CN211142020U

CN211142020U - Energy-saving jet liquefaction system for producing alcohol by starchy raw materials

Info

Publication number: CN211142020U
Application number: CN201921872588.4U
Authority: CN
Inventors: 孙发喜; 李文娟; 孙帅强; 李世航; 张兆奇; 孙帅文; 李宇恒
Original assignee: Zhengzhou Boda Concentrated Drying Equipment Co ltd
Current assignee: Zhengzhou Boda Concentrated Drying Equipment Co ltd
Priority date: 2019-11-02
Filing date: 2019-11-02
Publication date: 2020-07-31
Anticipated expiration: 2029-11-02

Abstract

The utility model belongs to the technical field of equipment for starchiness raw materials production alcohol, concretely relates to energy-conserving injection liquefaction system of starchiness raw materials production alcohol, wherein: including mixing material screw conveyer, elementary preheating device, liquefaction system of preheating, injection liquefaction pump, injection liquefier, liquefaction system, liquefaction mash cooling system, saccharification jar, saccharification liquid cooling system, saccharification liquid buffer tank, saccharification liquid high temperature pump, saccharification liquid cryopump, heat exchanger and tail gas condensation washing discharging equipment, the utility model discloses a heat that gives off in the liquefaction mash cooling process after with starchy material liquefaction and the heat recovery that gives off in the saccharification liquid cooling process after the saccharification, then utilize the heat of retrieving to carry out multistage preheating to starchy material, make it warm up the liquefaction step by step to realize that the waste heat of liquefaction mash and saccharification liquid is retrieved and is recycled, reach energy saving and emission reduction, reduce the manufacturing cost of alcohol, improve enterprise competitiveness's purpose.

Description

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

The technical field is as follows:

the utility model belongs to the technical field of equipment for starchiness raw materials production alcohol, concretely relates to energy-conserving injection liquefaction system of starchiness raw materials production alcohol.

Background art:

in the prior art, when starchy raw materials such as corn, cassava, rice, wheat, sorghum and the like are utilized to produce alcohol, the adopted process method generally comprises the process steps of raw material crushing, liquefaction, saccharification, fermentation, distillation, residue separation and the like, after the raw materials are crushed, the starchy raw materials are required to be mixed and stirred with liquefying enzyme firstly during liquefaction, the temperature is raised to 95-103 ℃ for liquefaction after the injection liquefaction, the liquefied raw materials are subjected to heat exchange with cold water through a plate heat exchanger, liquefied mash is cooled to about 60 ℃ and enters a saccharification tank for saccharification, the cold water is cooled through a glass fiber reinforced plastic cooling tower after being heated and is recycled, the saccharified liquid is subjected to heat exchange with cooling water through the plate heat exchanger to about 45 ℃ and then enters a saccharification temporary storage tank for storage, the saccharified mash is cooled and then fermented, and the cooled and recycled cold water after being heated not only causes heat waste during the cooling recycling process of the liquefied, meanwhile, cooling water is consumed, and heat is consumed and wasted in the process that the saccharification liquid is cooled to 45 ℃ for storage, so that when the existing starchy raw material is used for producing alcohol, energy consumption is large, a large amount of energy is wasted, and a large amount of cooling water is consumed in the process of liquefying and saccharifying the starchy raw material. The method has the advantages of high cost of producing alcohol by using the starchy raw material, few ways for reducing the cost, and recycling and reusing the heat of high-temperature steam, the heat of liquefied mash and the heat of saccharified liquid after the starchy raw material is cooked, so that the purposes of reducing the production cost of alcohol, saving energy, reducing emission and improving the enterprise competitiveness are achieved, and the method is a difficult problem for technical personnel in the industry.

The utility model has the following contents:

to sum up, in order to overcome prior art problem not enough, the utility model provides an energy-conserving injection liquefaction system of starchiness raw materials production alcohol, it is the heat that gives off in the liquefaction mash cooling process after the starchiness raw materials liquefaction and the heat recovery that gives off in the saccharification liquid cooling process after the saccharification, then utilize the heat of retrieving to carry out multistage preheating to the starchiness raw materials, make it heat up the liquefaction step by step, thereby realize that the waste heat of liquefaction mash and saccharification liquid is retrieved and is recycled, reach energy saving and emission reduction, reduce the manufacturing cost of alcohol, improve enterprise competitiveness's purpose.

In order to solve the technical problem, the utility model discloses a technical scheme does:

an energy-saving jet liquefaction system for producing alcohol by using starchy raw materials, wherein: the device comprises a material 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 cache tank, a saccharification liquid high-temperature pump, a saccharification liquid low-temperature pump, a heat exchanger and a tail gas condensation washing and discharging device, wherein the material mixing screw conveyor uniformly mixes and stirs a starchy material, a liquefied enzyme, a distilled residual mash filtrate and wine gas cooling water in a conveying process to form a mixture; the primary preheating device preheats the mixture by using secondary steam emitted by cooling the saccharification liquid, and the mixture is preliminarily heated and liquefied; the liquefaction preheating system preheats the preliminarily heated and liquefied mixture by utilizing the secondary steam evaporated from the liquefied mash, and the mixture is heated and liquefied step by step; the liquefaction system heats the liquefied mixture by using raw steam, the temperature of the liquefied mixture is gradually raised, the mixed liquid is converted into liquefied mash, and the liquefied mash cooling system cools the liquefied mash and flashes secondary steam out; the saccharifying tank saccharifies the cooled liquefied mash by using saccharifying enzyme; the saccharification liquid cooling system is used for cooling saccharification liquid and evaporating secondary steam, the tail gas condensation washing and discharging device is used for condensing and cleaning tail gas discharged by the primary preheating device and then discharging the tail gas, the discharge port of the material mixing screw conveyor is communicated with the primary preheating device, the discharge port of the primary preheating device is communicated with the feed port of the liquefaction preheating system, the discharge port of the liquefaction preheating system is connected with the feed port of the injection liquefier through an injection liquefying pump, the air inlet of the injection liquefier is communicated with a steam source, the discharge port of the injection liquefier is communicated with the feed port of the liquefaction system, the discharge port of the liquefaction system is communicated with the feed port of the liquefaction mash cooling system, the air outlet of the liquefaction mash cooling system is connected with the liquefaction preheating system, the discharge port of the liquefaction mash cooling system is communicated with the feed port of the saccharification tank through a saccharification liquid high-temperature pump, the discharge port of the saccharified liquid cooling system is communicated with the feed port of the saccharified liquid cache tank, the gas outlet of the saccharified liquid cooling system is communicated with the gas inlet of the primary preheating device, the gas outlet of the primary preheating device is communicated with the tail gas condensation washing and discharging device, and the discharge port of the saccharified liquid cache tank is communicated with the heat exchanger through a saccharified liquid low-temperature pump.

Further, the material mixing screw conveyer is connected with a starchiness material source, a liquefying enzyme source, the distilled residual mash filtrate and wine gas cooling water.

Further, elementary preheating device including preheat the agitator tank, preheat the absorption tower, preheat circulating pump, preheat the circulating valve and preheat the bleeder valve, the feed inlet intercommunication of preheating the agitator tank mix the discharge gate of material screw conveyer, the circulation material mouth of preheating the agitator tank connects discharging pipe and row's material pipe, the discharging pipe feed inlet of preheating the absorption tower through preheating the circulating pump intercommunication, be provided with on the discharging pipe and preheat the circulating valve, row's material pipe intercommunication spray liquefaction pump, be provided with on the row's material pipe and preheat the bleeder valve, the discharge gate of preheating the agitator tank pass through pipe connection liquefaction system of preheating, the air inlet of preheating the absorption tower air inlet intercommunication saccharification liquid cooling system's gas outlet and liquefaction system of preheating's gas outlet, the gas outlet of preheating the absorption tower communicate tail gas condensation washing discharging device, preheating the absorption tower multistage absorption tower of integral type, the preheating absorption cavity comprises a plurality of mutually independent preheating absorption cavities, and each preheating absorption cavity is provided with an air inlet.

Further, liquefaction preheating system include a plurality of preliquefaction devices, a plurality of preliquefaction devices are series connection in proper order, preliquefaction device include preliquefaction agitator tank, preliquefaction absorption tower, preliquefaction circulating pump, preliquefaction circulating valve and preliquefaction blow-off valve, the upper portion of preliquefaction agitator tank set up feed inlet and discharge gate, the lower extreme of preliquefaction agitator tank sets up the circulation mouth, the circulation mouth of preliquefaction agitator tank connects circulation discharging pipe and row material pipe, circulation discharging pipe pass through the feed inlet of preliquefaction circulating pump intercommunication preliquefaction absorption tower, row material pipe intercommunication jet liquefaction pump's feed inlet, the circulation discharging pipe on be provided with the preliquefaction circulating valve, row material pipe on be provided with the preliquefaction valve, the air inlet intercommunication liquefaction mash cooling system's of preliquefaction absorption tower gas outlet, the preliquefaction absorption tower multistage, the pre-liquefaction device comprises a plurality of mutually independent pre-liquefaction absorption cavities, wherein an air inlet is formed in each pre-liquefaction absorption cavity, a feed port of a pre-liquefaction stirring tank of a first pre-liquefaction device in the pre-liquefaction devices connected in series is communicated with a discharge port of a pre-preheating tank of the primary preheating device, a discharge port of a pre-liquefaction stirring tank of a previous pre-liquefaction device is communicated with a feed port of a pre-liquefaction stirring tank of a next pre-liquefaction device, an air outlet of a pre-liquefaction absorption tower of the previous pre-liquefaction device is communicated with an air inlet of a pre-liquefaction absorption tower of the next pre-liquefaction device, a discharge port of a pre-liquefaction stirring tank of a last pre-liquefaction device is communicated with a feed port of an injection liquefaction pump, and an air outlet of the pre-liquefaction absorption tower of the last pre-liquefaction device.

Further, the liquefaction system include a plurality of laminar flow liquefaction columns, a plurality of laminar flow liquefaction columns are connected in series in proper order, the discharge gate of first laminar flow liquefaction column intercommunication injection liquefier, the discharge gate of preceding laminar flow liquefaction column intercommunication the feed gate of the laminar flow liquefaction column of back, the discharge gate of last laminar flow liquefaction column intercommunication liquefaction mash cooling system's feed gate.

Further, the liquefaction system include a plurality of liquefaction agitator tanks, a plurality of liquefaction agitator tanks are series connection in proper order, the discharge gate of the feed inlet intercommunication injection liquefier of first liquefaction agitator tank, the feed inlet of the last liquefaction agitator tank, the feed inlet of the discharge gate intercommunication back liquefaction agitator tank of preceding liquefaction agitator tank, the feed inlet of the discharge gate intercommunication liquefaction mash cooling system of last liquefaction agitator tank.

Further, the liquefied mash cooling system comprises a plurality of flash tanks, the flash tanks are sequentially connected in series, a feed inlet of a first flash tank is communicated with a discharge outlet of the liquefaction system, a discharge outlet of a previous flash tank is communicated with a feed inlet of a next flash tank, a discharge outlet of a last flash tank is communicated with a feed inlet of the saccharification tank, n adjacent flash tanks in the flash tanks are in a group, n is equal to the number of pre-liquefaction absorption cavities in the pre-liquefaction absorption tower, each flash tank is provided with a gas outlet, and n gas outlets of the flash tanks are respectively communicated with a plurality of gas inlets of the pre-liquefaction absorption tower of the pre-liquefaction device.

Further, the saccharified liquid cooling system comprises a plurality of saccharified liquid flash evaporation heat release tanks, the plurality of saccharified liquid flash evaporation heat release tanks are connected in series, a feed inlet of a first saccharified liquid flash evaporation heat release tank is communicated with a discharge outlet of the saccharified liquid high-temperature pump, a discharge outlet of a previous saccharified liquid flash evaporation heat release tank is communicated with a feed inlet of a next saccharified liquid flash evaporation heat release tank, a discharge outlet of a last saccharified liquid flash evaporation heat release tank is communicated with the saccharified liquid cache tank, the number of the saccharified liquid flash evaporation heat release tanks is the same as that of preheating absorption cavities of a preheating absorption tower of the primary preheating device, and a gas outlet of one saccharified liquid flash evaporation heat release tank is communicated with a gas inlet of a preheating absorption cavity of the preheating absorption.

The utility model has the advantages that:

1. the utility model discloses a heat recovery that gives off and saccharification after saccharify in the saccharification liquid cooling process in the heat that gives off in the liquefaction mash cooling process after the starchy raw materials liquefaction, then utilize the heat of retrieving to carry out the multistage preheating to starchy raw materials, make it heat up the liquefaction step by step to the waste heat that realizes liquefaction mash and saccharification liquid retrieves and recycles, reaches energy saving and emission reduction, reduces the manufacturing cost of alcohol, improves enterprise competitiveness's purpose.

2. The utility model discloses set up elementary preheating device, the air inlet intercommunication saccharification liquid cooling system's of elementary preheating device's the absorption tower air outlet that preheats, in the saccharification liquid cooling in-process produced secondary steam gets into preheats the absorption tower, in preheating the absorption tower, the secondary steam that the saccharification liquid cooling produced is absorbed by starchiness mixture to with starchiness mixture by initial 40 ℃ heaies up to 54 ℃, the utility model discloses an elementary preheating device's preheating absorption tower contains three absorption chamber that preheats, corresponds saccharification liquid cooling system's three flash distillation heat release jar respectively, realizes the tertiary staged intensification of starchiness mixture in preheating the absorption tower, and secondary steam absorption utilization is high, and is efficient, the heat that the absorption saccharification liquid heat dissipation that can be abundant releases.

3. The utility model discloses a liquefaction system of preheating includes the liquefaction device in advance that three series connection set up, the utility model discloses a liquefaction glutinous rice cooling system includes the flash tank that six series connections set up, every liquefaction device corresponds two flash tanks in advance, the flash tank that six series connections set up makes the liquefaction glutinous rice flash distillation cooling after the liquefaction stage by stage, cooling interval divides more finely and finely divided, per two flash tanks correspond a liquefaction device in advance, and the liquefaction absorption tower in advance of liquefaction device contains two liquefaction and preheats the absorption chamber, then the starchiness raw materials that gets into the absorption tower in advance divide the secondary steam of twice absorption different temperatures, the secondary steam that the absorption flash tank that can be more effective quick evaporated, be favorable to the recovery of the steam that the liquefaction glutinous rice evaporated and send to recycle.

4. The utility model discloses an inner chamber of primary preheating device's preheating absorption tower is cut apart into three absorption chamber by preheating liquid seal device, preheat the mutual independence of liquid seal device realization two adjacent absorption chambers, the utility model discloses an inner chamber of pre-liquefaction absorption tower of pre-liquefaction device is cut apart into two absorption chambers by pre-liquefaction liquid seal device, pre-liquefaction liquid seal device realizes the mutual independence of two absorption chambers, preheat liquid seal device and pre-liquefaction liquid seal device structure the same, all insert in the overflow weir through the unloading pipe lower extreme, the unloading speed of overflow weir is less than feed rate far away, thereby make the material store the weir in the overflow weir, utilize the material of storage in the overflow weir to realize the sealed between two adjacent absorption chambers, realize the mutual independence in two adjacent absorption chambers, moreover, the steam generator is simple in structure, think about ingenious, utilize the material sealed, and is effectual, simultaneously reduce cost.

5. The utility model discloses simple structure, the design is novel ingenious, and convenient operation is swift, can be effectual the heat that runs off among the recovery starchiness material production alcohol process, be used for preheating and precooking starchiness material once more with this heat simultaneously, realize the liquefaction of starchiness raw materials to energy consumption in the greatly reduced alcohol production process reduces the emission of hot gas, practices thrift the required cooling water quantity of hot gas cooling, reduces the manufacturing cost of starchiness material production alcohol, realizes energy saving and emission reduction purpose.

Description of the drawings:

fig. 1 is a schematic structural view of the present invention;

FIG. 2 is a schematic structural view of the preheating absorption tower of the present invention;

fig. 3 is a schematic structural view of a pre-liquefaction absorption tower of the present invention;

fig. 4 is another schematic structural diagram of the present invention.

Detailed Description

The present invention will be described in further detail with reference to the accompanying drawings and examples.

Example one

As shown in fig. 1, 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 temperature reduction system 7, a saccharification tank 8, a saccharification liquid temperature reduction system 9, a saccharification liquid cache tank 10, a saccharification liquid high-temperature pump 11, a saccharification liquid low-temperature pump 12, a heat exchanger 13 and a tail gas condensation washing discharge device 18, wherein the mixing screw conveyor 1 uniformly mixes and stirs starchy raw materials, liquefied enzymes, distilled residual mash filtrate and wine gas cooling water in a conveying process to form a mixture; the primary preheating device 2 preheats the mixture by using secondary steam emitted by cooling the saccharification liquid, and the mixture is preliminarily heated and liquefied; the liquefaction preheating system 3 preheats the mixture which is preliminarily heated and liquefied by using the secondary steam evaporated from the liquefied mash, and the mixture is heated and liquefied step by step; the liquefaction system 6 heats the liquefied mixture by using the raw steam, the temperature of the liquefied mixture is gradually raised, the mixed liquid is converted into liquefied mash, and the liquefied mash cooling system 7 cools the liquefied mash and flashes secondary steam out; the saccharification tank 8 saccharifies the cooled liquefied mash by using saccharifying enzyme; the saccharified liquid cooling system 9 is used for cooling saccharified liquid and evaporating secondary steam, the tail gas condensing, washing and discharging device 18 is used for condensing and cleaning tail gas discharged by the primary preheating device and then discharging the tail gas, the material mixing screw conveyor 1 is connected with a starchiness material source 14, a liquefied enzyme source 15, distilled residual mash filtrate 16 and wine gas cooling water 17, a discharge port of the material mixing screw conveyor 1 is communicated with the primary preheating device 2, the primary preheating device 2 comprises a preheating stirring tank 21, a preheating absorption tower 22, a preheating circulating pump 23, a preheating circulating valve 24 and a preheating discharge valve 25, a feed port of the preheating stirring tank 21 is communicated with a discharge port of the material mixing screw conveyor 1, a circulating material port of the preheating stirring tank 21 is connected with a discharge pipe and a discharge pipe, the discharge pipe is communicated with a feed port of the preheating absorption tower 22 through the preheating circulating pump 23, and the preheating circulating valve 24 is arranged on the discharge pipe, arrange material pipe intercommunication jet liquefaction pump 4, be provided with on the material pipe and preheat the relief valve 25, the discharge gate of preheating agitator tank 21 pass through pipe connection liquefaction and preheat system 3, the gas inlet intercommunication saccharification liquid cooling system 9 of preheating absorption tower 22 the gas outlet and the liquefaction of preheating system 3 the gas outlet, the gas outlet intercommunication tail gas condensation washing discharging equipment 18 of preheating absorption tower 22. The preheating absorption tower 22 is an integrated multistage absorption tower, and comprises three mutually independent preheating absorption cavities, and each preheating absorption cavity is provided with an air inlet.

The liquefaction preheating system 3 comprises three pre-liquefaction devices, the three pre-liquefaction devices are sequentially connected in series and are divided into a first pre-liquefaction device 31, a second pre-liquefaction device 32 and a third pre-liquefaction device 33, the three pre-liquefaction devices are identical in structure and respectively comprise a pre-liquefaction stirring tank 301, a pre-liquefaction absorption tower 302, a pre-liquefaction circulating pump 303, a pre-liquefaction circulating valve 304 and a pre-liquefaction discharge valve 305, a feed inlet and a discharge outlet are formed in the upper part of the pre-liquefaction stirring tank 301, a circulating material port is formed in the lower end of the pre-liquefaction stirring tank 301, the circulating material port of the pre-liquefaction stirring tank 301 is connected with a circulating discharge pipe and a discharge pipe, the circulating discharge pipe is communicated with the feed inlet of the pre-liquefaction absorption tower 302 through the pre-liquefaction circulating pump 303, the discharge pipe is communicated with the feed inlet of the injection liquefaction pump 4, the pre-liquefaction circulating discharge valve 304 is arranged on the circulating, the air inlet of the pre-liquefaction absorption tower 302 is communicated with the air outlet of the liquefied mash cooling system 7.

The liquefied mash cooling system 7 comprises six flash tanks, the six flash tanks are sequentially connected in series and are respectively 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, a feed inlet of the first flash tank 71 is communicated with a discharge outlet of the liquefaction system 6, a discharge outlet of the first flash tank 71 is communicated with a feed inlet of the second flash tank 72, a discharge outlet of the second flash tank 72 is communicated with a feed inlet of the third flash tank 73, a discharge outlet of the third flash tank 73 is communicated with a feed inlet of the fourth flash tank 74, a discharge outlet of the fourth flash tank 74 is communicated with a feed inlet of the fifth flash tank 75, a discharge outlet of the fifth flash tank 75 is communicated with a feed inlet of the sixth flash tank 76, and a discharge outlet of the sixth flash tank 76 is communicated with a feed.

The feed inlet intercommunication of the pre-liquefaction agitator tank 301 of first pre-liquefaction device 31 preheats the discharge gate of agitator tank 21, the discharge gate intercommunication of the pre-liquefaction agitator tank 301 of first pre-liquefaction device 31 the feed inlet of the pre-liquefaction agitator tank 301 of second pre-liquefaction device 32, the discharge gate intercommunication of the pre-liquefaction agitator tank 301 of second pre-liquefaction device 32 the feed inlet of the pre-liquefaction agitator tank 301 of third pre-liquefaction device 33, the discharge gate intercommunication of the pre-liquefaction agitator tank 301 of third pre-liquefaction device 33 sprays the feed inlet of liquefaction pump 4, the discharge gate intercommunication of spraying liquefaction pump 4 sprays the feed inlet of liquefier 5, the air inlet intercommunication steam source 19 of spraying liquefier 5, the discharge gate intercommunication of spraying liquefier 5 the feed inlet of liquefaction system 6.

The liquefaction system 6 comprises a plurality of laminar flow liquefaction columns 601, the laminar flow liquefaction columns 601 are sequentially connected in series, a feed inlet of the first laminar flow liquefaction column 601 is communicated with a discharge outlet of the injection liquefier 5, a discharge outlet of the previous laminar flow liquefaction column 601 is communicated with a feed inlet of the next laminar flow liquefaction column 601, and a discharge outlet of the last laminar flow liquefaction column 601 is communicated with a feed inlet of the first flash tank 71 of the liquefied mash cooling system 7.

The gas inlet of the pre-liquefaction absorption tower 302 of the first pre-liquefaction device 31 is communicated with the gas outlets of the fifth flash tank 75 and the sixth flash tank 76, the gas outlet of the pre-liquefaction absorption tower 302 of the first pre-liquefaction device 31 is communicated with the gas inlet of the preheating absorption tower 22 of the primary preheating device 2, the gas inlet of the pre-liquefaction absorption tower 302 of the second pre-liquefaction device 32 is communicated with the gas outlets of the third flash tank 73 and the fourth flash tank 74, the gas outlet of the pre-liquefaction absorption tower 302 of the second pre-liquefaction device 32 is communicated with the gas inlet of the pre-liquefaction absorption tower 302 of the first pre-liquefaction device 31, the gas inlet of the pre-liquefaction absorption tower 302 of the third pre-liquefaction device 33 is communicated with the gas outlets of the first flash tank 71 and the second flash tank 72, the gas outlet of the pre-liquefaction absorption tower 302 of the third pre-liquefaction device 33 is communicated with the gas inlet of the pre-liquefaction absorption tower 302 of the second pre-liquefaction device 32,

a discharge port of the saccharification tank 8 is communicated with a feed port of a saccharification liquid cooling system 9 through a saccharification liquid high-temperature pump 11, a discharge port of the saccharification liquid cooling system 9 is communicated with a feed port of a saccharification liquid cache tank 10, an air outlet of the saccharification liquid cooling system 9 is communicated with an air inlet of the primary preheating device 2, a discharge port of the saccharification liquid cache tank 10 is communicated with a heat exchanger 13 through a saccharification liquid low-temperature pump 12, the saccharification liquid cooling system 9 comprises three saccharification liquid flash evaporation heat release tanks which are connected in series, the feed port of a first saccharification liquid flash evaporation heat release tank 91 is communicated with a discharge port of the saccharification liquid high-temperature pump 11, the discharge port of a first saccharification liquid flash evaporation heat release tank 91 is communicated with a feed port of a second saccharification liquid flash evaporation heat release tank 92, the discharge port of the second saccharification liquid flash evaporation heat release tank 92 is communicated with a feed port of a third saccharification liquid flash evaporation heat release tank 93, and the discharge port of the third saccharification liquid flash evaporation heat release tank 93, the air outlet of the first saccharified liquid flash evaporation heat release tank 91, the air outlet of the second saccharified liquid flash evaporation heat release tank 92 and the air outlet of the third saccharified liquid flash evaporation heat release tank 93 are respectively communicated with the air inlets of three mutually independent preheating absorption cavities of the preheating absorption tower 22 of the primary preheating device 2.

As shown in fig. 2, the preheating absorption tower 22 of the primary preheating device 2 includes a preheating tank 221, a preheating feed pipe 222, a preheating spray head 223, a preheating collecting ring 224 and a preheating distribution plate 225, the lower end of the preheating tank 221 is funnel-shaped, a hot material outlet is provided thereon, two preheating liquid seal devices are provided in the preheating tank 221, the two preheating liquid seal devices divide the inner cavity of the preheating tank 221 into three absorption cavities which are sequentially arranged from top to bottom, and are respectively a preheating upper absorption cavity 226, a preheating middle absorption cavity 227 and a preheating lower absorption cavity 228, the preheating collecting ring 224 and the preheating distribution plate 225 are provided in each of the three absorption cavities, the preheating collecting ring 224 and the preheating distribution plate 225 are arranged above and below, the preheating feed pipe 222 is provided in the preheating upper absorption cavity 226, and the preheating spray head 223 is provided at one end of the preheating feed pipe 222 in the preheating tank 221, the air outlet is arranged at the upper end of the preheating upper absorption cavity 226, the three absorption cavities are all provided with air inlets, the air inlets are arranged on the preheating tank body 221 below the preheating distribution disc 225, the three absorption cavities are all provided with air outlets, the preheating liquid sealing device comprises an inner cone 229, a blanking pipe 2210, an overflow weir 2211 and tower plate groups 2212, the inner cone 229 is arranged in the preheating tank body 221 and fixedly connected with the inner wall of the preheating tank body 221, the lower end of the inner cone 229 is provided with a blanking pipe 2210, the blanking pipe 2210 is inserted into the overflow weir 2211, the tower plate groups 2212 support the overflow weir 2211, the tower plate groups 2212 are connected with 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, the sealing plate at the lower end of the overflow weir 2211 is provided with small water holes 2210 is inserted into the overflow weir 2211, the column plate group 2212 comprises a lower water eaves 2213 and a lower support, the lower support is connected with the inner wall of the preheating tank body 221, the lower support supports the lower water eaves 2213, the lower water eaves 2213 are of a hollow conical structure with openings at the upper end and the lower end, the upper end opening of the lower water eaves 2213 is connected with the lower end of the overflow weir 2211, the lower end of the lower water eaves 2213 is suspended, a blanking channel is formed between the lower end of the lower water eaves 2213 and the inner wall of the preheating tank body 221, an annular water retaining ring 2214 is arranged on the lower water eaves 2213, the upper end of the water retaining ring 2214 is provided with the zigzag weir, the outer wall of the water retaining ring 2214 is connected with the inner wall of the preheating tank body 221 through a support, a blanking gap is formed between the lower end of the water retaining ring 2214 and the lower water eaves 2213, and a blanking channel is formed between the outer wall of the; the preheating collecting ring 224 is a funnel-shaped structure with a large opening at the upper end and a small opening at the lower end, and the upper end of the preheating collecting ring 224 is connected with the inner wall of the preheating tank body 221; the preheating distribution disc 225 is of a funnel-shaped structure, a support used for being connected with the inner wall of the preheating tank body 221 is arranged on the circumferential direction of the preheating distribution disc 225, an upper end opening of the preheating distribution disc 225 corresponds to a lower end opening of the preheating collection ring 224, the upper end opening of the preheating distribution disc 225 is larger than or equal to the lower end opening of the preheating collection ring 224, a through hole is formed in the lower end of the preheating distribution disc 225, a small blanking hole is formed in the side wall of the funnel-shaped preheating distribution disc 225, the size of the small blanking hole is smaller than that of the through hole, the size of the through hole is smaller than that of the upper end opening, and a sawtooth-shaped weir plate; the preheating upper absorption cavity 226 is internally provided with a grid which is arranged above the preheating collecting ring 224 in the preheating upper absorption cavity 226.

As shown in fig. 3, the pre-liquefaction absorption tower 302 of the pre-liquefaction device includes a pre-liquefaction tank 3021, a pre-liquefaction feed pipe 3022, a pre-liquefaction spray head 3023, a pre-liquefaction collecting ring 3024, and a pre-liquefaction distribution tray 3025, the pre-liquefaction tank 3021 has a funnel-shaped lower end on which a hot material outlet is provided, the pre-liquefaction tank 3021 has a pre-liquefaction liquid seal device therein, the pre-liquefaction liquid seal device divides an inner cavity of the pre-liquefaction tank 3021 into two absorption cavities sequentially arranged from top to bottom, which are a pre-liquefaction upper absorption cavity 3026 and a pre-liquefaction lower absorption cavity 3027, the two absorption cavities have a pre-liquefaction collecting ring 3024 and a pre-liquefaction distribution tray 3025 arranged therein, the pre-liquefaction collecting ring 3024 and the pre-liquefaction distribution tray 3025 are arranged from top to bottom, the pre-liquefaction upper absorption cavity 3026 has a pre-liquefaction feed pipe 3022 therein, one end of the pre-liquefaction feed pipe 3022 in the pre-liquefaction tank 3021 is provided with a, the gas outlet setting absorb the upper end of chamber 3026 on the preliquefaction, two absorb the chamber on all be provided with the air inlet, the air inlet sets up on the preliquefaction jar body 3021 under preliquefaction distributor disk 3025, two absorb the chamber on all be provided with the gas outlet, the preliquefaction liquid seal device the same with preheating liquid seal device structure, preliquefaction collector ring 3024 the same with preheating collector ring 224 structure, preliquefaction distributor disk 3025 the same with preheating distributor disk 225 structure, the preliquefaction on be provided with the grid in absorbing the chamber 3026, the grid set up the top of preliquefaction collector ring 3024 in absorbing the chamber 3026 on the preliquefaction.

When in use, the starchy raw material, the liquefied enzyme, the distilled residual mash filtrate 16 and the wine gas cooling water 17 are mixed and stirred uniformly in the material mixing screw conveyor 1, the wine gas cooling water 17 and the distilled residual mash filtrate 16 both contain heat, then the raw materials mixed in the material mixing screw conveyor 1 are mixed and stirred into a starchy mixture, and the temperature of the mixed and stirred mixture is about 40 ℃.

The starch mixture after mixing and stirring is conveyed by the stirring screw conveyor 1 to enter the preheating stirring tank 21, the preheating circulating pump 23 is started, the preheating circulating valve 24 is opened, the mixture in the preheating stirring tank 21 is conveyed to the preheating absorption tower 22, enters from a feeding pipe at the upper part of the preheating absorption tower 22, is sprayed into a conical shape by the preheating spray head 223 to enter a preheating upper absorption cavity 226 of the preheating absorption tower 22, falls along the inner wall of the preheating stirring tank 21 and then slides along the inner wall of the preheating collection ring 224, the starch mixture is gathered from the periphery to the center due to the funnel-shaped structure of the preheating collection ring 224, and when the starch mixture falls into the preheating distribution disc 225 from the preheating collection ring 224 due to a certain distance between the lower end of the preheating collection ring 224 and the preheating distribution disc 225, a water curtain-shaped material flow is formed between the preheating collection ring 224 and the preheating distribution disc 225, the starch mixture falls into the preheating distribution disc 225, because the preheating distribution disc 225 is in a funnel-shaped structure, the side wall of the preheating distribution disc 225 is provided with a feeding small hole, the lower end of the preheating distribution disc is provided with a through hole, the starchy mixture entering the preheating distribution disc 225 falls along the feeding small hole and the through hole at the lower end of the preheating distribution disc 225 to form a water curtain-shaped material flow, the secondary steam with the temperature of about 50 ℃ for cooling evaporation of the saccharifying liquid in the third saccharifying liquid flash evaporation heat-release tank 93 enters the preheating upper absorption cavity 226 from the air inlet of the preheating upper absorption cavity 226, flows upwards in the preheating upper absorption cavity 226 and meets the water curtain-shaped material flow below the preheating distribution disc 225 for heat exchange, the material absorbs the secondary steam, the temperature rises and liquefies, the secondary steam is cooled, and then the secondary steam continues to flow upwards, is blocked by the preheating distribution disc 225 when meeting the preheating distribution disc 225, the secondary steam flows upwards in a scattered manner, and then enters the preheating collection ring 224 from the lower end opening of the, the secondary steam flows upwards along the inner cavity of the preheating collecting ring 224, in the process, the secondary steam needs to pass through the water curtain-shaped material flow between the preheating collecting ring 224 and the preheating distribution disc 225, the material absorbs the secondary steam again to heat up, the secondary steam cools down, the secondary steam continues to flow upwards, the secondary steam passes through the cone-shaped material flow sprayed by the preheating spray head 223, the material absorbs the secondary steam again to heat up, finally the non-condensable gas is discharged from a non-condensable gas outlet at the upper end of the preheating upper absorbing cavity 226 and enters the tail gas condensation washing and discharging device 18, and the tail gas is discharged to the atmosphere after being condensed and cleaned.

The starch mixture absorbs secondary steam while heating in the preheating upper absorption cavity 226, the starch mixture is further liquefied, then the mixture flows out of the preheating upper absorption cavity 226 from the inner cone 229 and the blanking tube 2210 at the lower end of the preheating upper absorption cavity 226, the mixture enters the overflow weir 2211 through the blanking tube 2210, because the blanking speed of the overflow weir 2211 is far less than the feeding speed, the mixture is stored in the overflow weir 2211, the lower end of the blanking tube 2210 extends into the overflow weir 2211, liquid seal is realized, the material stored in the overflow weir 2211 flows out of the upper end of the overflow weir 2211, enters the preheating middle absorption cavity 227, the mixture overflowing from the overflow weir 2211 falls on the lower eave 2213 of the tower plate set 2212 and slides along the lower eave 2213, the lower eave 2214 is arranged on the lower eave 2213, part of the mixture slides along the blanking gap formed between the lower end of the water retaining ring 2214 and the lower eave 2213, and part of the mixture accumulates on the lower eave 2213, finally, the mixture overflows and slides down from the upper end of the lower water eaves 2213, the mixture entering the preheating middle absorption cavity 227 finally falls down in the form of a conical material flow under the action of the lower water eaves 2213 and the water retaining ring 2214 of the tower plate group 2212, then the mixture is collected under the action of the preheating collection ring 224 in the preheating middle absorption cavity 227 and falls into the preheating distribution disc 225 in the preheating middle absorption cavity 227 along the inner wall of the preheating collection ring 224, a water curtain-shaped material flow is formed between the preheating collection ring 224 and the preheating distribution disc 225, then the mixture falls down along the preheating distribution disc 225, a water curtain-shaped material flow is formed between the preheating distribution disc 225 and a preheating liquid sealing device, secondary steam which is released by cooling of the saccharification liquid in the second saccharification liquid flash evaporation heat release tank 92 and has the temperature of about 55 ℃ enters from the air inlet of the preheating middle absorption cavity 227, then flows upwards to meet and mix with the mixture in the absorption cavity 227 for multiple times, the mixture absorbs the secondary steam to further heat and liquefy, the non-condensable gas is discharged from a middle air outlet at the upper part of the preheating middle absorption cavity 227,

similarly, a preheating liquid sealing device is also arranged between the preheating middle absorption cavity 227 and the preheating lower absorption cavity 228, the mixture in the preheating middle absorption cavity 227 enters the preheating lower absorption cavity 228 through the preheating liquid sealing device and flows downwards, the secondary steam with the temperature of about 60 ℃ is released by cooling the saccharification liquid in the first saccharification liquid flash evaporation heat release tank 91, enters from the air inlet of the preheating middle absorption cavity 227 and then flows upwards, the mixture entering the preheating lower absorption cavity 228 is heated again and absorbs moisture in hot air, the mixture is further heated and liquefied, and 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 upper part of the preheating lower absorption cavity 228. The flow process of the starchy mixture in the preheating middle absorption cavity 227 and the preheating lower absorption cavity 228 is the same, and the flow process of the hot gas in the preheating middle absorption cavity 227 and the preheating lower absorption cavity 228 is the same.

The starchy mixture which is heated and liquefied after absorbing the secondary steam by the three preheating absorption cavities of the preheating absorption tower 22 flows out of a hot material outlet at the lower end of the preheating absorption tower 22 and enters the preheating agitation tank 21 again, so that the starchy mixture is heated to about 54 ℃ under the action of the preheating circulation pump 23, the starchy mixture heated by the primary preheating device 2 enters the pre-liquefaction agitation tank 301 of the first pre-liquefaction device 31 under the action of the injection liquefaction pump 4, and then is sent to the pre-liquefaction absorption tower 302 of the first pre-liquefaction device 31 under the action of the pre-liquefaction circulation pump 303 of the first pre-liquefaction device 31, the working principle of the pre-liquefaction absorption tower 302 is the same as that of the preheating absorption tower 22, the starchy mixture in the pre-liquefaction agitation tank 301 of the first pre-liquefaction device 31 enters the pre-liquefaction upper absorption cavity 3026 from the pre-liquefaction feeding pipe 3022 of the pre-liquefaction upper absorption cavity 3026 of the pre-liquefaction absorption tower 302 under the action of the pre-liquefaction circulation pump 303, the conical spray is directed into the pre-liquefaction upper absorption chamber 3026 by the pre-liquefaction spray head 3023 to form a conical stream of material, which, thereafter, then falls into a pre-liquefaction distribution disc 3025 after being collected by a pre-liquefaction collection ring 3024, a curtain-like material flow is formed between the pre-liquefaction collection ring 3024 and the pre-liquefaction distribution disc 3025 and then falls from the pre-liquefaction distribution disc 3025, and the 65 c secondary vapor evaporated by the sixth flash tank 76 enters from the air inlet of the pre-liquefaction upper absorption chamber 3026, flows upward, contacts with the starchiness mixture, the starchiness mixture absorbs the secondary steam, then the starchiness mixture enters the pre-liquefaction lower absorption cavity 3027 through the pre-liquefaction liquid seal device, in the pre-liquefaction lower absorption cavity 3027, the starchy mixture absorbs the 70 ℃ secondary steam evaporated by the fifth flash tank 75, and the starchy mixture entering the first pre-liquefaction device 31 is finally heated to 63 ℃.

The 63 ℃ starchy mixture enters the second pre-liquefaction device 32, and in the pre-liquefaction absorption tower 302 of the second pre-liquefaction device 32, the 63 ℃ starchy mixture absorbs the 79 ℃ secondary steam evaporated by the third flash tank 73 and the 74 ℃ secondary steam evaporated by the fourth flash tank 74, and the temperature of the starchy mixture is raised to 72 ℃. Then, the 72 ℃ starch mixture enters the third pre-liquefaction device 33, and in the pre-liquefaction absorption tower 302 of the third boiling liquefaction device, the 72 ℃ starch mixture absorbs the 83 ℃ secondary steam evaporated by the second flash tank 72 and the 88 ℃ secondary steam evaporated by the first flash tank 71, and the starch mixture is heated to 81 ℃.

The 81 ℃ starchy mixture is conveyed to the jet liquefier 5 through the jet liquefier pump 4, the high-temperature steam also enters the jet liquefier 5, the 81 ℃ starchy mixture is subjected to jet liquefaction in the jet liquefier 5 by the high-temperature steam, the starchy mixture absorbs the high-temperature steam, the temperature of the starchy mixture is raised to 88 ℃ and enters the liquefying system 6 in a jet state, and the starchy mixture is cooked and liquefied in the laminar flow liquefying column 601 of the liquefying system 6. The starchy mixture is steamed and liquefied to generate liquefied mash, and the temperature of the liquefied mash is 88 ℃.

The liquefied mash at 88 ℃ sequentially passes through 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 temperature of the liquefied mash is respectively reduced to 83 ℃, 79 ℃, 74 ℃, 70 ℃, 65 ℃ and 60 ℃, the liquefied mash at 60 ℃ discharged from the sixth flash tank 76 enters a saccharification tank 8, and the steam at 88 ℃, 83 ℃, 79 ℃, 74 ℃, 70 ℃ and 65 ℃ generated in the first flash tank 71, the second flash tank 72, the third flash tank 73, the fifth flash tank 75 and the sixth flash tank 76 enters three pre-liquefaction devices of a liquefaction preheating system 3 to be used for preheating and liquefying starch mixture.

Saccharifying enzyme is added into a saccharifying tank 8, liquefied mash is saccharified into saccharifying liquid, the temperature of the saccharifying liquid is 60 ℃, the saccharifying liquid at 60 ℃ enters a saccharifying liquid cooling system 9 under the action of a saccharifying liquid high-temperature pump 11, the saccharifying liquid sequentially passes through a first saccharifying liquid flash evaporation heat-releasing tank 91, a second saccharifying liquid flash evaporation heat-releasing tank 92 and a third saccharifying liquid flash evaporation heat-releasing tank 93 and is cooled to 55 ℃, 50 ℃ and 45 ℃ respectively, steam formed by heat dissipation of three saccharifying liquid flash evaporation heat-releasing tanks of the saccharifying liquid cooling system 9 enters three absorption cavities of a preheating absorption tower 22 of a primary preheating device 2 respectively for preheating starch mixture, and meanwhile, non-condensing gas discharged from pre-liquefying absorption towers 302 of three pre-liquefying devices of a liquefying system 3 also enters the preheating absorption tower 22 of the primary preheating device 2 for preheating the starch mixture.

The saccharified liquid with the temperature of 45 ℃ cooled by the saccharified liquid cooling system 9 enters a saccharified liquid temporary storage tank for temporary storage, and is finally conveyed to a heat exchanger 13 by a saccharified liquid low-temperature pump 12 for heat exchange and cooling, and then is sent to a fermentation tank for fermentation to produce alcohol.

When production is stopped, the starchy mixture in the equipment needs to be emptied, the preheating discharge valve 25 of the primary preheating device 2 and the pre-liquefaction discharge valve 305 of the pre-liquefaction device of the liquefaction preheating system 3 are opened, and under the action of the injection liquefaction pump 4, the starchy mixture in the preheating stirring tank 21 and the pre-liquefaction stirring tank 301 is emptied and conveyed to the liquefaction system 6 for liquefaction.

The utility model discloses a preheating in primary preheating device 2's the preheating absorption tower 22 collects ring 224 and preheats the plate of distributor 225 and mutually supports, realized the change of the many times of switching-over of material and entering the hot gas flow in preheating absorption tower 22 the multi-direction, the upflow of hot gas flow needs to pass the material stream many times, material stream and the contact many times of secondary steam air current, make between material stream and the hot gas flow heat exchange more abundant thoroughly, be favorable to the material stream to absorb temperature and moisture in the hot gas flow, the liquefaction of starchiness mixture with higher speed. Similarly, the cooperation of the pre-liquefaction collection ring 3024 and the pre-liquefaction distribution tray 3025 in the pre-liquefaction absorber 302 of the pre-liquefaction apparatus also provides multiple contact between the hot gas stream and the material stream, and the operation principle is the same as that of the pre-heating absorber 22.

Example two

As shown in fig. 4, the first embodiment is repeated with the following differences: liquefaction system 6 includes three liquefaction agitator tank 602, three liquefaction agitator tank 602 is series connection in proper order, including first liquefaction agitator tank, second liquefaction agitator tank and third liquefaction agitator tank, the discharge gate of the feed inlet intercommunication injection liquefier 5 of first liquefaction agitator tank, the discharge gate intercommunication second liquefaction agitator tank's of first liquefaction agitator tank feed inlet, the discharge gate intercommunication third liquefaction agitator tank's of second liquefaction agitator tank feed inlet, the discharge gate intercommunication liquefaction mash cooling system 7's of third liquefaction agitator tank feed inlet of first flash tank 71.

It should be noted that the above-mentioned embodiments are illustrative and not restrictive of the technical solutions of the present invention, and equivalents of those skilled in the art or other modifications made according to the prior art are intended to be included within the scope of the claims of the present invention as long as they do not exceed the spirit and scope of the technical solutions of the present invention.

Claims

1. An energy-saving jet liquefaction system for producing alcohol by using starchy raw materials is characterized in that: the device comprises a material 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 a tail gas condensation washing and discharging device (18), wherein the material mixing screw conveyor (1) uniformly mixes and stirs a starch raw material, a liquefying enzyme, a distilled residual mash filtrate (16) and wine gas cooling water (17) in a conveying process to form a mixture; the primary preheating device (2) preheats the mixture by using secondary steam emitted by cooling the saccharification liquid, and the mixture is preliminarily heated and liquefied; the liquefaction preheating system (3) preheats the mixture which is preliminarily heated and liquefied by using secondary steam evaporated from the liquefied mash, and the mixture is heated and liquefied step by step; the liquefaction system (6) heats the liquefied mixture by using raw steam, the temperature of the liquefied mixture is gradually raised, the mixed liquid is converted into liquefied mash, and the liquefied mash cooling system (7) cools the liquefied mash and flashes secondary steam out; a saccharification tank (8) saccharifies the cooled liquefied mash by using saccharifying enzyme; the saccharification liquid cooling system (9) is used for cooling saccharification liquid and evaporating secondary steam, the tail gas condensation washing and discharging device (18) is used for discharging the tail gas discharged by the primary preheating device after condensation cleaning, the discharge hole of the mixing screw conveyor (1) is communicated with the primary preheating device (2), the discharge hole of the primary preheating device (2) is communicated with the feed hole of the liquefaction preheating system (3), the discharge hole of the liquefaction preheating system (3) is connected with the feed hole of the injection liquefier (5) through the injection liquefaction pump (4), the air inlet of the injection liquefier (5) is communicated with a steam source, the discharge hole of the injection liquefier (5) is communicated with the feed hole of the liquefaction system (6), the discharge hole of the liquefaction system (6) is communicated with the feed hole of the liquefaction mash cooling system (7), the air outlet of the liquefaction mash cooling system (7) is connected with the liquefaction preheating system (3), the device is characterized in that a discharge port of the liquefied mash cooling system (7) is communicated with a feed port of a saccharification tank (8), a discharge port of the saccharification tank (8) is communicated with a feed port of a saccharification liquid cooling system (9) through a saccharification liquid high-temperature pump (11), a discharge port of the saccharification liquid cooling system (9) is communicated with a feed port of a saccharification liquid cache tank (10), a gas outlet of the saccharification liquid cooling system (9) is communicated with a gas inlet of a primary preheating device (2), a gas outlet of the primary preheating device (2) is communicated with a tail gas condensation washing and discharging device (18), and a discharge port of the saccharification liquid cache tank (10) is communicated with a heat exchanger (13) through a saccharification liquid low-temperature pump (12).

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

3. The energy-saving jet liquefaction system for producing alcohol from starchy raw materials according to claim 1, characterized in that: elementary preheating device (2) including preheating agitator tank (21), preheating absorption tower (22), preheating circulating pump (23), preheating circulating valve (24) and preheating bleeder valve (25), the feed inlet intercommunication of preheating agitator tank (21) mix the discharge gate of material screw conveyer (1), the circulation material mouth of preheating agitator tank (21) connects discharging pipe and row's material pipe, the discharging pipe feed inlet of preheating absorption tower (22) through preheating circulating pump (23), be provided with preheating circulating valve (24) on the discharging pipe, row's material pipe intercommunication spray liquefaction pump (4), be provided with on the discharging pipe and preheat bleeder valve (25), the discharge gate of preheating agitator tank (21) pass through pipe connection liquefaction preheating system (3), the air inlet intercommunication saccharification liquid cooling system (9) of preheating absorber tower (22) the gas outlet and the gas outlet of liquefaction preheating system (3), the gas outlet of the preheating absorption tower (22) is communicated with a tail gas condensation washing discharge device (18), the preheating absorption tower (22) is an integrated multi-stage absorption tower and comprises a plurality of mutually independent preheating absorption cavities, and each preheating absorption cavity is provided with a gas inlet.

4. The energy-saving jet liquefaction system for producing alcohol from starchy raw materials according to claim 1, characterized in that: liquefaction preheating system (3) include a plurality of liquefaction device in advance, a plurality of liquefaction device in advance series connection in proper order, the liquefaction device in advance including liquefaction agitator tank (301), liquefaction absorption tower (302) in advance, liquefaction circulating pump (303), liquefaction circulation valve (304) in advance and liquefaction discharge valve (305), the upper portion of liquefaction agitator tank (301) in advance set up feed inlet and discharge gate, the lower extreme of liquefaction agitator tank (301) in advance sets up the circulation material mouth, the circulation material mouth of liquefaction agitator tank (301) in advance connects circulation discharging pipe and row's material pipe, the circulation discharging pipe pass through the feed inlet of liquefaction circulation pump (303) intercommunication liquefaction absorption tower (302) in advance, the discharge pipe feed inlet of jet liquefaction pump (4) of intercommunication, the circulation discharging pipe on be provided with liquefaction circulation valve (304) in advance, the row's material pipe on be provided with liquefaction discharge valve (305) in advance, the gas inlet of the pre-liquefaction absorption tower (302) is communicated with the gas outlet of the liquefied mash cooling system (7), the pre-liquefaction absorption tower (302) is an integrated multi-stage absorption tower and comprises a plurality of pre-liquefaction absorption cavities which are mutually independent, a gas inlet is arranged on each pre-liquefaction absorption cavity, the feed inlet of a pre-liquefaction stirring tank (301) of a first pre-liquefaction device in the plurality of pre-liquefaction devices which are connected in series is communicated with the discharge outlet of a preheating stirring tank (21) of the primary preheating device (2), the discharge outlet of a pre-liquefaction stirring tank (301) of a previous pre-liquefaction device is communicated with the feed inlet of a pre-liquefaction stirring tank (301) of a next pre-liquefaction device, the gas outlet of the pre-liquefaction absorption tower (302) of the previous pre-liquefaction device is communicated with the gas inlet of the pre-liquefaction absorption tower (302) of the next pre-liquefaction device, and the discharge outlet of the pre-liquefaction stirring tank (301) of the last pre-liquefaction device is communicated with the, the air outlet of the pre-liquefaction absorption tower (302) of the last pre-liquefaction device is communicated with the air inlet of the preheating absorption tower (22) of the primary preheating device (2).

5. The energy-saving jet liquefaction system for producing alcohol from starchy raw materials according to claim 1, characterized in that: the liquefaction system (6) include a plurality of laminar flow liquefaction columns (601), a plurality of laminar flow liquefaction columns (601) are connected in series in proper order, the feed inlet of first laminar flow liquefaction column (601) communicates the discharge gate of injection liquefier (5), the discharge gate of preceding laminar flow liquefaction column (601) communicates the feed inlet of next laminar flow liquefaction column (601), the discharge gate of last laminar flow liquefaction column (601) communicates the feed inlet of liquefied mash cooling system (7).

6. The energy-saving jet liquefaction system for producing alcohol from starchy raw materials according to claim 1, characterized in that: the liquefaction system (6) include a plurality of liquefaction agitator tanks (602), a plurality of liquefaction agitator tanks (602) are series connection in proper order, the feed inlet of first liquefaction agitator tank (602) communicates the discharge gate of injection liquefier (5), the discharge gate of the preceding liquefaction agitator tank (602) communicates the feed inlet of the following liquefaction agitator tank (602), the discharge gate of the last liquefaction agitator tank (602) communicates the feed inlet of liquefied mash cooling system (7).

7. The energy-saving jet liquefaction system for producing alcohol from starchy raw materials according to claim 1, characterized in that: liquefied mash cooling system (7) include a plurality of flash tanks, a plurality of flash tanks are series connection in proper order, the discharge gate of first flash tank intercommunication liquefaction system (6), the discharge gate of preceding flash tank communicates the feed gate of later flash tank, the discharge gate of last flash tank communicates the feed gate of saccharification jar (8), adjacent n flash tanks are a set of in a plurality of series connection flash tanks, n equals the quantity of the absorption chamber of pre-liquefaction in pre-liquefaction absorption tower (302), every flash tank sets up a gas outlet, a plurality of n gas outlets of a set of flash tanks communicate a plurality of air inlets of pre-liquefaction absorption tower (302) of a pre-liquefaction device respectively.

8. The energy-saving jet liquefaction system for producing alcohol from starchy raw materials according to claim 1, characterized in that: the saccharification liquid cooling system (9) comprises a plurality of saccharification liquid flash evaporation heat release tanks, the saccharification liquid flash evaporation heat release tanks are connected in series, a feed inlet of a first saccharification liquid flash evaporation heat release tank is communicated with a discharge outlet of a saccharification liquid high-temperature pump (11), a discharge outlet of a previous saccharification liquid flash evaporation heat release tank is communicated with a feed inlet of a next saccharification liquid flash evaporation heat release tank, a discharge outlet of a last saccharification liquid flash evaporation heat release tank is communicated with a saccharification liquid cache tank (10), the number of the saccharification liquid flash evaporation heat release tanks is the same as that of absorption cavities of a preheating absorption tower (22) of a primary preheating device (2), and a gas outlet of one saccharification liquid flash evaporation heat release tank is communicated with a gas inlet of a preheating absorption cavity of the preheating absorption tower (22).