CN115433677B - Starch hydrolysis system and hydrolysis method thereof - Google Patents
Starch hydrolysis system and hydrolysis method thereof Download PDFInfo
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- CN115433677B CN115433677B CN202211229500.3A CN202211229500A CN115433677B CN 115433677 B CN115433677 B CN 115433677B CN 202211229500 A CN202211229500 A CN 202211229500A CN 115433677 B CN115433677 B CN 115433677B
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- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
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- C12M41/24—Heat exchange systems, e.g. heat jackets or outer envelopes inside the vessel
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Abstract
The invention discloses a starch hydrolysis system which comprises an ejector, a heating tank, a hydrolysis tank and a flash evaporation device, wherein a vapor-liquid mixing cavity and a liquefaction coil are arranged in the heating tank, the flash evaporation device is arranged in the hydrolysis tank, a hydrolysis pipeline which surrounds the flash evaporation device upwards in a spiral manner is arranged in the hydrolysis tank, the ejector is communicated with the vapor-liquid mixing cavity, the vapor-liquid mixing cavity is communicated with a feeding pipeline filled with starch slurry, the liquefaction coil is communicated with the flash evaporation device through a pipeline, one end of the flash evaporation device is communicated with the hydrolysis pipeline through a feeding pump, and the other end of the flash evaporation device is communicated with the ejector. The starch hydrolysis system provided by the invention has the advantages that the equipment is simple, the occupied area is small, and the hydrolysis pipeline is spirally arranged around the flash evaporation device from bottom to top, so that the first-in first-out of hydrolysis liquid is realized, and the uniformity of hydrolysis is ensured.
Description
Technical Field
The invention belongs to the technical field of starch sugar production, and particularly relates to a starch hydrolysis system and a starch hydrolysis method.
Background
In the existing production process for preparing glucose by hydrolyzing starch by a double enzyme method, the starch is liquefied into paste or oligosaccharide by using alpha-amylase, and the process is called hydrolysis. The hydrolysis process includes mixing commercial starch with water to form starch slurry of certain concentration, adding hydrochloric acid or caustic soda to regulate pH value of the starch slurry, adding alpha-amylase to mix homogeneously, pumping to steam jetting heater, raising the temperature of starch milk instantaneously and maintaining for certain period, flash evaporation in flash tank, cooling, and centrifugal pumping to hydrolysis in laminar flow tank. In addition, in order to meet the time requirement of hydrolysis, a plurality of hydrolysis laminar flow tanks are usually installed, each laminar flow tank is connected in series, liquid flows in from the bottom of the first hydrolysis laminar flow tank and flows out from the top of the last hydrolysis laminar flow tank, and the hydrolysis process is completed.
And cooling the hydrolyzed liquefied liquid, regulating the pH value, adding saccharifying enzyme according to a certain proportion, and then sending the liquefied liquid into a saccharifying tank to complete the conversion from dextrin or oligosaccharide to glucose.
In the conventional hydrolysis method, there is a major problem in that, firstly, the number of hydrolysis laminar flow tanks required is large because a certain hydrolysis time is required, and the first-in first-out of feed liquid in each laminar flow tank cannot be ensured, so that the hydrolysis time is inconsistent, and the hydrolysis is uneven. Secondly, flash steam in the flash tank is directly discharged, so that waste of heat energy and equipment investment cost for flash steam treatment are caused. Thirdly, the whole hydrolysis process needs a large number of equipment and occupies a large area. Fourth, each equipment is connected through the pipeline, causes the feed liquid loss big, and the resistance in the feed liquid transmission process is big, and the power cost that needs increases, increases equipment and pipeline abluent time and cost of labor after the hydrolysis simultaneously.
In view of the above-described problems, there have been disclosed patents which improve some of the problems. Patent CN204369870U discloses a laminar flow tank for starch sugar liquefaction, the laminar flow tank be equipped with conical upper seal and round head column lower seal, the body inner wall of laminar flow tank be equipped with multichannel parallel helical groove, the export at helical groove both ends be the slope shape, laminar flow tank lower part be equipped with liquefied liquid inlet pipe, liquefied liquid inlet pipe entering direction and laminar flow tank be connected along tangential direction and helical groove's spiral direction unanimous, round head column lower seal be concave arc connector with laminar flow tank junction, arc connector on be equipped with the discharge opening. The liquid inlet enters the spiral groove tangentially, spiral flow is generated inside, and the liquid in the whole laminar flow tank is further induced to generate rotary flow. Although the spiral groove is favorable for forming the rotary flow of the liquid in the tank, the liquid in the tank can still have mixed flow condition, and the liquid entering the tank firstly can not be ensured to be discharged firstly.
Patent CN210314241U discloses a starch sugar liquefaction laminar flow jar, including the jar body, the bottom fixedly connected with low head of jar body, the outside fixedly connected with fixed plate of low head, the top fixedly connected with upper head of the jar body, the inside fixedly connected with filter screen of the jar body, the top fixedly mounted of filter screen has electric telescopic handle, the inside of the jar body just is located electric telescopic handle's top sliding connection has first piston. Through setting up the piston of simultaneous movement for get into the inside feed liquid of laminar flow jar and liquefy earlier, after the liquefaction is accomplished, after the feed liquid accumulation certain volume, respond to the liquid level through the liquid level probe, then discharge the inside feed liquid of laminar flow jar, prevent simultaneously that the feed liquid from continuously getting into, adopt helical blade to guarantee the feed liquid first in first out after the liquefaction in the liquefaction, back feeding back goes out, and front and back feed liquid does not have the mixture, makes the effect of liquefaction better. This patent uses a batch mode to ensure liquid first-in first-out in a laminar flow tank, but this mode produces discontinuities and the process is less efficient for applications requiring large amounts of starch hydrolysis. If a large amount of hydrolysis is satisfied by increasing the volume of the laminar flow tank, the resistance to upward movement of the first piston will greatly increase due to the increase in the tank, and the risk of liquid leakage will easily occur between the first piston and the inner wall of the laminar flow tank.
Patent CN203487158U discloses a starch sugar liquefaction laminar flow jar, and it includes the jar body, is connected with upper cover and low head respectively at the upper end and the lower extreme of jar body, and the shape of upper cover is the cone, and the shape of low head is the inverted cone, and the top of upper cover is provided with the discharge gate, and the bottom of low head is provided with the feed inlet, is provided with spiral loading attachment in the low head, spiral loading attachment include helical blade, helical blade is the heliciform and extends to the bottom from the top of low head, helical blade's spiral radius reduces gradually from the top of low head to the bottom of low head, helical blade welds the inner wall surface at the low head. The spiral blade is arranged in the lower sealing head, so that the feed liquid in the laminar flow tank can not gather at the bottom of the tank body, and the rising of the feed liquid is facilitated. However, since the spiral structure is not arranged at the upper part of the laminar flow tank, the possibility of blanking of the feed liquid rising to the upper region of the tank body still exists, and thus the first-in first-out of the feed liquid in the laminar flow tank cannot be completely ensured.
In the known patent publication, the problem of the hydrolysis of starch is mostly that the liquid in the hydrolysis laminar flow tank cannot ensure the first-in first-out, so that the uneven hydrolysis is improved and solved, but the problems of the prior starch hydrolysis are also overcome. And the solution to other problems of the existing starch hydrolysis method is rarely involved.
Disclosure of Invention
The invention aims to provide a starch hydrolysis system and a hydrolysis method thereof, which are used for solving the problem that the waste of heat and the uneven hydrolysis caused by first-in first-out cannot be ensured by liquid in a hydrolysis laminar flow tank in the existing hydrolysis system and method.
The aim of the invention is achieved by the following technical scheme:
A starch hydrolyzing system comprising an eductor, a heating tank, a hydrolyzing tank, and a flash device;
The heating tank is internally provided with a vapor-liquid mixing cavity and a liquefying coil pipe which are communicated, the flash evaporation device is arranged in the hydrolysis tank, and the periphery of the flash evaporation device is spirally provided with a hydrolysis pipeline from bottom to top;
The ejector is communicated with the vapor-liquid mixing cavity, the vapor-liquid mixing cavity is communicated with a feeding pipeline filled with starch slurry, and the liquefying coil is communicated with the flash evaporation device through a pipeline;
one end of the flash evaporation device is communicated with the hydrolysis pipeline through a feeding pump, and the other end of the flash evaporation device is communicated with the ejector.
Further, a bottom plate is arranged between the gas-liquid mixing cavity and the liquefaction coil, the gas-liquid mixing cavity is positioned above the liquefaction coil, a liquid outlet is formed in the bottom plate, and a baffle is arranged above the liquid outlet;
The liquid outlet is communicated with the liquefaction coil;
preferably, the liquefaction coil is provided with three sections, and a valve capable of controlling opening and closing is arranged on a pipeline communicated between each section and the flash evaporation device;
preferably, the valve capable of being controlled to be opened and closed is a three-way valve.
Further, a rotary spray head is arranged at the outlet end of the feeding pipeline in the gas-liquid mixing cavity;
Preferably, the outer wall of the liquefaction coil is provided with a pipeline heat insulation layer, and the bottom of the heating tank is provided with a support column for supporting the tank body;
Preferably, a cleaning pipeline is arranged on the pipeline of the feeding pipeline positioned outside the heating tank, and a sixth control valve is arranged on the cleaning pipeline.
Further, the flash evaporation device is provided with a liquid inlet, and a pressure reducing valve is arranged on a pipeline connected with the liquid inlet;
The height of the lowest part of the liquefying coil is higher than the height of the liquid inlet;
preferably, the liquid inlet is arranged at a position of 1/2-3/4 of the whole height of the flash evaporation device;
more preferably, the liquid inlet is arranged at a position of 2/3 of the total height of the flash evaporation device.
Further, the flash evaporation device penetrates through the hydrolysis tank body, and a pipeline heat insulation layer is arranged on the outer wall of the hydrolysis pipeline;
The device comprises a flash evaporation device, a hydrolysis pipeline, a liquid discharge pipe, a liquid discharge port, a liquid pump and a second control valve, wherein the check valve is arranged on the pipeline connected with the flash evaporation device and the ejector;
Preferably, the included angle between the spiral upward direction of the hydrolysis pipeline around the flash evaporation device and the horizontal line direction is 5 degrees;
preferably, the bottom of the flash evaporation device is of a conical structure, and the liquid outlet is arranged at the lowest part of the bottom of the flash evaporation device;
Preferably, an enzyme mixer for supplementing amylase is arranged on a pipeline connected with the hydrolysis pipeline by the feeding pump;
preferably, the feed pump is a centrifugal pump.
Further, a liquid outlet pipe is arranged outside the hydrolysis tank and is communicated with the hydrolysis pipeline;
the liquid outlet pipe is provided with a branch pipe for exhausting, and the branch pipe is provided with a fourth control valve.
Further, the sprayer is arranged above the hydrolysis tank through a first support column, and a third support column for supporting the hydrolysis tank is arranged at the bottom of the hydrolysis tank;
steam of the ejector enters a steam-liquid mixing cavity of the heating tank through an injection port, and the injection port is arranged below the rotary spray head;
preferably, the jet orifice is arranged in the middle of the vapor-liquid mixing cavity.
A starch hydrolysis method comprises the following specific steps of:
(a) The high-temperature steam in the ejector and the starch slurry in the feeding pipeline enter a vapor-liquid mixing cavity of the heating tank to heat the starch slurry, and the heated starch slurry enters a liquefying coil;
(b) Starch slurry in the liquefying coil pipe enters a flash evaporation device to form vapor phase and liquid phase, the liquid phase enters a hydrolysis tank in a hydrolysis tank for hydrolysis through a feeding pump d, and the liquid phase is discharged from a hydrolysis pipeline after the hydrolysis is completed;
(c) The high temperature vapor phase in the flash device enters the ejector and enters the heating tank together with the high temperature vapor in the ejector.
Further, the heated starch slurry in step (a) is incubated for a period of time as required to determine the specific section of the liquefaction coil to be used;
If the slurry discharged from the hydrolysis pipeline in the step (b) needs secondary hydrolysis, the hydrolyzed slurry enters a vapor-liquid mixing zone of the heating tank through a feeding pipeline, and the second heating, flash evaporation and hydrolysis processes are carried out.
Further, the specific step of starch hydrolysis further comprises a cleaning operation of the hydrolysis system:
(d) And opening a sixth control valve, and introducing cleaning liquid to clean the heating tank, the flash evaporation device and the hydrolysis pipeline, wherein the cleaning liquid is discharged through a branch pipeline of the liquid outlet pipe until the pipeline is cleaned. The beneficial effects of the invention are as follows:
The beneficial effects of the invention are as follows:
1. Compared with the existing hydrolysis system which needs a plurality of laminar flow tanks, the starch hydrolysis system provided by the invention reduces the investment of equipment, reduces the workload of operators and simultaneously reduces the problem of high misoperation probability.
2. According to the starch hydrolysis system provided by the invention, a hydrolysis pipeline is spirally upwards arranged around the flash evaporation device, so that on one hand, the internal space of the hydrolysis tank is fully utilized, the occupied area of equipment is reduced, and on the other hand, the feed liquid is first in first out in the hydrolysis process, and the uniform hydrolysis is ensured.
3. According to the starch hydrolysis system provided by the invention, steam generated in the flash evaporation device is fed into the ejector again, so that the steam is used for heating starch slurry in the heating tank, the heat loss is avoided, the heat is recycled, and the heat energy is saved.
4. According to the starch hydrolysis system provided by the invention, the pressure in the gas-liquid mixing cavity and the gravity of the liquid in the liquefaction coil are utilized to transfer, and the compact design among units reduces the power cost of the liquid in a pipeline due to the transmission resistance.
5. The starch hydrolysis system provided by the invention is also provided with the cleaning pipeline, so that the hydrolysis system can be sufficiently cleaned, the blockage of the pipeline is avoided, and the cleaning of the pipeline is ensured.
Drawings
FIG. 1 is a schematic diagram of the hydrolysis system of the present invention;
FIG. 2 is a schematic diagram of the positional relationship between a hydrolysis tank and a flash evaporation device in the hydrolysis tank of the present invention;
FIG. 3 is a schematic block diagram of a liquefaction coil of the present invention;
FIG. 4 is a schematic view of the pipe insulation layer structure of the outer wall of the hydrolysis pipe of the present invention;
FIG. 5 is a schematic view of the pipe insulation layer structure of the outer wall of the liquefaction coil of the present invention.
The device comprises the following components of 11, an ejector, 12, a heating tank, 13, a hydrolysis tank, 14, a flash evaporation device, 15, a gas-liquid mixing cavity, 16, a liquefaction coil, 17, a pressure reducing valve, 18, a hydrolysis pipeline, 19, a feed pump, 20, a feed pipe, 21, a fixed surface, 111, a steam inlet, 112, an injection port, 141, a check valve, 142, a liquid discharge port, 143, a first control valve, 144, a liquid inlet, 151, a baffle, 152, a liquid outlet, 161, a pipeline heat insulating layer, 162, a first three-way valve, 163, a second three-way valve, 164, a third three-way valve, 181, a liquid discharge pipe, 182, a second control valve, 183, a liquid outlet pipe, 184, a third control valve, 185, a fourth control valve, 201, a rotary nozzle, 202, a fifth control valve, 203, a cleaning pipeline, 204, a sixth control valve, 211, a first support column, 212, a second support column, 213 and a third support column.
Detailed Description
In order to fully understand the beneficial effects of lime milk sterilization in the technical scheme, the following examples are specifically and specifically described.
Example 1
The embodiment provides a starch hydrolysis system, as shown in fig. 1, the hydrolysis system includes an ejector 11, a heating tank 12, a hydrolysis tank 13 and a flash evaporation device 14, a vapor-liquid mixing cavity 15 and a liquefying coil 16 are arranged in the heating tank 12, the vapor-liquid mixing cavity 15 is communicated with the ejector 11, the vapor-liquid mixing cavity 15 is communicated with a feeding pipe 20 filled with starch slurry, the liquefying coil 16 is communicated with the flash evaporation device 14 through a pipeline, the flash evaporation device 14 is arranged in the hydrolysis tank 13, the flash evaporation device 14 is communicated with a hydrolysis pipeline 18 in the hydrolysis tank 13 through a pipeline, and the flash evaporation device 14 is communicated with the ejector 11 through a pipeline.
The ejector 11 is installed above the hydrolysis tank 13 through a first support column 211, one end of the ejector 11 is provided with a steam inlet 111, the other end of the ejector 11 is provided with an injection port 112, the injection port 112 is arranged in a steam-liquid mixing cavity 15 of the heating tank 12, and steam in the ejector 11 is used for injecting high-temperature steam into the steam-liquid mixing cavity 15 in the heating tank 12 to heat starch slurry entering the steam-liquid mixing cavity 15. The pipe of the ejector 11 communicating with the flash evaporation device 14 is provided with a check valve 141, and the check valve 141 is used for preventing the steam in the ejector 11 from entering the flash evaporation device, but the steam generated in the flash evaporation device 14 can enter the ejector 11 through the opening of the check valve 141.
The gas-liquid mixing cavity 15 in the tank body of the heating tank 12 and the liquefying coil 16 are separated by a bottom plate, a liquid outlet 152 is arranged on the bottom plate, the liquid outlet 152 is close to the inner wall of the heating tank 12, the liquid outlet 152 is communicated with the liquefying coil 16, a rotary spray nozzle 201 is arranged at the outlet end of the feeding pipe 20 in the gas-liquid mixing cavity 15, the liquid outlet 152 is preferably arranged in a direction away from the spray opening 112 and the rotary spray nozzle 201, a baffle 151 is arranged above the liquid outlet 152, and the baffle 151 is used for preventing starch slurry sprayed by the rotary spray nozzle 201 from falling into the liquid outlet 152 without being heated and mixed by high-temperature steam.
The rotary nozzle 201 sprays the starch slurry into the vapor-liquid mixing cavity 15 in a spray shape, which is favorable for fully mixing the high-temperature steam sprayed by the sprayer 11 with the starch slurry, and heating is more uniform. The rotary spray nozzle 201 is located above the injection port 112, and the rotary spray nozzle 201 is located in the area between the center line of the vapor-liquid mixing cavity 15 and the injection port 112, so that starch slurry is beneficial to being quickly mixed with high-temperature steam injected from the injection port 112 after being injected from the rotary spray nozzle 201.
The starch slurry heated and mixed by the high-temperature steam is discharged to the liquefaction coil 16 through the liquid outlet 152, and a pipeline heat insulation layer 161 is arranged on the outer wall of the liquefaction coil 16 for heat preservation. The total length of the liquefaction coil 16 is set according to the process time requirement of maintaining heat preservation, the liquefaction coil 16 is set into a plurality of sections, three-way valves are installed between each section and between pipelines connected with the flash evaporation device 14 in each section, and the liquefaction coils 16 in different sections are selected to be used according to different process time requirements by controlling the opening and closing of the three-way valves.
As shown in fig. 3, the liquefaction coil 16 in this embodiment is divided into three usage sections:
The liquefaction coil 16 is sequentially divided into a first section, a second section and a third section from top to bottom, each section is communicated with the liquid inlet 144 of the flash evaporation device 14 through a pipeline, a first three-way valve 162, a second three-way valve 163 and a third three-way valve 164 are respectively arranged on the connected pipelines, the first three-way valve 162, the second three-way valve 163 and the third three-way valve 164 execute opening and closing instructions according to a set program through a DCS control system to realize opening or closing of the valves, the first three-way valve 162 controls opening and closing of the first section, the second section and the pipeline leading to the liquid inlet 144 of the flash evaporation device 14, the second three-way valve 163 controls opening and closing of the second section, the third section and the pipeline leading to the liquid inlet 144 of the flash evaporation device 14, and the third three-way valve 164 controls opening and closing of the first section, the third section and the pipeline leading to the liquid inlet 144 of the flash evaporation device 14.
When the first section of the liquefaction coil 16 is in use, the first three-way valve 162 is opened to the liquid inlet 144 of the flash unit 14 and the other directional valve is closed to ensure that liquid in the first section of the liquefaction coil 16 is discharged directly into the flash unit 14 without entering the liquefaction coils 16 in the second and third sections.
When the first and second sections of the liquefaction coil 16 are used, the first three-way valve 162 is opened in the direction of the second section, while the second three-way valve 162 is opened to the liquid inlet 144 of the flash unit 14, and the other directional valves are closed, ensuring that the liquid in the first and second sections of the liquefaction coil 16 is discharged directly into the flash unit 14 without entering the liquefaction coil 16 in the third section.
When the whole liquefaction coil 16 is used, the first three-way valve 162 is opened to the direction of the second section, the second three-way valve 163 is opened to the direction of the third section, meanwhile, the channel of the third three-way valve 163 to the liquid inlet 144 of the flash evaporation device 14 is opened, the valves in other directions are closed, and the heated liquid is ensured to be discharged into the flash evaporation device 14 after passing through the liquefaction coil 16 completely.
The bottom of the heating tank 12 is provided with a third support column 213 for supporting the tank.
The lowest position of the liquefaction coil 16 is higher than the liquid inlet 144 of the flash evaporation device 14, and the flowing direction of the slurry flowing to the liquid inlet 144 at the lowest position of the liquefaction coil 16 forms an included angle of 5 degrees with the horizontal line. The height of the liquid inlet 144 in this embodiment is set in the middle of the flash evaporation device 14, so as to ensure that the liquid in the liquefaction coil 16 can enter the flash evaporation device 14 through the liquid inlet 144 by the pressure in the vapor-liquid mixing cavity 15 and the gravity of the liquid in the liquefaction coil 16.
The pipeline connecting the liquefaction coil 16 with the liquid inlet 144 of the flash evaporation device 14 is provided with a pressure reducing valve 17, the starch slurry enters the flash evaporation device 14 after being depressurized through the pressure reducing valve 17, and the high-temperature liquid transmitted to the flash evaporation device 14 through the liquefaction coil 16 has abrupt boiling point change due to the pressure reduction, so that the slurry rapidly forms a vapor phase and a liquid phase. The liquid flows to the bottom of the flash evaporation device 14, the vapor phase is upwards transferred in the flash evaporation device 14, the check valve 141 is opened, the vapor phase enters the ejector 11, and the vapor phase and the high-temperature vapor entering from the vapor inlet 111 of the ejector 11 enter the vapor-liquid mixing cavity 15 again to heat the starch slurry, so that the heat energy of the flash vapor is reused.
When high-temperature steam enters the ejector 11 from the steam inlet 111 of the ejector 11 at a high speed, the vapor phase in the flash evaporation device 14 enters the ejector 11, and at this time, negative pressure is formed in the region of the inlet of the vapor phase into the ejector 11, which is further advantageous for the vapor phase to enter the ejector 11.
The liquid phase in the flash evaporation device 14 flows to the bottom of the flash evaporation device 14, the bottom of the flash evaporation device 14 is in a conical structure, and the liquid outlet 142 of the flash evaporation device 14 is arranged at the lowest part of the bottom, so that the liquid can completely reach the liquid outlet 142. The liquid outlet 142 is connected with the hydrolysis pipeline 18 through a pipeline, a feed pump 19 and a liquid discharge pipe 181 are arranged on the connected pipeline, and a second control valve 182 is arranged on the liquid discharge pipe 181. The second control valve 182 is normally closed during normal starch hydrolysis processes, and the second control valve 182 is opened during equipment maintenance to drain residual liquid or cleaning liquid from the flash device 14.
As shown in fig. 2, the flash evaporation device 14 is arranged in the hydrolysis tank 13 in a penetrating manner, the hydrolysis pipe 18 is arranged in the hydrolysis tank 13 in a spiral upward manner around the flash evaporation device 14, and a pipe heat insulation layer 161 is arranged on the outer wall of the hydrolysis pipe 18 for maintaining the liquid temperature in the hydrolysis pipe 18.
The caliber of the hydrolysis pipe 18, the total length of the pipe and the flow rate of the slurry in the pipe are determined according to the requirements of specific technology, and the total length of the hydrolysis pipe 18 can be realized by controlling the diameter and the height of the hydrolysis tank 13 and the included angle between the central line and the horizontal central line of the hydrolysis pipe 18. Increasing the inner diameter of the spiral structure of the hydrolysis pipe 18, increasing the height of the hydrolysis tank 13, and reducing the included angle between the central line of the hydrolysis pipe 18 and the horizontal line can increase the distance that liquid flows through the hydrolysis pipe 18, thereby realizing the control of hydrolysis time.
In the case of a certain length of the hydrolysis conduit 18, this can be achieved by controlling the size of the aperture of the hydrolysis conduit 18 in order to meet a certain yield.
The diameter and height of the hydrolysis tank 13, the caliber of the hydrolysis pipe 18 and the distance between the upper and lower adjacent pipes need to be determined in advance before manufacturing according to the requirements of the process conditions. This can be achieved by controlling the flow rate of the liquid in the hydrolysis conduit 18 when it is still necessary to adjust the hydrolysis time during production use.
The hydrolysis pipe 18 can control the hydrolysis time of the slurry through different sections, and the hydrolysis time between the different sections and between the sections and the liquid outlet pipe 183 outside the hydrolysis tank 13 are realized by arranging valves capable of being controlled to open and close, such as three-way valves. When a different section of hydrolysis conduit is desired, the valves of the corresponding section are opened to allow slurry to flow out of the outlet conduit 183.
To increase the stability of the hydrolysis conduit 18, a support structure (not shown in the drawings) may be provided in sections, secured to the inner wall of the hydrolysis tank 13.
An enzyme adding mixer (not shown in the drawing) can be added on the pipeline between the feeding pump 19 and the hydrolysis pipeline 18 for supplementing amylase before hydrolysis. The caliber of the hydrolysis pipeline 18 is consistent with that of the outlet of the feed pump 19, and the liquid fed into the hydrolysis pipeline 18 by the feed pump 19 can continuously push the liquid in the hydrolysis pipeline 18 to flow upwards, so that the disturbance of the liquid when the small caliber is fed into the large caliber is avoided.
Example 2
The height of the liquid inlet 144 in this embodiment is set at 2/3 of the height of the flash evaporation device 14, the feed pump 19 is a centrifugal pump, and the hydrolysis pipe 18 is inclined upward by an angle of 5 ° from the horizontal direction, i.e. the center line of the liquid flow in the pipe. The arrangement and connection relation of other devices are the same as in embodiment 1.
Example 3
The embodiment provides a hydrolysis method, which specifically comprises the following steps:
(a) The high-temperature steam enters the ejector 11 from the steam inlet 111 of the ejector 11 at a high speed and is sprayed into the steam-liquid mixing cavity 15 of the heating tank 12 through the spray opening 112, and at the moment, the steam-liquid mixing cavity 15 is filled with the high-temperature steam, and the temperature is 105-108 ℃.
The starch slurry obtained through the previous process enters the vapor-liquid mixing cavity 15 of the heating tank 12 through the feeding pipe 20, the starch slurry is sprayed into the vapor-liquid mixing cavity 15 under the action of the rotary spray head 201, high-temperature steam is synchronously sprayed out of the spraying port 112 of the sprayer 11 while the starch slurry is sprayed out of the rotary spray head 201, the starch slurry and the high-temperature steam are fully mixed in the vapor-liquid mixing cavity 15, and the starch slurry is heated to 105-108 ℃ by the high-temperature steam.
The pressure is increased continuously along with the continuous spraying of the high-temperature steam in the steam-liquid mixing cavity 15, and the starch slurry heated at high temperature enters the liquefying coil 16 from the liquid outlet 152 on the bottom plate.
(B) The pipeline insulating layer 161 arranged on the outer wall of the liquefaction coil 16 maintains the temperature of the slurry in the liquefaction coil 16, and the high-temperature slurry in the liquefaction coil 16 is maintained in the liquefaction coil 16 for 6min, so that thorough gelatinization of starch is facilitated.
After the slurry in the liquefaction coil 16 was maintained for 6 minutes, it was depressurized through the depressurization valve 17 from the inlet 144 in the middle of the flash unit 14 into the flash unit 14.
The slurry after the pressure jump undergoes gas-liquid phase separation in the flash device 14.
The temperature of the liquid separated in the flash evaporation device 14 is 95-98 ℃, the liquid flows to the bottom of the flash evaporation device 14, and is discharged from a liquid outlet 142 arranged at the bottom of the flash evaporation device 14, and the liquid is pressurized by a feed pump 19 and then is conveyed into the hydrolysis pipeline 18.
The flow rate and pressure of the feed pump 19 are controlled, and the liquid slowly rises in the hydrolysis pipe 18 along a spiral rising pipeline, and a pipe heat insulation layer 161 is arranged on the outer wall of the hydrolysis pipe 18 and used for maintaining the temperature of the liquid in the pipe. The hydrolysis is continuously carried out for 120min under the condition of maintaining the temperature of 95-98 ℃ in the liquid rising process in the hydrolysis pipeline 18.
When the liquefied liquid rises to the top end of the hydrolysis pipe 18, the hydrolysis process is completed, and the liquid is discharged from the liquid outlet pipe 183 provided at the upper portion of the hydrolysis tank 13 to the downstream process, so that the hydrolysis process of starch is completed.
(C) The separated gas phase is discharged from the top outlet of the flash evaporation device 14 into the ejector 11, mixed with high-temperature steam entering from the steam inlet 111 of the ejector 11, and ejected from the ejection port 112, and the starch slurry is heated.
When secondary hydrolysis is required:
The hydrolyzed liquid discharged from the liquid outlet pipe 183 is continuously fed into the heating tank through the feeding pipe 20, the operation procedure shown in example 3 is repeated, and meanwhile, an enzyme mixer for supplementing amylase is additionally arranged on a pipe between the feeding pump 19 and the hydrolysis pipe 18, and finally, the liquid with a secondary water structure is discharged from the liquid outlet pipe 183 and is sent to a downstream process.
Example 4
After the hydrolysis is completed, the whole hydrolysis system is also required to be cleaned, and the specific operation is as follows:
The ejector 11 is stopped, and the fifth control valve 202 on the feeding pipe 20 is closed to stop feeding the starch slurry. The liquefied liquid in the liquefaction coil 16, flash unit 14 and hydrolysis pipe 18 is discharged by a feed pump 19.
The feed pump 19 is stopped, the third control valve 184 on the outlet pipe 183 is closed, the fourth control valve 185 on the branch pipe of the outlet pipe 183 is opened, and the gas in the hydrolysis pipe 18 is discharged. And then the second control valve 182 on the liquid discharge pipe 181 below the hydrolysis pipe 18 is opened to discharge the residual liquid in the hydrolysis pipe 18.
A first control valve 143 on a branch line below a drain port 142 at the bottom of the flash evaporator 14 is opened to discharge the residual liquid in the flash evaporator 14.
After the residual liquid of each unit is discharged, the fifth control valve 202 is kept closed, the open/close state of other control valves in the hydrolysis process is recovered, and the sixth control valve 204 on the cleaning pipeline 203 is opened.
Water or cleaning liquid is injected into the vapor-liquid mixing cavity 15 through the cleaning pipeline 203, and the cleaning operation is performed on the device by using the cleaning liquid according to the flow route of the starch slurry and the liquefied liquid in the hydrolysis process.
During cleaning, the injector 11 can be started to inject high-temperature steam into the steam-liquid mixing cavity 15, and the cleaning solution introduced into the steam-liquid mixing cavity 15 is heated and then the device is cleaned. The high-temperature cleaning liquid has higher cleaning effect on the device.
After the cleaning is finished, the residual cleaning liquid in each unit is discharged through opening and closing the control valve in the same operation as the operation of discharging the residual liquid of the liquefied liquid.
After the residual cleaning liquid is drained, the state of the control valve of each unit is restored to the state in the hydrolysis process, and the next starch hydrolysis is waited.
In the present invention, terms such as "upper", "lower", "one end", "the other end", "the bottom" and "the top" are described according to the positional relationship in the drawings of the present invention, and are not intended to limit the scope of the present invention, but rather to change or adjust the relative relationship without substantially changing the technical content, and are considered as the scope of the present invention.
The foregoing description is directed to the preferred embodiments of the present invention, but the embodiments are not intended to limit the scope of the invention, and all equivalent changes or modifications made under the technical spirit of the present invention should be construed to fall within the scope of the present invention.
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| US9085472B2 (en) * | 2010-02-26 | 2015-07-21 | General Electric Company | Gasification system employing ejectors |
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| CN107964554A (en) * | 2018-01-22 | 2018-04-27 | 武汉中粮食品科技有限公司 | A kind of amylolytic method |
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| CN111424063B (en) * | 2020-04-07 | 2024-08-02 | 河北广玉淀粉糖业有限公司 | Starch liquefaction production process and production system thereof |
| CN215162738U (en) * | 2021-05-12 | 2021-12-14 | 江苏省奥谷生物科技有限公司 | Starch jet liquefaction device in sugar production |
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