Energy-saving jet liquefaction system for producing alcohol from starchy raw materials

Abstract

The present invention belongs to the technical field of equipment for producing alcohol from starchy raw materials, and specifically relates to an energy-saving jet liquefaction system for producing alcohol from starchy raw materials, which includes: a mixing screw conveyor, a primary preheating device, a liquefaction preheating system, a jet liquefaction pump, a jet liquefier, a liquefaction system, a liquefied mash cooling system, a saccharification tank, a saccharification liquid cooling system, a saccharification liquid buffer tank, a saccharification liquid high-temperature pump, a saccharification liquid low-temperature pump, a heat exchanger and an exhaust gas condensation washing and discharge device. The present invention recovers the heat dissipated during the cooling process of the liquefied mash after the starchy raw material is liquefied and the heat dissipated during the cooling process of the saccharification liquid after saccharification, and then uses the recovered heat to perform multi-stage preheating on the starchy raw material, so that it is heated up and liquefied step by step, thereby realizing the recovery and reuse of the waste heat of the liquefied mash and the saccharification liquid, so as to achieve the purpose of energy saving and emission reduction, reduce the production cost of alcohol, and improve the competitiveness of the enterprise.

Description

Technical field:

[0001] The invention belongs to the technical field of equipment for producing alcohol from starchy raw materials, and in particular relates to an energy-saving jet liquefaction system for producing alcohol from starchy raw materials. Background technology:

[0002] In the prior art, when using starchy raw materials such as corn, cassava, rice, wheat, and sorghum to produce alcohol, the process method generally includes the following process steps: raw material crushing - liquefaction - saccharification - fermentation - distillation - dregs separation, etc. After the raw materials are crushed, the starchy raw materials need to be mixed and stirred with liquefaction enzymes in the liquefaction process, and then heated to 95-103°C for liquefaction after jet liquefaction. After liquefaction, the liquefied mash is heat-exchanged with cold water through a plate heat exchanger, and the liquefied mash is cooled to about 60°C and enters the saccharification tank for saccharification. The cold water is heated and then cooled by glass fiber reinforced plastic. After cooling down the tower, the saccharification liquid is recycled. The saccharification liquid is then heat-exchanged with cooling water to about 45°C through a plate heat exchanger and sent to a saccharification temporary storage tank for storage. It is then cooled and fermented. During the cooling of the liquefied mash, the cold water after heating is cooled and recycled, which not only causes heat consumption waste, but also causes cooling water consumption. During the storage process of the saccharification liquid cooled to 45°C, heat consumption is also wasted. Therefore, when the existing starchy raw materials are used to produce alcohol, the energy consumption is large and a large amount of energy is wasted during the liquefaction and saccharification process of the starchy raw materials. At the same time, a large amount of cooling water is consumed. The cost of producing alcohol from starchy raw materials is high, and there are few ways to reduce the cost. How to recycle the heat of the high-temperature steam after the starchy raw materials are boiled, the heat of the liquefied mash, and the heat of the saccharification liquid to reduce the cost of alcohol production, save energy and reduce emissions, and improve the competitiveness of enterprises is still a difficult problem for industry technicians. Summary of the invention:

[0003] To sum up, in order to overcome the shortcomings of the prior art problems, the present invention provides an energy-saving jet liquefaction system for producing alcohol from starchy raw materials, which recovers the heat dissipated during the cooling process of the liquefied mash after the starchy raw material is liquefied and the heat dissipated during the cooling process of the saccharified liquid after saccharification, and then uses the recovered heat to perform multi-stage preheating on the starchy raw material, so that it is heated up and liquefied step by step, thereby realizing the recovery and reuse of the waste heat of the liquefied mash and the saccharified liquid, achieving the purpose of energy saving and emission reduction, reducing the production cost of alcohol, and improving the competitiveness of the enterprise.

[0004] In order to solve the above technical problems, the technical solution adopted by the present invention is:

[0005] An energy-saving jet liquefaction system for producing alcohol from starchy raw materials, including: a mixing screw conveyor, a primary preheating device, a liquefaction preheating system, a jet liquefaction pump, a jet liquefier, a liquefaction system, a liquefied mash cooling system, a saccharification tank, a saccharification liquid cooling system, a saccharification liquid buffer tank, a saccharification liquid high-temperature pump, a saccharification liquid low-temperature pump, a heat exchanger and an exhaust gas condensation washing and discharge device. The mixing screw conveyor mixes and stirs the starchy raw materials, liquefaction enzyme, residual mash filtrate after distillation and wine cooling water to form a mixed material during the conveying process; The primary preheating device uses the secondary steam emitted by the saccharification liquid to preheat the mixture, and the mixture is initially heated and liquefied; the liquefaction preheating system uses the secondary steam evaporated by the liquefied mash to preheat the initially heated and liquefied mixture, and the mixture is gradually heated and liquefied; the liquefaction system uses raw steam to heat the gradually heated and liquefied mixture to liquefy the mixture into liquefied mash, and the liquefied mash cooling system cools the liquefied mash and flashes out the secondary steam; the saccharification tank uses saccharifying enzymes to saccharify the cooled liquefied mash; the saccharification liquid cooling system is used for saccharification liquid The heat is dissipated and the temperature is reduced and secondary steam is evaporated. The tail gas condensation washing and discharge device condenses and cleans the tail gas discharged by the primary preheating device and then discharges it. The discharge port of the mixing screw conveyor is connected to the primary preheating device, and the discharge port of the primary preheating device is connected to the feed port of the liquefaction preheating system. The discharge port of the liquefaction preheating system is connected to the feed port of the jet liquefier through the jet liquefaction pump. The air inlet of the jet liquefier is connected to the steam source. The discharge port of the jet liquefier is connected to the feed port of the liquefaction system. The discharge port of the liquefaction system is connected to the liquefied mash for cooling. The feed inlet of the system and the air outlet of the liquefied mash cooling system are connected to the liquefaction preheating system, the discharge port of the liquefied mash cooling system is connected to the feed inlet of the saccharification tank, the discharge port of the saccharification tank is connected to the feed inlet of the saccharification liquid cooling system through a saccharification liquid high-temperature pump, the discharge port of the saccharification liquid cooling system is connected to the feed inlet of the saccharification liquid buffer tank, the air outlet of the saccharification liquid cooling system is connected to the air inlet of the primary preheating device, the air outlet of the primary preheating device is connected to the tail gas condensation washing and discharge device, and the discharge port of the saccharification liquid buffer tank is connected to the heat exchanger through a saccharification liquid low-temperature pump.

[0006] The technical solution of the present invention can also be implemented as follows: the mixing screw conveyor is connected to a starch material source, a liquefaction enzyme source, residual mash filtrate after distillation, and wine cooling water.

[0007] The technical solution of the present invention can also be implemented as follows: the primary preheating device includes a preheating stirring tank, a preheating absorption tower, a preheating circulation pump, a preheating circulation valve and a preheating discharge valve. The feed port of the preheating stirring tank is connected to the discharge port of the mixing screw conveyor, the circulation port of the preheating stirring tank is connected to the discharge pipe and the discharge pipe, the discharge pipe is connected to the feed port of the preheating absorption tower through the preheating circulation pump, the discharge pipe is provided with a preheating circulation valve, the discharge pipe is connected to the jet liquefaction pump, the discharge pipe is provided with a preheating discharge valve, the discharge port of the preheating stirring tank is connected to the liquefaction preheating system through a pipeline, the air inlet of the preheating absorption tower is connected to the air outlet of the saccharification liquid cooling system and the air outlet of the liquefaction preheating system, the air outlet of the preheating absorption tower is connected to the tail gas condensation washing discharge device, and the preheating absorption tower is an integrated multi-stage absorption tower, which includes a plurality of independent preheating absorption chambers, and each preheating absorption chamber is provided with an air inlet.

[0008] The technical solution of the present invention can also be implemented as follows: the liquefaction preheating system includes a plurality of preliquefaction devices, which are connected in series in sequence. The preliquefaction device includes a preliquefaction stirring tank, a preliquefaction absorption tower, a preliquefaction circulation pump, a preliquefaction circulation valve and a preliquefaction discharge valve. A feed inlet and a discharge inlet are arranged on the upper part of the preliquefaction stirring tank, and a circulation inlet is arranged on the lower end of the preliquefaction stirring tank. The circulation inlet of the preliquefaction stirring tank is connected to a circulation discharge pipe and a discharge pipe. The circulation discharge pipe is connected to the feed inlet of the preliquefaction absorption tower through the preliquefaction circulation pump, and the discharge pipe is connected to the feed inlet of the jet liquefaction pump. The circulation discharge pipe is provided with a preliquefaction circulation valve, and the discharge pipe is provided with a preliquefaction discharge valve. The air inlet of the preliquefaction absorption tower is connected to the liquefied mash cooling system. The pre-liquefaction absorption tower is an integrated multi-stage absorption tower, which includes a plurality of independent pre-liquefaction absorption chambers, each of which is provided with an air inlet, the feed inlet of the pre-liquefaction stirring tank of the first pre-liquefaction device among the plurality of pre-liquefaction devices connected in series is connected to the discharge port of the pre-heating stirring tank of the primary pre-heating device, the discharge port of the pre-liquefaction stirring tank of the previous pre-liquefaction device is connected to the feed inlet of the pre-liquefaction stirring tank of the next pre-liquefaction device, the exhaust port of the pre-liquefaction absorption tower of the previous pre-liquefaction device is connected to the air inlet of the pre-liquefaction absorption tower of the next pre-liquefaction device, the discharge port of the pre-liquefaction stirring tank of the last pre-liquefaction device is connected to the feed inlet of the jet liquefaction pump, and the air outlet of the pre-liquefaction absorption tower of the last pre-liquefaction device is connected to the air inlet of the pre-heating absorption tower of the primary pre-heating device.

[0009] The technical solution of the present invention can also be implemented as follows: the liquefaction system comprises a plurality of laminar flow liquefaction columns, the plurality of laminar flow liquefaction columns are connected in series in sequence, the feed port of the first laminar flow liquefaction column is connected to the discharge port of the injection liquefier, the discharge port of the previous laminar flow liquefaction column is connected to the feed port of the next laminar flow liquefaction column, and the discharge port of the last laminar flow liquefaction column is connected to the feed port of the liquefied mash cooling system.

[0010] The technical solution of the present invention can also be implemented as follows: the liquefaction system includes multiple liquefaction stirring tanks, the multiple liquefaction stirring tanks are connected in series in sequence, the feed port of the first liquefaction stirring tank is connected to the discharge port of the injection liquefier, the discharge port of the previous liquefaction stirring tank is connected to the feed port of the next liquefaction stirring tank, and the discharge port of the last liquefaction stirring tank is connected to the feed port of the liquefied mash cooling system.

[0011] The technical solution of the present invention can also be implemented as follows: the liquefied mash cooling system comprises a plurality of flash tanks, which are connected in series in sequence, the feed port of the first flash tank is connected to the discharge port of the liquefaction system, the discharge port of the previous flash tank is connected to the feed port of the next flash tank, and the discharge port of the last flash tank is connected to the feed port of the saccharification tank, and n adjacent flash tanks in the plurality of serially connected flash tanks form a group, where n is equal to the number of pre-liquefaction absorption chambers in the pre-liquefaction absorption tower, and each flash tank is provided with an air outlet, and the n air outlets of a group of flash tanks are respectively connected to multiple air inlets of a pre-liquefaction absorption tower of a pre-liquefaction device.

[0012] The technical solution of the present invention can also be implemented as follows: the saccharification liquid cooling system comprises a plurality of saccharification liquid flash evaporation heat release tanks, which are connected in series, the feed port of the first saccharification liquid flash evaporation heat release tank is connected to the discharge port of the saccharification liquid high-temperature pump, the discharge port of the previous saccharification liquid flash evaporation heat release tank is connected to the feed port of the next saccharification liquid flash evaporation heat release tank, the discharge port of the last saccharification liquid flash evaporation heat release tank is connected to the saccharification liquid buffer tank, the number of the saccharification liquid flash evaporation heat release tanks is the same as the number of preheating absorption chambers of the preheating absorption tower of the primary preheating device, and the air outlet of one saccharification liquid flash evaporation heat release tank is connected to the air inlet of one preheating absorption chamber of the preheating absorption tower.

[0013] The beneficial effects of the present invention are:

[0014] 1. The present invention recovers the heat emitted during the cooling process of the liquefied mash after the starchy raw material is liquefied and the heat emitted during the cooling process of the saccharified liquid after saccharification, and then uses the recovered heat to perform multi-stage preheating on the starchy raw material to gradually increase the temperature and liquefy it, thereby realizing the recovery and reuse of the waste heat of the liquefied mash and the saccharified liquid, achieving the purpose of energy saving and emission reduction, reducing the production cost of alcohol, and improving the competitiveness of the enterprise.

[0015] 2. The present invention provides a primary preheating device, and the air inlet of the preheating absorption tower of the primary preheating device is connected to the air outlet of the saccharification liquid cooling system. The secondary steam generated during the cooling of the saccharification liquid enters the preheating absorption tower. In the preheating absorption tower, the secondary steam generated by the cooling of the saccharification liquid is absorbed by the starchy mixture, thereby raising the temperature of the starchy mixture from the initial 40°C to 54°C. The preheating absorption tower of the primary preheating device of the present invention comprises three preheating absorption chambers, which respectively correspond to the three flash heat release tanks of the saccharification liquid cooling system. The three-stage staged heating of the starchy mixture is realized in the preheating absorption tower. The secondary steam absorption utilization rate is high and the efficiency is fast, and the heat released by the heat dissipation of the saccharification liquid can be fully absorbed.

[0016] 3. The liquefaction preheating system of the present invention includes three pre-liquefaction devices arranged in series, and the liquefied mash cooling system of the present invention includes six flash tanks arranged in series, each pre-liquefaction device corresponds to two flash tanks, and the six flash tanks arranged in series enable the liquefied mash to be flash cooled and cooled in stages after liquefaction, and the cooling interval division is more delicate. Every two flash tanks correspond to a pre-liquefaction device, and the pre-liquefaction absorption tower of the pre-liquefaction device includes two liquefaction preheating absorption chambers. The starchy raw material entering the pre-liquefaction absorption tower absorbs secondary steam of different temperatures twice, and can more effectively and quickly absorb the secondary steam evaporated from the flash tank, which is beneficial to the recovery and reuse of the steam evaporated from the liquefied mash.

[0017] 4. The inner cavity of the preheating absorption tower of the primary preheating device of the present invention is divided into three absorption chambers by the preheating liquid sealing device, and the preheating liquid sealing device realizes the mutual independence of two adjacent absorption chambers. The inner cavity of the preliquefaction absorption tower of the preliquefaction device of the present invention is divided into two absorption chambers by the preliquefaction liquid sealing device, and the preliquefaction liquid sealing device realizes the mutual independence of the two absorption chambers. The preheating liquid sealing device and the preliquefaction liquid sealing device have the same structure, and both are inserted into the overflow weir through the lower end of the discharge pipe. The discharge speed of the overflow weir is much lower than the feeding speed, so that the material is stored in the overflow weir, and the material stored in the overflow weir is used to achieve the sealing between the two adjacent absorption chambers, so as to realize the mutual independence of the two adjacent absorption chambers. The structure is simple, the conception is ingenious, and the sealing effect is good by using the material to reduce the cost.

[0018] 5. The present invention has a simple structure, a novel and ingenious concept, and is convenient and quick to operate. It can effectively recover the heat lost in the process of producing alcohol from starchy materials, and at the same time use the heat again to preheat and precook the starchy materials to achieve the liquefaction of the starchy raw materials, thereby greatly reducing the energy consumption in the alcohol production process, reducing the emission of hot gases, saving the amount of cooling water required for hot gas cooling, reducing the production cost of producing alcohol from starchy materials, and achieving the purpose of energy saving and emission reduction. Description of the drawings:

[0019] Figure 1 A structural schematic diagram of the present invention;

[0020] Figure 2 It is a structural schematic diagram of the preheating absorption tower of the present invention;

[0021] Figure 3 It is a structural schematic diagram of the pre-liquefaction absorption tower of the present invention;

[0022] Figure 4 Another structural schematic diagram of the present invention. Specific implementation method:

[0023] The present invention will be further described in detail below in conjunction with the accompanying drawings and embodiments.

[0024] Embodiment 1

[0025] like Figure 1As shown, an energy-saving jet liquefaction system for producing alcohol from starchy raw materials comprises a mixing screw conveyor 1, a primary preheating device 2, a liquefaction preheating system 3, a jet liquefaction pump 4, a jet liquefier 5, a liquefaction system 6, a liquefied mash cooling system 7, a saccharification tank 8, a saccharification liquid cooling system 9, a saccharification liquid buffer tank 10, a saccharification liquid high-temperature pump 11, a saccharification liquid low-temperature pump 12, a heat exchanger 13 and an exhaust gas condensation washing and discharge device 18. The mixing screw conveyor 1 mixes and stirs the starchy raw material, liquefaction enzyme, residual mash filtrate after distillation and wine cooling water to form a mixed material during the conveying process. The primary preheating device 2 uses the secondary steam emitted by the saccharification liquid to preheat the mixture, and the mixture is initially heated and liquefied; the liquefaction preheating system 3 uses the secondary steam evaporated by the liquefied mash to preheat the initially heated and liquefied mixture, and the mixture is gradually heated and liquefied; the liquefaction system 6 uses raw steam to heat the gradually heated and liquefied mixture to liquefy the mixture into liquefied mash, and the liquefied mash cooling system 7 cools the liquefied mash and flashes out the secondary steam; the saccharification tank 8 uses saccharifying enzymes to saccharify the cooled liquefied mash; the saccharification liquid cooling system 9 is used to dissipate heat and cool the saccharification liquid and evaporate Secondary steam is emitted, the tail gas condensation washing and discharging device 18 condenses and cleans the tail gas discharged from the primary preheating device and then discharges it, the mixing screw conveyor 1 is connected to the starch material source 14, the liquefaction enzyme source 15, the residual mash filtrate 16 after distillation and the wine cooling water 17, the discharge port of the mixing screw conveyor 1 is connected to the primary preheating device 2, the primary preheating device 2 includes a preheating stirring tank 21, a preheating absorption tower 22, a preheating circulation pump 23, a preheating circulation valve 24 and a preheating discharge valve 25, the feed port of the preheating stirring tank 21 is connected to the discharge port of the mixing screw conveyor 1, The circulation port of the preheating stirring tank 21 is connected to the discharge pipe and the discharge pipe, the discharge pipe is connected to the feed port of the preheating absorption tower 22 through the preheating circulation pump 23, the discharge pipe is provided with a preheating circulation valve 24, the discharge pipe is connected to the jet liquefaction pump 4, the discharge pipe is provided with a preheating discharge valve 25, the discharge port of the preheating stirring tank 21 is connected to the liquefaction preheating system 3 through a pipeline, the air inlet of the preheating absorption tower 22 is connected to the air outlet of the saccharification liquid cooling system 9 and the air outlet of the liquefaction preheating system 3, and the air outlet of the preheating absorption tower 22 is connected to the tail gas condensation washing discharge device 18. The preheating absorption tower 22 is an integrated multi-stage absorption tower, which includes three independent preheating absorption chambers, each of which is provided with an air inlet.

[0026] The liquefaction preheating system 3 includes three preliquefaction devices, which are connected in series in sequence, and are divided into a first preliquefaction device 31, a second preliquefaction device 32 and a third preliquefaction device 33. The three preliquefaction devices have the same structure, and all include a preliquefaction stirring tank 301, a preliquefaction absorption tower 302, a preliquefaction circulation pump 303, a preliquefaction circulation valve 304 and a preliquefaction discharge valve 305. The upper part of the preliquefaction stirring tank 301 is provided with a feed inlet and a discharge port. A circulation port is set at the lower end of 01, and the circulation port of the pre-liquefaction stirring tank 301 is connected to the circulation discharge pipe and the discharge pipe. The circulation discharge pipe is connected to the feed port of the pre-liquefaction absorption tower 302 through the pre-liquefaction circulation pump 303, and the discharge pipe is connected to the feed port of the jet liquefaction pump 4. The circulation discharge pipe is provided with a pre-liquefaction circulation valve 304, and the discharge pipe is provided with a pre-liquefaction discharge valve 305. The air inlet of the pre-liquefaction absorption tower 302 is connected to the air outlet of the liquefied mash cooling system 7.

[0027] The liquefied mash cooling system 7 includes six flash tanks, which are connected in series in sequence, namely a first flash tank 71, a second flash tank 72, a third flash tank 73, a fourth flash tank 74, a fifth flash tank 75 and a sixth flash tank 76. The feed port of the first flash tank 71 is connected to the discharge port of the liquefaction system 6, the discharge port of the first flash tank 71 is connected to the feed port of the second flash tank 72, the discharge port of the second flash tank 72 is connected to the feed port of the third flash tank 73, the discharge port of the third flash tank 73 is connected to the feed port of the fourth flash tank 74, the discharge port of the fourth flash tank 74 is connected to the feed port of the fifth flash tank 75, the discharge port of the fifth flash tank 75 is connected to the feed port of the sixth flash tank 76, and the discharge port of the sixth flash tank 76 is connected to the feed port of the saccharification tank 8.

[0028] The feed port of the preliquefaction stirring tank 301 of the first preliquefaction device 31 is connected to the discharge port of the preheating stirring tank 21, the discharge port of the preliquefaction stirring tank 301 of the first preliquefaction device 31 is connected to the feed port of the preliquefaction stirring tank 301 of the second preliquefaction device 32, the discharge port of the preliquefaction stirring tank 301 of the second preliquefaction device 32 is connected to the feed port of the preliquefaction stirring tank 301 of the third preliquefaction device 33, the discharge port of the preliquefaction stirring tank 301 of the third preliquefaction device 33 is connected to the feed port of the jet liquefaction pump 4, the discharge port of the jet liquefaction pump 4 is connected to the feed port of the jet liquefier 5, the air inlet of the jet liquefier 5 is connected to the steam source 19, and the discharge port of the jet liquefier 5 is connected to the feed port of the liquefaction system 6.

[0029] The liquefaction system 6 includes multiple laminar flow liquefaction columns 601, which are connected in series in sequence. The feed port of the first laminar flow liquefaction column 601 is connected to the discharge port of the injection liquefier 5, the discharge port of the previous laminar flow liquefaction column 601 is connected to the feed port of the next laminar flow liquefaction column 601, and the discharge port of the last laminar flow liquefaction column 601 is connected to the feed port of the first flash tank 71 of the liquefied mash cooling system 7.

[0030] The air inlet of the preliquefaction absorption tower 302 of the first preliquefaction device 31 is connected to the air outlet of the fifth flash tank 75 and the sixth flash tank 76, the air outlet of the preliquefaction absorption tower 302 of the first preliquefaction device 31 is connected to the air inlet of the preheating absorption tower 22 of the primary preheating device 2, the air inlet of the preliquefaction absorption tower 302 of the second preliquefaction device 32 is connected to the air outlet of the third flash tank 73 and the fourth flash tank 74, the air outlet of the preliquefaction absorption tower 302 of the second preliquefaction device 32 is connected to the air inlet of the preliquefaction absorption tower 302 of the first preliquefaction device 31, the air inlet of the preliquefaction absorption tower 302 of the third preliquefaction device 33 is connected to the air outlet of the first flash tank 71 and the second flash tank 72, and the air outlet of the preliquefaction absorption tower 302 of the third preliquefaction device 33 is connected to the air inlet of the preliquefaction absorption tower 302 of the second preliquefaction device 32.

[0031] The discharge port of the saccharification tank 8 is connected to the feed port of the saccharification liquid cooling system 9 through the saccharification liquid high-temperature pump 11, the discharge port of the saccharification liquid cooling system 9 is connected to the feed port of the saccharification liquid buffer tank 10, the air outlet of the saccharification liquid cooling system 9 is connected to the air inlet of the primary preheating device 2, the discharge port of the saccharification liquid buffer tank 10 is connected to the heat exchanger 13 through the saccharification liquid low-temperature pump 12, and the saccharification liquid cooling system 9 includes three saccharification liquid flash exothermic tanks, which are connected in series, and the feed port of the first saccharification liquid flash exothermic tank 91 is connected to the discharge port of the saccharification liquid high-temperature pump 11. The outlet of the first saccharification liquid flash evaporation heat release tank 91 is connected to the feed inlet of the second saccharification liquid flash evaporation heat release tank 92, the outlet of the second saccharification liquid flash evaporation heat release tank 92 is connected to the feed inlet of the third saccharification liquid flash evaporation heat release tank 93, the outlet of the third saccharification liquid flash evaporation heat release tank 93 is connected to the saccharification liquid buffer tank 10, and the gas outlet of the first saccharification liquid flash evaporation heat release tank 91, the gas outlet of the second saccharification liquid flash evaporation heat release tank 92 and the gas outlet of the third saccharification liquid flash evaporation heat release tank 93 are respectively connected to the gas inlets of three mutually independent preheating absorption chambers of the preheating absorption tower 22 of the primary preheating device 2.

[0032] like Figure 2As shown, the preheating absorption tower 22 of the primary preheating device 2 includes a preheating tank body 221, a preheating feed pipe 222, a preheating nozzle 223, a preheating collection ring 224 and a preheating distribution plate 225. The lower end of the preheating tank body 221 is funnel-shaped, and a hot material outlet is arranged on it. Two preheating liquid sealing devices are arranged in the preheating tank body 221. The two preheating liquid sealing devices divide the inner cavity of the preheating tank body 221 into three absorption chambers arranged in sequence from top to bottom, namely, a preheating upper absorption chamber 226, a preheating middle absorption chamber 227 and a preheating lower absorption chamber 228. The three absorption chambers are all provided with a preheating collection ring 224 and a preheating distribution plate 225. The preheating collection ring 224 and the preheating distribution plate 225 are arranged up and down. A preheating feed pipe 222 is arranged in the preheating upper absorption chamber 226, and a preheating nozzle 223 is arranged at one end of the preheating feed pipe 222 located in the preheating tank body 221, and the gas outlet is arranged at the upper end of the preheating upper absorption chamber 226, and the three absorption chambers are all provided with an air inlet, and the air inlet is arranged on the preheating tank body 221 under the preheating distribution plate 225, and the three absorption chambers are all provided with an air outlet, and the preheating liquid sealing device includes an inner cone 229, a feed pipe 2210, an overflow weir 2211 and a tower plate group 2212, and the inner cone 229 is arranged in the preheating tank body 221 and fixedly connected to the inner wall of the preheating tank body 221, and the lower end of the inner cone 229 is provided with a feed pipe 2210, and the feed pipe 221 0 is inserted in the overflow weir 2211, the tower plate group 2212 supports the overflow weir 2211, the tower plate group 2212 is connected to the inner wall of the preheating tank body 221, the overflow weir 2211 is a barrel-shaped structure with an open upper end and a closed lower end, and a water-permeable small hole is arranged on the lower end sealing plate of the overflow weir 2211. The feed pipe 2210 is inserted in the overflow weir 2211 and extends into the lower part of the overflow weir 2211. The upper end of the overflow weir 2211 is provided with a sawtooth weir platform, the tower plate group 2212 includes a water eave 2213 and a lower bracket, the lower bracket is connected to the inner wall of the preheating tank body 221, and the lower bracket supports the water eave 2213, and the water eave 2213 is a hollow conical structure with upper and lower ends open. The structure has an upper opening connected to the lower end of the overflow weir 2211, and its lower end is suspended, and a material discharge channel is formed between the lower end of the lower water eaves 2213 and the inner wall of the preheating tank body 221, and an annular water retaining ring 2214 is arranged on the lower water eaves 2213, and a sawtooth-shaped weir platform is arranged on the upper end of the water retaining ring 2214, and the outer wall of the water retaining ring 2214 is connected to the inner wall of the preheating tank body 221 through a bracket, and a material discharge gap is formed between the lower end of the water retaining ring 2214 and the lower water eaves 2213, and a material discharge channel is formed between the outer wall of the water retaining ring 2214 and the inner wall of the preheating tank body 221; the preheating collecting ring 224 is a funnel-shaped structure with a large upper opening and a small lower opening, and the upper end of the preheating collecting ring 224 is connected to the inner wall of the preheating tank body 221;The preheating distribution plate 225 is a funnel-shaped structure, and a bracket for connecting the inner wall of the preheating tank 221 is arranged in the circumference thereof. The upper end opening of the preheating distribution plate 225 corresponds to the lower end opening of the preheating collection ring 224, and the upper end opening of the preheating distribution plate 225 is greater than or equal to the lower end opening of the preheating collection ring 224. The lower end of the preheating distribution plate 225 is provided with a through hole, and the side wall of the funnel-shaped preheating distribution plate 225 is provided with a feeding hole, the size of the feeding hole is smaller than the size of the through hole, and the size of the through hole is smaller than the size of the upper end opening. A sawtooth-shaped weir is arranged on the upper end opening of the preheating distribution plate 225; a grid is arranged in the preheating upper absorption chamber 226, and the grid is arranged above the preheating collection ring 224 in the preheating upper absorption chamber 226. ;

[0033] like Figure 3 As shown, the pre-liquefaction absorption tower 302 of the pre-liquefaction device includes a pre-liquefaction tank body 3021, a pre-liquefaction feed pipe 3022, a pre-liquefaction nozzle 3023, a pre-liquefaction collection ring 3024 and a pre-liquefaction distribution plate 3025. The lower end of the pre-liquefaction tank body 3021 is funnel-shaped and is provided with a hot material outlet. A pre-liquefaction liquid sealing device is provided in the pre-liquefaction tank body 3021. The pre-liquefaction liquid sealing device divides the inner cavity of the pre-liquefaction tank body 3021 into two absorption chambers arranged in sequence from top to bottom, namely, a pre-liquefaction upper absorption chamber 3026 and a pre-liquefaction lower absorption chamber 3027. The two absorption chambers are both provided with a pre-liquefaction collection ring 3024 and a pre-liquefaction distribution plate 3025. The pre-liquefaction collection ring 3024 and the pre-liquefaction distribution plate 3025 are arranged up and down. A pre-liquefaction feed pipe 3022 is provided in 26, and a pre-liquefaction nozzle 3023 is provided at one end of the pre-liquefaction feed pipe 3022 located in the pre-liquefaction tank body 3021, the gas outlet is provided at the upper end of the pre-liquefaction upper absorption chamber 3026, and the two absorption chambers are provided with gas inlets, and the gas inlets are provided on the pre-liquefaction tank body 3021 under the pre-liquefaction distribution plate 3025, and the two absorption chambers are provided with gas outlets. The pre-liquefaction liquid sealing device has the same structure as the pre-heating liquid sealing device, the pre-liquefaction collecting ring 3024 has the same structure as the pre-heating collecting ring 224, the pre-liquefaction distribution plate 3025 has the same structure as the pre-heating distribution plate 225, and a grille is provided in the pre-liquefaction upper absorption chamber 3026, and the grille is provided above the pre-liquefaction collecting ring 3024 in the pre-liquefaction upper absorption chamber 3026.

[0034] When in use, the starchy raw material, liquefaction enzyme, residual mash filtrate 16 after distillation and wine cooling water 17 are mixed and stirred evenly in the mixing screw conveyor 1. The wine cooling water 17 and the residual mash filtrate 16 after distillation both contain heat, so the raw materials mixed in the mixing screw conveyor 1 are mixed and stirred into a starchy mixture, and the temperature of the mixture after mixing and stirring is about 40°C.

[0035] The starchy mixture after mixing and stirring is conveyed into the preheating mixing tank 21 by the mixing screw conveyor 1, the preheating circulation pump 23 is started, the preheating circulation valve 24 is opened, and the mixture in the preheating mixing tank 21 is conveyed to the preheating absorption tower 22, enters from the feed pipe at the upper part of the preheating absorption tower 22, and is sprayed into a cone shape by the preheating nozzle 223 and enters the preheating upper absorption chamber 226 of the preheating absorption tower 22, falls along the inner wall of the preheating mixing tank 21, and then slides along the inner wall of the preheating collection ring 224. Since the preheating collection ring 224 is a funnel-shaped structure, the starchy mixture converges from the periphery to the center. Since there is a certain distance between the lower end of the preheating collection ring 224 and the preheating distribution plate 225, when the starchy mixture falls from the preheating collection ring 224 into the preheating distribution plate 225, a water curtain-like material flow is formed between the preheating collection ring 224 and the preheating distribution plate 225. The starchy mixture falls into the preheating distribution plate 225. Since the preheating distribution plate 225 is a funnel-shaped structure, a material discharge hole is provided on its side wall, and a through hole is provided at its lower end, the starchy mixture entering the preheating distribution plate 225 falls along the material discharge hole and the through hole at the lower end of the preheating distribution plate 225, forming a water curtain-like material flow. The saccharified liquid in the third saccharified liquid flash evaporation heat release tank 93 is cooled and evaporated to a temperature of about 50°C. The secondary steam enters the preheating upper absorption chamber 226 from the air inlet of the preheating upper absorption chamber 226, flows upward in the preheating upper absorption chamber 226, and meets the water curtain-shaped material flow under the preheating distribution plate 225 to exchange heat. The material absorbs the secondary steam, the temperature rises and liquefies, and the secondary steam cools down. After that, the secondary steam continues to flow upward. When it meets the preheating distribution plate 225, it is blocked by the preheating distribution plate 225 and flows upward in all directions. After that, it is collected by the preheating collection ring 225. The lower end opening of 224 enters the preheating collection ring 224 and flows upward along the inner cavity of the preheating collection ring 224. During this process, the secondary steam needs to pass through the water curtain-shaped material flow between the preheating collection ring 224 and the preheating distribution plate 225. The material absorbs the secondary steam again to heat up, and the secondary steam cools down and continues to flow upward, and then passes through the conical material flow sprayed by the preheating nozzle 223. The material absorbs the secondary steam again to heat up, and finally the non-condensable gas is discharged from the non-condensable gas outlet at the upper end of the preheating upper absorption chamber 226 and enters the exhaust gas condensation washing discharge device 18. The exhaust gas is condensed and cleaned and then discharged into the atmosphere.

[0036] The starchy mixture absorbs secondary steam while the temperature is rising in the preheating upper absorption chamber 226, and the starchy mixture is further liquefied. After that, the mixture flows out of the preheating upper absorption chamber 226 from the inner cone 229 at the lower end of the preheating upper absorption chamber 226 and the discharge pipe 2210. The mixture first enters the overflow weir 2211 through the discharge pipe 2210. Since the discharge speed of the overflow weir 2211 is much lower than the feeding speed, the mixture is stored in the overflow weir 2211, and the lower end of the discharge pipe 2210 goes deep into the overflow weir 2211. To achieve liquid sealing, the material stored in the overflow weir 2211 overflows from the upper end of the overflow weir 2211 and enters the preheating absorption chamber 227. The mixed material overflowing from the overflow weir 2211 falls on the lower eaves 2213 of the tower plate group 2212 and slides down along the lower eaves 2213. The lower eaves 2213 is provided with a water retaining ring 2214. Part of the mixed material slides down along the material discharge gap formed between the lower end of the water retaining ring 2214 and the lower eaves 2213, and part of the mixed material accumulates on the lower eaves 2213 and finally flows out from the lower eaves. The overflow from the upper end of 2213 slides down, and under the action of the lower water eaves 2213 and the water retaining ring 2214 of the tower plate group 2212, the mixed material entering the preheating middle absorption chamber 227 finally falls in the form of a conical material flow. Afterwards, the mixed material is collected by the preheating collection ring 224 in the preheating middle absorption chamber 227, and falls into the preheating distribution plate 225 in the preheating middle absorption chamber 227 along the inner wall of the preheating collection ring 224, and a water curtain-shaped material flow is also formed between the preheating collection ring 224 and the preheating distribution plate 225. After that, the mixed material falls along the preheating distribution plate 225, and a water curtain-shaped material flow is formed between the preheating distribution plate 225 and the preheating liquid sealing device. The saccharified liquid in the second saccharified liquid flash heat release tank 92 is cooled and released with a secondary steam of about 55°C, which enters from the air inlet of the preheating middle absorption chamber 227, and then flows upward, and meets and mixes with the mixed material in the preheating middle absorption chamber 227 for many times. The mixed material absorbs the secondary steam to further heat up and liquefy, and the non-condensable gas is discharged from the middle air outlet at the upper part of the preheating middle absorption chamber 227.

[0037] Similarly, a preheating liquid seal device is also provided between the preheating middle absorption chamber 227 and the preheating lower absorption chamber 228. The mixture in the preheating middle absorption chamber 227 enters the preheating lower absorption chamber 228 through the preheating liquid seal device and flows downward. The saccharification liquid in the first saccharification liquid flash evaporation heat release tank 91 is cooled and released with a temperature of about 60°C. The secondary steam enters from the air inlet of the preheating middle absorption chamber 227 and then flows upward. The mixture entering the preheating lower absorption chamber 228 is heated again and absorbs moisture in the hot air. The mixture is further heated and liquefied. After the secondary steam evaporated in the first saccharification liquid flash evaporation heat release tank 91 is absorbed, the non-condensable gas is discharged from the middle air outlet at the top of the preheating lower absorption chamber 228. The starchy mixture has the same flow process in the preheating middle absorption chamber 227 and the preheating lower absorption chamber 228, and the hot air has the same flow process in the preheating middle absorption chamber 227 and the preheating lower absorption chamber 228.

[0038] The starchy mixture that is heated and liquefied after absorbing secondary steam in the three preheating absorption chambers of the preheating absorption tower 22 flows out from the hot material outlet at the lower end of the preheating absorption tower 22 and enters the preheating stirring tank 21 again. In this way, the starchy mixture circulates back and forth under the action of the preheating circulation pump 23, and the starchy mixture is heated to about 54°C. Under the action of the jet liquefaction pump 4, the starchy mixture heated by the primary preheating device 2 enters the preliquefaction stirring tank 301 of the first preliquefaction device 31, and then is sent to the preliquefaction absorption tower 302 of the first preliquefaction device 31 under the action of the preliquefaction circulation pump 303 of the first preliquefaction device 31. The working principle of the preliquefaction absorption tower 302 is the same as that of the preheating absorption tower 22. The starchy mixture in the preliquefaction stirring tank 301 of the first preliquefaction device 31 enters the preliquefaction absorption tower 302 from the preliquefaction feed pipe 3022 of the preliquefaction upper absorption chamber 3026 of the preliquefaction absorption tower 302 under the action of the preliquefaction circulation pump 303. The liquid is sprayed into the upper absorption chamber 3026 in a cone shape under the action of the pre-liquefaction nozzle 3023, forming a cone-shaped material flow, and then collected by the pre-liquefaction collection ring 3024 and falls into the pre-liquefaction distribution plate 3025, forming a water curtain-shaped material flow between the pre-liquefaction collection ring 3024 and the pre-liquefaction distribution plate 3025, and then falls from the pre-liquefaction distribution plate 3025 to form a water curtain-shaped material flow, and the sixth flash tank 76 evaporates out The 65°C secondary steam enters from the air inlet of the pre-liquefaction upper absorption chamber 3026, flows upward, and contacts with the starchy mixture. The starchy mixture absorbs the secondary steam, and then the starchy mixture enters the pre-liquefaction lower absorption chamber 3027 through the pre-liquefaction liquid seal device. In the pre-liquefaction lower absorption chamber 3027, the starchy mixture absorbs the 70°C secondary steam evaporated from the fifth flash tank 75. The starchy mixture entering the first pre-liquefaction device 31 is finally heated to 63°C.

[0039] The starchy mixture at 63°C enters the second pre-liquefaction device 32. In the pre-liquefaction absorption tower 302 of the second pre-liquefaction device 32, the starchy mixture at 63°C absorbs the secondary steam at 79°C evaporated from the third flash tank 73 and the secondary steam at 74°C evaporated from the fourth flash tank 74, and the starchy mixture is heated to 72°C. Afterwards, the starchy mixture at 72°C enters the third pre-liquefaction device 33. In the pre-liquefaction absorption tower 302 of the third pre-liquefaction device, the starchy mixture at 72°C absorbs the secondary steam at 83°C evaporated from the second flash tank 72 and the secondary steam at 88°C evaporated from the first flash tank 71, and the starchy mixture is heated to 81°C.

[0040] The starchy mixture at 81°C is transported into the jet liquefier 5 through the jet liquefier 4, and the high-temperature steam also enters the jet liquefier 5. The starchy mixture at 81°C is jet liquefied by the high-temperature steam in the jet liquefier 5. At the same time, the starchy mixture absorbs the high-temperature steam, and the starchy mixture is heated to 88°C and enters the liquefaction system 6 in a jet state, and is boiled and liquefied in the laminar liquefaction column 601 of the liquefaction system 6. After boiling and liquefaction, the starchy mixture generates liquefied mash, and the temperature of the liquefied mash is 88°C.

[0041] The liquefied mash at 88°C passes through the first flash tank 71, the second flash tank 72, the third flash tank 73, the fourth flash tank 74, the fifth flash tank 75, and the sixth flash tank 76 in turn, and is cooled to 83°C, 79°C, 74°C, 70°C, 65°C, and 60°C respectively. The liquefied mash at 60°C discharged from the sixth flash tank 76 enters the saccharification tank 8, and the steam at 88°C, 83°C, 79°C, 74°C, 70°C, and 65°C generated in the first flash tank 71, the second flash tank 72, the third flash tank 73, the fourth flash tank 74, the fifth flash tank 75, and the sixth flash tank 76 enters the three pre-liquefaction devices of the liquefaction preheating system 3 for preheating and liquefying the starchy mixture.

[0042] Saccharifying enzyme is added into the saccharification tank 8, and the liquefied mash is saccharified to become saccharified liquid with a temperature of 60°C. The saccharified liquid at 60°C enters the saccharified liquid cooling system 9 under the action of the saccharified liquid high-temperature pump 11, and passes through the first saccharified liquid flash evaporation heat release tank 91, the second saccharified liquid flash evaporation heat release tank 92, and the third saccharified liquid flash evaporation heat release tank 93 in sequence, and is cooled to 55°C, 50°C, and 45°C respectively. The steam formed by the heat dissipation of the three saccharified liquid flash evaporation heat release tanks of the saccharified liquid cooling system 9 enters the three absorption chambers of the preheating absorption tower 22 of the primary preheating device 2 respectively, for preheating the starchy mixture. At the same time, the non-condensable gas discharged from the preliquefaction absorption tower 302 of the three preliquefaction devices of the liquefaction preheating system 3 also enters the preheating absorption tower 22 of the primary preheating device 2, for preheating the starchy mixture.

[0043] The saccharified liquid at 45° C. cooled by the saccharified liquid cooling system 9 enters the saccharified liquid temporary storage tank for temporary storage, and is finally transported to the heat exchanger 13 through the saccharified liquid low-temperature pump 12 for heat exchange and cooling, and then is sent to the fermentation tank for fermentation to produce alcohol.

[0044] When production is stopped, the starch mixture in the equipment needs to be emptied, and the preheating discharge valve 25 of the primary preheating device 2 and the preliquefaction discharge valve 305 of the preliquefaction device of the liquefaction preheating system 3 are opened. Under the action of the jet liquefaction pump 4, the starch mixture in the preheating stirring tank 21 and the preliquefaction stirring tank 301 is emptied and transported to the liquefaction system 6 for liquefaction.

[0045] The preheating collection ring 224 and the preheating distribution plate 225 in the preheating absorption tower 22 of the primary preheating device 2 of the present invention cooperate with each other to achieve multiple reversals of the material and multiple changes in the direction of the hot air flow entering the preheating absorption tower 22. The upward flow of the hot air flow needs to pass through the material flow multiple times, and the multiple contacts between the material flow and the secondary steam air flow make the heat exchange between the material flow and the hot air flow more complete and thorough, which is conducive to the material flow absorbing the temperature and moisture in the hot air flow and accelerating the liquefaction of the starchy mixture. Similarly, the preliquefaction collection ring 3024 and the preliquefaction distribution plate 3025 in the preliquefaction absorption tower 302 of the preliquefaction device cooperate with each other to also achieve multiple contacts between the hot air flow and the material flow, and its working principle is the same as that of the preheating absorption tower 22.

[0046] Embodiment 2

[0047] like Figure 4 As shown, Example 1 is repeated with the following differences: the liquefaction system 6 includes three liquefaction stirring tanks 602, and the three liquefaction stirring tanks 602 are connected in series in sequence, including a first liquefaction stirring tank, a second liquefaction stirring tank and a third liquefaction stirring tank, the feed port of the first liquefaction stirring tank is connected to the discharge port of the injection liquefier 5, the discharge port of the first liquefaction stirring tank is connected to the feed port of the second liquefaction stirring tank, the discharge port of the second liquefaction stirring tank is connected to the feed port of the third liquefaction stirring tank, and the discharge port of the third liquefaction stirring tank is connected to the feed port of the first flash tank 71 of the liquefied mash cooling system 7.

[0048] It should be noted that the above-described embodiments are illustrative of the technical solution of the present invention rather than limiting. Equivalent substitutions made by ordinary technicians in the relevant technical field or other modifications made according to the prior art should be included in the scope of rights required by the present invention as long as they do not exceed the concept and scope of the technical solution of the present invention.

Claims

1. An energy-saving jet liquefaction system for producing alcohol from starchy raw materials. Features: The invention comprises a mixing screw conveyor (1), a primary preheating device (2), a liquefaction preheating system (3), a jet liquefaction pump (4), a jet liquefier (5), a liquefaction system (6), a liquefied mash cooling system (7), a saccharification tank (8), a saccharification liquid cooling system (9), a saccharification liquid buffer tank (10), a saccharification liquid high-temperature pump (11), a saccharification liquid low-temperature pump (12), a heat exchanger (13) and an exhaust gas condensation washing and discharge device (18). The mixing screw conveyor (1) mixes and stirs starchy raw materials, liquefaction enzymes, residual mash filtrate (16) and wine gas cooling water (17) during the conveying process to form a mixed material; the primary preheating device (2) is used to mix and stir starchy raw materials, liquefaction enzymes, residual mash filtrate (16) and wine gas cooling water (17) to form a mixed material; the primary preheating device (4) is used to mix and stir starchy raw materials, liquefaction enzymes, residual mash filtrate (16) and wine gas cooling water (17) to form a mixed material; the primary preheating device (5 ... The heating device (2) uses the secondary steam emitted by the saccharification liquid to preheat the mixture, and the mixture is initially heated and liquefied; the liquefaction preheating system (3) uses the secondary steam evaporated from the liquefied mash to preheat the initially heated and liquefied mixture, and the mixture is gradually heated and liquefied; the liquefaction system (6) uses raw steam to heat the gradually heated and liquefied mixture, so that the mixture is liquefied into liquefied mash, and the liquefied mash cooling system (7) cools the liquefied mash and flashes out the secondary steam; the saccharification tank (8) uses saccharifying enzymes to saccharify the cooled liquefied mash; the saccharification liquid cooling system (9) is used to dissipate heat and cool the saccharification liquid and evaporate the secondary steam, and the tail gas condensation washing The exhaust gas discharged from the primary preheating device is condensed and cleaned by the exhaust gas discharge device (18), the exhaust port of the mixing screw conveyor (1) is connected to the primary preheating device (2), the exhaust port of the primary preheating device (2) is connected to the feed port of the liquefaction preheating system (3), the exhaust port of the liquefaction preheating system (3) is connected to the feed port of the jet liquefier (5) through the jet liquefaction pump (4), the air inlet of the jet liquefier (5) is connected to the steam source, the exhaust port of the jet liquefier (5) is connected to the feed port of the liquefaction system (6), the exhaust port of the liquefaction system (6) is connected to the feed port of the liquefied mash cooling system (7), and the exhaust port of the liquefied mash cooling system (7) is connected to the feed port of the liquefied mash cooling system (7). The gas outlet is connected to the liquefaction preheating system (3), the material outlet of the liquefied mash cooling system (7) is connected to the material inlet of the saccharification tank (8), the material outlet of the saccharification tank (8) is connected to the material inlet of the saccharification liquid cooling system (9) through the saccharification liquid high temperature pump (11), the material outlet of the saccharification liquid cooling system (9) is connected to the material inlet of the saccharification liquid buffer tank (10), the gas outlet of the saccharification liquid cooling system (9) is connected to the gas inlet of the primary preheating device (2), the gas outlet of the primary preheating device (2) is connected to the tail gas condensation washing and discharge device (18), the material outlet of the saccharification liquid buffer tank (10) is connected to the heat exchanger (13) through the saccharification liquid low temperature pump (12), The primary preheating device (2) comprises a preheating stirring tank (21), a preheating absorption tower (22), a preheating circulation pump (23), a preheating circulation valve (24) and a preheating discharge valve (25). The feed inlet of the preheating stirring tank (21) is connected to the discharge outlet of the mixing screw conveyor (1). The circulation outlet of the preheating stirring tank (21) is connected to the discharge pipe and the discharge pipe. The discharge pipe is connected to the feed inlet of the preheating absorption tower (22) through the preheating circulation pump (23). The discharge pipe is provided with a preheating circulation valve (24). ), the discharge pipe is connected to the jet liquefaction pump (4), a preheating discharge valve (25) is provided on the discharge pipe, the discharge port of the preheating stirring tank (21) is connected to the liquefaction preheating system (3) through a pipeline, the air inlet of the preheating absorption tower (22) is connected to the air outlet of the saccharification liquid cooling system (9) and the air outlet of the liquefaction preheating system (3), the air outlet of the preheating absorption tower (22) is connected to the tail gas condensation washing discharge device (18), and the preheating absorption tower (22) is an integrated three-stage absorption tower, The preheating absorption tower (22) comprises a preheating tank body (221), a preheating feed pipe (222), a preheating nozzle (223), a preheating collection ring (224) and a preheating distribution plate (225). The lower end of the preheating tank body (221) is funnel-shaped and is provided with a hot material outlet. Two preheating liquid sealing devices are provided in the preheating tank body (221). The two preheating liquid sealing devices divide the inner cavity of the preheating tank body (221) into three absorption chambers arranged in sequence from top to bottom, namely, a preheating upper absorption chamber (226), a preheating middle absorption chamber (227) and a preheating lower absorption chamber (228). The three absorption chambers are A preheating collection ring (224) and a preheating distribution plate (225) are provided, and the preheating collection ring (224) and the preheating distribution plate (225) are arranged up and down. A preheating feed pipe (222) is provided in the preheating upper absorption chamber (226), and a preheating nozzle (223) is provided at one end of the preheating feed pipe (222) located in the preheating tank body (221). The air outlet is provided at the upper end of the preheating upper absorption chamber (226). The three absorption chambers are all provided with air inlets, and the air inlets are provided on the preheating tank body (221) below the preheating distribution plate (225). The three absorption chambers are all provided with air outlets. The preheating collection ring (224) is a funnel-shaped structure with a larger opening at the upper end and a smaller opening at the lower end. The upper end of the preheating collection ring (224) is connected to the inner wall of the preheating tank body (221). The preheating distribution plate (225) is a funnel-shaped structure, and a bracket for connecting to the inner wall of the preheating tank body (221) is arranged in its circumference. The upper opening of the preheating distribution plate (225) corresponds to the lower opening of the preheating collection ring (224), and the upper opening of the preheating distribution plate (225) is larger than or equal to the lower opening of the preheating collection ring (224). The saccharification liquid cooling system (9) comprises three saccharification liquid flash evaporation heat release tanks, which are connected in series. The feed port of the first saccharification liquid flash evaporation heat release tank is connected to the discharge port of the saccharification liquid high-temperature pump (11), the discharge port of the previous saccharification liquid flash evaporation heat release tank is connected to the feed port of the next saccharification liquid flash evaporation heat release tank, and the discharge port of the last saccharification liquid flash evaporation heat release tank is connected to the saccharification liquid buffer tank (10). The gas outlets of the three saccharification liquid flash evaporation heat release tanks are respectively connected to the gas inlets of three preheating absorption chambers of the preheating absorption tower (22).

2. The energy-saving jet liquefaction system for producing alcohol from starchy raw materials according to claim 1, Features: The mixing screw conveyor (1) is connected to a starch material source (14), a liquefaction enzyme source (15), residual mash filtrate (16) after distillation, and wine gas cooling water (17).

3. The energy-saving jet liquefaction system for producing alcohol from starchy raw materials according to claim 1, Features: The liquefaction preheating system (3) comprises a plurality of preliquefaction devices, which are connected in series in sequence. The preliquefaction devices comprise a preliquefaction stirring tank (301), a preliquefaction absorption tower (302), a preliquefaction circulation pump (303), a preliquefaction circulation valve (304) and a preliquefaction discharge valve (305). The upper part of the preliquefaction stirring tank (301) is provided with a feed inlet and a discharge outlet, the lower end of the preliquefaction stirring tank (301) is provided with a circulation outlet, and the preliquefaction stirring tank (301) is provided with a circulation outlet. The circulating material port of the mixing tank (301) is connected to a circulating material discharge pipe and a discharge pipe. The circulating material discharge pipe is connected to the feed port of the pre-liquefaction absorption tower (302) through a pre-liquefaction circulating pump (303). The discharge pipe is connected to the feed port of the jet liquefaction pump (4). The circulating material discharge pipe is provided with a pre-liquefaction circulating valve (304). The discharge pipe is provided with a pre-liquefaction discharge valve (305). The air inlet of the pre-liquefaction absorption tower (302) is connected to the liquefied mash cooling system (7). The pre-liquefaction absorption tower (302) is an integrated multi-stage absorption tower, which includes a plurality of mutually independent pre-liquefaction absorption chambers, each pre-liquefaction absorption chamber is provided with an air inlet, the feed inlet of the pre-liquefaction stirring tank (301) of the first pre-liquefaction device among the plurality of pre-liquefaction devices connected in series is connected to the discharge port of the pre-heating stirring tank (21) of the primary pre-heating device (2), and the discharge port of the pre-liquefaction stirring tank (301) of the first pre-liquefaction device is connected to the discharge port of the pre-heating stirring tank (21) of the second pre-heating device (2). The feed inlet of the preliquefaction stirring tank (301) of the preliquefaction device, the exhaust port of the preliquefaction absorption tower (302) of the previous preliquefaction device is connected to the air inlet of the preliquefaction absorption tower (302) of the next preliquefaction device, the discharge port of the preliquefaction stirring tank (301) of the last preliquefaction device is connected to the feed inlet of the jet liquefaction pump (4), and the air outlet of the preliquefaction absorption tower (302) of the last preliquefaction device is connected to the air inlet of the preheating absorption tower (22) of the primary preheating device (2).

4. The energy-saving jet liquefaction system for producing alcohol from starchy raw materials according to claim 1, Features: The liquefaction system (6) comprises a plurality of laminar flow liquefaction columns (601), wherein the plurality of laminar flow liquefaction columns (601) are connected in series in sequence, wherein the feed port of the first laminar flow liquefaction column (601) is connected to the discharge port of the jet liquefier (5), the discharge port of the previous laminar flow liquefaction column (601) is connected to the feed port of the next laminar flow liquefaction column (601), and the discharge port of the last laminar flow liquefaction column (601) is connected to the feed port of the liquefied mash cooling system (7).

5. The energy-saving jet liquefaction system for producing alcohol from starchy raw materials according to claim 1, Features: The liquefaction system (6) comprises a plurality of liquefaction stirring tanks (602), wherein the plurality of liquefaction stirring tanks (602) are connected in series in sequence, wherein the feed port of the first liquefaction stirring tank (602) is connected to the discharge port of the jet liquefier (5), the discharge port of the previous liquefaction stirring tank (602) is connected to the feed port of the next liquefaction stirring tank (602), and the discharge port of the last liquefaction stirring tank (602) is connected to the feed port of the liquefied mash cooling system (7).

6. The energy-saving jet liquefaction system for producing alcohol from starchy raw materials according to claim 1, Features: The liquefied mash cooling system (7) comprises a plurality of flash tanks, which are connected in series in sequence. The feed port of the first flash tank is connected to the feed port of the liquefaction system (6), the feed port of the previous flash tank is connected to the feed port of the next flash tank, and the feed port of the last flash tank is connected to the feed port of the saccharification tank (8). The n adjacent flash tanks in the plurality of flash tanks connected in series form a group, where n is equal to the number of pre-liquefaction absorption chambers in the pre-liquefaction absorption tower (302). Each flash tank is provided with an air outlet, and the n air outlets of a group of flash tanks are respectively connected to the multiple air inlets of a pre-liquefaction absorption tower (302) of a pre-liquefaction device.

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