Oil wet meal desolventizing and evaporating device and technology

Abstract

The invention relates to the technical field of oil processing, in particular to an oil wet meal desolventizing and evaporating device and process, which comprises a DTDC desolventizing machine, and the DTDC desolventizing machine comprises a desolventizing layer and a drying layer; an inlet of the desolventizing layer is communicated with a water-vapor-free outlet of the independent steam production unit, and a dead steam outlet of the independent steam production unit is communicated with an inlet of the low-pressure dead steam recycling unit; an inlet of the drying layer is communicated with an air outlet of the environment-friendly gas circulating unit, an outlet of the drying layer is communicated with an inlet of the meal trapping unit, and a steam outlet of the low-pressure dead steam recycling unit is communicated with the inlet of the drying layer. Through redesign and optimization of an existing oil wet meal desolventizing and hot air drying process route and structural improvement of part of equipment, the steam utilization rate is increased, the surrounding environment is improved, cost is saved for enterprises, and benefits are improved.

Description

Technical Field

[0001] The invention relates to the technical field of oil processing, and in particular to an oil wet meal desolventizing and evaporating device and process. Background Art

[0002] Wet meal refers to oil that contains residual organic solvents and water after leaching and oil extraction. Wet meal is a high-protein raw material and is widely used as a raw material for feed, food, fertilizer and antibiotics. Since wet meal contains a certain amount of organic solvents, harmful toxins and anti-nutritional components, in order to reduce production costs, ensure the safety of meal during transportation, storage and use, and improve the quality of meal, it is usually necessary to desolventize, bake, dry and cool the wet meal. The solvent is removed from the defatted wet meal through desolventization and the solvent is recycled and reused; the anti-nutritional components in the wet meal are passivated through baking; the water content of the wet meal is reduced through drying; and the temperature of the meal is reduced to close to the ambient temperature through cooling to facilitate storage and transportation. DTDC degassing machine is a key equipment for processing wet meal in vegetable oil processing plants. This equipment integrates desolventizing, drying and cooling, and has the advantages of simple operation and stable product quality. However, there are problems such as large steam consumption in the desolventizing layer and leakage of oil meal from the hot air drying layer outlet pipe equipped with a shackle. This not only increases energy consumption and causes waste of resources, but also seriously affects the plant and surrounding environment.

[0003] In addition, the desolventizing layer of the DTDC desolventizer uses direct steam containing water and non-condensable gas, which will also lead to a decrease in the heating efficiency of steam-using equipment, and the accumulation of water and air inside the equipment will greatly reduce the effective heat exchange area and production capacity of the equipment. The water content of steam will increase the agglomeration of soybean meal, and the steam of agglomerated soybean meal is not suitable for blowing through, and the solvent inside is not suitable for steaming out, which will eventually cause the solvent in the meal to exceed the standard seriously. At the same time, overheating of steam will cause a cliff-like drop in the heat exchange efficiency of the equipment. Summary of the invention

[0004] Aiming at the technical problems that the desolventizing layer of the existing DTDC desolventizer has large steam consumption, low heating efficiency, and oil meal dust in the drying layer escapes, the present invention provides an oil wet meal desolventizing and evaporating device and process, by arranging an independent steam production unit, a low-pressure exhaust steam recycling unit, an environmentally friendly gas circulation unit and a meal dust capturing unit outside the desolventizing layer and the drying layer of the DTDC desolventizer, the steam and air inside the oil wet meal desolventizing and evaporating device are recycled, the steam utilization rate and the heating efficiency of the desolventizing layer are improved, the oil meal dust in the drying layer is effectively prevented from escaping, the surrounding environment is improved, the cost is saved and the energy consumption is reduced.

[0005] In a first aspect, the present invention provides an oilseed wet meal desolventizing and evaporating device, comprising a DTDC desolventizing machine, the DTDC desolventizing machine comprising a desolventizing layer and a drying layer, the desolventizing layer being located above the drying layer; The inlet of the desolvation layer is connected to the water-free steam outlet of the independent steam production unit, the exhaust steam outlet of the independent steam production unit is connected to the inlet of the low-pressure exhaust steam recycling unit, the outlet of the low-pressure exhaust steam recycling unit is connected to the inlet of the independent steam production unit, and the inlet of the independent steam production unit is connected to the condensed water source; The inlet of the drying layer is connected to the air outlet of the environmentally friendly gas circulation unit, the outlet of the drying layer is connected to the inlet of the meal fines collection unit, the air outlet of the meal fines collection unit is connected to the inlet of the independent steam production unit, the air outlet of the independent steam production unit is connected to the air inlet of the environmentally friendly gas circulation unit, and the exhaust steam outlet of the environmentally friendly gas circulation unit is connected to the inlet of the low-pressure exhaust steam recycling unit; The steam outlet of the low-pressure exhaust steam recycling unit is connected with the inlet of the drying layer.

[0006] Furthermore, the independent steam production unit includes a falling film evaporator, the falling film evaporator is connected to a steam ejector, and the steam ejector is connected to a steam-water separator, wherein the inlet of the falling film evaporator is connected to a condensate water source, a circulating pump is arranged between the falling film evaporator and the condensate water source, the condensate is pumped from the condensate water source to the falling film evaporator for heating to generate low-temperature steam, the steam ejector continuously takes the low-temperature steam away from the falling film evaporator, so that the working chamber of the falling film evaporator becomes a negative pressure state, thereby generating low-temperature, low-pressure steam; the steam ejector is connected to a high-pressure steam source, and the high-pressure steam is introduced into the independent steam production unit, the high-pressure steam from the high-pressure steam source is mixed with the low-temperature, low-pressure steam to obtain medium-pressure steam, and the medium-pressure steam becomes a desolvation heat source; the steam after desolvation is discharged from the outlet of the desolvation layer and can be further recovered for heat utilization. The anhydrous steam outlet of the steam-water separator is connected to the inlet of the desolventizing layer. Using anhydrous steam for desolventizing can reduce the internal water accumulation of the DTDC desolventizing machine. The independent steam production unit discharges the exhaust steam, which is beneficial to reduce the internal air accumulation of the DTDC desolventizing machine and improve the heating efficiency and desolventizing efficiency. The exhaust steam outlet of the steam-water separator is connected to the inlet of the low-pressure exhaust steam recycling unit.

[0007] Furthermore, the low-pressure exhaust steam recycling unit includes a steam-water separation tank, which is connected to a condensate tank, which is connected to a hot water tank, wherein the inlet of the steam-water separation tank is connected to the exhaust steam outlet of the steam-water separator, the exhaust steam discharged from the steam-water separator enters the steam-water separation tank for steam-water separation, and the obtained condensed water is condensed in the condensate tank and the hot water tank in turn, the condensate tank provides condensate for the environmentally friendly gas circulation unit, the outlet of the hot water tank is connected to the inlet of the falling film evaporator, the hot water tank provides condensate for the falling film evaporator, and the steam outlet of the hot water tank is connected to the inlet of the drying layer.

[0008] Furthermore, the environmentally friendly gas circulation unit includes a blower, which is connected to at least two hot air heaters. The hot air heaters can be connected in parallel or in series as needed, wherein the blower is provided with a damper, which is connected to the air inlet of the blower through a main air inlet duct, the air inlet of the blower is connected to the air outlet of the falling film evaporator, the hot air heater is connected to the drain port of the condensate tank, and the condensate tank can be heated by the hot air heater; the air outlet of the hot air heater is connected to the inlet of the drying layer, the exhaust steam outlet of the hot air heater is connected to the inlet of the steam-water separation tank, the exhaust steam enters the low-pressure exhaust steam recycling unit from the inlet of the steam-water separation tank and can be converted into condensate and / or low-temperature steam to avoid overheating of the steam.

[0009] Furthermore, the meal dust collection unit includes a first cyclone dust collector, the first cyclone dust collector is connected to the second cyclone dust collector, the first cyclone dust collector and the second cyclone dust collector can be connected in parallel or in series, the second cyclone dust collector is connected to the dry collector, and the dry collector is connected to the sedimentation box, wherein the inlet of the first cyclone dust collector is connected to the outlet of the drying layer, the air outlet of the dry collector is connected to the inlet of the falling film evaporator, and the falling film evaporator can use the hot air discharged from the dry collector to circulate and heat the condensed water.

[0010] Furthermore, a first film-distributing device is arranged at the upper part of the falling film evaporator, and a coil opening type liquid inlet device, a first bubble cap type distributor, a first disc type distributor and a first plug cone type distributor are arranged in sequence from top to bottom in the first film-distributing device; a second film-distributing device is arranged at the middle part of the falling film evaporator, and a second bubble cap type distributor, a second disc type distributor and a second plug cone type distributor are arranged in sequence from top to bottom in the second film-distributing device. Both the first disc type distributor and the second disc type distributor are annular tubes, and sieve holes are arranged below the annular tubes.

[0011] Furthermore, the coil perforated liquid inlet device is connected to the inlet of the falling film evaporator through the liquid inlet pipe, the first plug cone distributor and the second plug cone distributor both include a cone distributor, the inlet end of the cone distributor is fixedly connected to the lower liquid distribution plate through an adjustable structure, and the outlet end of the cone distributor is inserted into the heat exchange tube, and the heat exchange tube is located below the lower liquid distribution plate. Furthermore, the condensed water source comes from a pretreatment workshop and / or a leaching workshop.

[0012] Furthermore, the DTDC degassing machine, independent steam production unit, low-pressure exhaust steam recycling unit, environmentally friendly gas circulation unit, and meal capture unit are all connected to the automatic control system.

[0013] In a second aspect, the present invention further provides a process for desolventizing and evaporating using the above-mentioned oilseed wet meal desolventizing and evaporating device, comprising the following steps: Step 1: First, the condensed water is introduced into an independent steam production unit to obtain low-pressure steam with a pressure of 0.2-0.3 MPa, and then high-pressure steam with a pressure of 0.8-0.9 MPa is introduced into the independent steam production unit to mix with the low-pressure steam to obtain mixed steam, and the mixed steam is separated into water-free steam and exhaust steam after steam-water separation; Step 2: Desolventizing the soluble soybean meal with anhydrous steam to obtain high-temperature wet meal and discharge the soluble steam, which can be recovered and processed separately; Step 3: passing air into an environmentally friendly gas circulation unit to prepare hot air and exhaust steam, using the hot air to dry the high-temperature wet meal in the drying layer to obtain oil meal and discharge the hot air containing the meal; The exhaust steam in step 1 and the exhaust steam in step 3 are introduced into a low-pressure exhaust steam recycling unit to prepare secondary condensed water and secondary hot air, the secondary condensed water enters an independent steam production unit and / or an environmentally friendly gas circulation unit for recycling, and the secondary hot air enters a drying layer to dry the high-temperature wet meal; The hot air containing meal in step three is processed by the meal collecting unit and then enters the independent steam production unit for recycling.

[0014] The beneficial effects of the present invention are: The oil-wet meal desolventizing and evaporating device and process provided by the present invention utilize an independent steam production unit to prepare water-free steam for desolventizing and separate exhaust steam, thereby improving the heating efficiency and desolventizing efficiency of the DTDC desolventizer; utilize an environmentally friendly gas circulation unit to heat air and gas discharged from the independent steam production unit for drying and separate exhaust steam, thereby improving the gas utilization rate inside the oil-wet meal desolventizing and evaporating device and improving the drying efficiency; utilize a meal dust capture unit to recover meal dust remaining in meal-containing hot air, then remove moisture from the hot air after removing the meal dust in the independent steam production unit, then re-introduce the hot air into the environmentally friendly gas circulation unit for heating and drying again, thereby reducing the amount of external air introduced and improving the waste heat utilization rate; the present invention also uses a low-pressure exhaust steam circulation unit to separate steam and water from the exhaust steam, thereby avoiding the reduction of heat exchange efficiency due to overheating of the exhaust steam and improving the moisture utilization rate in the exhaust steam.

[0015] The invention increases steam utilization, improves the surrounding environment, saves costs for enterprises and improves benefits by redesigning and optimizing the existing oilseed wet meal desolventizing and hot air drying process routes and improving the structure of some equipment. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, for ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0017] Figure 1 It is a schematic diagram of the connection relationship of the oilseed wet meal desolventizing energy-saving and consumption-reducing evaporation device of Example 1.

[0018] Figure 2 It is a bottom view of the first disc distributor and the second disc distributor of Example 1.

[0019] Figure 3 It is a schematic diagram of the structure of the first plug-cone distributor and the second plug-cone distributor of Example 1.

[0020] In the figure, 1-independent steam production unit, 2-low-pressure exhaust steam recycling unit, 3-environmentally friendly gas circulation unit, 4-meal collecting unit, 5-lower liquid distribution tray, 6-tube sheet, 7-heat exchange tubes, 8-falling film evaporator, 9-steam ejector, 10-steam-water separator, 11-desolventization layer, 12-steam-water separation tank, 13-condensate tank, 14-hot water tank, 15-damper, 16-blower, 17-first hot air heater, 18-second hot air heater, 19-drying layer, 20-first cyclone dust collector, 21-second cyclone dust collector, 22-dry collector, 23-sedimentation box. DETAILED DESCRIPTION

[0021] In order to enable those skilled in the art to better understand the technical solutions in the present invention, the technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work should fall within the scope of protection of the present invention.

[0022] Example 1 A device for desolventizing and evaporating wet meal of oilseeds, such as Figure 1As shown, it includes an independent steam production unit 1, which includes a falling film evaporator 8. The inlet of the falling film evaporator 8 is connected to a condensed water source, and the condensed water source comes from a pretreatment workshop and / or a leaching workshop. A circulating pump (not shown in the figure) is arranged between the falling film evaporator 8 and the condensed water source. The steam outlet of the falling film evaporator 8 is connected to the low-pressure inlet of the steam ejector 9, and the high-pressure inlet of the steam ejector 9 is connected to a high-pressure steam source. The mixer outlet of the steam ejector 9 is connected to the inlet of the steam-water separator 10. The steam-water separator 10 is provided with a water-free steam outlet and an exhaust steam outlet. The water-free steam outlet of the steam-water separator 10 is connected to the inlet of the desolventizing layer 11 of the DTDC desolventizer, and the exhaust steam outlet of the steam-water separator 10 is connected to the inlet of the steam-water separation tank 12 in the low-pressure exhaust steam recycling unit 2. The outlet of the steam-water separation tank 12 is connected to the inlet of the condensed water tank 13, and the outlet of the condensed water tank 13 is connected to the hot water tank 14. The inlet of the condensed water tank 13 is connected, the discharge port of the condensed water tank 13 is connected to the first hot air heater 17 and the second hot air heater 18 respectively, and a power pump (not shown in the figure) is respectively arranged on the pipeline between the discharge port of the condensed water tank 13 and the first hot air heater 17 and the pipeline between the discharge port of the condensed water tank 13 and the second hot air heater 18. The outlet of the hot water tank 14 is connected to the inlet of the falling film evaporator 8, and the steam outlet of the hot water tank 14 is connected to the inlet of the drying layer 19 of the DTDC degassing machine. The desolvation layer 11 of the DTDC degassing machine is located above the drying layer 19. Among them, as Figure 2-3 As shown, a first film-distributing device is arranged at the upper part of the falling film evaporator 8, and a coil opening type liquid inlet device, a first bubble cap type distributor, a first disk type distributor and a first plug cone type distributor are arranged in sequence from top to bottom in the first film-distributing device; a second film-distributing device is arranged at the middle part of the falling film evaporator 8, and a second bubble cap type distributor, a second disk type distributor and a second plug cone type distributor are arranged in sequence from top to bottom in the second film-distributing device. The coil open hole type liquid inlet device is connected with the inlet of the falling film evaporator 8 through the liquid inlet pipe. The first plug cone type distributor and the second plug cone type distributor are both provided with a lower liquid distribution pan 5 and a tube sheet 6 from top to bottom in sequence. The lower liquid distribution pan 5 is provided with a plurality of tube sheet tube holes and liquid distribution holes. The liquid distribution holes are annularly distributed on the periphery of the tube sheet tube holes. The inlet end of the cone distributor passes through the tube sheet tube holes. The inlet end of the cone distributor is fixed in the tube sheet tube holes through an adjustable structure. A thread is provided on the outer side of the cone distributor. The adjustable structure is an upper nut and a lower nut. The upper nut is located above the lower liquid distribution pan 5, and the lower nut is located below the lower liquid distribution pan 5. The upper nut and the lower nut are both threadedly connected with the cone distributor. The height of the cone distributor can be adjusted by using the upper nut and the lower nut. The outlet end of the cone distributor is a conical structure with a small top and a large bottom. The outlet end of the cone distributor passes downward and extends to the bottom of the tube sheet 6. The outlet end of the cone distributor is inserted into the heat exchange tube 7, and the heat exchange tube 8 is fixed below the tube sheet 6.

[0023] The oilseed wet meal desolventizing and evaporating device also includes an environmentally friendly gas circulation unit 3, which includes a blower 16. The blower 16 is provided with a damper 15. The damper 15 is connected to the air inlet of the blower 16 through the main air inlet duct. The damper 15 is connected to the air outlet of the falling film evaporator 8. The air outlet of the blower 16 is respectively connected to the inlet of the first hot air heater 17 and the inlet of the second hot air heater 18. The outlet of the first hot air heater 17 and the outlet of the second hot air heater 18 are connected to the inlet of the drying layer 19. The exhaust steam outlet of the first hot air heater 17 and the exhaust steam outlet of the second hot air heater 18 are respectively connected to the inlet of the steam-water separation tank 12. The outlet of the drying layer 19 is connected to the inlet of the first cyclone dust collector 20, the outlet of the first cyclone dust collector 20 is connected to the inlet of the second cyclone dust collector 21, the outlet of the second cyclone dust collector 21 is connected to the inlet of the dry collector 22, the outlet of the dry collector 22 is connected to the inlet of the sedimentation box 23, and the dry collector 22 is also provided with an air outlet, and the air outlet of the dry collector 22 is connected to the inlet of the falling film evaporator 8.

[0024] The DTDC degassing machine, the independent steam production unit 1, the low-pressure exhaust steam recycling unit 2, the environmentally friendly gas circulation unit 3, and the meal capture unit 4 are all connected to the automatic control system.

[0025] Example 2 A process for desolventizing and evaporating the oilseed wet meal desolventizing and evaporating device according to Example 1 comprises the following steps: Step 1: First, the condensed water is introduced into an independent steam production unit to obtain low-pressure steam with a temperature of 90-95°C and a pressure of 0.2-0.3MPa, and then high-pressure steam with a temperature of 185°C and a pressure of 0.8-0.9MPa is introduced into the independent steam production unit to mix with the low-pressure steam to obtain mixed steam. After steam-water separation, the mixed steam is obtained to obtain anhydrous steam and exhaust steam. The temperature of the anhydrous steam is 145°C, and the pressure of the anhydrous steam is 0.4MPa. Step 2: The pre-desolventized soybean meal is transported to the desolventizing layer and stays there for 25 minutes. The temperature of the soybean meal is 67°C, the solvent content is 19wt%, and the moisture content is 13wt%-14wt%. During the stay, anhydrous steam is sprayed from the pores of the bottom plate of the desolventizing layer into the soybean meal to desolventize, and a high-temperature wet meal with a temperature of 100-105°C is obtained and the solvent-containing steam is discharged. The diameter of the bottom plate pores is 3mm, the solvent content of the high-temperature wet meal is 500mg / kg, and the moisture content is 17wt%-18wt%. During the desolventizing process, the anhydrous steam is in countercurrent contact with the soybean meal. Since the anhydrous steam and the soybean meal are in dynamic contact, the soybean meal provides a large amount of heat and mass transfer surfaces, which can prevent short circuit and bridging phenomena, ensure reasonable time and distance to achieve steam-meal mass and heat transfer, fully passivate urease activity, and ensure the lowest denaturation of water-soluble protein, and less anhydrous steam. The steam containing the solvent can be recovered and processed separately.

[0026] Step 3: After the high-temperature wet meal is transported to the drying layer, the air is passed into the environmentally friendly gas circulation unit to prepare hot air and exhaust steam with a temperature of 85-90°C. After the hot air enters the drying layer from the air inlet, it is sprayed into the fluidized high-temperature wet meal from the bottom plate spray hole of the drying layer to dry the high-temperature wet meal, obtain the oil meal and discharge the hot air containing the meal. The moisture content of the oil meal is 14wt%-15wt%, the temperature of the oil meal is 50-55°C, and the aperture of the bottom plate spray hole is 6mm. During the drying process, the moisture in the high-temperature wet meal is vaporized by heat and diffused from the surface of the high-temperature wet meal into the hot air, the meal temperature drops, the moisture in the meal decreases, and the hot air takes away the moisture to achieve drying. The temperature of the hot air containing the meal is 105-110°C, the moisture content is 30wt%, and the meal content is 0.5wt%.

[0027] The hot air containing meal is subjected to the first solid-gas separation in the first cyclone dust collector, and then enters the second cyclone dust collector for the second solid-gas separation, and then enters the dry collector for the third solid-gas separation to obtain the hot air de-mealed. The meal recovered by the dry collector enters the settling box, and the hot air de-mealed enters the falling film evaporator, and the temperature is reduced to 75℃ after being indirectly heated by condensed water. Then, it is sent to the first hot air heater and the second hot air heater by the blower through the circulating air duct, and is heated to 85-90℃ by condensed water before re-entering the drying layer for drying.

[0028] All exhaust steam from the pretreatment and leaching workshops is collected through pipelines and first passed through a steam-water separator for steam-water separation to obtain low-pressure steam at 95°C and secondary condensate. The low-pressure steam is mixed with the low-pressure steam prepared by the falling film evaporator and the high-pressure steam with a temperature of 185°C and a pressure of 0.85MPa introduced by the steam ejector to generate medium-pressure steam with a temperature of 145°C and a pressure of 0.4MPa. The medium-pressure steam enters the steam-water separator for steam-water separation and is sent to the steam stripping layer for desolventizing after water removal.

[0029] The exhaust steam separated by the gas-liquid separator is sent back to the gas-liquid separation tank for recycling. The secondary condensed water separated by the gas-liquid separation tank flows into the condensed water tank for temporary storage. After the condensed water pump is used to pump part of the secondary condensed water in the condensed water tank into the hot water tank for temporary storage, it is pumped into the falling film evaporator by the hot water pump and circulated and heated by the circulating pump. The circulation volume is 80m³ / h. The temperature of the secondary condensed water before entering the falling film evaporator is 70℃. It is heated to 95℃ flash gas under the condition of -228kpa of circulating working pressure in the falling film evaporator, and enters the steam ejector through the pipeline to mix with high-pressure steam. The excess secondary condensed water overflows back to the hot water tank for recycling.

[0030] Through the interlocking of the wind temperature entering the first hot air heater and the second hot air heater with the steam intake volume, the interlocking of the valve opening of the condensate pipe entering the falling film evaporator with the low liquid level of the lower shell, the interlocking of the low-pressure gas pressure of the gas-liquid separation tank with the valve opening, the interlocking of the valve opening of the hot water tank with the minimum liquid level of the hot water tank, and the interlocking of the high-pressure steam valve with the steam inlet pressure of the falling film evaporator, the above multiple interlocking controls run automatically and do not require manual operation.

[0031] The process of this embodiment is applied to a production line with 1000t of wet oilseed meal / d, and 3wt% of the moisture in the wet oilseed meal can be removed per hour, reducing heat emission by 2.8×10 6 KJ, among which, the heat utilization rate of the independent steam production unit is as high as over 60%, reducing heat loss by at least 1.68×10 6 KJ, the recovered heat is not less than 40.32×10 6 KJ; Under negative pressure working conditions, the generation of low-pressure steam is 15-25kg / t oilseed wet meal.

[0032] Although the present invention has been described in detail with reference to the accompanying drawings and in combination with the preferred embodiments, the present invention is not limited thereto. Without departing from the spirit and essence of the present invention, a person of ordinary skill in the art may make various equivalent modifications or substitutions to the embodiments of the present invention, and these modifications or substitutions shall be within the scope of the present invention. Any person of ordinary skill in the art may easily think of changes or substitutions within the technical scope disclosed by the present invention, and these shall be within the scope of protection of the present invention.

Claims

1. A device for desolventizing and evaporating wet meal of oilseeds, comprising a DTDC desolventizer, characterized in that: The DTDC degassing machine includes a desolventizing layer and a drying layer, wherein the desolventizing layer is located above the drying layer; The inlet of the desolvation layer is connected to the water-free steam outlet of the independent steam production unit, the exhaust steam outlet of the independent steam production unit is connected to the inlet of the low-pressure exhaust steam recycling unit, the outlet of the low-pressure exhaust steam recycling unit is connected to the inlet of the independent steam production unit, and the inlet of the independent steam production unit is connected to the condensed water source; The inlet of the drying layer is connected to the air outlet of the environmentally friendly gas circulation unit, the outlet of the drying layer is connected to the inlet of the meal fines collection unit, the air outlet of the meal fines collection unit is connected to the inlet of the independent steam production unit, the air outlet of the independent steam production unit is connected to the air inlet of the environmentally friendly gas circulation unit, and the exhaust steam outlet of the environmentally friendly gas circulation unit is connected to the inlet of the low-pressure exhaust steam recycling unit; The steam outlet of the low-pressure exhaust steam recycling unit is connected with the inlet of the drying layer.

2. The oil-wet meal desolventizing and evaporating device according to claim 1, characterized in that: The independent steam production unit includes a falling film evaporator, the falling film evaporator is connected to the steam ejector, the steam ejector is connected to the steam-water separator, wherein the inlet of the falling film evaporator is connected to the condensed water source, the steam ejector is connected to the high-pressure steam source, the water-free steam outlet of the steam-water separator is connected to the inlet of the desolvation layer, and the exhaust steam outlet of the steam-water separator is connected to the inlet of the low-pressure exhaust steam recycling unit.

3. The oil-wet meal desolventizing and evaporating device according to claim 2, characterized in that: The low-pressure exhaust steam recycling unit includes a steam-water separation tank, which is connected to a condensed water tank, which is connected to a hot water tank, wherein the inlet of the steam-water separation tank is connected to the exhaust steam outlet of the steam-water separator, the outlet of the hot water tank is connected to the inlet of the falling film evaporator, and the steam outlet of the hot water tank is connected to the inlet of the drying layer.

4. The oil-wet meal desolventizing and evaporating device according to claim 3, characterized in that: The environmentally friendly gas circulation unit includes a blower, which is connected to at least two hot air heaters, wherein the blower is provided with a damper, the air inlet of the blower is connected to the air outlet of the falling film evaporator, the hot air heater is connected to the drain port of the condensate tank, the air outlet of the hot air heater is connected to the inlet of the drying layer, and the exhaust steam outlet of the hot air heater is connected to the inlet of the steam-water separation tank.

5. The oil-wet meal desolventizing and evaporating device according to claim 2, characterized in that: The meal powder collection unit includes a first cyclone dust collector, the first cyclone dust collector is connected to the second cyclone dust collector, the second cyclone dust collector is connected to the dry collector, and the dry collector is connected to the sedimentation box, wherein the inlet of the first cyclone dust collector is connected to the outlet of the drying layer, and the air outlet of the dry collector is connected to the inlet of the falling film evaporator.

6. The oil-wet meal desolventizing and evaporating device according to claim 2, characterized in that: A first film-distributing device is arranged at the upper part of the falling film evaporator, and a coil opening type liquid inlet device, a first bubble cap type distributor, a first disc type distributor and a first plug cone type distributor are arranged in sequence from top to bottom in the first film-distributing device; a second film-distributing device is arranged at the middle part of the falling film evaporator, and a second bubble cap type distributor, a second disc type distributor and a second plug cone type distributor are arranged in sequence from top to bottom in the second film-distributing device.

7. The oil-wet meal desolventizing and evaporating device according to claim 6, characterized in that: The coil open hole liquid inlet device is connected to the inlet of the falling film evaporator through the liquid inlet pipe. The first plug cone distributor and the second plug cone distributor both include a cone distributor. The inlet end of the cone distributor is fixedly connected to the lower liquid distribution plate through an adjustable structure. The outlet end of the cone distributor is inserted into the heat exchange tubes, and the heat exchange tubes are located below the lower liquid distribution plate.

8. The oilseed wet meal desolventizing and evaporating device according to claim 1, characterized in that: The condensate source comes from the pretreatment plant and / or the leaching plant.

9. The oilseed wet meal desolventizing and evaporating device according to any one of claims 1 to 8, characterized in that: The DTDC degassing machine, independent steam production unit, low-pressure exhaust steam recycling unit, environmentally friendly gas circulation unit, and meal capture unit are all connected to the automatic control system.

10. A process for desolventizing and evaporating oilseed wet meal using the desolventizing and evaporating device according to any one of claims 1 to 8, characterized in that: The steps include: Step 1: First, the condensed water is introduced into an independent steam production unit to obtain low-pressure steam with a pressure of 0.2-0.3 MPa, and then high-pressure steam with a pressure of 0.8-0.9 MPa is introduced into the independent steam production unit to mix with the low-pressure steam to obtain mixed steam, and the mixed steam is separated into water-free steam and exhaust steam after steam-water separation; Step 2: Desolventize the soluble soybean meal using anhydrous steam to obtain high-temperature wet meal and discharge the soluble steam; Step 3: passing air into an environmentally friendly gas circulation unit to prepare hot air and exhaust steam, using the hot air to dry the high-temperature wet meal in the drying layer to obtain oil meal and discharge the hot air containing the meal; The exhaust steam in step 1 and the exhaust steam in step 3 are introduced into a low-pressure exhaust steam recycling unit to prepare secondary condensed water and secondary hot air, the secondary condensed water enters an independent steam production unit and / or an environmentally friendly gas circulation unit for recycling, and the secondary hot air enters a drying layer to dry the high-temperature wet meal; The hot air containing meal in step three is processed by the meal collecting unit and then enters the independent steam production unit for recycling.

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