Liquor lees fermentation system and fermentation method for comprehensive resource utilization

Abstract

The present invention discloses a white wine lees fermentation system and fermentation method for comprehensive resource utilization. The outlet of the fermentation feed conveyor feeds the feed chute of the rotary arm fermentation machine, and the inlet of the fermentation feed conveyor is connected to the outlet of the wine lees squeezer and the bacterial powder adding device. The wine lees filtrate and wine lees leachate separated by the wine lees squeezer are mixed evenly with the fermented wine lees discharged from the rotary arm fermentation machine after passing through the leachate evaporation and concentration unit, and then enter the tube bundle dryer for drying. The hot air discharged from the top of the tube bundle dryer enters the cyclone dust collector for dust removal, and then enters the waste heat absorption tower to be washed and heat-exchanged layer by layer by hot water. The heated washing circulating water enters the hot side of the secondary waste heat exchanger and the primary waste heat exchanger in turn to heat the circulating preheated water on the cold side; the circulating preheated water preheats the hot air required for fermentation. The present invention adopts continuous fermentation and does not require the replenishment of bacterial strains. The drying system has low energy consumption and can recover heat and nutrients, reducing pollution to the environment.

Description

Technical Field

[0001] The present invention relates to distiller's grains fermentation, in particular to a distiller's grains fermentation system with comprehensive resource utilization. The present invention also relates to a distiller's grains fermentation method with comprehensive resource utilization, belonging to the technical field of distiller's grains fermentation. Background Art

[0002] Liquor lees are the largest waste product or byproduct of liquor production. Every ton of liquor produced generates 6-10 tons of lees. The nutrients in lees come not only from residual raw materials left over from incomplete saccharification and fermentation, but also from the bacteria, their metabolites, and autolyzed products. Liquor lees are high in moisture, with fresh lees containing 65-70% moisture. They are rich in nutrients and do not easily age well. Therefore, the utilization of lees has become a key focus for the industry. Liquor companies should promptly sell or dispose of wet lees to prevent the proliferation of microorganisms, which reduces their nutritional value and pollutes the environment. Nationally, nearly 100 million tons of wet lees were produced in 2022.

[0003] Distiller's grains can be used as feed, but if fed directly to animals, they may cause malnutrition or indigestion, and in severe cases, may even lead to alcohol poisoning. However, through distiller's grains fermentation, harmful substances in the grains can be absorbed and decomposed through the metabolic process of probiotics, thereby achieving the effect of non-toxic treatment. After fermentation, the content of yeast protein and organic acids in the distiller's grains is increased, which is beneficial for animal digestion and absorption, and improves animal intestinal health. Using distiller's grains as feed is inexpensive and can be effectively used as a supplementary raw material in the breeding industry. It has good use effect and economic benefits, which has also promoted the development of distiller's grains fermented feed.

[0004] Because distiller's grains contain up to 65-70% moisture, have a low bulk density, a large unit volume, and require aerobic fermentation, their use as a fermentable feed presents several challenges: The high moisture content of wet distiller's grains leads to leakage during storage. This leakage contains a variety of nutrients, which not only pollutes the environment but also wastes these nutrients. High-moisture distiller's grains are bulky, occupying a large volume in the fermentation machine. Drying requires high energy consumption and consumes a large amount of bacterial strain, leading to high production costs.

[0005] The Chinese utility model patent, publication number CN 218507749U, discloses a distiller's grains mixed inoculation batch fermentation system. The upper end of the wet distiller's grains lifting scraper 1 is connected to the wet material inlet of the tube bundle pre-dryer. The dry material outlet of the tube bundle pre-dryer is connected to the dry distiller's grains hopper via a dry distiller's grains transfer conveyor. A dry distiller's grains conveying auger is provided at the bottom of the dry distiller's grains hopper. The outlet of the dry distiller's grains conveying auger is connected to the lower inlet of the dry distiller's grains lifting scraper. The upper outlet of the dry distiller's grains lifting scraper is connected to the inlet of a continuous mixing inoculator. The upper outlet of the wet distiller's grains lifting scraper 2 and the strain injection pipe of the bacterial powder bin are also connected to the inlet of the continuous mixing inoculator, respectively. The outlet of the continuous mixing inoculator is connected to the lower inlet of a bucket elevator via a mixing inoculation auger. The upper end of the bucket elevator is connected to the feed chute of the corresponding distiller's grains fermentation machine via a fermentation feeding auger.

[0006] The white wine lees fermentation system has the following disadvantages:

[0007] ⑴. The wet distiller's grains are large in size. Batch fermentation machines are required, which require large and numerous fermentation machines and high project investment. The process continuity is poor when multiple batch fermentation machines are used.

[0008] ⑵. During the production process, the exhaust heat generated by the drying process was only simply utilized without comprehensive utilization, resulting in high energy consumption and high production costs;

[0009] ⑶. The wet lees were not squeezed and filtered before fermentation, and the leachate was not filtered out, resulting in high moisture content in the fermented material and high moisture content in the dryer feed, which increased the drying energy consumption and further increased the production cost.

[0010] (4) The leachate is not concentrated and then added to the fermented finished product, but is discharged on site or sent to a sewage treatment plant for sewage treatment, resulting in waste of nutrients in the leachate and pollution of the environment;

[0011] ⑸. Adding composite bacteria before fermentation. Since the output and volume of wet distiller's grains are large, a large amount of composite bacteria is added, and the production cost is high. Summary of the Invention

[0012] The primary purpose of the present invention is to overcome the problems existing in the prior art and provide a white wine lees fermentation system with comprehensive resource utilization, which adopts continuous fermentation and does not require the replenishment of bacteria. The drying system has low energy consumption and can recycle heat and nutrients, thereby reducing pollution to the environment.

[0013] In order to solve the above technical problems, the present invention provides a white wine lees fermentation system with comprehensive resource utilization, including a fermentation feed conveyor and a rotary arm fermentation machine. The outlet of the fermentation feed conveyor supplies material to the feed chute of the rotary arm fermentation machine, and the inlet of the fermentation feed conveyor is connected to the outlet of the wine lees squeezer and the bacterial powder adding device. The wine lees filtrate and wine lees leachate separated by the wine lees squeezer are mixed evenly with the fermented wine lees discharged from the rotary arm fermentation machine after passing through the leachate evaporation and concentration unit, and enter the tube bundle dryer for drying.

[0014] As an improvement of the present invention, the upper end of the rotary arm fermenter is provided with a rotary arm extending along the radius, the front edge of the rotary arm is installed with a discharging auger, a cloth auger is installed below the axis of the rotary arm, the discharging auger is lower than the cloth auger by a certain height, and the rear edge of the rotary arm is installed with multiple downward extending turning augers.

[0015] As a further improvement of the present invention, the raw steam releases heat in the tube bundle dryer to become high-temperature condensed water, and the high-temperature condensed water enters the condensed water flash tank and flashes to generate secondary steam as the heat source of the leachate evaporation and concentration unit.

[0016] As a further improvement of the present invention, the hot air discharged from the top of the tube bundle dryer enters the cyclone dust collector for dust removal, and then enters the waste heat absorption tower to be washed and heat exchanged layer by layer by hot water. The heated washing circulating water enters the hot side of the secondary waste heat exchanger and the primary waste heat exchanger in sequence to heat the circulating preheated water on the cold side.

[0017] The fresh air sent by the blower is preheated in sequence by the first-stage air preheater, the second-stage air preheater and the third-stage air preheater, and then sent to the bottom of the material bed of the rotary arm fermenter, and passes upward through the material layer to realize aerobic fermentation;

[0018] The circulating preheated water sequentially enters the hot sides of the secondary air preheater and the primary air preheater to perform two-stage preheating of the fresh air.

[0019] As a further improvement of the present invention, the high-temperature condensed water discharged from the condensed water flash tank enters the hot side of the three-stage air preheater to perform third-stage preheating of the fresh air.

[0020] As a further improvement of the present invention, the lees filtrate squeezed out by the lees squeezer and the lees leachate generated by the accumulation of raw lees are collected in a leachate tank, pumped out by a leachate pump, and sent to the cold side of a plate heat exchanger, and the lees leachate is preheated by the medium-temperature condensed water discharged from the hot side of the three-stage air preheater;

[0021] The low-temperature condensed water discharged from the hot side of the plate heat exchanger is collected in a condensed water tank and pumped into the top cover of the rotary arm fermenter by a low-temperature condensed water pump for circulation and heating. The excess low-temperature condensed water is used as boiler feed water.

[0022] As a further improvement of the present invention, the leachate evaporation and concentration unit includes a single-effect heat exchanger, a second-effect heat exchanger, and a third-effect heat exchanger, and the bottoms of the first to third-effect heat exchangers are connected to the first to third-effect separators respectively;

[0023] The preheated lees percolate enters the tube side of the second-effect heat exchanger and is heated in the second effect by the first-effect flash steam from the first-effect separator. The second-effect concentrate enters the second-effect separator for separation and is partially fed into the third-effect circulation pipe through the second-effect transfer pipe. The flash steam from the second-effect separator enters the shell side of the third-effect heat exchanger to perform third-effect heating on the third-effect concentrate.

[0024] The triple-effect concentrated liquid enters the triple-effect separator for separation and is partially sent to the single-effect circulation pipe through the triple-effect transfer pipe. The flash steam generated by the condensed water flash tank enters the shell side of the single-effect heat exchanger to heat the single-effect concentrated liquid. The single-effect concentrated liquid enters the single-effect separator for flash evaporation.

[0025] As a further improvement of the present invention, part of the first-effect concentrated liquid enters the thick slurry tank through the first-effect liquid outlet pipe for temporary storage, is sent into the mixer by the thick slurry pump, is mixed evenly with the fermented lees and the returned dry lees, and then enters the tube bundle dryer for drying.

[0026] As a further improvement of the present invention, the alkali liquid pump extracts the cleaning alkali liquid from the alkali liquid tank and sends it into the first-effect separator, the second-effect separator, the third-effect separator and the thick slurry tank respectively to clean the first to third-effect evaporation devices and the thick slurry tank. The cleaned alkali liquid returns to the alkali liquid tank through the first-effect liquid outlet pipe for circulation.

[0027] As a further improvement of the present invention, the upper side wall of the waste heat absorption tower is provided with an absorption tower circulation water inlet pipe, the inner end of the absorption tower circulation water inlet pipe extends to the axis of the absorption tower and turns downward, and a multi-component water tray and a tower tray are provided below the inner end of the absorption tower circulation water inlet pipe, the water distribution tray is dome-shaped, the opening of the tower tray is upward and fixed on the inner wall of the waste heat absorption tower, and the center hole of the tower tray is covered by the water distribution tray above, and the absorption tower circulating hot water is sprinkled on the center of the water distribution tray, falls from the outer periphery of the water distribution tray into the tower tray of the next layer, continues to fall from the circumferential edge of the center hole of the tower tray, sprinkles on the circumference of the water distribution tray of the next layer, splashes and continues to fall from the circumference of the water distribution tray into the tower tray of the next layer, and so on; the hot air goes up along the center hole of the tower tray, and then continues to flow from the outer periphery of the water distribution tray to the center hole of the upper tower tray, realizing reverse heat exchange washing of hot air and water.

[0028] As a further improvement of the present invention, the wine lees squeezing machine comprises a coaxial screen frame and an extrusion shaft, wherein the extrusion shaft passes through the screen frame and has spiral blades wound around its periphery;

[0029] The screen frame includes a fixed screen frame and a movable screen frame. A feed port is provided above the inlet end of the fixed screen frame. The inlet end of the movable screen frame is nested in the outer periphery of the terminal end of the fixed screen frame and can be axially translated. A guide plate is connected below the outlet end of the movable screen frame. The terminal end of the guide plate extends above the discharge port. The closer to the feed port, the smaller the diameter of the extrusion shaft.

[0030] The outer periphery of the two ports of the movable screen frame is respectively fixed with a screen frame support plate, and the two sides of the screen frame support plate are respectively fixed with a guide sleeve, and the guide sleeves on the same side are respectively sleeved on the guide rods, and the two guide rods are parallel to the axis of the extrusion shaft and the two ends are respectively fixed to the machine base or the ground through the guide rod supports;

[0031] Both ends of the screen frame support plate near the discharge port are driven by hydraulic push rods respectively. The roots of the two hydraulic push rods are respectively hinged on the push rod hinge ears, and the bottoms of the push rod hinge ears are respectively fixed on the machine base.

[0032] Another object of the present invention is to overcome the problems existing in the prior art and provide a distiller's grains fermentation method with comprehensive resource utilization, which adopts continuous fermentation and does not require the replenishment of bacterial strains. The drying system has low energy consumption and can recover heat and nutrients, thereby reducing pollution to the environment.

[0033] To solve the above technical problems, the present invention provides a method for fermenting distiller's grains with comprehensive resource utilization, which adopts the white distiller's grains fermentation system according to claim 9 and comprises the following steps in sequence:

[0034] S1, the raw material distiller's grains are squeezed dry by the distiller's grains squeezer, evenly inoculated with bacterial powder and enter the feed chute of the rotary arm fermentation machine;

[0035] S2. The wet distiller's grains from the feed chute fall into the center of the material bed. When the inoculated distiller's grains reach the highest position, the rotating arm of the fermenter drives the distribution auger, the discharge auger and the turning auger to rotate continuously.

[0036] S3, the feeding auger starts to feed the material to the peripheral area. When the material layer reaches the bottom of the discharging auger, the feeding stops and the fermentation begins. During the fermentation process, the rotating arm keeps rotating and each turning auger continues to stir.

[0037] S4. After the scheduled fermentation time is reached, the feeding auger is started, and the new material that has not been inoculated with bacterial powder is spread on the top of the old material layer, so that the material layer is raised to the bottom of the feeding auger; after the new material enters, it is mixed evenly with the old material under the stirring of the feeding auger, and the inoculation of the new material is automatically completed;

[0038] S5. The arm rotates one circle, and a round of fermentation is completed while spreading the material. At this time, the discharging auger and the spreading auger operate synchronously. The discharging auger discharges the material layer on the top, and then the spreading auger adds new material to the original height. Each turning auger continues to stir and inoculate, and the cycle continues.

[0039] As an improvement of the present invention, the fermented vinasse discharged from the rotary arm fermentation machine and the returned dry fermented vinasse and vinasse concentrate are fed into a mixer for uniform mixing, and then fed into a tube bundle dryer for drying;

[0040] The exhaust gas from the tube bundle dryer enters the waste heat absorption tower after cyclone dust removal, and is washed and heat-exchanged by the circulating hot water in the absorption tower. The circulating hot water in the absorption tower serves as the hot side of the waste heat heat exchanger to heat the preheating circulating water on the hot side of the air preheater. The preheating circulating water sequentially preheats the air on the cold side of the secondary air preheater and the primary air preheater.

[0041] As a further improvement of the present invention, the high-temperature condensed water discharged from the tube bundle dryer enters the condensed water flash tank for flash evaporation, and the secondary steam generated by the flash evaporation is used as the heat source of the leachate evaporation and concentration unit. The medium-temperature condensed water discharged from the condensed water flash tank enters the hot side of the three-stage air preheater to perform three-stage preheating on the air after the second-stage preheating. The hot air after the three-stage preheating enters the bottom of the material layer of the rotary arm fermenter to provide the air required for fermentation.

[0042] As a further improvement of the present invention, the lees leachate discharged from the raw lees and the lees filtrate discharged from the lees squeezer are collected together in a leachate tank. The lees leachate is preheated by the low-temperature condensed water discharged from the hot side of the three-stage air preheater and then sent to the leachate evaporation and concentration unit for evaporation and concentration. The obtained lees concentrate is sent to the mixer.

[0043] Compared with the existing technology, the present invention has achieved the following beneficial effects: based on a conventional distiller's grains fermentation project with a wet distiller's grains processing capacity of 26 t / h, the annual wet distiller's grains processing capacity is 200,000 tons, and 10 t / h of fermented commercial distiller's grains is produced, resulting in an annual fermented distiller's grains production capacity of 10,000 tons; the benefits are as follows:

[0044] 1. After the 65% leachate of wet distiller's grains is exuded, the moisture content is reduced to 63%. This system recovers 2.033t / h of distiller's grains leachate, which can produce 256kg / h of fermented feed after drying. The unit price is 2,000 yuan, and an additional income of 511 yuan / h can be achieved.

[0045] 2. After squeezing and dehydration, the moisture content of the lees is reduced from 63% to 58%. The tube bundle dryer can reduce the evaporation of water by 2.9t / h and save 4.2t / h of steam. The unit price of steam is 260 yuan / ton, and the steam cost saving is 1,100 yuan / h.

[0046] 3. The waste heat recovered by this system is used to heat the fermentation machine inlet air temperature, which can reduce the moisture content of wet lees from 58% to 55%. The tube bundle dryer can reduce the evaporation of water by 1.5t / h, saving 2.07t / h of steam. The unit price of steam is 260 yuan / ton, and the steam cost saving is 540 yuan / h.

[0047] 4. Using a mixture of old fermented distiller's grains and wet fermented distiller's grains for inoculation in the fermentation machine can save the cost of composite bacteria: 1,000 yuan / h;

[0048] 5. The total additional income from the above is: 3,150 yuan / hour, with an hourly product output of 10.5 tons, and an annual economic benefit of 0.315*24*330=24.95 million yuan. The hourly output value is 21,000 yuan, and the adoption of the technical solution of the present invention can increase the economic benefit by 0.315 / 2.1=15%. That is, the production line for fermented distiller's grains of the present invention can increase the economic benefit by 15%;

[0049] 6. In 2022, my country's liquor industry actually produced 100 million tons of wet distiller's grains. Assuming that 50% of the production adopts the technical solution of the present invention to produce fermented distiller's grains, the annual economic benefits can be increased by: 10,000*50% / 20*2495=623.75 million yuan. That is, if half of the production lines adopt the technical solution of the present invention, the annual economic benefits can be generated by 6.2 billion yuan.

[0050] 7. The present invention also avoids environmental pollution caused by distiller's grains leachate and the wastewater treatment required to meet emission standards, achieving zero discharge of distiller's grains leachate. The present invention also avoids thermal pollution caused by high-temperature exhaust gas, resulting in excellent environmental and social benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0051] The present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments. The accompanying drawings are only provided for reference and illustration and are not intended to limit the present invention.

[0052] Figure 1 This is a flow chart of the white wine lees fermentation system for comprehensive resource utilization of the present invention;

[0053] Figure 2 This is a front view of the wine lees squeezing machine of the present invention;

[0054] Figure 3 for Figure 2 A top view of

[0055] Figure 4 for Figure 2 Stereoscopic image of

[0056] Figure 5 for Figure 2 A three-dimensional diagram of the middle screen frame moving mechanism;

[0057] Figure 6 It is a top view of the rotary arm fermentation machine of the present invention;

[0058] Figure 7 Schematic diagram of the structure of the waste heat absorption tower in the present invention;

[0059] Figure: 1. Wine lees squeezer; 1a. Squeeze inlet; 1b. Squeeze shaft; 1c. Spiral blade; 1d. Fixed screen frame; 1e. Movable screen frame; 1e1. Screen frame support plate; 1e2. Guide sleeve; 1e3. Annular reinforcement rib; 1e4. Guide plate; 1f. Guide rod; 1f1. Guide rod support; 1g. Squeeze outlet; 1h. Hydraulic push rod; 1h1. Push rod hinge lug; 1j. Liquid collection tray; 1j1. Wine lees filtrate outlet; 1k. Squeeze drive motor; 1m. Squeeze base;

[0060] 2. Bacteria powder adding device; 3. Fermentation feed conveyor; 4. Rotating arm fermenter; 4a. Distribution auger; 4b. Discharge auger; 4c. Turning auger; 4d. Fermentation air inlet; 5. Fermentation discharge conveyor; 6. Material distribution conveyor; 7. Mixer; 8. Tube bundle dryer; 9. Return material conveyor; 10. Dry material conveyor; 11. Cyclone dust collector; 12. Waste heat absorption tower; 12a. Absorption tower air inlet; 12b. Absorption tower circulating water inlet pipe; 12c. Water distribution tray; 12d. Tower tray; 12e. Collector Water pan; 12f. Absorber circulating water outlet pipe; 12g. Ventilation pipe; 12h. Absorber drain pipe; 12i. Air hood; 12j. Droplet collection tray; 12k. Droplet water return pipe; 12m. Absorber circulating pump; 12n. Absorber drain pump; 12p. Primary waste heat exchanger; 12q. Secondary waste heat exchanger; 13. Blower; 14. Primary air preheater; 15. Secondary air preheater; 16. Third-stage air preheater; 17. Exhaust fan; 18. Waste gas treatment facility; 19. Preheating Circulating pump; 20. Condensate flash tank; 21. Medium-temperature condensate pump; 22. Plate heat exchanger; 23. Condensate tank; 24. Low-temperature condensate pump; 25. Leachate tank; 26. Leachate pump; 27. Leachate regulating valve; 28. First-effect heat exchanger; 29. ​​First-effect separator; 30. First-effect circulating pump; 31. First-effect liquid outlet pipe; 32. Thick slurry flowmeter; 33. Thick slurry regulating valve; 34. Second-effect heat exchanger; 35. Second-effect separator; 36. Second-effect circulating pump; 37. Second-effect transfer pipe; 38. Second-effect 39. Three-effect heat exchanger; 40. Three-effect separator; 41. Three-effect circulation pump; 42. Three-effect transfer pipe; 43. Three-effect transfer regulating valve; 44. Thick slurry tank; 45. Thick slurry pump; 46. Thick slurry addition pipe; 47. Alkali liquid tank; 48. Alkali liquid supply pipe; 49. Alkali liquid pump; 50. Alkali liquid cleaning pipe; 51. Condensate water tank; 52. Sewage transfer pump; 53. Sewage treatment station; 54. Condenser; 55. Vacuum pump; 56. Cooling tower; 57. Cooling water pump; 58. Boiler room. Implementation Method

[0061] In the following description of the present invention, the terms "up", "down", "front", "back", "left", "right", "inside", "outside", etc. indicate directions or positional relationships based on the directions or positional relationships shown in the accompanying drawings. They are only for the convenience of describing the present invention and simplifying the description, and do not mean that the device must have a specific direction.

[0062] In order to make the technical means, creative features, objectives and effects achieved by the present invention easier to understand, the present invention is further described below with reference to specific illustrations.

[0063] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as those commonly understood by those skilled in the art of the present invention. The terms used in the specification of the present invention are only for the purpose of describing specific embodiments and are not intended to limit the present invention.

[0064] like Figure 1 As shown, the white wine lees fermentation system for comprehensive resource utilization of the present invention includes a wine lees squeezer 1, a bacterial powder adding device 2, a fermentation feed conveyor 3, a rotary arm fermentation machine 4, a fermentation discharge conveyor 5, a tube bundle dryer 8, a dry material conveyor 10, a leachate evaporation and concentration unit and a waste heat absorption tower 12.

[0065] The outlets of the lees squeezer 1 and the bacterial powder addition device 2 are both connected to the inlet of the fermentation feed conveyor 3. The outlet of the fermentation feed conveyor 3 is connected to the feed chute of the rotary arm fermenter 4 via an air lock. The bottom discharge port of the rotary arm fermenter 4 is connected to the inlet of the fermentation discharge conveyor 5, and the outlet of the fermentation discharge conveyor 5 is connected to the inlet of the distribution conveyor 6 via an air lock. Two tube bundle dryers 8 are typically installed in parallel, each equipped with a mixer 7. The distribution conveyor 6 distributes the fermented lees to each mixer 7. The outlet of the mixer 7 is connected to the feed auger of the tube bundle dryer 8. The outlet of the tube bundle dryer 8 is connected to the inlet of the return conveyor 9 and the dry material conveyor 10 respectively via a distribution valve. The upper outlet of the return conveyor 9 is also connected to the inlet of the corresponding mixer 7. The finished fermented lees are discharged by the dry material conveyor 10.

[0066] The exhaust gas outlets of the tube bundle at the top of the tube bundle dryer 8 are respectively connected to the inlets of the cyclone dust collector 11, and the exhaust ports at the top of the cyclone dust collector 11 are connected to the absorption tower air inlet 12a at the bottom of the waste heat absorption tower 12 through an induced draft fan.

[0067] The steam rotary joint at the discharge end of tube bundle dryer 8 is connected to the saturated steam pipe. The condensate rotary joint at the feed end of tube bundle dryer 8 is connected to the high-temperature condensate pipe via a steam trap. The outlet of the high-temperature condensate pipe is connected to the inlet of condensate flash tank 20. The bottom outlet of condensate flash tank 20 is connected to the inlet of medium-temperature condensate pump 21. The flash steam outlet at the top of condensate flash tank 20 is connected to the upper shell-side inlet of single-effect heat exchanger 28, serving as the heat source for single-effect evaporation.

[0068] The outlet of the medium-temperature condensate pump 21 is connected to three branches. Branch 1 is connected to the hot side inlet of the three-stage air preheater 16. The hot side outlet of the three-stage air preheater 16 is connected to the hot side inlet of the plate heat exchanger 22. The hot side outlet of the plate heat exchanger 22 is connected to the inlet of the condensate tank 23.

[0069] Branch 2 is connected to the water supply port of the waste heat absorption tower 12 for supplying water to the waste heat absorption tower 12. Branch 3 is connected to the lower shell inlet of the primary heat exchanger 28, and excess medium-temperature condensed water also enters the shell of the primary heat exchanger 28.

[0070] The outlet of the condensed water tank 23 is connected to the inlet of the low-temperature condensed water pump 24, and the outlet of the low-temperature condensed water pump 24 is connected to the top cover circulation pipe of the rotary arm fermenter 4 and is also connected to the water supply pipe of the boiler room 58.

[0071] like Figures 2 to 5 As shown, the wine lees squeezing machine in the present invention includes a squeezing feed port 1a, an extrusion shaft 1b, a screen frame, a squeezing discharge port 1g, a liquid collecting tray 1j, a squeezing drive mechanism and a squeezing machine base 1m. The screen frame includes a fixed screen frame 1d and a movable screen frame 1e, and is coaxial with the extrusion shaft 1b. The squeezing feed port 1a is fixedly connected above the inlet end of the fixed screen frame 1d, and the squeezing discharge port 1g is close to the bottom of the outlet end of the movable screen frame 1e. The extrusion shaft 1b passes through the screen frame and is wrapped with spiral blades 1c on the periphery.

[0072] The drive mechanism for the extrusion shaft 1b is located at the discharge end and includes a squeeze drive motor 1k. The shaft end of the squeeze drive motor 1k drives the extrusion shaft 1b via a belt. After granular material enters the squeeze feed inlet 1a, it is conveyed toward the discharge end by spiral blades 1c, where it enters the annular space between the extrusion shaft 1b and the screen frame. The diameter of the extrusion shaft 1b decreases as it approaches the squeeze feed inlet 1a, while it increases as it approaches the screen frame outlet. This narrows the annular space containing the material, causing it to be squeezed more and more as it moves toward the discharge end, allowing moisture to be filtered out through the pores of the screen frame.

[0073] A liquid collecting pan 1j is provided below both the fixed screen frame 1d and the movable screen frame 1e. A lees filtrate outlet 1j1 is provided at the lowest point of the liquid collecting pan 1j. The filtered water falls into the liquid collecting pan 1j and is collected, and then flows out from the lowest lees filtrate outlet 1j1.

[0074] The inlet end of the mobile screen frame 1e is nested within the outer periphery of the fixed screen frame 1d and is capable of axial translation. Multiple annular reinforcing ribs 1e3 are provided along the length of the mobile screen frame 1e to enhance its strength, rigidity, and resistance to extrusion. Connecting flanges are provided on the front and rear sides of the mobile screen frame 1e for easy attachment, fixing, and removal.

[0075] A guide plate 1e4 is connected below the outlet of the mobile screen frame 1e. The distal end of the guide plate 1e4 extends above the squeeze outlet 1g and can be tilted toward the squeeze outlet 1g. Regardless of the position to which the mobile screen frame 1e is translated, material exiting the mobile screen frame 1e can flow through the guide plate 1e4 into the squeeze outlet 1g for discharge.

[0076] A screen frame support plate 1e1 is fixed to the outer periphery of each port of the mobile screen frame 1e. Guide sleeves 1e2 are fixed to the front and rear sides of the support plate 1e1. The guide sleeves 1e2 on each side are respectively mounted on guide rods 1f and can slide along them. Both guide rods 1f are parallel to the axis of the extrusion shaft 1b and secured at both ends to the squeezer base 1m or the ground via guide rod supports 1f1. The screen frame support plates 1e1 at the inlet and outlet sections of the mobile screen frame 1e are guided by the guide sleeves 1e2 and guide rods 1f, ensuring translation of the mobile screen frame 1e along the axis of the extrusion shaft 1b.

[0077] Both ends of the screen frame support plate 1e1 near the squeeze outlet 1g are driven by hydraulic push rods 1h respectively. The roots of the two hydraulic push rods 1h are respectively hinged on the push rod hinge ears 1h1, and the bottoms of the push rod hinge ears 1h1 are respectively fixed on the squeeze machine base 1m.

[0078] For relatively dry materials, the two hydraulic push rods 1h are pushed out synchronously, pushing the screen frame support plate 1e1 and then driving the mobile screen frame 1e to move toward the squeezing feed port 1a. The overlapping length of the mobile screen frame 1e and the fixed screen frame 1d becomes longer, and the overall length of the screen frame becomes shorter, reducing the compression ratio.

[0079] For relatively moist materials, the two hydraulic push rods 1h retract synchronously, pulling the screen frame support plate 1e1, which in turn drives the mobile screen frame 1e toward the squeeze outlet 1g. This shortens the overlap between the mobile screen frame 1e and the fixed screen frame 1d, lengthening the overall screen frame length and improving the compression ratio. By adjusting the compression ratio, the moisture content of the discharge material can be controlled or maintained stable.

[0080] like Figure 6 As shown, the upper end of the rotary arm fermenter 4 is provided with a rotary arm extending along the radius, and a discharge auger 4b is installed on the front side edge of the rotary arm relative to the rotation and forward direction of the material bed. The discharge auger 4b feeds the peripheral material to the central cylinder along the radius.

[0081] A feeding auger 4a is mounted below the axis of the rotating arm. It conveys material from the center of the bed toward the periphery along a radial path. The discharge auger 4b is 10-15 cm lower than the feeding auger 4a. One rotation of the rotating arm constitutes one fermentation cycle, and the discharge height during one fermentation cycle is 10-15 cm, which is the height difference between the feeding auger 4a and the discharge auger 4b.

[0082] A plurality of downwardly extending turning augers 4c are installed side by side on the rear edge of the rotating arm. The turning augers 4c rotate around the vertical axis to turn the material in the height direction of the material layer, so that the upper and lower materials are evenly mixed.

[0083] Below the material bed of the rotary arm fermentation machine 4 is an air inlet chamber, and the fermentation air inlet 4d is tangentially connected to the side wall of the air inlet chamber.

[0084] The bottom of the rotary arm fermentation machine 4 can be divided into multiple fan-shaped air distribution chambers, and each air distribution chamber independently controls the hot air intake. For thin material layers with a short fermentation time, all materials on the material bed can be cleared out during discharging, and the material can be distributed while discharging. The gap between the discharging auger and the feeding auger is an empty material bed. At this time, the air blowing of the corresponding fan-shaped air distribution chamber below the empty material bed can be turned off, and the fan-shaped air distribution chambers can be closed in turn following the rotation of the rotary arm to avoid air leakage. This can save the waiting time for discharging and realize continuous fermentation of the thin material layer.

[0085] The rotating arm fermentation machine 4 can also be a machine in which the rotating arm is stationary and the material bed rotates while carrying the material, thereby still achieving relative rotation between the rotating arm and the material bed.

[0086] like Figure 7 As shown, the upper sidewall of the waste heat absorption tower 12 is equipped with an absorber circulating water inlet pipe 12b. A conical water collection tray 12e is located at the bottom of the waste heat absorption tower 12. The inner end of the absorber circulating water inlet pipe 12b extends to the axis of the absorption tower, bends downward, and has a bell mouth. The absorber circulating water outlet pipe 12f passes through the conical bottom of the water collection tray 12e. The bell mouth at its upper end is lower than the upper end of the water collection tray 12e, and the lower end bends and exits through the bottom sidewall of the waste heat absorption tower 12.

[0087] The outer port of the absorption tower circulation outlet pipe 12f is connected to the inlet of the absorption tower circulation pump 12m, the outlet of the absorption tower circulation pump 12m is connected to the hot side inlet of the secondary waste heat exchanger 12q, the hot side outlet of the secondary waste heat exchanger 12q is connected to the hot side inlet of the primary waste heat exchanger 12p, and the hot side outlet of the primary waste heat exchanger 12p is connected to the absorption tower circulation inlet pipe 12b.

[0088] The upper part of the waste heat absorption tower 12 is reduced in diameter and a hood 12i is installed on the top. A droplet collection tray 12j is provided at the lower part of the droplet collection tray 12j. A droplet water return pipe 12k is connected to the lowest point of the droplet collection tray 12j. The lower end of the droplet water return pipe 12k extends into the tower body and is provided with an S-shaped liquid seal.

[0089] A multi-component water tray 12c and a tower tray 12d are provided below the inner end of the absorption tower circulating water inlet pipe 12b. The water tray 12c is dome-shaped, and the opening of the tower tray 12d is upward and fixed to the inner wall of the waste heat absorption tower 12. The center hole of the tower tray is covered by the water tray 12c above. The hot water circulating in the absorption tower is poured on the center of the water tray 12c, and falls from the outer edge of the water tray 12c into the tower tray 12d of the next layer. It continues to fall from the circumferential edge of the center hole of the tower tray, pours on the circumference of the water tray 12c of the next layer, splashes and continues to fall from the circumference of the water tray 12c of the next layer, and so on.

[0090] An absorption tower air inlet 12a is provided on the lower side wall of the waste heat absorption tower 12. Hot air enters the lower inner cavity of the tower body and flows upward along the center hole of the tower plate, and then continues to flow from the outer periphery of the water separation plate 12c to the center hole of the upper tower plate, realizing reverse heat exchange and washing between hot air and water.

[0091] The lowest point of the water collection tray 12e is connected to the absorption tower drain pipe 12h. The upper end of the vent pipe 12g is higher than the water level of the water collection tray 12e. The vent pipe 12g passes through the water collection tray 12e and its lower end is connected to the absorption tower drain pipe 12h through an S-bend. The outer end of the absorption tower drain pipe 12h is connected to the inlet of the absorption tower sewage pump 12n.

[0092] The hot air discharged from the top of the tube bundle dryer 8 enters the cyclone dust collector 11 for dust removal, and then enters the waste heat absorption tower 12 to be washed and heat exchanged layer by layer with hot water. The heated washing circulating water enters the hot side of the secondary waste heat exchanger 12q and the primary waste heat exchanger 12p in turn to heat the circulating preheated water on the cold side.

[0093] The circulating preheated water is powered by preheating circulation pump 19. The outlet of preheating circulation pump 19 is connected to the cold-side inlet of primary waste heat exchanger 12p, which is in turn connected to the cold-side inlet of secondary waste heat exchanger 12q. The cold-side outlet of secondary waste heat exchanger 12q is connected to the hot-side inlet of secondary air preheater 15. The hot-side outlet of secondary air preheater 15 is connected to the hot-side inlet of primary air preheater 14, which is in turn connected to the outlet of preheating circulation pump 19, forming a circulation loop. The circulating preheated water sequentially enters the hot sides of secondary air preheater 15 and primary air preheater 14, performing two-stage preheating of the fresh air.

[0094] The leachate evaporation and concentration unit includes a first-effect heat exchanger 28, a second-effect heat exchanger 34 and a third-effect heat exchanger 39. The bottom of the first-effect heat exchanger 28 is connected to the first-effect separator 29, the bottom of the second-effect heat exchanger 34 is connected to the second-effect separator 35, and the bottom of the third-effect heat exchanger 39 is connected to the third-effect separator 40.

[0095] The preheated distiller's grains percolate enters the tube side of the second-effect heat exchanger 34, where it is heated by the first-effect flash steam from the first-effect separator 29. The second-effect concentrate enters the second-effect separator 35 for separation, and a portion of it is fed into the third-effect circulation pipe through the second-effect transfer pipe 37. The flash steam from the second-effect separator 35 enters the shell side of the third-effect heat exchanger 39 to heat the third-effect concentrate in the third effect.

[0096] The triple-effect concentrated liquid enters the triple-effect separator 40 for separation and is partially sent to the single-effect circulation pipe through the triple-effect transfer pipe 42. The flash steam generated by the condensate flash tank 20 enters the shell side of the single-effect heat exchanger 28 to heat the single-effect concentrated liquid. The single-effect concentrated liquid enters the single-effect separator 29 for flash evaporation.

[0097] Part of the first-effect concentrated liquid enters the thick slurry tank 44 through the first-effect liquid outlet pipe 31 for temporary storage, and is sent to the mixer 7 by the thick slurry pump 45 through the thick slurry addition pipe 46 to be evenly mixed with the fermented vinasse and the returned dry vinasse, and then enters the tube bundle dryer 8 for drying.

[0098] The alkali liquid pump 49 extracts the cleaning alkali liquid from the alkali liquid tank 47 and sends it to the first-effect separator 29, the second-effect separator 35, the third-effect separator 40 and the thick slurry tank 44 respectively to clean the first to third-effect evaporation devices and the thick slurry tank 44. The cleaned alkali liquid returns to the alkali liquid tank 47 through the first-effect liquid outlet pipe 31 for circulation.

[0099] Taking a production line with a raw distiller's grain output of 26t / h as an example, after storage, the moisture content of 26t / h of raw distiller's grains with a moisture content of up to 65% reaches 88.9% in the 2.1t / h leachate. After storage, the moisture content of 24t / h of wet distiller's grains is 63%. After entering the distiller's grain squeezer 1 for squeezing, 21.5t / h of wet distiller's grains with a moisture content of 58% are discharged. The moisture content of the 3.68t / h filtrate squeezed out by the distiller's grain squeezer 1 is 7.9%.

[0100] After squeezing out the wet lees, the fermentation feed conveyor 3 feeds the fermentation machine 4 to the rotating arm fermenter. During distribution, the fermentation machine 4 raises the distribution auger 4a and the discharge auger 4b to a high position. The rotating arm then rotates these three augers 4a, 4b, and 4c around their central axis. The wet lees from the feed chute land in the center of the bed. When the inoculated lees reach a high position, the distribution auger 4a distributes the lees to the surrounding area, ensuring a smooth top layer. Distribution is complete when the bed reaches below the discharge auger 4b.

[0101] Fresh air from blower 13 is preheated to 75°C by primary, secondary, and tertiary air preheaters 14, 15, and 16. It is then fed into the fermentation machine 4 beneath the material bed, where it passes upward through the material layer for aerobic fermentation. Fermentation exhaust gases are discharged from the upper exhaust port of fermentation machine 4 and fed by exhaust fan 17 to waste gas treatment facility 18 for treatment. During fermentation, the arm rotates continuously, and the augers 4c rotate to turn the material along the height of the material layer, ensuring uniform fermentation.

[0102] The raw material lees enters the rotary arm fermenter 4 for fermentation, which includes the following steps in sequence:

[0103] S1, when the raw material lees is piled up, the exudate seeps out first, then is squeezed out by the lees squeezer 1, and enters the fermentation feed conveyor 3. The bacterial powder sent out by the bacterial powder adding device 2 also enters the fermentation feed conveyor 3. The two are mixed evenly while being transported to the feed chute of the rotary arm fermenter 4;

[0104] S2, the wet distiller's grains from the feed chute fall into the center area of ​​the material bed of the rotary arm fermenter 4. When the inoculated distiller's grains reach the highest position, the rotating arm of the rotary arm fermenter 4 drives the distribution auger 4a, the discharge auger 4b and the turning auger 4c to rotate continuously;

[0105] S3, the feeding auger 4a starts to feed the material to the peripheral area. When the material layer reaches the bottom of the discharging auger 4b, the feeding stops and the fermentation begins. During the fermentation process, the rotating arm keeps rotating and the turning augers 4c continue to stir.

[0106] S4. After the predetermined fermentation time is reached, the feeding screw 4a is started, and the new material that has not been inoculated with bacterial powder is spread on the old material layer, so that the material layer is raised to the bottom of the feeding screw 4a; after the new material enters, it is mixed evenly with the old material under the stirring of the turning screw 4c, and the inoculation of the new material is automatically completed; except for the first feeding, which requires inoculation with bacterial powder, the inoculation of the new material can be automatically completed by the fermented distiller's grains thereafter;

[0107] S5. The arm rotates one circle, and a round of fermentation is completed while distributing the material. At this time, the discharging auger 4b and the distributing auger 4a operate synchronously. The discharging auger 4b discharges the material layer on the top, and then the distributing auger 4a replenishes the new material to the original height. Each turning auger 4c continues to stir and inoculate, and the cycle continues. The arm rotates one circle continuously to complete a round of feeding, fermentation and discharging.

[0108] The fermentation discharge conveyor 5 sends out 17.8t / h of fermented distiller's grains with a moisture content of 47.1%, which are sent to the distribution conveyor 6 and fed to two mixers 7 respectively. Part of the dried distiller's grains are returned to the mixer 7. There is also 0.65t / h of concentrated slurry from the leachate evaporation and concentration unit with a moisture content of 40%. After the above three materials are mixed evenly, they are sent to the tube bundle dryer 8 by the feeding auger for drying. Raw steam enters each tube bundle to heat and dry the distiller's grains. Part of the dried distiller's grains are sent back to the mixer 7 through the return conveyor 9, and the other part of the dried distiller's grains are sent out by the dry material conveyor 10. The moisture content of the dried distiller's grains is 10%, and the output is 10t / h.

[0109] After releasing heat in tube bundle dryer 8, the raw steam becomes high-temperature condensate at 143°C, which then enters condensate flash tank 20 for flash evaporation. To prevent condensation caused by the temperature drop in cyclone dust collector 11, a heated steam pipe is wrapped around the cyclone dust collector 11. The high-temperature condensate at 143°C discharged from the heated steam pipe also enters condensate flash tank 20 for flash evaporation due to the pressure drop. The 100°C secondary steam generated by the flash evaporation serves as the heat source for the leachate evaporation and concentration unit.

[0110] The 100°C condensate discharged from the bottom of the condensate flash tank 20 is sent out by the medium-temperature condensate pump 21. The medium-temperature condensate pump 21 sends a part of the 100°C condensate into the hot side of the three-stage air preheater 16, and after the third-stage heating of the fermentation hot air, it becomes 75°C medium-temperature condensate, and then enters the hot side of the plate heat exchanger 22. After further heat exchange and heat recovery, it becomes 50°C low-temperature condensate and enters the condensate tank 23 for collection.

[0111] The top cover of the rotary arm fermenter 4 is prone to condensation. This condensation dripping into the material layer not only affects the temperature and humidity of the top material but also causes bacterial contamination. In the present invention, a low-temperature condensate pump 24 is used to extract the 50°C low-temperature condensate from the condensate tank 23 and return it to the top cover of the rotary arm fermenter 4 for heat circulation, thereby preventing condensation on the top cover. The circulated condensate returns to the condensate tank 23, and the excess low-temperature condensate is returned to the boiler room 58 as boiler feed water.

[0112] The bundle exhaust gas generated during the bundle drying process has a dry-bulb temperature of 85°C and a wet-bulb temperature of 78°C. It is discharged from the top exhaust hood and enters the cyclone dust collector 11 for centrifugal separation. The separated lees powder falls into the return conveyor 9 and enters the mixer 7 along with the return material.

[0113] The high-temperature exhaust gas from the top of the cyclone dust collector 11 enters the lower part of the waste heat absorption tower 12, and flows upward through each layer of the tower tray 12d from bottom to top. The 78°C absorption tower circulating hot water in the water collecting tray 12e at the bottom of the waste heat absorption tower 12 is pumped out by the absorption tower circulating pump 12m and enters the hot side of the secondary waste heat heat exchanger 12q. After heat exchange, it enters the hot side of the primary waste heat heat exchanger 12p. After further heat exchange, it becomes 50°C absorption tower circulating hot water and enters the circulating water inlet at the top of the waste heat absorption tower 12, first falls on the center of the water separation tray 12c, and falls from the outer edge of the water separation tray 12c into the tower tray 12d of the next layer, and continues to fall from the circumferential edge of the center hole of the tower tray, splashing on the circumference of the water separation tray 12c of the next layer, splashing and continuing to fall from the outer edge of the water separation tray 12c into the tower tray 12d of the next layer. Similarly, the hot air flows upward along the center hole of the tower tray, and then continues to flow upward from the outer periphery of the water separation tray 12c. This creates a countercurrent flow of hot air and water, ensuring sufficient heat and moisture exchange. The cooled and cleaned 52°C exhaust gas is discharged from the top of waste heat absorption tower 12. The heated, circulating hot water from the absorption tower falls into a water collection tray 12e at the bottom of the waste heat absorption tower 12 and is pumped out for circulation by absorption tower circulation pump 12m.

[0114] The preheating circulation pump 19 sends the 45°C preheated water into the cold side of the first-stage waste heat exchanger 12p and heats it to 65°C. The water then enters the cold side of the second-stage waste heat exchanger 12q and continues to be heated to 74°C. The water then enters the hot side inlet of the second-stage air preheater 15 and is discharged from the hot side outlet of the second-stage air preheater 15. The water then enters the hot side inlet of the first-stage air preheater 14 and is discharged from the hot side outlet of the first-stage air preheater 14 as 45°C preheated water. The water then enters the inlet of the preheating circulation pump 19 to form a cycle. Natural air at room temperature of 25°C is sent by the blower 13 into the first-stage air preheater 14 and heated to 60°C. The air is then heated to 71°C by the second-stage air preheater 15 and heated to 75°C by the third-stage air preheater 16 and sent to the bottom of the material bed of the rotary arm fermenter 4.

[0115] The medium-temperature condensate pump 21 delivers another portion of the 100° C. condensate into the shell side inlet of the first-effect heat exchanger 28 , serving as a heat source for the first-effect heat exchanger 28 .

[0116] The medium-temperature condensate pump 21 delivers a portion of the 100°C condensate into the water collection tray of the waste heat absorption tower 12 as high-temperature make-up water to compensate for its evaporation and increase the circulating water temperature of the waste heat absorption tower 12.

[0117] The lees filtrate squeezed out by the lees squeezer 1 and the lees leachate generated by the accumulation of raw lees are collected in the leachate tank 25. When the water quality of the circulating water in the waste heat absorption tower 12 does not meet the requirements, it is discharged from the lowest point of the bottom water tray and sent to the leachate tank 25 by the absorption tower sewage pump 12n.

[0118] Leachate, with a moisture content of 9%, is pumped out by leachate pump 26 at a rate of 5.778 t / h and fed into the cold side of plate heat exchanger 22, where it is preheated by 75°C condensate. A leachate regulating valve 27 is installed in the pipeline from the cold side outlet of plate heat exchanger 22 to the inlet of the secondary heat exchanger 34. The opening of leachate regulating valve 27 is controlled by the liquid level in secondary heat exchanger 34.

[0119] The preheated vinasse leachate enters the top tube-side inlet of the second-effect heat exchanger 34. During its downward flow, it is heated by the first-effect flash steam from the first-effect separator 29 for the second effect. After heating, it enters the second-effect separator 35 for the second-effect separation. The second-effect concentrated liquid is sent back to the top tube-side inlet of the second-effect heat exchanger 34 through the second-effect circulation pipe by the second-effect circulation pump 36 for circulation.

[0120] A portion of the second-effect concentrate is fed into the third-effect circulation pipe via the second-effect transfer pipe 37. A second-effect transfer regulating valve 38 is installed on this pipe, and its opening is controlled by the liquid level in the third-effect heat exchanger 39. The second-effect concentrate from the second-effect transfer pipe 37 is fed along with the third-effect concentrate by a third-effect circulation pump 41 to the top tube inlet of the third-effect heat exchanger 39, where it enters the third-effect circulation. As it flows downward, it is heated by the second-effect flash steam from the second-effect separator 35, undergoing third-effect heating. After heating, it enters the third-effect separator 40 for third-effect separation. A portion of the third-effect concentrate is maintained in circulation by the third-effect circulation pump 41, while the remaining portion is fed into the first-effect circulation pipe via the third-effect transfer pipe 42. A third-effect transfer regulating valve 43 is installed on this pipe, and its opening is controlled by the liquid level in the first-effect separator 29.

[0121] The first-effect concentrated liquid is sent to the left inlet of the bottom pipe side of the first-effect heat exchanger 28 by the first-effect circulation pump 30, flows upward first, and is heated by the 100°C steam generated by flash evaporation from the condensate flash tank 20. After reaching the top of the first-effect heat exchanger 28, it turns back and flows downward, and is heated by the 100°C steam again. The first-effect concentrated liquid enters the first-effect separator 29 for flash evaporation and separation, and the first-effect flash steam is used as the heat source of the second-effect heater.

[0122] A portion of the first-effect concentrate from the outlet of the first-effect circulation pump 30 flows through the first-effect outlet pipe 31 into the thick slurry tank 44 for temporary storage. The first-effect outlet pipe 31 is equipped with a thick slurry flowmeter 32 and a thick slurry regulating valve 33. The thick slurry regulating valve 33 adjusts its opening according to the thick slurry flowmeter 32 to control the thick slurry output flow rate at 1.3 tons / hour with a moisture content of 40%. A thick slurry pump 45 delivers 1.3 tons / hour of thick slurry with a moisture content of 40% to the mixer 7, where it is mixed evenly with the fermented lees and returned dried lees. The mixture then flows into the tube bundle dryer 8 for drying, completely recovering all nutrients from the lees filtrate and lees permeate.

[0123] A portion of the high-temperature washing water delivered by the washing circulation pump is sent to the leachate tank 25 as its makeup water or cleaning water.

[0124] The condensed water discharged from the bottom of the shell side of the first-effect heat exchanger 28 enters the shell side of the second-effect heat exchanger 34 through a U-shaped tube for flash evaporation. The condensed water discharged from the bottom of the shell side of the second-effect heat exchanger 34 enters the bottom of the shell side of the third-effect heat exchanger 39 through a U-shaped tube. The condensed water discharged from the bottom of the shell side of the third-effect heat exchanger 39 enters the dirty condensed water tank 51 for collection and is sent to the sewage treatment station 53 for treatment by the sewage transfer pump 52.

[0125] The non-condensable gases and evaporated water vapor in the shell side of the first-effect heat exchanger 28, the second-effect heat exchanger 34, and the third-effect heat exchanger 39 are discharged from the vacuum ports of their respective shell sides, enter the shell side of the condenser 54 through a common vacuum pipe, are cooled by the cooling water in the tube side, and are then pumped out by the vacuum pump 55 to maintain the negative pressure of the evaporation system.

[0126] The exhaust gas from the top of the triple-effect separator 40 and the waste condensate tank 51 also enters the shell side of the condenser 54 to maintain the vacuum. The condensate discharged from the bottom of the shell side of the condenser 54 is collected in the waste condensate tank 51. The tube side of the condenser 54 is provided with circulating cooling water by a cooling tower 56 and its cooling water pump 57.

[0127] The tubes of the first-effect heat exchanger 28, the second-effect heat exchanger 34 and the third-effect heat exchanger 39 are prone to scaling. To ensure stable and continuous operation of the system, they need to be cleaned regularly. This system is provided with an alkali liquid tank 47. Fresh sodium hydroxide solution enters the alkali liquid tank 47 through the alkali liquid supply pipe 48, is pumped out by the alkali liquid pump 49, and is respectively sent to the first-effect separator 29, the second-effect separator 35, the third-effect separator 40 and the thick slurry tank 44 through the alkali liquid cleaning pipe 50. Then, it enters the pipe process of the first-effect heat exchanger 28, the second-effect heat exchanger 34 and the third-effect heat exchanger 39 to clean the inner wall of the heat exchange tube. At the same time, it also enters the first-effect circulation pipe, the second-effect circulation pipe and the third-effect circulation pipe. The first-effect circulation pump 30, the second-effect circulation pump 36 and the third-effect circulation pump 41 can be turned on to strengthen the circulation of alkali liquid. The first to third effects are communicated with each other through the second-effect transfer pipe 37 and the third-effect transfer pipe 42, and return to the alkali liquid tank 47 through the first-effect liquid outlet pipe 31 to realize the circulation of alkali liquid until the dirt is cleaned, so as to improve the heat exchange efficiency and ensure the smooth flow of the process.

[0128] The above description is only a preferred embodiment of the present invention, which shows and describes the basic principles, main features and advantages of the present invention, but does not limit the scope of patent protection of the present invention. Those skilled in the art should understand that the present invention is not limited by the above embodiments. In addition to the above embodiments, the present invention may have other implementation modes without departing from the spirit and scope of the present invention. The present invention may also have various changes and improvements, and all technical solutions formed by equivalent replacement or equivalent transformation fall within the scope of protection required by the present invention. The scope of protection required by the present invention is defined by the attached claims and their equivalents. Technical features not described in the present invention can be achieved by or using existing technologies, and will not be described here.

Claims

1. A white wine lees fermentation system for comprehensive resource utilization, comprising a fermentation feed conveyor and a rotary arm fermentation machine, wherein the outlet of the fermentation feed conveyor feeds the feed chute of the rotary arm fermentation machine, characterized in that: The inlet of the fermentation feed conveyor is connected to the outlet of the lees squeezer and the bacterial powder adding device. The lees filtrate and lees leachate separated by the lees squeezer are mixed evenly with the fermented lees discharged from the rotary arm fermentation machine after passing through the leachate evaporation and concentration unit, and then enter the tube bundle dryer for drying. The upper end of the rotating arm fermentation machine is provided with a rotating arm extending along a radius, a discharging auger is installed on the front edge of the rotating arm, a material distribution auger is installed below the axis of the rotating arm, the discharging auger is lower than the material distribution auger by a certain height, and a plurality of downwardly extending material turning auger are installed on the rear edge of the rotating arm; The feeding auger distributes the material to the peripheral area. When the material layer reaches the bottom of the discharging auger, the feeding stops and the fermentation begins. During the fermentation process, the rotating arm keeps rotating and each turning auger keeps stirring. After the scheduled fermentation time is reached, the feeding auger starts again to spread the new material that has not been inoculated with bacterial powder on top of the old material layer, so that the material layer rises to the bottom of the feeding auger; after the new material enters, it is mixed evenly with the old material under the stirring of the feeding auger, and the inoculation of the new material is automatically completed; The arm rotates one circle and completes a round of fermentation while spreading the material. At this time, the discharging auger and the spreading auger operate synchronously. The discharging auger discharges the material layer on the top, and then the spreading auger adds new material to the original height. Then each turning auger continues to stir and inoculate, and the cycle continues.

2. The white wine lees fermentation system for comprehensive resource utilization according to claim 1, characterized in that: The raw steam releases heat in the tube bundle dryer and becomes high-temperature condensed water. The high-temperature condensed water enters the condensed water flash tank and flash evaporates to generate secondary steam which serves as the heat source for the leachate evaporation and concentration unit.

3. The white wine lees fermentation system for comprehensive resource utilization according to claim 2, characterized in that: The hot air discharged from the top of the tube bundle dryer enters the cyclone dust collector for dust removal, and then enters the waste heat absorption tower to be washed and heat-exchanged layer by layer by hot water. The heated washing circulating water enters the hot side of the secondary waste heat exchanger and the primary waste heat exchanger in turn to heat the circulating preheated water on the cold side. The fresh air sent by the blower is preheated in sequence by the first-stage air preheater, the second-stage air preheater and the third-stage air preheater, and then sent to the bottom of the material bed of the rotary arm fermenter, and passes upward through the material layer to realize aerobic fermentation; The circulating preheated water sequentially enters the hot sides of the secondary air preheater and the primary air preheater to perform two-stage preheating of the fresh air.

4. The white wine lees fermentation system for comprehensive resource utilization according to claim 3, characterized in that: The high-temperature condensed water discharged from the condensed water flash tank enters the hot side of the three-stage air preheater to perform the third-stage preheating of the fresh air.

5. The white wine lees fermentation system for comprehensive resource utilization according to claim 4, characterized in that: The lees filtrate squeezed out by the lees squeezer and the lees leachate generated by the accumulation of raw lees are collected in a leachate tank, pumped out by a leachate pump, and sent to the cold side of a plate heat exchanger. The lees leachate is preheated by the medium-temperature condensed water discharged from the hot side of the three-stage air preheater. The low-temperature condensed water discharged from the hot side of the plate heat exchanger is collected in a condensed water tank and pumped into the top cover of the rotary arm fermenter by a low-temperature condensed water pump for circulation and heating. The excess low-temperature condensed water is used as boiler feed water.

6. The white wine lees fermentation system for comprehensive resource utilization according to claim 2, characterized in that: The leachate evaporation and concentration unit includes a single-effect heat exchanger, a double-effect heat exchanger, and a triple-effect heat exchanger, and the bottoms of the single-effect to triple-effect heat exchangers are connected to single-effect to triple-effect separators respectively; The preheated lees percolate enters the tube side of the second-effect heat exchanger and is heated in the second effect by the first-effect flash steam from the first-effect separator. The second-effect concentrate enters the second-effect separator for separation and is partially fed into the third-effect circulation pipe through the second-effect transfer pipe. The flash steam from the second-effect separator enters the shell side of the third-effect heat exchanger to perform third-effect heating on the third-effect concentrate. The triple-effect concentrated liquid enters the triple-effect separator for separation and is partially sent to the single-effect circulation pipe through the triple-effect transfer pipe. The flash steam generated by the condensed water flash tank enters the shell side of the single-effect heat exchanger to heat the single-effect concentrated liquid. The single-effect concentrated liquid enters the single-effect separator for flash evaporation.

7. The white wine lees fermentation system for comprehensive resource utilization according to claim 6, characterized in that: Part of the first-effect concentrated liquid enters the thick slurry tank through the first-effect liquid outlet pipe for temporary storage, is sent to the mixer by the thick slurry pump, and is evenly mixed with the fermented vinasse and the returned dry vinasse, and then enters the tube bundle dryer for drying.

8. The white wine lees fermentation system for comprehensive resource utilization according to claim 6, characterized in that: The alkali liquid pump extracts the cleaning alkali liquid from the alkali liquid tank and sends it to the first-effect separator, second-effect separator, third-effect separator and thick slurry tank respectively to clean the first to third-effect evaporation devices and thick slurry tank. The cleaned alkali liquid returns to the alkali liquid tank through the first-effect liquid outlet pipe for circulation.

9. The white wine lees fermentation system for comprehensive resource utilization according to claim 3, characterized in that: An absorption tower circulation water inlet pipe is provided on the upper side wall of the waste heat absorption tower, and the inner end of the absorption tower circulation water inlet pipe extends to the axis of the absorption tower and turns downward. A multi-component water tray and a tower tray are provided below the inner end of the absorption tower circulation water inlet pipe. The water distribution tray is dome-shaped, and the opening of the tower tray is upward and fixed to the inner wall of the waste heat absorption tower. The center hole of the tower tray is covered by the water distribution tray above. The absorption tower circulating hot water is sprinkled on the center of the water distribution tray, falls from the outer periphery of the water distribution tray into the tower tray of the next layer, continues to fall from the circumferential edge of the center hole of the tower tray, sprinkles on the circumference of the water distribution tray of the next layer, splashes and continues to fall from the circumference of the water distribution tray into the tower tray of the next layer, and so on; the hot air goes up along the center hole of the tower tray, and then continues to flow from the outer periphery of the water distribution tray to the center hole of the upper tower tray, realizing reverse heat exchange washing of hot air and water.

10. The white wine lees fermentation system for comprehensive resource utilization according to claim 1, characterized in that: The wine lees squeezing machine comprises a coaxial screen frame and an extrusion shaft, wherein the extrusion shaft passes through the screen frame and is wound with spiral blades on its outer circumference; The screen frame includes a fixed screen frame and a movable screen frame. A feed port is provided above the inlet end of the fixed screen frame. The inlet end of the movable screen frame is nested in the outer periphery of the terminal end of the fixed screen frame and can be axially translated. A guide plate is connected below the outlet end of the movable screen frame. The terminal end of the guide plate extends above the discharge port. The closer to the feed port, the smaller the diameter of the extrusion shaft. The outer periphery of the two ports of the movable screen frame is respectively fixed with a screen frame support plate, and the two sides of the screen frame support plate are respectively fixed with a guide sleeve, and the guide sleeves on the same side are respectively sleeved on the guide rods, and the two guide rods are parallel to the axis of the extrusion shaft and the two ends are respectively fixed to the machine base or the ground through the guide rod supports; Both ends of the screen frame support plate near the discharge port are driven by hydraulic push rods respectively. The roots of the two hydraulic push rods are respectively hinged on the push rod hinge ears, and the bottoms of the push rod hinge ears are respectively fixed on the machine base.

11. A method for fermenting distiller's grains with comprehensive resource utilization, characterized in that: The white wine lees fermentation system according to claim 8 comprises the following steps in sequence: S1, the raw material distiller's grains are squeezed dry by the distiller's grains squeezer, evenly inoculated with bacterial powder and enter the feed chute of the rotary arm fermentation machine; S2. The wet distiller's grains from the feed chute fall into the center of the material bed. When the inoculated distiller's grains reach the highest position, the rotating arm of the fermenter drives the distribution auger, the discharge auger and the turning auger to rotate continuously. S3, the feeding auger starts to feed the material to the peripheral area. When the material layer reaches the bottom of the discharging auger, the feeding stops and the fermentation begins. During the fermentation process, the rotating arm keeps rotating and each turning auger continues to stir. S4. After the scheduled fermentation time is reached, the feeding auger is started, and the new material that has not been inoculated with bacterial powder is spread on the top of the old material layer, so that the material layer is raised to the bottom of the feeding auger; after the new material enters, it is mixed evenly with the old material under the stirring of the feeding auger, and the inoculation of the new material is automatically completed; S5. The arm rotates one circle, and a round of fermentation is completed while spreading the material. At this time, the discharging auger and the spreading auger operate synchronously. The discharging auger discharges the material layer on the top, and then the spreading auger adds new material to the original height. Each turning auger continues to stir and inoculate, and the cycle continues.

12. The method for fermenting distiller's grains for comprehensive resource utilization according to claim 11, characterized in that: The fermented vinasse discharged from the rotary arm fermentation machine, the returned dry fermented vinasse and the vinasse concentrate are mixed together in a mixer and then dried in a tube bundle dryer; The exhaust gas from the tube bundle dryer enters the waste heat absorption tower after cyclone dust removal, and is washed and heat-exchanged by the circulating hot water in the absorption tower. The circulating hot water in the absorption tower serves as the hot side of the waste heat heat exchanger to heat the preheating circulating water on the hot side of the air preheater. The preheating circulating water sequentially preheats the air on the cold side of the secondary air preheater and the primary air preheater.

13. The method for fermenting distiller's grains for comprehensive resource utilization according to claim 12, characterized in that: The high-temperature condensed water discharged from the tube bundle dryer enters the condensed water flash tank for flash evaporation, and the secondary steam generated by the flash evaporation serves as the heat source of the leachate evaporation and concentration unit; the medium-temperature condensed water discharged from the condensed water flash tank enters the hot side of the three-stage air preheater to perform three-stage preheating on the air after the second-stage preheating, and the hot air after the three-stage preheating enters the bottom of the material layer of the rotary arm fermenter to provide the air required for fermentation.

14. The method for fermentation of distiller's grains for comprehensive resource utilization according to claim 13, characterized in that: The lees leachate discharged from the raw lees and the lees filtrate discharged from the lees squeezer are collected together in a leachate tank. The lees leachate is preheated by the low-temperature condensed water discharged from the hot side of the three-stage air preheater and then sent to the leachate evaporation and concentration unit for evaporation and concentration. The obtained lees concentrate is sent to the mixer.

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