CN115304683A

CN115304683A - Wheat starch production system using posterior powder as raw material

Info

Publication number: CN115304683A
Application number: CN202210954726.3A
Authority: CN
Inventors: 冯纪网; 刘世源; 周斌; 常寨成; 胡明辉; 葛飞鹏; 韦璐; 李建华
Original assignee: Myande Group Co Ltd
Current assignee: Myande Group Co Ltd
Priority date: 2022-08-10
Filing date: 2022-08-10
Publication date: 2022-11-08
Anticipated expiration: 2042-08-10
Also published as: CN115304683B

Abstract

The invention discloses a wheat starch production system taking posterior wheat flour as a raw material, which comprises a storage flour mixing section, a horizontal screw separation section, an A starch refining dehydration section and an A starch crushing drying section, wherein a flour bin discharge port is connected with a high-position scraper blade through a low-position scraper blade and a lifter in sequence, each outlet of the high-position scraper blade is connected with an inlet of a flour mixing bin through a proportioning valve, a bin bottom discharger of each flour mixing bin is connected with an inlet of a flour mixing machine through a flour mixing bin discharge screw, a buffer bin is arranged at the bottom of the flour mixing machine, an outlet at the bottom of the mixing machine buffer bin is connected with an inlet of a mixture discharge screw, an outlet of the mixture discharge screw is connected with an inlet of a pneumatic conveying buffer bin, the bottom of the pneumatic conveying buffer bin is connected with a bypass inlet of a flour pneumatic conveying pipeline through a positive pressure air seal machine, a main inlet of the flour pneumatic conveying pipeline is connected with an air outlet of a Roots blower, and an outlet of the flour pneumatic conveying pipeline is connected with the flour mixing drying section. The system can prepare starch A and wheat gluten which are superior to the national standard, and realizes the recovery of all elements.

Description

Wheat starch production system using posterior powder as raw material

Technical Field

The invention relates to a wheat starch production system, in particular to a wheat starch production system taking posterior wheat flour as a raw material, and belongs to the technical field of wheat starch production.

Background

The wheat occupies an important position in the world grain crop yield, and the total grain yield in 2021/2022 year is 28 hundred million tons according to the statistical data of the grain crop organization in the United nations, wherein the predicted value of the total wheat yield is 7.767 hundred million tons, and the ratio is nearly 28 percent. However, wheat is only a few part of raw materials in starch production in the world, and the main reasons are high raw material cost, low yield in the production process and incapability of maximizing resource utilization, so that the production cost of enterprises is high and the profit is low.

The normal flour yield of wheat flour production in a flour mill can reach more than 78 percent, and the production flour is divided into three types: the powder comprises 30% of the powder for the front path, 35% of the powder for the middle path and 13% of the powder for the back path.

The posterior powder needs to be ground for a plurality of times compared with the anterior powder, the damaged starch is more, the quality is poor, and the price is relatively cheap compared with the anterior powder and the middle powder. The posterior flour also has the advantages that the protein content is high compared with the prior middle flour, the content of wet gluten in the posterior flour can reach more than 35%, the wet gluten content of the prior flour is about 30%, the difference between the wet gluten content and the wet gluten content is about 5%, the protein extraction rate of unit flour is higher, and the processing profit of a production factory can be improved to the maximum extent. Although the content of the protein in the next meal is high, the quality is relatively poor, the strength is weak, and the gluten index is low.

The process for processing wheat starch by using flour as a raw material generally comprises the working procedures of flour after-ripening, dough making, three-phase horizontal screw, starch refining, gluten separation and washing, dehydration, drying and the like.

The aging of flour is also called after-ripening and aging. The dough prepared from the flour which is just produced has high viscosity, lacks elasticity and toughness and has weak strength. After about 10 days of storage, the prepared dough is not sticky and strong in toughness. In order to improve the profit of enterprises, the posterior flour of a flour mill is adopted, the protein quality is poorer, the strength is weaker, and the flour is inelastic, so the flour needs to be stored for a certain period to improve the flour quality.

Mixing the after-cooked flour with water, kneading, and separating out starch A, starch B, gluten and pentosan by three-phase horizontal screw. And purifying, dehydrating and drying the starch A to obtain the product for taking out.

The starch B and the gluten are separated by separating and washing the gluten from the starch B, and the gluten after washing has high content of mucedin after dehydration and drying, and can be taken out as a food-grade protein product with high added value. The separated starch B gluten content is still high, and if direct drying is carried out subsequently, the energy consumption is high, and if the starch B gluten is difficult to filter and is not well utilized as a raw material for deep processing of sugar, the starch B gluten is usually used as a carbon source for fermentation production of alcohol in an alcohol plant.

Pentosan is a by-product of flour processing and contains about 7-8% solids. The main components are as follows: small granular starch (broken starch, more broken starch in the next powder, and great waste if directly discharged), soluble protein, water-soluble pentosan, water-soluble cellulose and the like. Because the impurities are more and pentosan is difficult to treat, the original wheat starch factory can directly discharge sewage, and because COD (chemical oxygen demand) is too high, the burden of the sewage treatment factory is heavy and resources are greatly wasted.

For the reasons, the wheat starch deep processing plant is matched with an alcohol plant for processing the pentosan solution. The starch of the pentosan is consumed by alcoholic fermentation, other components are discharged from DDGS and dried to be taken out as feed, and the value of each component of the pentosan phase is fully utilized.

However, the concentration of the pentosan solution is low, the viscosity of the pentosan is high, and a large amount of water is also brought in when the pentosan solution enters an alcohol fermentation system, so that the fermentation concentration is reduced, the viscosity is increased, and the fermentation effect is influenced. Therefore, the viscosity needs to be reduced by adding enzyme, and the required concentration is achieved after low-temperature evaporation in an alcohol fermentation plant, and the current process has the following problems:

1. the problem of unstable quality of flour raw materials often occurs in the production process. Different batches of flour quality difference is great, and gluten index, the landing number diverse in each storehouse, the gluten index is low, still leads to the garrulous face muscle more, can lead to the spiral shell that crouches to separate unclear, and the gluten yield is low, all causes very big influence to processes such as follow-up separation, dehydration, leads to whole production line can not the steady operation.

2. The viscosity of the wheat A starch is higher than that of the corn starch, so that the separation effect of the subsequent three-phase horizontal snail is poor, the oversize coarse powder is subjected to more return materials during screening, and the system burden is increased; starch B is encapsulated in the dough and is difficult to separate from the gluten by washing.

3. The product fineness can hardly meet the requirement by adopting the traditional air flow drying process. The tail gas is difficult to collect, if the tail gas is collected by a pulse dust collector, the investment cost is higher, a washing tower is adopted, a nozzle is easy to block, the cleaning tower has a sanitary dead angle, and the structure needs to be optimized.

4. The drying energy consumption of gluten is overlarge, the moisture content of gluten entering a drying system is 72 percent, the steam consumption of high-moisture-content drying is too large, and the energy consumption needs to be reduced. Secondly, the quality of the finished wheat gluten product has two key indexes of water absorption and moisture, the water absorption of the positive product needs to reach over 160 percent, and the moisture content is controlled to be 7-8 percent. The lower the moisture of the gluten dried final product is, the easier it is to achieve, but the lower the moisture of the product, the lower the profit of the final product is, and the water absorption rate cannot meet the required requirements. If the water content of the product is increased, the system is easy to block materials and does not meet the quality requirement, the problems are fully considered in the design, and the optimal production index is reached.

Secondly, the system is unstable in operation and is easy to generate bridging and blocking phenomena; and the gluten crushing has large power consumption, more equipment faults and insufficient product fineness. Secondly, the dust removal effect is not good, the cloth bag is easy to bond, the filtering effect is poor, and the wind resistance is large; the temperature of the discharged tail gas is high, and heat pollution is formed. More importantly, the system safety is poor, and the risk of dust explosion is high.

5. The pentosan concentration is 7-8%, and the fermentation concentration can be reduced when the pentosan enters a fermentation system, so that the fermentation efficiency is influenced; how to improve the concentration of pentosan is the processing difficulty of the current wheat starch factories; there are two methods for increasing the concentration: membrane filtration method dehydration or evaporation concentration method dehydration. The membrane filtration is not suitable for use because of the existence of pentosan, high viscosity and easy blockage of membrane pores. The evaporation concentration method is not suitable for high-temperature evaporation due to the existence of starch, and evaporation is required to be carried out at the starch gelatinization temperature of 60 ℃. However, multiple-effect evaporation is adopted, each effect needs a certain temperature difference to achieve the purpose of evaporation, so that one-effect temperature exceeds the starch gelatinization temperature and cannot be used, and if single-effect evaporation is adopted, the steam consumption is higher, the operation cost is high, and a proper concentration scheme is not available all the time.

6. Pentosan has high viscosity, affects the activity of strains in the fermentation process, and needs to be reduced as much as possible in both a membrane filtration concentration scheme and an evaporation scheme, if the evaporation concentration scheme is adopted, pentosan is easy to stick to a tube, so that the tube is easy to scale and the evaporation capacity is affected; if a membrane filtration scheme is used, it is easily clogged.

7. The pentosan contains soluble protein, foam is easily generated in the flash evaporation process, pentosan materials are easily entrained in secondary steam generated by flash evaporation, the phenomenon that materials are easily foamed and run out of a flash tank is generated, and the COD content in condensed water is high.

Disclosure of Invention

The invention aims to overcome the problems in the prior art, and provides a wheat starch production system using wheat middling as a raw material, which can prepare starch A and wheat gluten which are superior to national standards, realize the full-factor recovery of the wheat middling, have low energy consumption and improve the economic benefit of a factory.

In order to solve the technical problems, the wheat starch production system taking posterior flour as a raw material comprises a storage flour mixing working section, a horizontal screw separation working section, a starch refining dehydration working section A and a starch crushing drying working section A, wherein the storage flour mixing working section comprises a flour feeding pipe, an outlet of the flour feeding pipe is connected with an inlet of a double-way valve, two outlets of the double-way valve are respectively connected with inlets of flour bins, outlets of bin bottom dischargers of the two flour bins are respectively connected with inlets of flour bin discharge screws, outlets of the flour bin discharge screws are connected with inlets of a low-position scraper, outlets of the low-position scraper are connected with an inlet of a lower end of a lifter, an outlet of the upper end of the lifter is connected with an inlet of a high-position scraper, outlets of the high-position scraper are respectively connected with an inlet of a flour mixing bin through a mixing valve, outlets of the bin bottom of the flour mixing bin are respectively connected with an inlet of a spiral flour mixing machine, outlets of the flour mixing machine are connected with an outlet of the mixing machine, a buffer outlet of the mixing machine is connected with an outlet of the mixing machine, and an outlet of the mixing machine is connected with an inlet of a wind-feeding fan, and a wind-feeding pipeline of a wind-feeding air outlet of the mixing machine.

As an improvement of the invention, the dough kneading section comprises a dough kneading buffer bin and a dough kneading machine, the outlet of a flour air conveying pipeline is connected with the feeding hole of the dough kneading buffer bin, the outlet of a bin bottom discharger of the dough kneading buffer bin is connected with the inlet of a dough kneading discharge screw, the outlet of the dough kneading discharge screw is connected with the inlet of a permanent magnet drum, the outlet of the permanent magnet drum is connected with the feeding hole of the dough kneading machine, and the discharge hole of the dough kneading machine is connected with the inlet of a curing tank; a water pipe in the technical process is connected with a dough kneading regulating valve and a water inlet of the dough kneading machine through a dough kneading flow meter, and the opening degree of the dough kneading flow regulating valve is controlled by the rotating speed of the dough kneading discharge screw and a flow signal of the dough kneading flow meter; the dough kneading section is also provided with a first viscosity-reducing enzyme tank, an outlet of the first viscosity-reducing enzyme tank is connected with an inlet of a first metering pump, and an outlet pipeline of the first metering pump is connected with a feed inlet of the dough kneading machine through a first viscosity-reducing enzyme flowmeter; the flow of the metering pump I is controlled by the rotating speed of the dough kneading discharge screw and the flow monitored by the viscosity reducing enzyme flowmeter I.

As a further improvement of the invention, the bottom of the curing tank is provided with a screw pump of the curing tank, the outlet of the screw pump of the curing tank is connected with the inlet of the homogenizer, and the outlet of the homogenizer is connected with the separation section through a flour slurry pipe.

As a further improvement of the invention, the outlet of the surface slurry pipe is connected with the inlet of a three-phase horizontal screw centrifuge, the heavy phase outlet of the three-phase horizontal screw centrifuge is connected with the inlet of a coarse A starch milk buffer tank, the outlet of the coarse A starch milk buffer tank is connected with the inlet of a desanding cyclone through a coarse A starch milk delivery pump, the top flow outlet of the desanding cyclone is connected with the inlet of a fiber screen, the bottom flow of the desanding cyclone is connected with the inlet of a fine sand cyclone, and the top flow of the fine sand cyclone is connected with the inlet of the coarse A starch milk buffer tank; the fiber outlet of the fiber sieve is connected with the inlet of the pentosan buffer tank, and the A starch milk outlet of the fiber sieve is connected with the inlet of the fiber-removed A starch milk buffer tank.

As a further improvement of the invention, a light phase outlet of the three-phase horizontal screw centrifuge is connected with an inlet of the pentosan buffer tank, a middle phase outlet of the three-phase horizontal screw centrifuge is connected with an inlet of a post-curing tank, the bottom of the post-curing tank is connected with an inlet of a cured material shearing device through a screw pump of the post-curing tank, and an outlet of the cured material shearing device is connected with a gluten separation washing section.

As a further improvement of the invention, an outlet of the defibering A starch milk buffer tank is connected with an inlet of a two-phase horizontal screw centrifuge through a defibering buffer tank discharging pump, a heavy phase outlet of the two-phase horizontal screw centrifuge is connected with an inlet of a refined A starch milk buffer tank, an outlet of the refined A starch milk buffer tank is connected with an inlet of a high-level tank through a refined buffer tank output pump, an overflow port of the high-level tank is connected with a reflux port of the refined A starch milk buffer tank, a bottom outlet of the high-level tank is connected with an inlet of a scraper centrifuge, a liquid phase outlet of the scraper centrifuge is connected with an inlet of the horizontal screw clear liquid buffer tank, and a dry matter outlet of the scraper centrifuge is provided with a belt conveyor;

and the light phase outlet of the two-phase horizontal screw centrifuge is also connected with the inlet of the horizontal screw clear liquid buffer tank, the outlet of the horizontal screw clear liquid buffer tank is connected with the inlet of the clarifier through a centrifugal pump, the light phase outlet of the clarifier is connected with the inlet of the process water pipe, and the heavy phase outlet of the clarifier is connected with the inlet of the coarse A starch milk buffer tank.

As a further improvement of the invention, the outlet of the belt conveyor is butted with the inlet of the starch mixer, the outlet of the starch mixer is provided with a mixer discharging screw, the outlet chute of the mixer discharging screw is connected with the inlet of the lifting fan, the inlet of the lifting fan is also connected with the air outlet pipeline I of the air heater, the outlet of the lifting fan is connected with an airflow drying air pipe, the air outlet pipeline II of the air heater is connected with the lower part of the airflow drying air pipe, the upper outlet of the airflow drying air pipe is connected with the inlet of the cyclone separator, and the bottom outlet of the cyclone separator is connected with the inlet of the dry starch screw conveyor through an air seal-off device.

As a further improvement of the invention, an auxiliary outlet of the dry starch screw conveyor is connected with an inlet of the starch mixer through a dry starch return pipe, a main outlet of the dry starch screw conveyor is connected with an inlet of an iron removal winnowing machine, an outlet pipeline of the iron removal winnowing machine is connected with an inlet of a high-pressure fan, an outlet pipeline of the high-pressure fan is connected with an inlet of a starch dust remover, a bottom outlet of the starch dust remover is connected with inlets of the starch inspection sieves A through a rotary distributor, fine powder outlets of the starch inspection sieves A are respectively connected with a finished starch chute, coarse powder outlets of the starch inspection sieves A are respectively connected with an inlet of a coarse powder return screw, and an outlet of the coarse powder return screw is connected with an inlet of the dry starch return pipe.

As a further improvement of the invention, the top outlet of the cyclone separator is connected with the air inlet of the tail gas washing tower through an induced draft fan, the bottom water outlet of the tail gas washing tower is connected with the inlet of a washing circulating pump, the outlet of the washing circulating pump is connected with the upper water spraying pipe of the tail gas washing tower through a washing circulating pipe, and the middle part of the washing circulating pipe is also connected with the inlet of the pentosan buffer tank through a washing discharge valve.

As a further improvement of the invention, an expanding settling section is arranged along the airflow drying air pipe, and the top of the airflow drying air pipe is provided with an explosion door.

As a further improvement of the invention, the rotary distributor comprises a base, a distributor lower conical cylinder with a large upper part and a small lower part is fixed on the base, a distributor upper conical cylinder with a large upper part and a large lower part is fixed on the distributor lower conical cylinder, a plurality of starch discharge ports are uniformly arranged on the circumferential wall of the distributor lower conical cylinder, and starch discharge short sections are respectively connected below the starch discharge ports;

a starch inlet short pipe is arranged in the center of the top of the upper conical cylinder of the distributor, a rotatable vertical guide pipe is sleeved on the periphery of the starch inlet short pipe, the lower end of the vertical guide pipe is connected with an inclined guide pipe which is bent towards one side, and the lower port of the inclined guide pipe is butted with each starch discharge port;

be equipped with the pivot along the axis of conical cylinder under the distributor, the upper end of pivot through the revolving rack with oblique honeycomb duct is connected, the lower extreme of pivot is worn out and is linked to each other with the output of batching speed reducer from the diapire center of conical cylinder under the distributor, the input of batching speed reducer is by the motor drive of batching.

As a further improvement of the invention, a water accumulation conical disc is arranged at the lower part of the tower body of the tail gas washing tower, a washing air inlet is arranged above the water accumulation conical disc, a washing circulating water outlet which extends downwards to the outside of the tower body is arranged in the water accumulation conical disc, a water spraying pipe is arranged at the upper part of the tower body, the outer end of the water spraying pipe extends out of the tower body to form a washing circulating water inlet, the inner end of the water spraying pipe is downwards arranged along the axis of the tower body and is provided with a water spraying horn mouth, a first layer of sealing disc with a low center height and four sides is arranged below the water spraying horn mouth, a first layer of disc with a wide upper part and a narrow lower part is arranged below the first layer of sealing disc, the upper end of the disc is welded on the inner wall of the tower body, and the diameter of the lower port of the disc is smaller than the outer diameter of the sealing disc; the lower part of first layer dish is equipped with second layer sealing disc, and the below of second layer sealing disc is equipped with second layer dish, analogizes with this, and the bottom dish is located the top of washing air intake.

As a further improvement of the invention, a blast cap is arranged at the top of the tower body of the tail gas washing tower, the blast cap comprises a blast cap upper conical cylinder with a narrow upper part and a wide lower part, the lower end of the blast cap upper conical cylinder covers the upper port of the blast cap lower conical cylinder and exceeds the blast cap lower conical cylinder, the blast cap lower conical cylinder is of a structure with a wide upper part and a narrow lower part, the lower port of the blast cap lower conical cylinder is sleeved on the periphery of the blast cap short cylinder, and an annular rainwater discharge port is formed between the outer wall of the blast cap short cylinder and the inner wall of the lower port of the blast cap lower conical cylinder;

the inner chamber of hood is equipped with the cone center, the cone center includes main aspects welding as an organic whole just awl and back taper, the vertex of a cone of just awl and back taper all is located the tower axis, the last port of back taper is surpassed to the lower port of just awl, and just awl lower extreme diameter is greater than the diameter of annular rainwater drainage port place circumference.

As a further improvement of the invention, an outlet of the pentosan buffer tank is connected with an inlet of a pentosan feed pump, an outlet of the pentosan feed pump is connected with a cold side inlet of a plate preheater, a cold side outlet of the plate preheater is connected with a pentosan feed pipe, the pentosan feed pipe and a viscidity reducing enzyme adding pipe are respectively connected with an inlet of a static mixer, an outlet of the static mixer is connected with an inlet of an enzymolysis reaction tank, an inner cavity of the enzymolysis reaction tank is provided with a stirring device, and an outlet of the enzymolysis reaction tank is connected with an inlet of an evaporation feed tank;

the bottom outlet of the evaporation feed tank is connected with the inlet of an evaporation feed pump, the outlet of the evaporation feed pump is connected with the cold side inlet of the tubular preheater, the cold side outlet of the tubular preheater is connected with an evaporation feed pipe, the evaporation feed pipe and the bottom outlet of the falling-film evaporator are connected with the inlet of an evaporation circulating pump together, and the outlet of the evaporation circulating pump is connected with the top inlet of the falling-film evaporator through an evaporation circulating pipe;

the lower part of the falling-film evaporator is connected with a separator through a communicating pipe, a secondary steam outlet of the separator is connected with an inlet of a steam compressor, an outlet of the steam compressor is connected with a hot-side inlet of the falling-film evaporator, and a hot-side outlet of the falling-film evaporator is connected with a condensate water tank; the outlet at the bottom of the condensed water tank is connected with the inlet of a condensed water pump, the outlet of the condensed water pump is connected with the inlet at the hot side of the plate preheater, and the outlet at the hot side of the plate preheater is connected with an evaporated condensed water discharge pipe;

the device comprises an evaporation circulating pump, a pentosan discharge pipe, a concentration detector, a pentosan discharge adjusting valve and a three-way valve, wherein the outlet of the evaporation circulating pump is also connected with the pentosan discharge pipe, the concentration detector, the pentosan discharge adjusting valve and the three-way valve are installed on the pentosan discharge pipe, the opening degree of the pentosan discharge adjusting valve is controlled by the liquid level of the falling film evaporator, and a bypass outlet of the three-way valve is connected with a reflux port of the evaporation feeding tank through a pentosan reflux pipe.

As a further improvement of the invention, a pentosan feed flowmeter and a pentosan feed regulating valve are installed at the outlet of the pentosan feed pump, the outlet of the pentosan feed regulating valve is connected with the cold side inlet of the plate heat exchanger, and the opening degree of the pentosan feed regulating valve is controlled by a flow signal of the pentosan feed flowmeter;

the viscosity reducing enzyme adding pipe is connected with an outlet of the second metering pump, an inlet pipeline of the second metering pump is inserted into the bottom of the second viscosity reducing enzyme tank, a second viscosity reducing enzyme flow meter is installed on the viscosity reducing enzyme adding pipe, and the flow rate of the second metering pump is controlled by the flow rates monitored by the second pentosan feed flow meter and the second viscosity reducing enzyme flow meter;

as a further improvement of the invention, the secondary steam outlet of the condensed water tank is also connected with the inlet of the steam compressor; the non-condensable gas discharge port of the falling film evaporator is connected with the hot side inlet of the tube nest preheater, the hot side outlet of the tube nest preheater is connected with the hot side inlet of the condenser through a non-condensable gas conveying pipe, the hot side outlet of the condenser is connected with the vacuum pump, and the shell side water outlet of the condenser is connected with the inlet of the condensed water tank.

As a further improvement of the invention, a feed liquid level regulating valve is installed on the evaporation feed pipe, and the opening degree of the feed liquid level regulating valve is controlled by the liquid level of the evaporation feed tank;

the outlet of the condensed water pump is also connected with the outlet of the steam compressor through a condensed water regulating valve, and the opening degree of the condensed water regulating valve is controlled by the steam temperature at the outlet of the steam compressor.

And the hot side inlet of the falling-film evaporator is connected with a raw steam pipe through a steam regulating valve, and the opening degree of the steam regulating valve is controlled by the steam pressure of the hot side inlet of the falling-film evaporator.

As a further improvement of the invention, an outlet of the curing material conveying pipe is connected with an inlet of a first-stage gluten screen, a screen lower outlet of the first-stage gluten screen is connected with a B starch milk conveying pipe, a screen upper outlet of the first-stage gluten screen is connected with an inlet of a first-stage gluten buffer bin, an outlet of the first-stage gluten buffer bin is provided with a first-stage gluten screw pump, an outlet of the first-stage gluten screw pump is connected with an inlet of a first-stage static shearing device, an outlet of the first-stage static shearing device is connected with an inlet of a second-stage gluten screen, a screen lower outlet of the second-stage gluten screen is connected with an inlet of a second-stage slurry buffer bin, an outlet of the second-stage slurry buffer bin is provided with a second-stage slurry screw pump, and an outlet of the second-stage slurry screw pump is connected with the curing material conveying pipe through a second-stage slurry backflow pipe.

As a further improvement of the invention, an outlet on a sieve of the second-level gluten screen is connected with an inlet of a second-level gluten buffer bin, the second-level gluten buffer bin is provided with a second-level gluten screw pump, an outlet of the second-level gluten screw pump is connected with an inlet of a second-level static shearing device, an outlet of the second-level static shearing device is connected with an inlet of a third-level gluten screen, and an outlet under the sieve of the third-level gluten screen is connected with the inlet of the first-level gluten buffer bin through a third-level slurry return pipe; an outlet on the sieve of the third gluten screen is connected with an inlet of a third gluten buffer bin, and inlets of the second gluten buffer bin and the third gluten buffer bin are respectively connected with an outlet valve of the process water pipe; the bottom in tertiary gluten surge bin is equipped with tertiary gluten screw pump, and the export of tertiary gluten screw pump links to each other with the entry of tertiary static shears.

As a further improvement of the invention, the outlet of the three-stage static shearing device is connected with the inlet of the rotary screen, the outlet on the screen of the rotary screen is connected with the inlet of the gluten dehydrator, the dry matter outlet of the gluten dehydrator is connected with the inlet of the wringing machine, the filtrate outlets of the rotary screen, the gluten dehydrator and the wringing machine are respectively connected with a filtrate tank, the bottom of the filtrate tank is provided with a filtrate screw pump, and the outlet of the filtrate screw pump is connected with the inlet of the secondary gluten buffer bin through a gluten dehydration filtrate return pipe;

the outlet of the extruding dryer is connected with the inlet of the feeding buffer bin, the bottom of the feeding buffer bin is provided with a circulating screw pump, the outlet of the circulating screw pump is connected with a first circulating pipe and a second circulating pipe, the outlet of the first circulating pipe is connected with the inlet of the extruding dryer, the outlet of the second circulating pipe is connected with the inlet of the feeding buffer bin, the outlet pipeline of the circulating screw pump is further connected with the inlet of the feeding screw pump, and the outlet of the feeding screw pump is connected with a gluten crushing and drying system through a feeding pipe of a drying system.

As a further improvement of the invention, the outlet of a feeding pipe of the drying system is connected with a feeding port of the lifter, the outlet of the lifter is connected with a dry and wet wheat gluten inlet of the volute separator through a circulating pipeline, a hot air inlet of the volute separator is connected with an air outlet of the fin heat exchanger, a wet material outlet of the volute separator is connected with an air inlet of the lifter, and a dry wheat gluten outlet of the volute separator is connected with an air inlet of the double-bin dust remover;

the upper part of the double-bin dust remover is provided with a dust removal air outlet chamber, a dry powder dust removal chamber and a wet powder dust removal chamber are arranged below the dust removal air outlet chamber in parallel, the dry powder dust removal chamber is provided with a plurality of dust removal cloth bags, the wet powder dust removal chamber is of a cavity structure, and an air inlet of the double-bin dust remover is connected to the upper part of the wet powder dust removal chamber; a dry powder settling chamber is arranged below the dry powder dust removal chamber, and a dry powder discharging screw is arranged at the bottom of the dry powder settling chamber; a wet powder settling chamber is arranged below the wet powder dust removal chamber, and a wet powder discharging screw is arranged at the bottom of the wet powder settling chamber; the upper part of the dust-removing air outlet chamber is provided with an air outlet of a double-chamber dust remover which is communicated with the filtered space of the dust-removing cloth bag;

outlets of the dry powder discharging screw and the wet powder discharging screw are respectively connected with an inlet of the dry and wet powder returning screw, and an outlet of the dry and wet powder returning screw is connected with an air inlet of the lifter through a dry powder rotary valve;

the outlet of the dry powder discharging spiral and the outlet of the wet powder discharging spiral are respectively connected with the inlet of a vital gluten buffer bin, the outlet of the discharging spiral at the bottom of the vital gluten buffer bin is connected with the inlet of a pulverizer through an iron remover, the outlet of the pulverizer is connected with the inlet of a vital gluten dust remover, the outlet at the bottom of the vital gluten dust remover is connected with the inlet of a finished product inspection sieve, the outlet under the sieve of the finished product inspection sieve is connected with the inlet of a vital gluten finished product conveyor through an intermediate metering scale, the outlet of the vital gluten finished product conveyor is connected with the middle section of a vital gluten finished product pneumatic conveying pipe through a vital gluten air-shut discharging device, and the air outlet of a Roots blower II is connected with the air inlet of the vital gluten finished product pneumatic conveying pipe.

As a further improvement of the invention, the outlet on the screen of the finished product inspection screen is connected with the inlet of the vital gluten buffer bin through a vital gluten return screw;

the air outlet of the double-bin dust remover is connected with the inlet of an exhaust fan, the outlet of the exhaust fan is connected with the hot side of the gas-gas preheater through a hot tail gas pipe, and the air outlet of the gas-gas preheater is butted with the air inlet of the fin heat exchanger; the fin heat exchanger is sequentially provided with a condensate heat exchange section and a steam heat exchange section along the air flowing direction, a raw steam pipe is connected with a hot side inlet of the steam heat exchange section through a temperature control regulating valve, a hot side outlet of the steam heat exchange section is connected with a hot side inlet of the condensate heat exchange section through a steam trap and a condensate water return pipe, and a hot side outlet of the condensate heat exchange section is connected with a condensate water collecting pipe;

the opening degree of the temperature control regulating valve is controlled by the tail gas temperature of the double-bin dust remover, the steam generation pipe is connected with the air outlet of the finned heat exchanger through the humidity control regulating valve, and the opening degree of the humidity control regulating valve is controlled by the tail gas humidity of the double-bin dust remover.

As a further improvement of the invention, the outlet of the feeding pipe of the drying system is connected with the block-shaped gluten inlet of the fish mouth feeder, and the thin gluten outlet of the fish mouth feeder is connected with the feeding port of the lifter.

Compared with the prior art, the invention has the following beneficial effects: 1. a powder preparation section of storage: the lower the number of drops indicates that part of wheat is germinated and damaged, and the lower the number of drops indicates that the germinated wheat is more, the worse the quality is. When the falling number is less than 90S, the wheat can only be used as stored grain production feed and cannot be processed into flour.

The reduction of the falling number can lead to the reduction of gluten index, and the lower the gluten index is, shows that the gluten quality is worse, and the gluten is not tough and smooth, and the muscle is weak and inelastic. The horizontal spiral separation and vital gluten screening washing and the primary gluten dewatering section have great influence.

The gluten index is low, still leads to garrulous face muscle more, can lead to crouching the spiral shell to separate unclear, and the gluten yield is low. The broken gluten is more, the gluten flocculation is not good, the B starch milk and the gluten are not easy to separate when being screened, the B starch milk and the gluten are easy to paste and screen, the B starch gluten is more, and the gluten yield is low. Gluten that is not muscle say filters out from the screen mesh mouth of hydroextractor easily when the dehydration, leads to blockking up the filtrating pipeline, and production can not the steady operation.

Aiming at the reasons, in order to stably operate the flour kneading and separating system in the subsequent process, a flour mixing section is added after flour is subjected to post-curing, sampling detection is carried out on the flour subjected to post-curing in each bin, flour with unqualified quality and flour with qualified quality are mixed and proportioned, the flour kneading section can be carried out after the flour meets the requirement, the gluten index requirement after normal flour mixing reaches more than 50%, and the falling number is more than 500 s.

2. Dough kneading section: the quality of dough kneading directly influences the subsequent separation effect, and the concentration of dough kneading, the viscosity of dough paste and the effect of dough kneading directly influence the separation effect of the three-phase horizontal snail. The system is additionally provided with an automatic detection and adjustment function, can detect the concentration of flour slurry on line, realizes real-time control of flour discharge and water inflow, enables flour-water ratio to be mixed according to a set proportion, and achieves continuous and stable discharge concentration. Meanwhile, the viscosity of the flour paste is controlled by controlling the adding amount of the viscosity reducing enzyme through the frequency conversion of a metering pump. The viscosity of the metering pump and the discharge amount of flour realize automatic linkage and online control. The concentration and the viscosity of the flour slurry are strictly controlled on line, so that the optimal feeding parameters of the three-phase horizontal snail are achieved, and the separation effect of the three-phase horizontal snail is ensured.

The effect of dough kneading is another important sensory index, and the system achieves the optimal physical property index through once dough kneading, once after-ripening and once homogenization.

The dough kneading workshop section adopts the process water generated by the system, so that the consumption of fresh water can be saved, and the discharge of sewage can be reduced.

3. Horizontal spiral separation section: clear liquid generated by refining and dewatering is recycled and mixed with the surface slurry, so that the discharge of waste water is reduced, the consumption of fresh water is reduced, and substances in process water are recycled; the A starch milk, the B starch milk, gluten and pentosan in the flour slurry are separated by a three-phase horizontal decanter centrifuge, and a small amount of fiber and gluten carried in the A starch milk are further separated. The B starch milk and the gluten are subjected to post-curing and shearing to release the B starch wrapped in the dough, so that the subsequent washing is facilitated, the content of the gluten protein after washing is high, and the washed gluten protein is sold as a food-grade protein product with high added value. The B starch milk can be directly used as a carbon source of a brewery for brewing wine. The pentosan can also be used as a high-quality carbon source and nitrogen source raw material in the brewing fermentation process after being concentrated, so that the waste is changed into valuable, and the method has more objective economic benefits.

4. A, a starch refining dehydration section: starch milk is separated and refined through a two-phase horizontal screw separator, a ten-stage cyclone refining method is replaced, the calculation is carried out according to 40 cubic feed quantity, two 650-type horizontal screws are adopted according to the requirements of the horizontal screw method, the total power is 330KW, the total power of ten pumps refined through a traditional ten-stage cyclone is 630KW, and the power consumption of the horizontal screw method is basically half of that of the cyclone method. This system is through the dual technology of spiral shell that crouches + no filter screen hydroextractor, and through many times experimental verification adoption vertical no filter screen scraper centrifuge can effectively improve dehydration, and the wet starch moisture content after the dehydration can reach below 40%, and dehydration effect is obvious, and the amyloid content after the refining can be near below 0.35%.

5. A starch crushing and drying section: because the viscosity of the wheat A starch is higher than that of the corn starch, the product fineness can hardly meet the requirement by adopting the traditional air flow drying process, the oversize coarse powder is much returned during screening, and the system burden is increased. The tail gas is difficult to collect, if a pulse dust collector is adopted for collection, the investment cost is higher, a washing tower is adopted, a nozzle is easy to block, the cleaning tower has a sanitary dead angle, and the structure needs to be optimized.

The materials with low viscosity such as normal corn starch and the like enter air flow drying by giving an initial speed to the starch through a common lifter, but the rotating speed of the common lifter is low, so that the function of crushing the wheat starch cannot be achieved. After the wheat starch with high viscosity and the dry starch are mixed, the starch is seriously wrapped, the particle diameter is larger, and the fineness of the finished wheat starch product cannot meet the requirement. This system changes the riser into the lifting fan, and the high-speed rotation of fan wheel both can be smashed starch, can give starch again and get into the initial velocity that the air current is dry.

The viscosity of starch is high, and wet starch is easy to bridge; and a part of the dried starch returns to the starch mixer to be mixed with the wet starch, the viscosity of the starch A can be properly reduced after the moisture is reduced, and the starch has no bridging phenomenon in the process of conveying and mixing. The other part is discharged, the discharged starch passes through an iron removal air separator, and heavy metal and other impurities are precipitated at the bottom of the air separator and are periodically discharged.

In order to further reduce the fineness of the dry starch dried by the airflow, the system adopts a positive pressure conveying mode to convey and cool the dry starch. And (3) feeding the discharged dry starch into an inlet of a high-pressure fan, sucking the starch by the high-pressure fan under the action of negative pressure, crushing while conveying and cooling, and feeding the starch subjected to two-stage crushing into a starch A inspection sieve for sieving.

6. Because of the low separation efficiency of the airflow drying cyclone separator, the separation efficiency is normally about 99.5%, if the tail gas is not treated and 0.5% of starch is discharged out of the air, the environmental protection is affected, the starch yield is reduced, and the tail gas starch recovery and washing device is added in the system.

A traditional spray washing tower adopts a nozzle or spray holes for spraying, and the starch fineness is very thin and is normally more than 100 meshes, so that part of spray openings are easily blocked by starch, spray-formed fog drops cannot be uniformly scattered in the whole spray tower, and partial entrained starch tail gas is short-circuited to directly discharge air, and the adsorption effect is poor. The other structure adopts the pall ring structure, although the washing effect is better, sanitary dead angles exist in the tower body, bacteria are easy to breed after long-time use, and the quality of the recycled starch is poor, so that the method is not suitable for industrial production.

The tail gas washing tower of the system adopts a form that the central sealing disc and the annular disc are alternately superposed, and sprays water instead of spraying holes through splashing of a plurality of water curtains and water drops, so that the problem of blockage of a spraying opening is avoided, and no sanitary dead angle in the cavity can be ensured.

7. Pentosan enzymatic degradation and MVR evaporation section: the pentosan concentration is 7-8%, and the fermentation concentration can be reduced when the pentosan enters a fermentation system, so that the fermentation efficiency is influenced; how to increase the concentration of pentosan is the processing difficulty of the current wheat starch factories. The system adopts an evaporation concentration method to dehydrate, the viscosity of pentosan is high, the activity of strains is influenced in the fermentation process, before the system enters an evaporation system, the viscosity of pentosan is reduced through the viscosity-reducing enzyme and then the system enters an MVR evaporation system, the pentosan is prevented from being easily adhered to the tubes and scaling of the tubes, and the heat exchange efficiency of falling film evaporation is improved.

Because the starch exists, the high-temperature evaporation is not suitable, the viscosity reduction can not prevent C starch contained in pentosan from being gelatinized, the system adopts low-temperature evaporation, namely the evaporation temperature is not higher than the gelatinization temperature of the starch by 60 ℃, and MVR evaporation is adopted, so that the steam consumption can be reduced, and the system is superior to a multi-effect evaporation system, and ensures the low-temperature evaporation.

Pentosan which is preheated by non-condensable gas for the second time enters the falling film evaporator, secondary steam generated by evaporation is compressed, the pressure and the temperature are increased, the enthalpy is increased, and the secondary steam is returned to a heating chamber of the evaporator to be used as heating steam, so that the feed liquid is kept in a boiling state, and the heating steam is condensed into water. Compared with the multi-effect evaporation technology, the system compresses and recycles all secondary steam, and does not discharge energy to the outside, thereby greatly reducing energy consumption; and the consumption of the circulating cooling water can be greatly reduced compared with multiple effects. Pentosan evaporated by MVR can reach more than 30%, can be used as a carbon source for brewing wine, and improves the fermentation efficiency of a brewery.

8. Gluten separation washing section: separating the B starch milk from the gluten by the gluten phase and the B starch separated from the three-phase horizontal snail through a gluten sieve, wherein the separated B starch milk is difficult to be deeply processed into sugar due to the fine gluten contained and filtered, and is directly conveyed to wine brewing and fermentation as a carbon source.

And (4) washing and screening the separated gluten twice, further reducing the starch content in the gluten, and then sending the gluten to a drying section. When the gluten quality is low, the gluten is not well formed or can not be flocculated into large gluten, the protein content can normally reach more than 80%, but the gluten is easy to paste and sieve, and the dewatering effect is very poor. When the gluten quality is normal, the gluten index is high, and the gluten forms well, the muscle is said, can flocculate into bulk gluten, and the normal reduction of protein content leads to the finished product quality unqualified to below 80%.

The system accurately finds the reason and takes a targeted countermeasure, namely the gluten is wrapped by the B starch in the dough forming process, and the wrapped B starch is not easy to separate from the gluten after the gluten is formed into a large block. Therefore, the static shearing device is added in the gluten washing process, formed gluten is conveyed into the static shearing device through the screw pump, large gluten is cut into small blocks, B starch in the gluten after being cut into the small blocks is easier to separate, the starch content in the gluten can be reduced, the quality of finished products is improved, the gluten quality is gradually improved through three times of shearing and three times of screening subsequently, and the protein content can be more than or equal to 80%.

9. Gluten dehydration section: gluten drying energy consumption accounts for the proportion of whole factory operation energy consumption great, and in order to reduce the energy consumption that gluten was dried as far as possible, this system passes through tertiary dehydration to the gluten after the washing, and the one-level drum sieve passes through the screen cloth drainage, and the second grade gluten hydroextractor is dehydrated through the extruded mode of variable internal diameter, and the poor problem of gluten washing separation effect has been solved through the mode dehydration of variable pitch to tertiary gluten wringing machine. The three-stage combined action removes the free water in the gluten, reduces the free water in the gluten to the limit level less than or equal to 68 percent, and saves the consumption of gluten drying steam.

There are two drawbacks to normal screw pump direct delivery into the dryer: (1) when the gluten quality is poor, the screen mesh of the dehydrator and the wringing machine is easily screened by gluten paste, the moisture of the gluten after three times of dehydration is still large, the steam consumption is too high when the gluten directly enters the dryer, and waste is caused; (2) the pressure of the inlet of the feeding screw pump is unstable, the screw pump feeding influences the pressure of the feeding hole of the screw pump due to the material level of the gluten buffer bin, so that the whole drying system is unstable due to the difference of conveying capacity under the condition of the same feeding frequency, and the discharged water has deviation.

Based on above drawback, this system has increased circulation feed pump, and the gluten that gets into the surge bin through the cubic dehydration passes through circulation screw pump circular transportation, and partly gluten advances the wringing machine import, and partly advances the import of circulation screw pump, so both can further dewater, can guarantee the inlet pressure of feed screw pump again, maintain drying system's steady operation.

10. Gluten crushing and drying section: the fish mouth feeder presses gluten into flat slices to be fed into the lifter, so that the specific surface area is large and the drying efficiency is high; reducing the operating load of the lifter; the more important reason is safety, because of the gluten is more glutinous, welding slag that probably exists in the wet process workshop pipeline is easily taken into drying system by the gluten, and welding slag gets into in the drying-machine and through the striking with stoving pipeline and riser very easily produce the spark and lead to the system explosion. The system can intercept most of large-particle welding slag through narrow-slit feeding of the fish mouth feeder, and reduces the risk of explosion of the drying system.

Because the viscosity of gluten is very big, the drying is difficult, and this system adopts circulation drier drying, and drying temperature is low, and material thermal denaturation is little, is applicable to the drying of high viscosity and heat-sensitive material. The dry powder backflow technology is adopted, the viscosity of incoming materials is reduced by a method of mixing wet materials and dry materials, and the risk of bridging and material blocking of wet powder in equipment is reduced.

The gluten is in the in-process that rises with hot-blast heat exchange flash distillation, and hot-blast moisture in with the gluten is taken away and is dried into the wheat gluten, and partial wheat gluten that does not reach the moisture requirement separates with dry material under the effect in the spiral case separator. The requirements of the final product moisture and the product quality, namely the water absorption rate, are met by adjusting the proportion of the discharging and the returning of the dry and wet materials, and the production stability and the profit margin of the product are ensured.

The structure of the pulse dust collector is updated, the dry and wet materials are automatically separated and respectively collected, and the moisture content of discharged materials can be adjusted by adjusting the discharging proportion of the dry and wet materials.

The air temperature from the tail gas outlet of the gluten dryer is about 60 ℃, the system utilizes the waste heat of the part of tail gas, particularly in winter, the heat energy recovery effect is better when the outdoor temperature is lower, the initial temperature of inlet air is improved, the preheating is fully utilized, and the steam consumption is reduced.

Can the exhaust temperature of accurate control double-storehouse dust remover through the control by temperature change governing valve, can the exhaust humidity of accurate control double-storehouse dust remover through wet control governing valve, prevent that humidity from crossing the system and easily producing static excessively, lead to the system explosion.

11. The system not only adopts the wheat flour to produce the starch, but also realizes the production of the wheat starch by using the later flour in the wheat flour. Aiming at the characteristics of more damaged starch and low gluten index of the next meal, the system comprehensively considers and optimally designs each production section, solves various possible obstacles of the whole production line, ensures that the quality of the prepared A starch or wheat gluten reaches or is superior to the national standard level, improves the factory profit and the product added value, and realizes energy conservation and consumption reduction. More importantly, the system overcomes the defects of low gluten index and unsmooth gluten of the back flour, easy material blockage, screen pasting, easy foaming and pasting due to evaporation, poor dehydration effect, difficult tail gas washing and the like in the production process, and can safely and stably run.

Various emissions in the production process are recycled, and zero emission is realized except for tail gas. For example, the wastewater generated in the wheat starch processing process is recycled in the system, and the active ingredient pentosan in the wastewater is reasonably utilized, so that waste is changed into valuable, the product addition can be improved, the enterprise profit can be increased, and the load of a sewage treatment plant can be reduced.

Drawings

The invention will be described in further detail with reference to the following drawings and detailed description, which are provided for reference and illustration purposes only and are not intended to limit the invention.

FIG. 1 is a flow chart of a bin storing powder preparing section in the invention;

FIG. 2 is a flow chart of the dough kneading section of the present invention;

FIG. 3 is a flow diagram of the horizontal decanter separation section of the present invention;

FIG. 4 is a flow chart of the A starch refining and dewatering section in the present invention;

FIG. 5 is a flow chart of the starch pulverizing and drying section A according to the present invention;

FIG. 6 is a front view of the rotary distributor of the present invention;

FIG. 7 is a left side view of FIG. 6;

FIG. 8 is a perspective view of FIG. 6;

FIG. 9 is a front view of an off-gas wash column of the present invention;

FIG. 10 is an enlarged view of the tail gas wash tower hood;

FIG. 11 is a flow chart of the pentosan enzymatic degradation and MVR evaporation section of the present invention;

FIG. 12 is a flow chart of a gluten separation washing section in the present invention;

FIG. 13 is a flow chart of a gluten dewatering section in the present invention;

FIG. 14 is a flow diagram of the gluten crushing and drying section of the present invention;

FIG. 15 is a front view of a fish mouth feeder of the present invention;

FIG. 16 is a perspective view of a fish mouth feeder of the present invention;

fig. 17 is an enlarged view of the outlet of the flake gluten of fig. 15;

FIG. 18 is a front view of the double bin precipitator of the present invention.

In the figure: a powder preparation section of storage: 101. bulk loading of flour; 102. a two-way valve; 103. a flour bin; 104. a flour bin discharging screw; 105. a low-position scraper plate; 106. a hoist; 107. a high-position scraper; 108. a dosing valve; 109. a powder preparing bin; 110. a powder preparing bin discharging screw; 111. mixing powder in a mixer; 112. a mixer surge bin; 113. discharging the mixture spirally; 114. a positive pressure air seal machinery; 115. a Roots blower I; 116. a flour air conveying pipeline;

dough kneading section: 201. a dough kneading buffer bin; 201a, a dough mixer; 201b, a draught fan; 202. dough kneading and discharging spiral; 203. a permanent magnet drum; 204. a dough mixer; 205. a first viscoase reduction tank; 206. a first metering pump; 207. a curing tank; 208. a screw pump of the curing tank; 209. a homogenizer; 210. a dough pipe; G1. a process water pipe; FT1. A surface water flowmeter; fc1. Dough water regulating valve; FM1. A first visbreaking enzyme flow meter;

horizontal separation: 301. a three-phase horizontal decanter centrifuge; 302. a post-curing tank; 303. a post-curing tank screw pump; 304. a cured material cutter; 305. a cured material conveying pipe; 306. a coarse A starch milk buffer tank; 307. a coarse A starch milk delivery pump; 308. a sand removal swirler; 309. a fine sand cyclone; 310. screening the fiber; 311. a fiber delivery tube; 312. a defibering A starch milk buffer tank; 313. a pentosan conveying pipe; 314. a pentosan buffer tank; FT2, a horizontal screw water inlet flowmeter; FC2, horizontal screw water inlet regulating valve; FT3, screening the flowmeter; FC3, screening and regulating valve;

a, refining and dehydrating starch: 401. a discharging pump of the defibering buffer tank; 402. removing the fiber A starch milk conveying pipe; 403. a two-phase horizontal decanter centrifuge; 404. a refined A starch milk buffer tank; 405. a refining buffer tank output pump; 406. a high-level tank; 407. a scraper centrifuge; 408. a buffer tank for clear liquid of the decanter; 409. a centrifugal pump; 410. a clarifying machine; 411. a clarifier return pipe; 412. a belt conveyor; FT4, a dehydration feed flow meter; fc4. Dewatering feed regulating valve;

drying starch: 501. a starch mixer; 502. the discharging screw of the mixer is adopted; 503. a lifting fan; 504. an air filter; 505. an air heater; 506. air flow drying air pipe; 507. expanding a settling section; 508. an explosion vent; 509. a cyclone separator; 510. a dry starch screw conveyor; 511. a deironing winnower; 512. a muffler; 513. a high pressure fan; 514. a starch dust collector; 515. a rotating distributor; 515a, starch inlet stub; 515b, a distributor upper cone; 515c, a vertical guide pipe; 515d, an inclined guide pipe; 515e, distributor lower cone; 515f, starch discharge port; 515g, starch discharging short section; 515h, a batching motor; 515j, burdening speed reducer; 515k, a rotating shaft; 515m, rotating frame; 516.A starch inspection sieve; 517. a finished product of a starch chute; 518. returning the coarse powder to a screw; 519. a dry starch return conduit; 520. a tail gas wash tower; 520a, an upper cone of the blast cap; 520b, a lower cone of the blast cap; 520c, a positive cone; 520d, back taper; 520e. a cone center support; 520f, an annular rainwater discharge port; 520g of a water spraying pipe; 520h, sealing the disc; 520j, a disk; 520k, washing the air inlet; 520m. water accumulation conical disc; 520n, a washing circulating water outlet; 520p, washing water replenishing port; 520q, a washing sewage draining outlet; 520r, water seal overflow pipe; 521. a washing circulating pump; 522. a washing discharge valve; G2. a raw steam pipe; G3. a condensed water collecting pipe;

pentosan enzymatic degradation and MVR evaporation: 601. a pentosan feed pump; 602. a plate preheater; 603. a pentosan feed tube; 604. a viscosity reducing enzyme tank II; 605. a second metering pump; 606. a viscoenzyme reducing addition tube; 607. a static mixer; 608. an enzymolysis reaction tank; 609. evaporating the feed tank; 610. an evaporative feed pump; 611. a tubular preheater; 612. an evaporation feed pipe; 613. a falling film evaporator; 614. an evaporation circulating pump; 615. an evaporation circulation pipe; 616. a separator; 617. a vapor compressor; 618. a condensate tank; 619. a condensate pump; 620. an evaporation condensate discharge pipe; 621. a noncondensable gas delivery pipe; 622. a condenser; 623. a vacuum pump; 624. a pentosan reflux pipe; 625. a pentosan discharge pipe; FT5. A pentosan feed flowmeter; fc5 pentosan feed regulating valve; FC6. Condensate regulating valve; FM2. A second visbreaking enzyme flowmeter; LC1. Feed level regulating valve; LC2, pentosan discharge adjusting valve; dt, concentration detector; KV. Three-way valve; pa, pressure sensor; pc, steam regulating valve; G4. circulating a water inlet pipe; G5. circulating a water outlet pipe;

gluten separation and washing: 701. a first-level gluten screen; 702.B starch milk delivery pipe; 703. a first-level gluten buffer bin; 704. a first-stage gluten screw pump; 705. a first stage static shears; 706. a second gluten screen; 707. a secondary slurry buffer bin; 708. a two-stage slurry screw pump; 709. a secondary slurry return pipe; 710. a secondary gluten buffer bin; 711. a two-stage gluten screw pump; 712. a secondary static shears; 713. a third-level gluten screen; 714. a third stage slurry return pipe; 715. a third gluten buffer bin; 716. a three-level gluten screw pump; 717. a three-stage static shears; 718. gluten washing discharge pipe; 719. a brewery;

gluten dehydration: 801. a drum screen; 802. gluten dewaterer; 803. a squeezing machine; 804. a filtrate tank; 805. a filtrate screw pump; 806. gluten dehydration filtrate return pipe; 807. a feeding buffer bin; 808. circulating the screw pump; 809. a first circulation pipe; 810. a second circulation pipe; 811. a feed screw pump; 812. a drying system feed conduit; g6 compressed air pipe;

and (3) crushing and drying gluten: 901. an air cleaner; 902. a gas preheater; 903. a finned heat exchanger; 904. a condensed water return pipe; 905. a lifter; 905a fish mouth feeder; 905a1, a block-shaped gluten inlet; 905a2, a thin gluten outlet; 906. a volute separator; 907. a double-bin dust remover; 907a, dedusting and air outlet chamber; 907b, a dry powder dust removal chamber; 907c, wet powder dust removal chamber; 907d dry powder settling chamber; 907e wet powder settling chamber; 907f, air inlet of double-bin dust remover; 907g, air outlet of double-bin dust remover; 908a, dry powder discharge spiral; 908b, discharging the wet powder spirally; 909. feeding back the dry and wet powder spirally; 910. rotating the dry powder valve; 911. an exhaust fan; 912. a hot tail gas pipe; 913. a vital gluten buffer bin; 914. a de-ironing separator; 915. a pulverizer; 916. a gluten dust remover; 917. a finished product inspection sieve; 918. returning the gluten flour to a spiral; 919. a middle metering scale; 920. a vital gluten finished product conveyor; 921. wheat gluten air-turning off discharging device; 922. a Roots blower II; 923. conveying a finished wheat gluten product into a pipe by air; TC, temperature control regulating valve; hc, humidity control regulating valve.

Detailed Description

In the following description of the present invention, the terms "upper", "lower", "front", "rear", "left", "right", "inner", "outer", etc., indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience in describing the present invention and simplifying the description, but do not mean that the apparatus must have a specific orientation.

In order to make the technical means, the creation characteristics, the achievement purposes and the effects of the invention easy to understand, the invention is further explained by combining the specific drawings.

Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terminology used herein in the description of the invention is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention.

The wheat starch production system using the wheat flour as the raw material comprises a storage flour mixing section, a horizontal spiral separation section, a starch refining and dehydration section A, a starch crushing and drying section A, a pentosan enzymatic degradation and MVR evaporation section, a gluten separation and washing section, a gluten dehydration section and a gluten crushing and drying section.

As shown in figure 1, the powder proportioning bin comprises a flour feeding pipe, a flour bin 103, a powder proportioning bin 109 and a powder proportioning mixer 111, wherein an outlet of the flour feeding pipe is connected with an inlet of a two-way valve 102, two outlets of the two-way valve 102 are respectively connected with an inlet of the flour bin 103, and outlets of bin bottom dischargers of the two-way flour bin 103 are respectively connected with an inlet of a flour bin discharging screw 104.

After wheat in a flour mill is milled into powder, the flour yield of the next flour is about 13%, the next flour is transported to a factory area through a flour bulk truck 101, the next flour is pressure-fed into a flour bin 103 through a roots blower of the flour bulk truck 101, the two flour bins 103 are switched through a two-way valve 102, and when the high material level of one flour bin alarms, the bin is full. The feeding of the next flour bin is automatically switched by the two-way valve 102.

The outlet of the flour bin discharging screw 104 is connected with the inlet of the low-position scraper 105, the outlet of the low-position scraper 105 is connected with the lower end inlet of the lifting machine 106, the upper end outlet of the lifting machine 106 is connected with the inlet of the high-position scraper 107, and the outlets of the high-position scraper 107 are respectively connected with the inlet of the flour blending bin 109 through the blending valve 108. The flour bin 103 is vibrated and unloaded through a bin bottom discharger and respectively enters the flour bin discharging screws 104, and the discharging amount is controlled by controlling the motor frequency of the flour bin discharging screws 104; the flour is discharged and then sent to a lifter 106 through a low scraper 105, the lifter 106 lifts the flour to a high position and sends the flour to a high scraper 107, and the flour is conveyed into each powder blending bin 109 through a blending valve 108.

In the actual production process, the raw material quality of each batch of incoming materials can not be completely consistent, so that the gluten index and the falling number of each batch have certain difference, for the stable operation of the flour and flour separation system in the subsequent process, each batch of flour enters different flour mixing bins 109, the gluten index and the falling number are detected by a detection laboratory, and the flour with the same quality enters the same flour mixing bin 109.

Cysteine and cystine in newly produced flour contain unoxidized sulfhydryl-SH, and the sulfhydryl is an activator of protease, and when being stirred, the activated protease strongly decomposes protein in the flour, thereby causing the phenomenon of poor dough processing performance. After the flour is stored for a period of time, the thiamine group is oxidized and loses activity, gluten protein in the flour is not decomposed, the technological performance of the flour is improved, the strength is enhanced, and the protein quality is improved.

However, even if the gluten strength of partial batches of flour can not meet the requirement, the flour quality is poor, so that the separation and dehydration effects of the subsequent working sections are poor, the flour mixing working section is added in the system, and the gluten index is ensured to reach over 50 percent.

The storage time of the flour bin 103 is normally more than ten days, so that the flour has a later ripening period, the gluten index and the falling value of the flour are required to be tested after being stored for ten days, and the flour blending treatment is carried out after the value of each flour blending bin is determined to reach the required index.

The bottom of each powder preparing bin 109 is also provided with a bin bottom discharger for vibratory discharging, the outlet of the bin bottom discharger of each powder preparing bin 109 is respectively connected with the inlet of a powder preparing bin discharging screw 110, and the outlet of each powder preparing bin discharging screw 110 is respectively connected with the inlet of a powder preparing mixer 111. The flour is automatically prepared according to the quality difference of each flour preparation bin, the discharging speed of each flour preparation bin 109 is controlled by controlling the motor frequency of the discharging screw 110 of the flour preparation bin, and the quality of the discharged flour is ensured to meet the process control requirement, namely the gluten index reaches over 50 percent and the falling number reaches over 500 s. Therefore, the difference of the quality of the supplied materials is compensated, the relative stability of the quality of the raw materials is ensured, and the discharged flour enters the flour mixing machine 111. The powder mixing machine 111 is provided with a weighing device, and the discharge amount of each powder mixing bin 109 is controlled by a weighing sensor.

The bottom of the flour mixing machine 111 is provided with a mixing machine buffer bin 112, and the mixed flour enters the mixing machine buffer bin 112. Mix the bottom export of machine surge bin 112 and the entry of mixture ejection of compact spiral 113 and link to each other, the export of mixture ejection of compact spiral 113 links to each other with the entry that the surge bin was sent to the wind, mixes machine surge bin 112 and passes through the ejection of compact spiral 113 frequency conversion of mixture ejection of compact and ejection of compact, gets into the wind and send the surge bin.

The bottom of the pneumatic conveying buffer bin is connected with a bypass inlet of a flour pneumatic conveying pipeline 116 through a positive pressure air seal machine 114, a main inlet of the flour pneumatic conveying pipeline 116 is connected with an air outlet of a Roots blower I115, and an outlet of the flour pneumatic conveying pipeline 116 is connected with a dough kneading section. The flour is sent into a flour air supply pipeline 116 through a positive pressure air seal machine 114 and is sent out under the action of the wind power of a Roots blower I115 and enters a buffer bin of a dough kneading section.

As shown in FIG. 2, the dough kneading section comprises a dough kneading surge bin 201 and a dough kneading machine 204, the outlet of the flour air conveying pipeline 116 is connected with the feed inlet of the dough kneading surge bin 201, a dough kneading dust remover 201a is arranged at the top of the dough kneading surge bin 201, and the air outlet of the dough kneading dust remover 201a is communicated with the atmosphere through an induced draft fan 201b. The mixed flour sent out by the flour air conveying pipeline 116 enters the dough kneading buffer bin 201 for sedimentation, and the tail gas is discharged outdoors through the dough kneading dust remover 201a and the induced draft fan 201b.

The bottom of the dough kneading buffering bin 201 is provided with a bin bottom discharger for vibration discharging, the bin bottom discharger outlet of the dough kneading buffering bin 201 is connected with the inlet of the dough kneading discharging screw 202, and the frequency-variable discharging of the dough kneading discharging screw 202 changes the rotating speed of the dough kneading discharging screw 202 through controlling the motor frequency of the dough kneading discharging screw 202, so that the discharging amount of the dough kneading buffering bin is adjusted.

The outlet of the dough kneading and discharging screw 202 is connected with the inlet of the permanent magnet cylinder 203, the outlet of the permanent magnet cylinder 203 is connected with the inlet of the dough kneading machine 204, and the outlet of the dough kneading machine 204 is connected with the inlet of the curing tank 207. The process water pipe G1 is connected with the water inlet of the dough kneading machine 204 through a dough kneading flow meter FT1 and a dough kneading water regulating valve FC1.

The discharged flour is deironized by the permanent magnet cylinder 203 and then enters the flour-mixing machine 204 together with the process water for flour-mixing. The opening degree of the dough kneading water adjusting valve FC1 is controlled by the rotating speed of the dough kneading discharging screw 202 and a flow signal of the dough kneading water flow meter FT1, namely, the flow of the water in the dough kneading process and the motor frequency of the dough kneading discharging screw 202 realize automatic linkage, the proportion of flour and water is accurately controlled, flour and water which are well mixed are kneaded according to the proportion of 10.

In actual production, the problems that the separation effect of three-phase horizontal snails in a subsequent working section is poor due to high viscosity after dough kneading, and the content of dry matters in gluten or pentosan phase in the A starch phase is high frequently occur.

The dough kneading section is provided with a first viscosity-reducing enzyme tank 205, an outlet of the first viscosity-reducing enzyme tank 205 is connected with an inlet of a first metering pump 206, and an outlet pipeline of the first metering pump 206 is connected with a feed inlet of the dough kneading machine 204 through a first viscosity-reducing enzyme flowmeter FM 1; and (3) adding a viscosity reducing enzyme into the flour-mixing machine, wherein the addition amount of the viscosity reducing enzyme is 0.05kg/T of oven-dried flour, extracting the flour from a first viscosity reducing enzyme tank 205 by a first metering pump 206, and injecting the flour into the flour-mixing machine 204.

The flow rate of the metering pump one 206 is controlled by the rotational speed of the dough kneading discharge screw 202 and the flow rate monitored by the viscosity reducing enzyme flow meter one FM1. The feeding amount of the viscosity-reducing enzyme is controlled through the variable frequency regulation of the first metering pump 206, and the accurate proportion of the viscosity-reducing enzyme to the flour is kept. Due to the fact that the viscosity of the flour paste is reduced by the properly added visbreaking enzyme when flour is kneaded, the follow-up three-phase horizontal snail can be better separated.

The mixed flour paste stays in the flour-mixing machine 204 for about 10 minutes, so that the flour and the water are fully mixed, and the phenomenon of flour agglomeration is reduced. Then the gluten is gelatinized in a curing tank 207, the after-curing time of normal gluten is about 20 minutes, after curing, the gluten is flocculated to form a network structure, the molecular weight of the gluten is increased, and the gluten is favorable for the subsequent working section to separate through a three-phase horizontal screw.

The bottom of the curing tank 207 is provided with a curing tank screw pump 208, the outlet of the curing tank screw pump 208 is connected with the inlet of a homogenizer 209, and the outlet of the homogenizer 209 is sent to the horizontal screw separation section through a flour slurry pipe 210. The residence time in the curing tank 207 can be reduced to 10-15 minutes, then the mixture is sent to a homogenizer 209 by a screw pump 208 of the curing tank for high-speed mixing and homogenizing, the homogenizer 209 runs at the rotating speed of 960rpm, the flour and the water are fully mixed again, the dough possibly generated during dough kneading is broken up and sent to a horizontal screw for separation through a dough pipe 210.

As shown in FIG. 3, the horizontal screw separation section comprises a three-phase horizontal screw centrifuge 301, a fiber screen 310, an after-ripening tank 302 and buffer tanks, wherein the outlet of the flour slurry pipe 210 is connected with the inlet of the three-phase horizontal screw centrifuge 301. The homogenized flour paste flows out from the flour paste pipe 210, the process water is injected into the flour paste pipe 210 after passing through the horizontal screw water inlet flow meter FT2 and the horizontal screw water inlet adjusting valve FC2, the process water is injected in proportion according to the flow of the flour paste, and the horizontal screw water inlet adjusting valve FC2 adjusts the opening according to the flow of the horizontal screw water inlet flow meter FT2.

The process water and the flour slurry are mixed and then enter a three-phase horizontal decanter centrifuge 301 together for separation, the feed concentration of the three-phase horizontal decanter centrifuge 301 is 35-40%, the rotating speed is 3000rpm, the heavy phase is A starch milk, the middle phase is B starch milk plus gluten, and the light phase is pentosan after the separation of the three-phase horizontal decanter centrifuge.

The heavy phase outlet of the three-phase horizontal decanter centrifuge 301 is connected with the inlet of the coarse A starch milk buffer tank 306, the A starch milk flows out from the heavy phase outlet of the three-phase horizontal decanter centrifuge 301, the content of A coherent substances is 50-55%, and a small amount of fiber and gluten enter the coarse A starch milk buffer tank 306 for temporary storage.

The outlet of the coarse A starch milk buffer tank 306 is connected with the inlet of a desanding cyclone 308 through a coarse A starch milk delivery pump 307, and the A starch milk is pumped out by the coarse A starch milk delivery pump 307 and is sent into the desanding cyclone 308 for centrifugal separation to remove fine sand in the A starch milk.

The underflow of the desanding cyclone 308 is connected to the inlet of the fine sand cyclone 309, and the overflow of the fine sand cyclone 309 is connected to the inlet of the coarse a starch milk surge tank 306. The underflow of the desanding cyclone 308 enters a fine sand cyclone 309 for re-separation, and the clear liquid returns to the crude A starch milk buffer tank 306 for circulation.

The top flow outlet of the sand removal cyclone 308 is connected with the inlet of a fiber screen 310, the fiber outlet of the fiber screen 310 is connected with the inlet of a pentosan buffer tank 314, and the A starch milk outlet of the fiber screen 310 is connected with the inlet of a fiber-removed A starch milk buffer tank 312. The A starch milk after fine sand removal flows out of the top of the sand removal cyclone 308 and enters a fiber screen 310 to remove fibers. The inlet pipeline of the fiber sieve 310 is sequentially provided with a sieving flowmeter FT3 and a sieving regulating valve FC3, and the opening degree of the sieving regulating valve FC3 is adjusted according to the flow of the sieving flowmeter FT3.

The starch A from which the fibers and most of gluten, namely the flocculated large-grain gluten, are removed enters a fiber A-removed starch milk buffer tank 312 for temporary storage, and then a starch A-removed refining and dehydrating section is performed.

The fiber and large-granule gluten discharged from the oversize outlet of the fiber screen 310 enter the pentosan buffer tank 314 for temporary storage through the fiber conveying pipe 311.

The light phase outlet of the three-phase horizontal screw centrifuge 301 is connected with the inlet of a pentosan buffer tank 314 through a pentosan conveying pipe 313, and the dry matter content of the pentosan discharged from the light phase outlet of the three-phase horizontal screw centrifuge is 7-8 percent, and the dry matter content enters the pentosan buffer tank 314 for temporary storage, and waits for further evaporation and concentration.

The well export in three-phase horizontal decanter centrifuge 301 links to each other with the entry of back curing jar 302, and the bottom of back curing jar 302 links to each other with the entry of curing material shears 304 through back curing jar screw pump 303, and the export of curing material shears 304 links to each other with gluten separation washing workshop section.

B starch milk and gluten discharged from a three-phase horizontal screw centrifuge enter a post-curing tank 302 for post-curing, the time is controlled to be about half an hour, and the cured B starch milk and the gluten are conveyed into a cured material shearing device 304 through a screw pump 303 of the post-curing tank, so that on one hand, welding slag and scrap iron in a pipeline are cut off in advance, and the scrap iron and the like are prevented from entering a gluten drying system to cause contact with a lifting fan blade to generate spark explosion; removing the cured material shearing device 304 for cleaning when the welding slag is accumulated to a certain amount; on the other hand, the cooked material shearing device 304 shears and breaks up the gluten formed by the dough, releases the B starch wrapped in the dough, discharges the B starch through the cooked material conveying pipe 305, enters a subsequent gluten separation washing section for screening, and improves the protein content in the gluten.

As shown in fig. 4, the a starch refining dehydration section includes a two-phase horizontal decanter centrifuge 403, a refined a starch milk buffer tank 404, a scraper centrifuge 407, and a clarifier 410, an outlet of the defibering a starch milk buffer tank 312 is connected to an inlet of the defibering buffer tank discharge pump 401, an outlet of the defibering buffer tank discharge pump 401 is connected to an inlet of the two-phase horizontal decanter centrifuge 403 through a defibering a starch milk delivery pipe 402, the defibered a starch enters the defibering a starch milk buffer tank 312 for temporary storage, the defibering buffer tank discharge pump 401 delivers the a starch milk to the two-phase horizontal decanter centrifuge 403 for refining, and a feed concentration of the two-phase horizontal decanter centrifuge 403 is 18% to 22%. At the rotating speed of 2000rpm, a small amount of gluten contained in the A starch is removed, so that the protein content is reduced to be within 0.35 percent. The flow rate into the two-phase horizontal screw centrifuge 403 is regulated by a dewatering feed regulating valve FC4, and a dewatering feed flow meter FT4 shows the flow rate into the two-phase horizontal screw centrifuge 403.

The heavy phase outlet of the two-phase horizontal decanter centrifuge 403 is connected with the inlet of the refined A starch milk buffer tank 404, the heavy phase of the two-phase horizontal decanter centrifuge 403 is A starch, and the discharge concentration is 32-35%. The A starch is discharged from the heavy phase of the two-phase horizontal decanter centrifuge 403 and enters a refined A starch milk buffer tank 404, and the conventional dehydration mode is adopted because the viscosity of the A starch milk is high, so that the filter screen of the scraper centrifuge 407 is often blocked by the starch, the dehydration effect is poor, or the normal dehydration cannot be performed.

The outlet of the refined A starch milk buffer tank 404 is connected with the inlet of the high-level tank 406 through a refined buffer tank output pump 405, the overflow port of the high-level tank 406 is connected with the return port of the refined A starch milk buffer tank 404, the refined A starch milk buffer tank is sent into the high-level tank 406 through the refined buffer tank output pump 405, and the liquid level of the high-level tank 406 is higher than the overflow port, and then automatically flows from the overflow port and returns to the refined A starch milk buffer tank 404.

The bottom outlet of the high-level tank 406 is connected with the inlet of a scraper centrifuge 407, the liquid phase outlet of the scraper centrifuge 407 is connected with the inlet of a decanter centrifuge buffer tank 408, and the dry matter outlet of the scraper centrifuge 407 is provided with a belt conveyor 412. The A starch milk of the ejection of compact from high-order tank bottom gets into scraper centrifuge 407 and carries out centrifugal dehydration, adopts vertical no filter screen scraper centrifuge to dewater, and starch milk gets into the back from the top and is got rid of on centrifugal inner wall under the effect of centrifugal force down, and starch proportion is great, hugs closely the inner wall, and water and albumen proportion are lighter to be taken out along the effect of centrifugal force on the centrifuge inner wall and export the overflow and get rid of from centrifuge. The scraper centrifuge 407 can remove water and remove residual proteins with small particle size and soluble proteins in the starch milk refining process.

The dehydrated A starch has a dry matter content of 60-62%, and is conveyed to the A starch crushing and drying section through a belt conveyor 412.

The light phase outlet of the two-phase decanter centrifuge 403 is also connected with the inlet of the decanter centrifuge clear liquid buffer tank 408, and the light phase is discharged as protein. An outlet of the decanter centrifuge buffer tank 408 is connected with an inlet of the clarifier 410 through a centrifugal pump 409, filtrate dehydrated by the scraper centrifuge 407 and a light phase of the two-phase decanter centrifuge 403 enter the decanter centrifuge 408 together, feed liquid of the decanter centrifuge 408 contains a small amount of protein and starch, the content of dry matters is still high, and the feed liquid is sent into the clarifier 410 through the centrifugal pump 409 to be separated, so that the content of dry matters in the process water is further removed.

The light phase outlet of the clarifier 410 is connected with the inlet of the process water pipe G1, the light phase separated by the clarifier 410 can be used as process water to enter the process water pipe G1 to a flour kneading section for flour size mixing, and can also be used to a horizontal screw separation section to be mixed with homogenized flour pulp.

The heavy phase outlet of the clarifier 410 is connected with the inlet of the crude A starch milk buffer tank 306, and the separated concentrated material flows out from the heavy phase of the clarifier 410 and returns to the crude A starch milk buffer tank 306 through a clarifier return pipe 411.

As shown in fig. 5, the a starch pulverizing and drying section includes a starch mixer 501, a lift fan 503, an air flow drying duct 506, a cyclone 509, a high pressure fan 513, a starch dust collector 514, a rotary distributor 515, an a starch inspection sieve 516 and a tail gas washing tower 520.

The outlet of the belt conveyor 412 is in butt joint with the inlet of the starch mixer 501, the outlet of the starch mixer 501 is provided with a mixer discharging screw 502, the outlet chute of the mixer discharging screw 502 is connected with the inlet of the lifting fan 503, the dehydrated starch A is conveyed into the starch mixer 501 through the belt conveyor 412 and mixed with the coarse starch discharged from the coarse powder return screw 518 and the dry starch returned from the dry starch screw conveyor 510, and the starch A is conveyed into the lifting fan 503 through the mixer discharging screw 502 after the moisture and viscosity of the starch are reduced.

An inlet of the air heater 505 is communicated with the atmosphere through the air filter 504, a heat medium inlet of the air heater 505 is connected with the steam generation pipe G2, and a heat medium outlet of the air heater 505 is connected with the condensed water collection pipe. The cold air is filtered by an air filter 504, the filtered fresh air is subjected to heat exchange with steam by an air heater 505, the air is heated, and the steam is cooled into condensed water which is returned to the boiler room through a condensed water collecting pipe.

An air outlet pipeline of the air heater 505 is connected with an inlet of the lift fan 503, and an outlet of the lift fan 503 is connected with an airflow drying air pipe 506. A part of heated hot air enters the lifting fan 503 to be mixed and crushed with wet starch, and the starch can be crushed and also can be given an initial speed of entering air flow for drying under the high-speed rotation of the fan impeller.

An air outlet pipeline II of the air heater 505 is connected with the lower part of the airflow drying air pipe 506, the other part of hot air directly enters the airflow drying air pipe 506, wet starch is subjected to heat and moisture exchange with the hot air in the airflow drying air pipe 506, moisture in the wet starch is removed by flash evaporation, and the flash evaporated moisture is taken away from tail gas by air.

After the starch advances for a certain distance along the airflow drying air pipe 506, the speeds of the starch and the airflow tend to be consistent, and the evaporation drying effect is reduced; an expanding settling section 507 is arranged at intervals along the airflow drying air pipe 506, and the sectional area of the airflow conveying pipe is changed to realize the sudden reduction of the airflow speed, so that the speed difference between starch and airflow is generated again, and the better evaporation effect is kept all the time.

The top symmetry of this system at air current drying tuber pipe 506 is equipped with three explosion vent 508, and when the dust explosion takes place, three explosion vent 508 break through rapidly, and outside pressure release avoids damaging equipment or causes bodily injury.

The upper outlet of the pneumatic drying air duct 506 is connected to the inlet of a cyclone 509, and the bottom outlet of the cyclone 509 is connected to the inlet of a dry starch screw conveyor 510 through an air seal. The evaporated and dried starch is separated in a cyclone, and the dried starch is discharged from the bottom of the cyclone 509, discharged from an air seal thereof, and discharged by a dried starch screw conveyor 510.

The dry starch screw conveyor 510 is provided with two discharge ports, an auxiliary outlet of the dry starch screw conveyor 510 is connected with an inlet of the starch mixer 501 through a dry starch return pipe 519, a part of the output dry starch enters the starch mixer 501 through an air seal machine return material, the water content of the mixture is reduced, the viscosity of the A starch is properly reduced, and the bridging phenomenon of the starch in the process of conveying and mixing is eliminated; and the drying strength is reduced, and the product quality is improved.

In the system installation process, impurities such as welding slag, scrap iron and the like are inevitably left on the inner wall of the pipeline, the impurities are difficult to clean, and in the initial operation stage, when the welding slag falls off and reaches the high-pressure fan 513, the welding slag collides with the impeller to generate sparks, so that dust explosion is easily caused.

The main outlet of the dry starch screw conveyer 510 is connected with the inlet of the de-ironing air separator 511, the outlet pipeline of the de-ironing air separator 511 is connected with the inlet of the high pressure fan 513, and the outlet pipeline of the high pressure fan 513 is connected with the inlet of the starch dust collector 514. The other part of the dry starch enters an iron removal air separator 511, the dry starch after the welding slag and the scrap iron are removed enters a high-pressure fan 513, and is sucked and sent by the high-pressure fan 513, and air-blowing and cooling are carried out simultaneously, and meanwhile, the dry starch is further crushed under the action of an impeller. The dry starch after being crushed and cooled is sent to a starch dust collector 514, the dry starch is adsorbed on a cloth bag, discharged and discharged, and the tail gas is directly emptied.

Because the high pressure fan 513 has a relatively high noise, the silencer 512 is disposed at the air suction opening of the iron removal air separator 511 to reduce the noise of the air suction opening and the high pressure fan 513. The iron chips with heavier specific gravity are discharged from the bottom of the iron removing air separator 511 by the air separation function.

The outlet at the bottom of the starch dust collector 514 is connected with the inlet of each A starch checking sieve 516 through a rotary distributor 515, the fine powder outlet of each A starch checking sieve 516 is respectively connected with a finished product starch chute 517, the coarse powder outlet of each A starch checking sieve 516 is respectively connected with the inlet of a coarse powder return screw 518, and the outlet of the coarse powder return screw 518 is connected with the inlet of a dry starch return pipe 519.

The bottom discharge from the starch dust collector 514 is uniformly distributed into each A starch inspection sieve 516 by a rotary distributor 515 for sieving, and oversize coarse powder returns to the starch mixer 501 through a coarse powder return screw 518 to be mixed with wet starch; the undersize reaches the fineness requirement, and the undersize is sent to a packaging workshop through a finished product starch chute 517. The yield of the starch A can reach 55 to 60 percent, and the market price is about 3000 yuan/ton.

The viscosity of the wheat A starch is high, so that the fineness after drying cannot meet the requirement, and the system adopts a two-stage crushing process of a lifting fan 503 and a high-pressure fan 513 to improve the fineness of the starch.

The top outlet of the cyclone 509 is connected with the air inlet of the tail gas washing tower 520 through a draught fan, the bottom water outlet of the tail gas washing tower 520 is connected with the inlet of a washing circulating pump 521, the outlet of the washing circulating pump 521 is connected with the upper water spraying pipe 520g of the tail gas washing tower 520 through a washing circulating pipe, and the middle part of the washing circulating pipe is also connected with the inlet of the pentosan buffer tank 314 through a washing discharge valve 522.

The tail gas discharged from the top of the cyclone separator is pumped out by a fan and enters the tail gas washing tower 520 to be washed, the tail gas washing tower 520 washes and adsorbs dust in the tail gas with water, and the washed tail gas is directly emptied. The concentration of the circulating washing water after adsorbing the tail gas dust is gradually increased, and the washing circulating water reaching a certain concentration is discharged into the pentosan buffer tank 314 through the washing discharge valve 522.

As shown in fig. 6 to 8, the rotary distributor 515 includes a base, a distributor lower cone 515e with a large top and a small bottom is fixed on the base, a distributor upper cone 515b with a small top and a large bottom is fixed on the distributor lower cone 515e, an access door and a lifting lug are arranged on the distributor upper cone 515b, and a starch inlet short pipe 515a is arranged at the top center of the distributor upper cone 515b.

The periphery of the starch inlet short pipe 515a is sleeved with a rotatable vertical flow guide pipe 515c, an annular seam between the upper end opening of the vertical flow guide pipe 515c and the outer wall of the starch inlet short pipe 515a is sealed by an annular sealing plate, and an annular hole between the upper end opening of the distributor upper cone 515b and the outer wall of the starch inlet short pipe 515a is also sealed by the annular sealing plate. The lower end of the vertical duct 515c is connected to an inclined duct 515d bent to one side.

A plurality of starch discharge ports 515f are uniformly arranged on the circumferential wall of the lower cone 515e of the distributor, the lower port of the inclined draft tube 515d is butted with each starch discharge port 515f, and a starch discharge short joint 515g is respectively connected below each starch discharge port 515f.

A rotating shaft 515k is arranged along the axis of the lower cone 515e of the distributor, the upper end of the rotating shaft 515k is connected with an inclined flow guide pipe 515d through a rotating frame 515m, the lower end of the rotating shaft 515k penetrates out of the center of the bottom wall of the lower cone 515e of the distributor and is connected with the output end of a batching speed reducer 515j, and the input end of the batching speed reducer 515j is driven by a batching motor 515h.

When the distributor works, the batching motor 515h drives the rotating shaft 515k to rotate through the batching speed reducer 515j, the rotating shaft 515k drives the vertical guide pipe 515c and the inclined guide pipe 515d to rotate around the axis of the rotary distributor 515 and the starch inlet short pipe 515a through the rotating frame 515m, and the lower ports of the inclined guide pipes 515d are sequentially aligned with the starch discharge ports 515f. After entering from the starch inlet short pipe 515a, the dry starch falls down along the vertical guide pipe 515c and the inclined guide pipe 515d, is fed to the starch discharge ports 515f one by one, flows out from each starch discharge short pipe 515g, and enters the corresponding starch A inspection sieve 516 for sieving. The rotating shaft 515k rotates at a constant speed, so that uniform discharging of each starch discharging short section 515g can be ensured.

As shown in fig. 9, a hood is disposed at the top of the tail gas washing tower 520, a water accumulation conical disc 520m is disposed at the lower portion of the tail gas washing tower 520, a washing air inlet 520k is disposed above the water accumulation conical disc 520m, a water outlet bell mouth is disposed in the water accumulation conical disc 520m, the water outlet bell mouth extends downward to a washing circulating water outlet 520n outside the tower, and the washing circulating water outlet 520n is connected to an inlet of a washing circulating pump 521.

A washing water replenishing port 520p is arranged at the lower part of the tower body and above the water level line, and a washing sewage draining port 520q is arranged at the conical bottom of the water accumulation conical disc 520m, so that the starch retained at the bottom of the water accumulation conical disc 520m can be drained conveniently. The upper part of the tower body is also provided with a water seal overflow pipe 520r, the upper port of the water seal overflow pipe 520r is arranged at the water level line, and the water seal overflow pipe 520r extends out of the bottom of the tower body after being bent downwards and upwards in an S shape. The washing sewage outlet 520q and the outlet of the water-sealed overflow pipe 520r can be connected to the pentosan buffer tank 314.

The upper part of the tower body is provided with a water spraying pipe 520g, the outer end of the water spraying pipe 520g extends out of the tower body to form a washing circulating water inlet, and a circulating pipeline at the outlet of a washing circulating pump 521 is connected with the washing circulating water inlet; the inner end of the water spraying pipe 520g is downward along the axis of the tower body and is provided with a water spraying bell mouth. And the washing circulating pump 521 pumps out the water in the water accumulation conical disc 520m and sends the water to the water spraying pipe 520g above to spray downwards.

The lower part of the water spraying bell mouth is provided with a first layer of sealing disc 520h with high center and low periphery, the lower part of the first layer of sealing disc 520h is provided with a first layer of disc 520j with wide upper part and narrow lower part, the upper end of the disc 520j is welded on the inner wall of the tower body, and the diameter of the lower port of the disc 520j is smaller than the outer diameter of the sealing disc 520h.

A second layer of sealing disc is arranged below the first layer of disc 520j, a second layer of disc is arranged below the second layer of sealing disc, and the like, and the bottom layer of disc is positioned above the washing air inlet 520k.

The tail gas from the cyclone 509 enters the inner cavity of the tower body from the washing air inlet 520k at the lower part and flows upwards, the spray water firstly falls on the center of the top of the dome shape of the first layer of sealing disc, and flows downwards to the lower port of the first layer of sealing disc along the outer wall of the first layer of sealing disc, and a first annular water curtain is formed at the lower edge of the first layer of sealing disc.

The first annular water curtain falls down on the inner wall of the first layer of disc, splashes and forms a second annular water curtain at the lower port of the first layer of disc; the water falling from the first layer of disc plate falls on the outer wall of the second layer of sealing disc, a third annular water curtain is formed on the lower edge of the second layer of sealing disc, then a fourth annular water curtain is formed at the lower port of the second layer of disc plate continuously, and the like.

The tail gas entering from the washing air inlet 520k firstly enters the inner cavity of the bottom layer disc, turns to pass through the bottom layer water curtain and then enters the peripheral space of the bottom layer sealing disc, then turns to pass through the secondary bottom layer water curtain and then enters the upper part of the bottom layer sealing disc, and so on, until turning to pass through the secondary second annular water curtain and then enter the inner cavity of the first layer disc, then turns to pass through the secondary first annular water curtain and then flows to the top of the tower, and finally flows out from the hood.

In the process of the opposite flow of the tail gas and the washing water, the tail gas passes through the water curtain for a plurality of times and is washed by splashed spray for a plurality of times, so that the starch carried in the tail gas is captured by the spray, and the clean tail gas is discharged outdoors. Not only avoids the problem of blockage of the spraying port, but also ensures no sanitary dead angle in the cavity.

Some water is lost with washing, and is replenished through the washing replenishment port 520p, and excess water flows out through the water seal overflow pipe 520r.

As shown in fig. 10, the funnel cap includes a funnel cap upper cone 520a with a narrow top and a wide bottom and a funnel cap lower cone 520b with a wide top and a narrow bottom, the lower end of the funnel cap upper cone 520a covers the upper port of the funnel cap lower cone 520b and exceeds the funnel cap lower cone 520b to form an outer cornice, when rainwater falls on the outer wall of the funnel cap upper cone 520a, the rainwater flows downwards to the lower edge of the funnel cap upper cone 520a and falls, so that the rainwater is prevented from flowing along the outer wall of the funnel cap lower cone 520b, and corrosion of the funnel cap lower cone 520b is reduced.

The lower port of the funnel cap lower cone 520b is sleeved on the periphery of the funnel cap short tube, and an annular rainwater discharge port 520f is formed between the outer wall of the funnel cap short tube and the inner wall of the lower port of the funnel cap lower cone 520b.

The inner cavity of hood is equipped with the cone center, and the cone center includes that main aspects weld positive awl 520c and back taper 520d as an organic whole, and the vertex of a cone of positive awl 520c and back taper 520d all is located the tower body axis, makes the last port and the lower port of hood all have complete draught area, reduces ventilation resistance. The middle of the inverted cone 520d is supported on the inner wall of the funnel lower cone 520b by a plurality of cone center supports 520e.

The lower port of the positive cone 520c exceeds the upper port of the inverted cone 520d, and rainwater on the outer wall of the positive cone is prevented from flowing downwards along the inverted cone 520d. The diameter of the lower end of the right cone 520c is larger than that of the circumference of the annular rainwater discharge port 520f, so that rainwater is prevented from falling into the lower port of the hood.

Rainwater falling from the upper port of the blast cap hits the outer wall of the positive cone 520c, flows downwards to the lower edge of the positive cone 520c, falls on the inner wall of the lower cone 520b of the blast cap and flows downwards, and is finally discharged from the annular rainwater discharge port 520f at the lower port of the lower cone 520b of the blast cap.

As shown in fig. 11, pentosan enzymatic degradation and MVR evaporation includes a plate preheater 602, a second visbreaker tank 604, a static mixer 607, an enzymatic reaction tank 608, an evaporation feed tank 609, a tube preheater 611, a falling film evaporator 613, an evaporation circulation pump 614, a separator 616 and a vapor compressor 617.

The outlet of the pentosan buffer tank 314 is connected with the inlet of a pentosan feed pump 601, the outlet of the pentosan feed pump 601 is provided with a pentosan feed flow meter FT5 and a pentosan feed adjusting valve FC5, the outlet of the pentosan feed adjusting valve FC5 is connected with the cold-side inlet of the plate heat exchanger, and the cold-side outlet of the plate preheater 602 is connected with a pentosan feed pipe 603. The opening of the pentosan feed regulating valve FC5 is controlled by a flow signal of the pentosan feed flow meter FT5.

The bottom outlet of the condensed water tank 618 is connected with the inlet of a condensed water pump 619, the outlet of the condensed water pump 619 is connected with the hot side inlet of the plate preheater 602, and the hot side outlet of the plate preheater 602 is connected with an evaporation condensed water discharge pipe 620. The condensed water pump 619 draws out the condensed water collected in the condensed water tank 618, and sends the condensed water to the hot side of the plate preheater 602 to preheat the pentosan, and the condensed water is discharged from the evaporated condensed water discharge pipe 620.

Pentosan is non-starch viscose polysaccharide, and araboxylan is the main component, and has high viscosity, and is easy to stick to evaporation tubes during evaporation to cause tube scaling, so that proper viscosity reducing enzyme is added before evaporation, the viscosity of the material is reduced, and the tube scaling phenomenon is reduced.

7-8% of pentosan in the pentosan buffer tank 314 is sent to the cold side of the plate preheater 602 through the evaporation feed pump 610, and the evaporation condensed water at the hot side preheats the feed liquid to 50 ℃, so that the activity of the enzyme preparation can be improved, the degradation reaction speed of the enzyme preparation on xylan can be improved, and the MVR evaporation steam consumption can be reduced.

An inlet pipeline of the second metering pump 605 is inserted into the bottom of the second viscosity-reducing enzyme tank 604, and an outlet of the second metering pump 605 is connected with a viscosity-reducing enzyme adding pipe 606.

The pentosan feed pipe 603 and the visbreaking enzyme adding pipe 606 are respectively connected with the inlet of a static mixer 607, the outlet of the static mixer 607 is connected with the inlet of an enzymolysis reaction tank 608, and the outlet of the enzymolysis reaction tank 608 is connected with the inlet of an evaporation feed tank 609. The preheated pentosan is sent into a static mixer 607 through a pentosan feed pipe 603; the second visbreaking enzyme tank 604 is pumped out by the second metering pump 605, and is also fed into the static mixer 607 through the second visbreaking enzyme adding pipe 606, and the preheated pentosan and the visbreaking enzyme are fully mixed by the static mixer 607 and enter the enzymolysis reaction tank 608.

The viscosity reducing enzyme adding pipe 606 is provided with a second viscosity reducing enzyme flow meter FM2, and the flow of the second metering pump 605 is controlled by the flow monitored by the pentosan feed flow meter FT5 and the second viscosity reducing enzyme flow meter FM2.

The feed flow rate of pentosan is adjusted by a pentosan feed adjusting valve FC5, and the opening degree of the pentosan feed adjusting valve FC5 is interlocked with a flow signal of a pentosan feed flow meter FT5. The addition amount of the viscosity reducing enzyme is controlled by the second metering pump 605 through frequency conversion, and the flow of the second viscosity reducing enzyme flow meter FM2 is automatically linked with the pentosan feed flow meter FT5.

The enzymolysis retort 608 is internally provided with a stirring device, pentosan added with the viscosity-reducing enzyme is mixed and reacted in the retort, the reaction efficiency is improved, the impurity precipitation can be prevented to ensure the first-in first-out of the material, meanwhile, a division plate is arranged in the enzymolysis retort 608, small holes are formed in the division plate, syrup uniformly passes through the enzymolysis retort 608 from top to bottom in sequence, the reaction time is controlled to be 20-30 minutes, and after the reaction is finished, the pentosan is discharged from the bottom and enters the evaporation feed tank 609.

The bottom outlet of the evaporation feed tank 609 is connected with the inlet of an evaporation feed pump 610, the outlet of the evaporation feed pump 610 is connected with the cold side inlet of a tube array preheater 611, the cold side outlet of the tube array preheater 611 is connected with an evaporation feed pipe 612, the evaporation feed pipe 612 and the bottom outlet of the falling film evaporator 613 are connected with the inlet of an evaporation circulating pump 614 together, and the outlet of the evaporation circulating pump 614 is connected with the top inlet of the falling film evaporator 613 through an evaporation circulating pipe 615. The preheated and viscosity-reduced pentosan enters an inlet of an evaporation circulating pump 614, enters an inlet at the upper end of a falling film evaporator 613 through the evaporation circulating pump 614 to form uniform falling films on the inner walls of falling film pipes, and exchanges heat with secondary steam outside the falling film pipes to evaporate water in syrup.

The non-condensable gas discharge port of the falling film evaporator 613 is connected with the hot side inlet of the tube bank preheater 611, the hot side outlet of the tube bank preheater 611 is connected with the hot side inlet of the condenser 622 through a non-condensable gas conveying pipe 621, and the hot side outlet of the condenser 622 is connected with the vacuum pump 623.

The circulating water inlet pipe G4 is connected with the cold side inlet of the condenser 622, and the cold side outlet of the condenser 622 is connected with the circulating water outlet pipe G5. The shell side drain of the condenser 622 is connected to the inlet of the condensate tank 618.

The enzymolysis syrup in the evaporation feed tank 609 is pumped out by the evaporation feed pump 610 and sent to the cold side of the tubular preheater 611 to be heated by the non-condensable gas from the falling film evaporator 613, so that the temperature of the liquid entering the MVR evaporation system is increased, and the steam consumption is reduced.

The lower part of the falling-film evaporator 613 is connected with a separator 616 through a communicating pipe, a secondary steam outlet of the separator 616 is connected with an inlet of a steam compressor 617, an outlet of the steam compressor 617 is connected with a hot-side inlet of the falling-film evaporator 613, and a hot-side outlet of the falling-film evaporator 613 is connected with a condensate water tank 618. The secondary vapor outlet of the condensate tank 618 is also connected to the inlet of the vapor compressor 617.

The evaporation feed tank 609 is provided with a liquid level sensor, the evaporation feed pipe 612 is provided with a feed liquid level regulating valve LC1, and the opening degree of the feed liquid level regulating valve LC1 is controlled by the liquid level of the evaporation feed tank 609. The cold side outlet of the tube still preheater 611 is provided with a feed level adjusting valve LC1, and the level of the evaporation feed tank 609 is kept stable by changing the opening degree of the feed level adjusting valve LC1.

The outlet of the condensate pump 619 is also connected to the outlet of the vapor compressor 617 via a condensate control valve FC6, and the opening of the condensate control valve FC6 is controlled by the temperature of the vapor at the outlet of the vapor compressor 617. A small amount of condensed water is injected into an outlet of the vapor compressor 617 through the condensed water regulating valve FC6, the temperature of the condensed water regulating valve FC6 is automatically interlocked with the temperature of the outlet of the vapor compressor 617, the amount of added condensed water is controlled, superheated steam is changed into saturated steam, the temperature is controlled at 66 ℃ so as to improve the heat exchange efficiency of the evaporator tube array, and the evaporation temperature of the falling-film evaporator 613 is evaporated at a low temperature not higher than 60 ℃ so as to avoid starch gelatinization.

The hot side inlet of the falling film evaporator 613 is connected to a raw steam pipe G2 through a steam regulating valve PC, and the opening degree of the steam regulating valve PC is controlled by the steam pressure at the hot side inlet of the falling film evaporator.

The evaporation of water in the falling film produces secondary steam and discharges from the top of separator 616, can smuggle partial material secretly when separator 616 top discharge secondary steam, and especially pentosan relative viscosity is high, and the composition is complicated, produces the foam easily, smugglies more easily, for reducing the condition of smuggleing secretly of material among the secondary steam, sets up two-stage defoaming device in the separator export.

The secondary steam after the two times of defoaming is compressed by a steam compressor 617, the steam pressure and temperature are increased, and the secondary steam is changed into superheated steam.

The compressed secondary steam enters the shell side inlet of the falling film evaporator 613, and condensed water generated after heat exchange enters the condensed water tank 618 for temporary storage. The pressure sensor PA is arranged at the outlet of the steam compressor 617, when the secondary steam pressure at the outlet of the steam compressor 617 is lower than a set value, fresh steam needs to be automatically supplemented, and the supplementing amount of the generated steam is controlled by the steam regulating valve PC. The steam regulating valve PC is automatically interlocked with the outlet pressure of the steam compressor 617 to realize on-line control.

The negative pressure condition of the MVR evaporation system is maintained by the condenser 622 and the vacuum pump 623, and the vacuum pump 623 continuously pumps out non-condensable gas in the system, so that the heat transfer condition is prevented from deteriorating and the pressure is prevented from rising; the condenser 622 condenses and cools the non-condensable gas and a small amount of steam pumped by the vacuum pump 623, so that the workload of the vacuum pump 623 can be reduced, and the condenser 622 and the vacuum pump guarantee the normal operation of each parameter of the evaporation system. The non-condensable gas and the cooling circulating water are subjected to heat exchange and temperature reduction in the condenser 622.

The outlet of the evaporation circulation pump 614 is provided with a regulating valve, and the liquid level in the evaporator cavity is controlled by the regulating valve.

The outlet of the evaporation circulating pump 614 is also connected with a pentosan discharging pipe 625, the pentosan discharging pipe 625 is provided with a concentration detector DT or a mass flow meter, a pentosan discharging adjusting valve LC2 and a three-way valve KV, the opening degree of the pentosan discharging adjusting valve LC2 is controlled by the liquid level of the falling film evaporator 613, and the bypass outlet of the three-way valve KV is connected with the return port of the evaporation feeding tank 609 through a pentosan return pipe 624.

When the concentration of the outlet detected by the concentration detector DT reaches 30%, the discharge port is opened by the three-way valve KV, and the pentosan discharge pipe 625 discharges the pentosan normally. When the concentration of the outlet detected by the concentration detector DT is less than 30%, the three-way valve KV opens the feed back port, and the pentosan returns to the evaporation feed tank 609 through the pentosan return pipe 624 to continue evaporation and concentration.

The effective components of the pentosan after evaporation and concentration are not changed, the concentration of starch and soluble protein in the pentosan is improved, the utilization value of the pentosan is greatly improved, the pentosan can be used as high-quality carbon source and nitrogen source raw materials in the brewing fermentation process, waste is changed into valuable, and the method has objective economic benefit.

As shown in fig. 12, the gluten separation washing section includes a primary gluten screen 701, a primary gluten surge bin 703, a primary gluten screw pump 704, a primary static shear 705, a secondary gluten screen 706, a secondary slurry surge bin 707, a secondary slurry screw pump 708, a secondary gluten surge bin 710, a secondary gluten screw pump 711, a secondary static shear 712, a tertiary gluten screen 713, a tertiary gluten surge bin 715, a tertiary gluten screw pump 716, and a tertiary static shear 717.

The outlet of the cured material conveying pipe 305 is connected with the inlet of the first-level gluten sieve 701, the B starch + gluten phase separated from the three-phase horizontal decanter centrifuge 301 is conveyed into the first-level gluten sieve 701 through the cured material conveying pipe 305 for first-level sieving, the undersize outlet of the first-level gluten sieve 701 is connected with the B starch milk conveying pipe 702, and the B starch milk separated under the first-level gluten sieve 701 is conveyed to a brewery 719 through the B starch milk conveying pipe 702 to be directly used as a carbon source for fermentation.

The outlet on the sieve of one-level gluten sieve 701 links to each other with the entry of one-level gluten surge bin 703, and the export of one-level gluten surge bin 703 is equipped with one-level gluten screw pump 704, and the export of one-level gluten screw pump 704 links to each other with the entry of one-level static shears 705. Gluten on the first-level gluten sieve 701 enters a first-level gluten buffer bin 703 and is washed by undersize slurry of the third-level gluten sieve 713. Then the mixture is sent into a first-stage static cutter 705 by a first-stage gluten screw pump 704, the first-stage gluten forming the dough is cut and scattered again, the B starch wrapped in the dough is released, the protein content in the gluten is improved, and the mixture enters a second-stage gluten screen 706 for secondary screening.

The sieve seam with the clearance of 1.5mm is arranged in the static shearing device, the feeding is carried through the screw pump, the pressure of the large gluten block with pressure penetrates through the sieve seam with the diameter of 1.5mm, the large gluten block is cut into small gluten blocks through the shearing force of the screen, and the B starch in the gluten block after being cut into small gluten blocks is easier to separate.

The export of one-level static shears 705 links to each other with the entry of second grade gluten sieve 706, and the export under the sieve of second grade gluten sieve 706 links to each other with the entry of second grade thick liquid surge bin 707, and the export of second grade thick liquid surge bin 707 is equipped with second grade thick liquid screw pump 708, and second grade thick liquid screw pump 708's export is passed through second grade thick liquid back flow pipe 709 and is linked to each other with curing material conveyer pipe 305. The B starch milk separated out by the second-stage gluten screen 706 enters a second-stage slurry buffer bin 707, is sent out by a second-stage slurry screw pump 708, and returns to the first-stage gluten screen 701 through a second-stage slurry return pipe 709 for secondary screening.

Export on the sieve of second grade gluten sieve 706 links to each other with the entry of second grade gluten surge bin 710, and the second grade gluten that second grade gluten sieve 706 was sieved gets into second grade gluten surge bin 710, mixes the washing with the process water that comes from technology process water pipe G1. Filtrate generated in the subsequent gluten dewatering section also enters the second-level gluten buffer bin 710 through a gluten dewatering filtrate return pipe 806 to wash second-level gluten.

Second grade gluten surge bin 710 is equipped with second grade gluten screw pump 711, and the export of second grade gluten screw pump 711 links to each other with the entry of second grade static shear 712, and the export of second grade static shear 712 links to each other with the entry of tertiary gluten sieve 713. The second grade gluten after washing is sent into second grade static shears 712 by second grade gluten screw pump 711, and the gluten that will form the dough continues to be sheared and is broken up, and the B starch that will wrap up in the dough continues to release, continues to improve the protein content in the gluten, and the washing is carried out against the current, washes the starch in the gluten, and reentrant tertiary gluten sieve 713 carries out tertiary screening.

The undersize outlet of the third gluten screen 713 is connected with the inlet of the first gluten buffer bin 703 through a third slurry return pipe 714; b starch milk separated under the screen of the third gluten screen 713 returns to the first gluten buffer bin 703 through a third slurry return pipe 714 to be mixed and washed, and is mixed, sheared and conveyed with the first gluten.

An oversize outlet of the third gluten screen 713 is connected with an inlet of a third gluten buffer bin 715, and inlets of the second gluten buffer bin 710 and the third gluten buffer bin 715 are respectively connected with an outlet valve of a process water pipe G1; the bottom of tertiary gluten surge bin 715 is equipped with tertiary gluten screw pump 716, and the export of tertiary gluten screw pump 716 links to each other with the entry of tertiary static shears 717.

Tertiary gluten that tertiary gluten sieve 713 sieved gets into tertiary gluten surge bin 715, mix the washing back with the process water that comes from technology process water pipe G1, send into tertiary static shears 717 by tertiary gluten screw pump 716, the gluten that will form the dough is sheared once more and is broken up, the B starch that will wrap up in the dough releases once more, continue to improve the protein content in the tertiary gluten, send out tertiary gluten and enter into the gluten dehydration workshop section through gluten washing discharging pipe 718.

As shown in fig. 13, the gluten dewatering section includes a drum screen 801, a gluten dewatering machine 802, a wringer 803, a filtrate tank 804, a feed surge bin 807, and a circulating screw pump 808. The gluten dehydration section adopts three levels of dehydration, wherein the first level is a roller screen 801, the second level is a gluten dehydrator 802, and the third level is a drying machine 803.

The outlet of the three-stage static shearing device 717 is connected with the inlet of a rotary screen 801, the rotary screen 801 is provided with a screen mesh, the inside of the screen mesh is provided with a helical blade, gluten is pushed by the helical blade to rotate and discharge in the rotating process of the rotary screen, and water passes through the screen mesh and enters a filtrate tank 804; the water content of the gluten after the third-level gluten is dehydrated by a roller screen 801 grade one is less than or equal to 73 percent.

The outlet on the screen of the drum screen 801 is connected with the inlet of the gluten dehydrator 802, the screw pitch of the gluten dehydrator 802 is the same, the inner diameter is reduced from large to small, the gluten is dehydrated in a variable inner diameter extrusion mode, and the moisture content of the gluten after the secondary dehydration is less than or equal to 70%.

The dry matter outlet of the gluten dehydrator 802 is connected with the inlet of the wringing machine 803, the internal diameters of the wringing machine 803 are consistent, the screw pitch is changed from big to small, the gluten is dehydrated in a variable screw pitch mode, and the moisture content of the gluten after the three-stage dehydration is less than or equal to 68 percent.

The outlet of the wringing machine 803 is connected with the inlet of the feeding buffer bin 807, the bottom of the feeding buffer bin 807 is provided with a circulating screw pump 808, the outlet of the circulating screw pump 808 is connected with a first circulating pipe 809, the outlet of the first circulating pipe 809 is connected with the inlet of the wringing machine 803, the wrung gluten enters the feeding buffer bin 807, is extruded by the circulating screw pump 808, returns to the wringing machine 803 through the first circulating pipe 809 for circulation, and enters the wringing machine 803 together with the discharge of the drum screen 801 for wringing.

The outlet of the circulating screw pump 808 is also connected with a second circulating pipe 810, the outlet of the second circulating pipe 810 is connected with the inlet of the feeding buffer cabin 807, and gluten extruded by the circulating screw pump 808 returns to the feeding buffer cabin 807 through the second circulating pipe 810 for circulating dehydration.

The outlet pipe of the circulating screw pump 808 is also connected to the inlet of the feed screw pump 811, and the outlet of the feed screw pump 811 is connected to the gluten crushing and drying system through the drying system feed pipe 812. Part of the gluten extruded by the circulating screw pump 808 enters a feeding screw pump 811 to feed a drying system feeding pipe 812.

Filtrate outlets of the rotary screen 801, the gluten dewatering machine 802 and the wringing machine 803 are respectively connected with the filtrate tank 804, washed gluten enters the rotary screen 801 through a gluten washing discharge pipe 718, and filtrate of the rotary screen 801 enters the filtrate tank 804; gluten on the screen of the drum screen 801 enters a gluten dewatering machine 802 for dewatering, and filtrate of the gluten dewatering machine 802 also enters a filtrate tank 804; the gluten dehydrated by the gluten dehydrator 802 enters a wringing machine 803 for wringing, and the filtrate of the wringing machine 803 also enters a filtrate tank 804.

The bottom of filtrating jar 804 is equipped with filtrating screw pump 805, and the export of filtrating screw pump 805 is passed through gluten dehydration filtrating back flow pipe 806 and is linked to each other with the entry of second grade gluten surge bin 710. And the three-stage dehydration filtrate in the filtrate tank 804 is sent out by a filtrate screw pump 805, and returns to the secondary gluten buffer bin 710 of the gluten separation washing section through a gluten dehydration filtrate return pipe 806 to wash secondary gluten.

Compressed air pipe G6 links to each other with the export of circulation screw pump 808 and the export of feed screw pump 811, blows through compressed air during the parking, will remain outside the gluten discharge system in the pipeline.

As shown in fig. 14 to 18, the gluten system includes a gas preheater 902, a finned heat exchanger 903, a fish mouth feeder 905a, a riser 905, a volute separator 906, a two-bin dust collector 907, a gluten buffer bin 913, a crusher 915, a gluten dust collector 916, and a gluten finished product conveyor 920.

The outlet of the drying system feeding pipe 812 is connected with the feeding port of the riser 905, the outlet of the riser 905 is connected with the wet and dry wheat gluten inlet of the volute separator 906 through a circulation pipeline, the volute separator 906 is further provided with a hot air inlet, a dry wheat gluten outlet and a wet wheat gluten outlet, the hot air inlet and the wet wheat gluten outlet are located on the same straight line, the wet and dry wheat gluten inlet enters from the upper part along an arc-shaped tangential direction, and the dry wheat gluten outlet enters from the upper part along the tangential direction and exits from the arc-shaped direction.

The export of air cleaner 901 links to each other with the cold side entry of gas heater 902, the cold side export of gas heater 902 links to each other with the air intake of fin heat exchanger 903, fin heat exchanger 903 is equipped with in proper order along the air flow direction and congeals water heat transfer section and steam heat transfer section, raw steam pipe G2 links to each other through the hot side entry of temperature control governing valve TC with steam heat transfer section, the hot side export of steam heat transfer section links to each other with the hot side entry of congealing water heat transfer section through steam trap and comdenstion water back flow 904, the hot side export of congealing water heat transfer section links to each other with the comdenstion water collecting pipe. The raw steam enters the steam heat exchange section to heat the air to form condensed water, and the condensed water is discharged through the steam trap and then enters the condensed water heat exchange section through the condensed water return pipe 904 to release waste heat.

An air outlet of the finned heat exchanger 903 is connected with a hot air inlet of a volute separator 906, a wet material outlet of the volute separator 906 is connected with an air inlet of a lifter 905, and a dry wheat gluten outlet of the volute separator 906 is connected with an air inlet of a double-bin dust remover 907.

As shown in fig. 18, the upper portion of the dual-bin dust remover 907 is provided with a dust-removing air-out chamber 907a, and the upper portion of the dust-removing air-out chamber 907a is provided with a dual-bin dust remover air outlet. A dry powder dust removal chamber 907b and a wet powder dust removal chamber 907c are arranged below the dust removal air outlet chamber 907a side by side, and a blind plate is arranged at the top of the wet powder dust removal chamber 907c and isolated from the dust removal air outlet chamber 907a to prevent short circuit of air flow; the top of the dry powder dust chamber 907b is communicated with the dust outlet chamber 907a.

The inner cavity of the dry powder dust removal chamber 907b is provided with a plurality of dust removal cloth bags, and the cloth bags are not arranged in the wet powder dust removal chamber 907 c; the air inlet 907f of the double-bin dust remover is connected to the upper side wall of the wet powder dust removal chamber 907c. Gluten powder enters the wet powder dust chamber 907c from the air inlet 907f of the dust remover, the air speed is reduced rapidly due to the cross section expansion, and the wet gluten powder with higher water content directly settles downwards due to higher specific gravity; the dry wheat gluten with low water content transversely floats to the dry powder dust removal chamber 907b along with the air flow due to low specific gravity, and the dry wheat gluten is adsorbed on the outer wall of the cloth bag, so that wet powder is prevented from being adsorbed on the outer wall of the cloth bag to form bonding; compressed air is blown into the cloth bag regularly, and dry wheat gluten can fall off easily, so that the cloth bag has high dust removal efficiency, small wind resistance, long service life and long-term stable operation.

A dry powder settling chamber 907d is arranged below the dry powder dust removing chamber 907b, a dry powder discharging spiral 908a is arranged at the bottom of the dry powder settling chamber 907d, and the dry powder discharging spiral 908a is provided with two outlets, one discharging and one returning. A wet powder settling chamber 907e is arranged below the wet powder dust removal chamber 907c, a wet powder discharging spiral 908b is arranged at the bottom of the wet powder settling chamber 907e, and the wet powder discharging spiral 908b is provided with two outlets, namely one discharging outlet and one returning outlet.

The first outlets of the dry powder discharging screw 908a and the wet powder discharging screw 908b are respectively connected with the inlet of the dry and wet powder returning screw 909, the outlet of the dry and wet powder returning screw 909 is connected with the air inlet of the lifter 905 through the dry powder rotary valve 910 to realize the returning of the dry wheat gluten, and the dry wheat gluten is fed into the air inlet pipeline of the lifter 905 through the dry powder rotary valve 910 to be mixed with the wet gluten.

Two outlets of the dry powder discharging screw 908a and the wet powder discharging screw 908b are respectively connected with an inlet of the vital gluten buffer bin 913, and are used for feeding the dry vital gluten and the wet vital gluten into the vital gluten buffer bin 913 in proportion. The spiral outlet of the discharge at the bottom of the gluten buffer bin 913 is connected with the inlet of the crusher 915 through the iron remover 914, so that iron impurities such as iron blocks, bolts and the like in the production process are prevented from entering the crusher 915 to damage equipment.

The outlet of the pulverizer 915 is connected with the inlet of a wheat gluten dust remover 916, and the top air outlet of the wheat gluten dust remover 916 is communicated with the atmosphere through an exhaust fan; the bottom outlet of the vital gluten dust collector 916 is connected with the inlet of a finished product inspection sieve 917, the undersize outlet of the finished product inspection sieve 917 is connected with the inlet of a vital gluten finished product conveyor 920 through an intermediate metering scale 919, the outlet of the vital gluten finished product conveyor 920 is connected with the middle section of a vital gluten finished product air conveying pipe 923 through a vital gluten air-closing discharger 921, and the air inlet of the vital gluten finished product air conveying pipe 923 is connected with the air outlet of a Roots blower II 922.

An air outlet 907g of the double-bin dust remover is connected with an inlet of an exhaust fan 911, and an outlet of the exhaust fan 911 is connected with the hot side of the gas preheater 902 through a hot tail gas pipe 912; the hot side of the gas preheater 902 is tail gas and the cold side is fresh air.

The opening degree of the temperature control regulating valve TC is controlled by the temperature of the tail gas of the double-bin dust remover 907, and when the temperature of the tail gas exhausted by the double-bin dust remover 907 is lower, the opening degree of the temperature control regulating valve TC is increased, and the supply amount of the generated steam is increased; when the temperature of the exhaust gas discharged by the double-bin dust remover 907 is higher, the opening of the temperature control regulating valve TC is reduced, and the supply of the raw steam is reduced.

The raw steam pipe G2 is also connected with an air outlet of the fin heat exchanger 903 through a humidity control regulating valve HC, when the tail gas humidity of the double-bin dust remover 907 is low, the opening degree of the humidity control regulating valve HC is increased, and proper saturated steam is added; when the humidity of the tail gas of the double-bin dust remover 907 is higher, the opening of the humidity control regulating valve HC is reduced; and a stable humidity range is maintained, so that the stable operation of the system is ensured, and the dust explosion risk is reduced.

As shown in fig. 15 to 17, the outlet of the drying system feeding pipe 812 is connected to the block-shaped gluten inlet 905a1 of the fish mouth feeder 905a, and the thin gluten outlet 905a2 of the fish mouth feeder 905a is connected to the feeding port of the lifter 905. After entering the fish mouth feeder 905a, the blocky or doughy gluten enters a channel with gradually narrowed thickness and gradually widened width, is gradually extruded into a sheet shape, and is discharged from a sheet gluten outlet 905a2 and enters a feeding port of the lifter 905. On one hand, the flaky gluten increases the specific surface area, has large contact area with hot air and is easier to dry; on the other hand, if large gluten blocks enter the system, the lifter beater requires more energy to break the gluten; the gluten is extruded in a flat shape, which reduces the running load of the riser 905.

The sheet gluten outlet 905a2 can also intercept welding slag and scrap iron in the pipeline, so as to prevent the scrap iron and the like from entering the lifter 905 to cause the contact with a lifter beater to generate spark explosion; when the slag is accumulated to a certain amount, the fish-mouth feeder 905a is removed for cleaning.

Gluten from the feeding pipe 812 of the drying system enters the fish mouth feeder 905a of the lifter 905, and the gluten is pressed into flat thin gluten slices by the fish mouth feeder 905a to enter the lifter 905, and is mixed and crushed with the dry gluten in the lifter 905. After the gluten is mixed with the hot air, the gluten is flash evaporated while moving along the outlet pipeline of the raiser 905, part of water in the gluten is removed, and the gluten enters from the dry and wet gluten inlet of the volute separator 906.

After impurities in fresh air are filtered by an air filter 901, the fresh air enters a gas preheater 902 to be preheated by tail gas, and the initial temperature is increased; then enters the finned heat exchanger 903, the air is preheated by the waste heat of the steam condensate water, then the steam is heated into high-temperature hot air, and the high-temperature hot air is sent into a hot air inlet of the volute separator 906 and mixed with the wheat gluten entering from the dry and wet wheat gluten inlet.

The dry gluten is discharged from the dry gluten outlet of the volute separator 906 into a two-bin duster 907 for separation. The wet wheat gluten is discharged from a wet wheat gluten outlet, mixed with the dry wheat gluten fed by the dry powder rotary valve 910, and then enters the air inlet of the lifter 905 along with hot air, and is mixed and crushed with the flat thin gluten fed by the fish mouth feeder 905a.

The dried wheat gluten enters a wet flour dust removing chamber 907c of a double-bin dust remover 907 and is discharged, and the wet wheat gluten and the wet flour with high specific gravity are directly settled in a wet flour settling chamber 907 e; the dry wheat gluten with light specific gravity enters the dry powder dust chamber 907b and is adsorbed on the outer wall of the cloth bag, and compressed air is blown into the cloth bag at regular time to enable the dry powder to fall into the dry powder settling chamber 907d below.

The tail gas filtered by each cloth bag is sucked by an exhaust fan 911 and discharged from an air outlet 907g of the double-bin dust remover, and the tail gas with higher temperature can be used as a preheating heat source of fresh air and enters the hot side of the gas preheater 902 through a hot tail gas pipe 912 to preheat the fresh air and then is discharged.

The dry powder discharge screw 908a and the wet powder discharge screw 908b are respectively provided with two outlets, a part of dry powder and wet powder enter the inlet of the dry and wet powder return screw 909 together, and are sent into the dry powder rotary valve 910 by the dry and wet powder return screw 909 to enter the drying system again. The other part of the dry powder and the wet powder enter the vital gluten buffer bin 913 together, and the water content of the finished vital gluten can be accurately controlled by adjusting the proportion of the dry powder to the wet powder.

Detecting the moisture of the finished wheat gluten, and if the moisture of the finished wheat gluten is low, reducing the return amount of the wet flour and increasing the discharge amount of the wet flour; the dry powder feed back quantity is increased, and the dry powder discharge quantity is reduced, so that the moisture content of the finished product can be increased.

If the moisture of the finished wheat gluten is higher, the return amount of the wet flour is increased, and the discharge amount of the wet flour is reduced; the feed back quantity of the dry powder is reduced, and the discharge quantity of the dry powder is increased, so that the moisture content of the finished product can be reduced.

The discharging screw of the gluten buffer bin 913 feeds the gluten into the iron remover 914, removes iron, and then feeds the gluten into the pulverizer 915 to pulverize the gluten into a desired particle size. Usually, an ultrafine pulverizer is used, and the pass rate of the pulverized gluten with the fineness of 200 μm reaches 99.5%.

The vital gluten buffer 913 has a weighing sensor, the discharge spiral frequency conversion of which is controlled, and the frequency of the motor is interlocked with the weighing sensor to determine the crushing amount fed into the crusher 915.

Under the suction action of the fan at the outlet of the wheat gluten dust remover, crushed wheat gluten enters the wheat gluten dust remover 916 along with a cold air conveying wind net, and tail gas is discharged out of a room through the fan. The gluten discharged by the gluten dust remover 916 enters a finished product inspection sieve 917 for sieving, and the sieve outlet of the finished product inspection sieve 917 is connected with the inlet of the gluten buffer bin 913 through a gluten return screw 918. The vital gluten whose oversize does not reach the pulverization fineness is returned to the vital gluten buffer bin 913 by the vital gluten return screw 918, and then pulverized by the pulverizer 915.

The undersize product wheat gluten is used for measuring the discharge capacity through the intermediate weighing scale 919, and the wheat gluten discharged from the intermediate weighing scale 919 enters the wheat gluten finished product conveyor 920 for conveying and discharging and enters a positive pressure conveying system.

And a second Roots blower 922 provides air supply power, and the finished wheat gluten enters a wheat gluten finished product air conveying pipe 923 to remove wheat gluten and prepare flour and a packaging section from the wheat gluten air-closing discharging device 921. The yield of the finished wheat gluten can reach 13-14%, and the market price is about 12000 yuan/ton.

While the foregoing is directed to the preferred embodiment of the present invention, other and further embodiments of the invention may be devised without departing from the basic scope thereof, and the scope thereof is determined by the claims that follow. In addition to the embodiments described above, other embodiments of the invention are possible without departing from the spirit and scope of the invention. The invention also comprises various changes and improvements, and all technical solutions formed by equivalent substitutions or equivalent transformations fall within the protection scope of the claims of the invention. The scope of the invention is defined by the appended claims and equivalents thereof. Technical features of the present invention which are not described may be implemented by or using the prior art, and will not be described herein.

Claims

1. A wheat starch production system taking posterior wheat flour as a raw material comprises a storage flour mixing working section, a dough kneading working section, a horizontal spiral separation working section, a starch refining dehydration working section A and a starch crushing drying working section A, wherein the storage flour mixing working section comprises a flour feeding pipe and is characterized in that: the outlet of the flour feeding pipe is connected with the inlet of a double-way valve, two outlets of the double-way valve are respectively connected with the inlet of a flour bin, the outlets of bin bottom dischargers of two flour bins are respectively connected with the inlet of a flour bin discharging screw, the outlet of the flour bin discharging screw is connected with the inlet of a low scraper, the outlet of the low scraper is connected with the lower end inlet of a lifter, the upper end outlet of the lifter is connected with the inlet of a high scraper, each outlet of the high scraper is respectively connected with the inlet of a powder mixing bin through a mixing valve, the outlet of the bin bottom discharger of each powder mixing bin is respectively connected with the inlet of a powder mixing bin discharging screw, the outlet of each Roots powder mixing bin discharging screw is respectively connected with the inlet of a powder mixing machine, the bottom of the powder mixing machine is provided with a buffering bin of the mixing machine, the outlet of the bottom of the mixing machine buffering bin is connected with the inlet of the mixing machine discharging screw, the outlet of the mixing material discharging screw is connected with the inlet of an air conveying buffering bin, the bottom of the air conveying buffering bin is connected with the inlet of a bypass air seal air supply pipeline, the outlet of the flour feeding pipeline is connected with the air outlet of a fan, and the air supply pipeline.

2. The wheat starch production system using wheat middling as a raw material according to claim 1, characterized in that: the dough kneading section comprises a dough kneading buffer bin and a dough kneading machine, the outlet of a flour air conveying pipeline is connected with the feeding hole of the dough kneading buffer bin, the outlet of a bin bottom discharger of the dough kneading buffer bin is connected with the inlet of a dough kneading discharge screw, the outlet of the dough kneading discharge screw is connected with the inlet of a permanent magnet cylinder, the outlet of the permanent magnet cylinder is connected with the feeding hole of the dough kneading machine, and the discharge hole of the dough kneading machine is connected with the inlet of a curing tank;

the technical process water pipe is connected with a water inlet of the dough mixer through a dough mixing flow meter and a dough mixing water regulating valve, and the opening degree of the dough mixing water regulating valve is controlled by the rotating speed of the dough mixing discharge screw and a flow signal of the dough mixing flow meter;

the dough kneading section is also provided with a first viscosity-reducing enzyme tank, an outlet of the first viscosity-reducing enzyme tank is connected with an inlet of a first metering pump, and an outlet pipeline of the first metering pump is connected with a feed inlet of the dough kneading machine through a first viscosity-reducing enzyme flowmeter; the flow of the first metering pump is controlled by the rotating speed of the dough kneading and discharging screw and the flow monitored by the first viscosity-reducing enzyme flowmeter.

3. The wheat starch production system using wheat middling as a raw material according to claim 2, characterized in that: the bottom of curing jar is equipped with curing jar screw pump, the export of curing jar screw pump links to each other with the entry of isotropic symmetry, the export of isotropic symmetry passes through the face thick liquid pipe and links to each other with the separation workshop section.

4. The wheat starch production system using wheat middling as a raw material according to claim 3, characterized in that: the outlet of the surface slurry pipe is connected with the inlet of a three-phase horizontal screw centrifuge, the heavy phase outlet of the three-phase horizontal screw centrifuge is connected with the inlet of a coarse A starch milk buffer tank, the outlet of the coarse A starch milk buffer tank is connected with the inlet of a desanding cyclone through a coarse A starch milk delivery pump, the top flow outlet of the desanding cyclone is connected with the inlet of a fiber screen, the bottom flow of the desanding cyclone is connected with the inlet of a fine sand cyclone, and the top flow of the fine sand cyclone is connected with the inlet of the coarse A starch milk buffer tank; the fiber outlet of the fiber sieve is connected with the inlet of the pentosan buffer tank, and the A starch milk outlet of the fiber sieve is connected with the inlet of the fiber-removed A starch milk buffer tank.

5. The wheat starch production system using wheat middling as a raw material according to claim 4, wherein: the light phase outlet of the three-phase horizontal decanter centrifuge is connected with the inlet of the pentosan buffer tank, the middle phase outlet of the three-phase horizontal decanter centrifuge is connected with the inlet of the post-curing tank, the bottom of the post-curing tank is connected with the inlet of the curing material shearing device through a screw pump of the post-curing tank, and the outlet of the curing material shearing device is connected with a gluten separation washing section.

6. The wheat starch production system using wheat middling as a raw material according to claim 4, wherein: an outlet of the defibering A starch milk buffer tank is connected with an inlet of a two-phase horizontal decanter centrifuge through a defibering buffer tank discharging pump, a heavy phase outlet of the two-phase horizontal decanter centrifuge is connected with an inlet of a refined A starch milk buffer tank, an outlet of the refined A starch milk buffer tank is connected with an inlet of a high-level tank through a refined buffer tank output pump, an overflow port of the high-level tank is connected with a reflux port of the refined A starch milk buffer tank, a bottom outlet of the high-level tank is connected with an inlet of a scraper centrifuge, a liquid phase outlet of the scraper centrifuge is connected with an inlet of a horizontal decanter clear liquid buffer tank, and a dry matter outlet of the scraper centrifuge is provided with a belt conveyor;

7. The wheat starch production system using wheat middling as a raw material according to claim 6, wherein: the utility model discloses a starch drying machine, including band conveyer's export and starch mixer, starch mixer's export is equipped with mixer ejection of compact spiral, the export elephant trunk that mixes mixer ejection of compact spiral links to each other with the entry of lift fan, the entry of lift fan still links to each other with air heater's air-out pipeline one, the exit linkage of lift fan has the air current drying tuber pipe, air heater's air-out pipeline two links to each other with the lower part of air current drying tuber pipe, the upper portion export of air current drying tuber pipe links to each other with cyclone's entry, and cyclone's bottom export links to each other through the entry of airlock and dry starch screw conveyer.

8. The wheat starch production system using wheat middling as a raw material according to claim 7, wherein: the vice export of dry starch screw conveyer through dry starch back flow with the entry that the starch mixes the machine links to each other, dry starch screw conveyer's main export links to each other with the entry of deironing air separator, and the export pipeline of deironing air separator links to each other with high pressure positive blower's entry, and high pressure positive blower's export pipeline links to each other with the entry of starch dust remover, and the bottom export of starch dust remover links to each other through the entry of rotatory distributor with each A starch inspection sieve, and the fine powder export of each A starch inspection sieve links to each other with finished product starch elephant trunk respectively, and the coarse powder export of each A starch inspection sieve links to each other with the entry of coarse powder feed back spiral respectively, the export of coarse powder feed back spiral with the entry of dry starch back flow links to each other.

9. The wheat starch production system using wheat middling as a raw material according to claim 7, wherein: the top outlet of the cyclone separator is connected with the air inlet of the tail gas washing tower through an induced draft fan, the bottom water outlet of the tail gas washing tower is connected with the inlet of a washing circulating pump, the outlet of the washing circulating pump is connected with the upper water spraying pipe of the tail gas washing tower through a washing circulating pipe, and the middle part of the washing circulating pipe is connected with the inlet of the pentosan buffer tank through a washing discharge valve.

10. The wheat starch production system using wheat middling as a raw material according to claim 7, wherein: an expanding and settling section is arranged along the airflow drying air pipe, and an explosion-proof door is arranged at the top of the airflow drying air pipe.

11. The wheat starch production system using wheat middling as a raw material according to claim 8, wherein: the rotary distributor comprises a base, a distributor lower conical cylinder with a large upper part and a small lower part is fixed on the base, a distributor upper conical cylinder with a large upper part and a small lower part is fixed on the distributor lower conical cylinder, a plurality of starch discharge ports are uniformly arranged on the circumferential wall of the distributor lower conical cylinder, and starch discharge short sections are respectively connected below the starch discharge ports;

a starch inlet short pipe is arranged in the center of the top of the upper conical cylinder of the distributor, a rotatable vertical guide pipe is sleeved on the periphery of the starch inlet short pipe, the lower end of the vertical guide pipe is connected with an inclined guide pipe bent towards one side, and the lower port of the inclined guide pipe is butted with each starch discharge port;

the axis of a cone is equipped with the pivot under the distributor, the upper end of pivot through the revolving rack with oblique honeycomb duct is connected, the lower extreme of pivot is worn out and is linked to each other with the output of batching speed reducer from the diapire center of a cone under the distributor, the input of batching speed reducer is by batching motor drive.

12. The wheat starch production system using wheat middling as a raw material according to claim 9, characterized in that: the tail gas washing tower is characterized in that a water accumulation conical disc is arranged at the lower part of the tower body of the tail gas washing tower, a washing air inlet is arranged above the water accumulation conical disc, a washing circulating water outlet which extends downwards to the outside of the tower body is arranged in the water accumulation conical disc, a water spraying pipe is arranged at the upper part of the tower body, the outer end of the water spraying pipe extends out of the tower body to form a washing circulating water inlet, the inner end of the water spraying pipe faces downwards along the axis of the tower body and is provided with a water spraying horn mouth, a first layer of sealing disc which is high in the center and low in the periphery is arranged below the water spraying horn mouth, a first layer of disc which is wide at the upper part and narrow at the lower part is arranged below the first layer of sealing disc, the upper end of the disc is welded on the inner wall of the tower body, and the diameter of the lower end opening of the disc is smaller than the outer diameter of the sealing disc; the lower part of the first layer of disc is provided with a second layer of disc, the lower part of the second layer of disc is provided with a second layer of disc, and the rest is done by analogy, and the bottom layer of disc is positioned above the washing air inlet.

13. The wheat starch production system using wheat middling as a raw material according to claim 12, wherein: the top of the tower body of the tail gas washing tower is provided with a hood, the hood comprises a hood upper conical barrel with a narrow upper part and a wide lower part, the lower end of the hood upper conical barrel covers the upper port of the hood lower conical barrel and exceeds the hood lower conical barrel, the hood lower conical barrel is of a structure with a wide upper part and a narrow lower part, the lower port of the hood lower conical barrel is sleeved on the periphery of the hood short barrel, and an annular rainwater drainage opening is formed between the outer wall of the hood short barrel and the inner wall of the lower port of the hood lower conical barrel;

14. The wheat starch production system using wheat middling as a raw material according to claim 4, wherein: the outlet of the pentosan buffer tank is connected with the inlet of a pentosan feed pump, the outlet of the pentosan feed pump is connected with the cold side inlet of the plate preheater, the cold side outlet of the plate preheater is connected with a pentosan feed pipe, the pentosan feed pipe and the viscidity reducing enzyme adding pipe are respectively connected with the inlet of a static mixer, the outlet of the static mixer is connected with the inlet of an enzymolysis reaction tank, a stirring device is arranged in the inner cavity of the enzymolysis reaction tank, and the outlet of the enzymolysis reaction tank is connected with the inlet of an evaporation feed tank;

15. The wheat starch production system using wheat middling as a raw material according to claim 14, wherein: a pentosan feed flowmeter and a pentosan feed regulating valve are installed at the outlet of the pentosan feed pump, the outlet of the pentosan feed regulating valve is connected with the cold side inlet of the plate heat exchanger, and the opening degree of the pentosan feed regulating valve is controlled by a flow signal of the pentosan feed flowmeter;

the second viscosity-reducing enzyme adding pipe is connected with an outlet of the second metering pump, an inlet pipeline of the second metering pump is inserted into the bottom of the second viscosity-reducing enzyme tank, a second viscosity-reducing enzyme flow meter is installed on the second viscosity-reducing enzyme adding pipe, and the flow of the second metering pump is controlled by the pentosan feed flow meter and the flow monitored by the second viscosity-reducing enzyme flow meter.

16. The wheat starch production system using wheat middling as a raw material according to claim 14, wherein: the secondary steam outlet of the condensed water tank is also connected with the inlet of the steam compressor;

the non-condensable gas discharge port of the falling film evaporator is connected with the hot side inlet of the tube nest preheater, the hot side outlet of the tube nest preheater is connected with the hot side inlet of the condenser through a non-condensable gas conveying pipe, the hot side outlet of the condenser is connected with the vacuum pump, and the shell side water outlet of the condenser is connected with the inlet of the condensed water tank.

17. The wheat starch production system using wheat middling as a raw material according to claim 14, wherein: a feeding liquid level regulating valve is installed on the evaporation feeding pipe, and the opening degree of the feeding liquid level regulating valve is controlled by the liquid level of the evaporation feeding tank;

the outlet of the condensed water pump is also connected with the outlet of the steam compressor through a condensed water regulating valve, and the opening degree of the condensed water regulating valve is controlled by the steam temperature at the outlet of the steam compressor;

18. The wheat starch production system using wheat middling as a raw material according to claim 4, wherein: the export of curing material conveyer pipe links to each other with the entry of one-level gluten sieve, the export under the sieve of one-level gluten sieve links to each other with B starch milk conveyer pipe, the export on the sieve of one-level gluten sieve links to each other with the entry of one-level gluten surge bin, the export of one-level gluten surge bin is equipped with one-level gluten screw pump, the export of one-level gluten screw pump links to each other with the entry of one-level static shears, the export under the sieve of one-level static shears links to each other with the entry of second grade gluten sieve, the export of second grade slurry surge bin is equipped with second grade slurry screw pump, the export of second grade slurry screw pump pass through second grade slurry back flow with curing material conveyer pipe links to each other.

19. The wheat starch production system using wheat middling as a raw material according to claim 18, wherein: the outlet on the sieve of second grade gluten sieve links to each other with the entry of second grade gluten surge bin, and the outlet of second grade gluten surge bin is equipped with second grade gluten screw pump, and the export of second grade gluten screw pump links to each other with the entry of second grade static shears, and the export of second grade static shears links to each other with the entry of tertiary gluten sieve, and the export is passed through tertiary slurry return pipe and under the sieve of tertiary gluten sieve with the entry of one-level gluten surge bin links to each other; an outlet on the sieve of the third gluten screen is connected with an inlet of a third gluten buffer bin, and inlets of the second gluten buffer bin and the third gluten buffer bin are respectively connected with an outlet valve of the process water pipe; the bottom in tertiary gluten surge bin is equipped with tertiary gluten screw pump, and the export of tertiary gluten screw pump links to each other with the entry of tertiary static shears.

20. The wheat starch production system using wheat middling as a raw material according to claim 19, wherein: the outlet of the three-stage static shearing device is connected with the inlet of the rotary screen, the outlet on the screen of the rotary screen is connected with the inlet of the gluten dewatering machine, the dry matter outlet of the gluten dewatering machine is connected with the inlet of the wringing machine, the filtrate outlets of the rotary screen, the gluten dewatering machine and the wringing machine are respectively connected with the filtrate tank, the bottom of the filtrate tank is provided with a filtrate screw pump, and the outlet of the filtrate screw pump is connected with the inlet of the second-stage gluten buffer bin through a gluten dewatering filtrate return pipe;

21. The wheat starch production system using wheat middling as a raw material according to claim 20, wherein: the outlet of a feeding pipe of the drying system is connected with a feeding port of the lifter, the outlet of the lifter is connected with a dry and wet wheat gluten inlet of the volute separator through a circulating pipeline, a hot air inlet of the volute separator is connected with an air outlet of the fin heat exchanger, a wet material outlet of the volute separator is connected with an air inlet of the lifter, and a dry wheat gluten outlet of the volute separator is connected with an air inlet of the double-bin dust remover;

22. The wheat starch production system using wheat middling as a raw material according to claim 21, wherein: an outlet on the screen of the finished product inspection screen is connected with an inlet of the vital gluten buffer bin through a vital gluten return screw;

23. The wheat starch production system using wheat middling as a raw material according to claim 21, wherein: the export of drying system feed pipe links to each other with the cubic gluten entry of fish mouth feeder, the thin slice gluten export of fish mouth feeder with the feed inlet of raiser links to each other.