of the condensation water tank A21 is communicated with the water inlet of the condensation pump A22, and the water outlet of the condensation pump A22 is communicated with the sewage treatment system.
The condensation water outlet of the double-effect heater B202 is communicated with the condensation water inlet of the triple-effect heater B302, the condensation water outlet of the triple-effect heater B302 is communicated with the condensation water inlet of the separation steam condenser 5, the condensation water outlet of the separation steam condenser 5 is communicated with the water inlet of the condensation water tank B23, the water outlet of the condensation water tank B23 is communicated with the water inlet of the condensation pump B24, and the water outlet of the condensation pump B24 is communicated with the sewage treatment system. Condensed water generated by the double-effect heater B202 directly enters the triple-effect heater B302, under the action of the vacuum pump 20, the inside of the triple-effect heater B302 is in a negative pressure vacuum state, because the boiling point of a substance is increased along with the increase of the pressure and is reduced along with the reduction of the pressure, the boiling point temperature of water in the triple-effect heater B302 is reduced, the temperature of the condensed water generated by the double-effect heater B202 is higher, after the condensed water at the temperature enters the triple-effect heater B302, the temperature of the condensed water is higher than that of the water in the triple-effect heater B302, the condensed water generated by the double-effect heater B202 enters the triple-effect heater B302 to form flash evaporation, the flash evaporation steam also heats and concentrates the material in the triple-effect heater B302, and similarly, the temperature of the condensed water generated by the triple-effect heater B302 is higher, the flash evaporation phenomenon also occurs after the condensed water enters the separation steam condenser 5, and the steam separated by the triple, thereby reducing the temperature of the condensed water entering the condensed water tank B23.
When in use, the first-effect feed valve 8 is opened, the distiller's grains filtered liquid separated by the solid-liquid separator of the distiller's grains liquid enters the tube pass of the first-effect heater 101 along the feed pipeline 7, the waste gas discharged by the distiller's grains liquid filter tube bundle dryer enters the shell pass of the first-effect heater 101 through the waste gas collecting pipeline 6, the waste gas exchanges heat with the distiller's grains filtered liquid in the first-effect heater 101, the waste gas is used as a heat source to heat the distiller's grains filtered liquid, the distiller's grains filtered liquid is subjected to first evaporation concentration, the distiller's grains filtered liquid after evaporation concentration enters the first-effect separator 102 to be subjected to gas-liquid separation, the separated separation steam enters the shell pass of the second-effect heater B202, the waste gas flowing out from the gas outlet of the first,
opening a three-effect feed valve B10, feeding the distiller's grains filtrate which flows out from a discharge port of the one-effect circulating pump 103 and is evaporated and concentrated by the one-effect evaporator 1 into a tube pass of a three-effect heater B302, feeding separated steam separated by the two-effect separator 203 into a shell pass of the three-effect heater B302, and carrying out secondary evaporation and concentration on the distiller's grains filtrate which is evaporated and concentrated by the one-effect evaporator 1 by the separated steam in the three-effect heater B302. Opening a three-effect feed valve A12, allowing the distiller's grains filtrate which flows out from a discharge port of a three-effect circulating pump and is evaporated and concentrated by a three-effect heater B302 to enter a tube pass of a three-effect heater A301 along a three-effect feed pipeline A11, allowing the waste gas which flows out of a two-effect heater A201 to enter a shell pass of the three-effect heater A301, and allowing the waste gas to evaporate and concentrate the distiller's grains filtrate which is evaporated and concentrated by the three-effect heater B302 for the third time in the three-effect heater A301.
Opening a two-effect feed valve B14, allowing the distiller's grains filtered solution which flows out from a discharge port of a three-effect circulating pump A304 and is evaporated and concentrated by a three-effect evaporator 3 to enter a tube pass of a two-effect heater B202 along a two-effect feed pipeline B13, allowing the separation steam separated by a one-effect separator 102 to enter a shell pass of the two-effect heater B202, allowing the separation steam separated by the one-effect separator 102 to evaporate and concentrate the distiller's grains filtered solution which is evaporated and concentrated by the three-effect evaporator 3 for the fourth time in the two-effect heater B202, opening a two-effect feed valve A16, allowing the distiller's grains filtered solution which flows out from a discharge port of a two-effect circulating pump B205 and is evaporated and concentrated by a two-effect heater B202 to enter a tube pass of a two-effect heater A201 through a two-effect feed pipeline A15, allowing the waste gas flowing out of the one-effect heater 101 to enter a shell pass of the two-effect heater. And opening a discharge valve 18, and allowing the distiller's grains filtered solution subjected to five times of evaporation concentration to enter a subsequent treatment process along a discharge pipeline 17.
The waste gas that triple effect heater A301 flowed out gets into exhaust gas condenser 4 under the effect of draught fan 19, and the waste gas is discharged after the cooling by the condensation, and the temperature of the waste gas of exhaust gas condenser 4 exhaust is close normal atmospheric temperature. The separated steam separated by the three-effect separator 303 enters a separated steam condenser 5, the separated steam is condensed, and the non-condensable gas is discharged under the action of the vacuum pump 20.
Condensed water in the shell pass of the first-effect heater 101, condensed water in the shell pass of the second-effect heater A201, condensed water in the shell pass of the third-effect heater A301 and condensed water generated by the waste gas condenser 4 enter a condensed water tank A21, and then the condensed water in the condensed water tank A21 is sent to a sewage treatment system under the action of a condensate pump A22.
The condensed water on the shell side of the two-effect heater B202, the condensed water on the shell side of the three-effect heater B302 and the condensed water generated by the separation steam condenser 5 enter a condensed water tank B23, and then the condensed water in the condensed water tank B23 is sent to the sewage treatment system under the action of a condensing pump B24.
It should be noted that the above-mentioned embodiments illustrate rather than limit the technical solutions of the present invention, and that equivalent substitutions or other modifications made by those skilled in the art according to the prior art are all included within the scope of the claims of the present invention as long as they do not exceed the spirit and scope of the technical solutions of the present invention.
Claims (5)
1. The utility model provides a lees albumen production fodder is with lees filtrate evaporation concentration system which characterized in that: including one effect evaporator (1), two effect evaporator (2), three effect evaporator (3), exhaust gas condenser (4) and separation steam condenser (5), the air inlet of one effect evaporator (1) communicate the waste gas collection pipeline (6) of lees liquid filter residue tube bank desiccator, the liquid outlet of the solid-liquid separator of the feed inlet intercommunication lees liquid of one effect evaporator (1), two effect evaporator (2) and three effect evaporator (3) all be provided with two heaters, be heater A and heater B respectively, the exhaust gas outlet intercommunication of one effect evaporator (1) the air inlet of heater A of two effect evaporator (2), the air outlet intercommunication of heater A of three effect evaporator (3) of heater A of two effect evaporator (2) the air inlet of heater A of one effect evaporator (1), the separation steam outlet intercommunication of one effect evaporator (1) the air inlet of heater B of two effect evaporator (2), the air inlet of heater B of separation steam outlet intercommunication triple effect evaporimeter (3) of two effect evaporimeter (2), the air inlet of separation steam outlet intercommunication separation steam condenser (5) of triple effect evaporimeter (3), the gas outlet intercommunication vacuum pump (20) of separation steam condenser (5), the air inlet of draught fan (19) is linked together to the gas outlet of heater A of triple effect evaporimeter (3), the gas outlet of draught fan (19) the air inlet of exhaust gas condenser (4), the gas outlet evacuation of exhaust gas condenser (4), the discharge gate of one effect evaporimeter (1) the feed inlet of feed inlet intercommunication triple effect evaporimeter (3), the feed inlet of discharge gate intercommunication two effect evaporimeter (2) of triple effect evaporimeter (3), the follow-up processing process of the concentrated lees filtrate of discharge gate intercommunication of two effect evaporimeter (2), one effect evaporimeter (1) utilize the waste gas of filter residue tube bank desiccator to carry out the first evaporation concentration to the filtrate The heater B of the three-effect evaporator (3) utilizes the steam separated when the vinasse filtrate is evaporated and concentrated in the two-effect evaporator (2) to carry out the second evaporation and concentration on the vinasse filtrate after the first evaporation and concentration, the heater A of the three-effect evaporator (3) utilizes the waste gas flowing out of the heater A of the two-effect evaporator (2) to carry out the third evaporation concentration on the vinasse filtrate after the second evaporation concentration, the heater B of the second-effect evaporator (2) utilizes the steam separated when the vinasse filtrate is evaporated and concentrated in the first-effect evaporator (1) to carry out fourth evaporation and concentration on the vinasse filtrate after the third evaporation and concentration, and a heater A of the second-effect evaporator (2) utilizes the waste gas flowing out of the first-effect evaporator (1) to carry out fifth evaporative concentration on the vinasse filtrate subjected to the fourth evaporative concentration.
2. The distiller's grain protein production feed distiller's grain filtrate evaporation and concentration system of claim 1, wherein: the single-effect evaporator (1) comprises a single-effect heater (101), a single-effect separator (102) and a single-effect circulating pump (103), an air inlet of the single-effect heater (101) is communicated with a waste gas collecting pipeline (6) of the distiller's grains liquid residue tube bundle dryer, a feed inlet of the single-effect heater (101) is communicated with a liquid outlet of a solid-liquid separator of the distiller's grains liquid, a discharge outlet of the single-effect heater (101) is communicated with a feed inlet of the single-effect separator (102), a discharge outlet of the single-effect separator (102) and a circulating discharge outlet of the single-effect heater (101) are communicated with a feed inlet of the single-effect circulating pump (103), and a discharge outlet of the single-effect circulating pump (103) is communicated with a circulating feed inlet of the single-effect heater (101.
3. The distiller's grain protein production feed distiller's grain filtrate evaporation and concentration system of claim 1, wherein: the double-effect evaporator (2) and the triple-effect evaporator (3) have the same structure and respectively comprise a heater A, a heater B, a separator, a circulating pump A and a circulating pump B, a discharge port of the heater A and a discharge port of the heater B are respectively communicated with a feed inlet of the separator, a discharge port of the separator and a circulation discharge port of the heater B are respectively communicated with a feed inlet of the circulating pump B, a discharge port of the circulating pump B is communicated with a circulation feed inlet of the heater B and a feed inlet of the heater A, a circulation discharge port of the heater A is communicated with a feed inlet of the circulating pump A, a discharge port of the circulating pump A is communicated with a circulation feed inlet of the heater A, a feed inlet of the heater B of the triple-effect evaporator (3) is communicated with a discharge port of the single-effect circulating pump (103) of the single-effect evaporator (1), a discharge port of the circulating, the discharge hole of a circulating pump A of the second-effect evaporator (2) is communicated with the subsequent treatment process of the concentrated vinasse filtrate, the air inlet of a heater A of the second-effect evaporator (2) is communicated with the air outlet of a first-effect heater (101) of the first-effect evaporator (1), the air outlet of the heater A of the second-effect evaporator (2) is communicated with the air inlet of a heater A of the third-effect evaporator (3), the air inlet of a heater B of the second-effect evaporator (2) is communicated with the air outlet of a first-effect separator (102) of the first-effect evaporator (1), and the air outlet of a separator of the second-effect evaporator (2) is communicated with the air inlet of a heater B of the third-effect evaporator (3.
4. The distiller's grain protein production feed distiller's grain filtrate evaporation and concentration system of claim 3, wherein: the condensation water outlet of the first-effect heater (101) of the first-effect evaporator (1) is communicated with the condensation water inlet of the heater A of the second-effect evaporator (2), the condensation water outlet of the heater A of the second-effect evaporator (2) is communicated with the condensation water inlet of the heater A of the third-effect evaporator (3), the condensation water outlet of the heater A of the third-effect evaporator (3) and the condensation water outlet of the waste gas condenser (4) are respectively communicated with the water inlet of a condensation water tank A (21), the water outlet of the condensation water tank A (21) is communicated with the water inlet of a condensation pump A (22), and the water outlet of the condensation pump A (22) is communicated with a sewage treatment system.
5. The distiller's grain protein production feed distiller's grain filtrate evaporation and concentration system of claim 3, wherein: the condensation water outlet of the heater B of the second-effect evaporator (2) is communicated with the condensation water inlet of the heater B of the third-effect evaporator (3), the condensation water outlet of the heater B of the third-effect evaporator (3) is communicated with the condensation water inlet of the separation steam condenser (5), the condensation water outlet of the separation steam condenser (5) is communicated with the water inlet of a condensation water tank B (23), the water outlet of the condensation water tank B (23) is communicated with the water inlet of a condensation pump B (24), and the water outlet of the condensation pump B (24) is communicated with a sewage treatment system.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113208139A (en) * | 2021-06-25 | 2021-08-06 | 东莞益海嘉里生物科技有限公司 | Modular equipment based on wheat vinasse animal feed and manufacturing method |
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Denomination of invention: Distilled lees protein production - Distilled lees filtration liquid evaporation and concentration system for feed Granted publication date: 20220812 Pledgee: Bank of China Limited Zhongmou Branch Pledgor: ZHENGZHOU BODA CONCENTRATED DRYING EQUIPMENT CO.,LTD. Registration number: Y2024980026956 |
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