CN111925933B - Starch milk size mixing and liquefying method - Google Patents
Starch milk size mixing and liquefying method Download PDFInfo
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Abstract
The invention discloses a starch milk size mixing and liquefying method, which comprises the following steps: mixing starch with water, stirring for a period of time, heating the stirred starch milk, mixing, adding dilute alkali, and stirring for a period of time; refluxing the stirred feed liquid through a branch, controlling the addition amount of dilute alkali through feedback of a first pH meter, adding a liquefying enzyme, and sending the feed liquid into a liquefying ejector after the pH value of the feed liquid reaches a set value; when the temperature of the liquefaction ejector reaches a set value, feeding the feed liquid into a flash tank, adding the liquefaction enzyme, feeding the feed liquid into a liquefaction tank, a second plate heat exchanger and a circulating water heat exchanger, feeding the feed liquid subjected to heat exchange into a buffer tank, adding the dilute acid, stirring for a period of time, and controlling the addition amount of the dilute acid; meanwhile, saccharifying enzyme is added into the buffer tank and is conveyed out after stirring, so that the method can improve the filtering speed of the liquefied liquid, save the secondary injection investment and the investment of the metering pump, avoid the liquefaction failure caused by the mechanical failure of the metering pump and also save the consumption of liquefied steam.
Description
Technical Field
The invention relates to a method for producing starch sugar, in particular to a method for mixing and liquefying starch milk.
Background
Starch sugar is a saccharide produced by using starch, particularly corn starch or rice flour as raw materials, the quality of the corn starch and the rice flour from various suppliers is uneven, a higher requirement is brought to liquefaction, most enterprises adopt a first spray with a temperature of 105 ℃ and a second spray with a temperature of 135 ℃ to facilitate subsequent filtration, but the steam consumption and the investment cost of the second spray are increased, although the secondary steam generated by the second spray can be utilized by a subsequent evaporation process, the chances of liquefaction and evaporation are smaller, more practically, the liquefaction process is stopped after the completion, the evaporation is always performed by using raw steam, and the fact that the two sprays of steam are evaporated and utilized is a little bit for saving steam of an evaporator manufacturer, and the real meaning is worthy of being consulted. Therefore, if one spray can solve the problem of starch quality irregularity and the solution of the liquefaction and filtration effects of the feed liquid, the investment cost of production enterprises and the steam cost of operation can be greatly reduced, in addition, in production, the problem of feed liquid liquefaction caused by sudden mechanical faults of a liquefying enzyme metering pump or an acid-base metering pump occurs occasionally, if an unpowered gravity type gravity flow mode can be adopted to add acid-base to adjust the pH value and add enzyme, the smooth liquefaction is facilitated, and the investment cost of the metering pump is saved.
Disclosure of Invention
The invention aims to provide a starch milk size mixing and liquefying method, which can not only improve the filtering speed of liquefied liquid, save the secondary injection investment and the metering pump investment, avoid the liquefaction failure caused by the mechanical failure of the metering pump, but also save the consumption of liquefied steam.
The purpose of the invention is realized by the following steps: a starch milk mixing and liquefying method, the adopted starch milk mixing and liquefying system comprises a first starch milk tank, a first plate heat exchanger, a second starch milk tank, a liquefying maintaining pipe, a liquefying flash tank, a liquefying tank, a second plate heat exchanger, a circulating water heat exchanger and a buffer tank, wherein an outlet of the first starch milk tank is connected with an inlet of the first plate heat exchanger, an outlet of the first plate heat exchanger and an outlet of a dilute alkali tank are connected with an inlet of the second starch milk tank through a first mixer, an outlet of the second starch milk tank is connected with a liquefying ejector, an outlet of the second starch milk tank is also connected with an outlet of a first liquefying enzyme tank through a branch pipe and another inlet of the second starch milk tank through a second mixer, the second mixer is provided with a first pH meter, the liquefying ejector is connected with the liquefying maintaining pipe, an outlet of the liquefying maintaining pipe is connected with the liquefying flash tank, the outlet of the liquefaction flash tank and the outlet of the second liquefaction enzyme tank are connected with the inlet of the liquefaction tank through a third mixer, the outlet of the liquefaction tank is connected with the inlet of a second plate heat exchanger, the outlet of the second plate heat exchanger is connected with the inlet of a circulating water heat exchanger, the outlet of the circulating water heat exchanger and the outlet of the dilute acid tank are connected with the inlet of a buffer tank through a fourth mixer, the outlet of the buffer tank is connected with a desugaring tank, the outlet of the buffer tank is also connected with the outlet of the saccharification enzyme tank through a branch pipe and the other inlet of the buffer tank through a fifth mixer, a second pH meter is arranged on the buffer tank, three groups of the liquefaction tanks are arranged and are sequentially connected with each other, the first plate heat exchanger, the second plate heat exchanger and the circulating water heat exchanger are water-material heat exchangers, the feeding pipelines in the first mixer, the second mixer, the third mixer, the fourth mixer and the fifth mixer are all inclined pipelines, the inclined pipelines are inclined pipelines, the inclined angles are 30-60 degrees, and are correspondingly connected with the dilute alkali tank, the system comprises a first liquefying enzyme tank, a second liquefying enzyme tank, a dilute acid tank and a saccharifying enzyme tank, wherein the liquefying flash tank is communicated with the atmosphere; characterized in that the method comprises the following steps:
step 1) adding water into a first starch milk tank, adding starch, stirring for a period of time, and feeding the stirred starch milk into a first plate heat exchanger for heating;
step 2), heating the starch milk by a first plate heat exchanger, sending the starch milk into a first mixer, adding dilute alkali into the first mixer by a dilute alkali tank, mixing the starch milk in the first mixer, sending the starch milk into a second starch milk tank, and stirring for a period of time;
step 3) feeding the material liquid stirred by the second starch milk tank into a second mixer through a branch, controlling the addition amount of dilute alkali through feedback of a first pH meter arranged in the second mixer, simultaneously adding liquefied enzyme into the second mixer through a first liquefied enzyme tank, feeding the material liquid into the second starch milk tank after the second mixer is mixed, and feeding the material liquid into a liquefaction ejector after the pH value of the material liquid reaches a set value;
step 4) adjusting the temperature of the discharged material liquid by adding steam into the liquefaction ejector, when the temperature reaches a set value, feeding the material liquid into a flash tank, wherein the flash tank is communicated with the atmosphere, feeding the material liquid in the flash tank into a third mixer, simultaneously adding liquefying enzyme into the third mixer through a second liquefying enzyme tank, and feeding the mixture into a liquefying tank after mixing by the third mixer;
step 5) after the previous liquefaction tank is filled with the set value, tangentially pressing the feed liquid into the next liquefaction tank, finally sending the feed liquid in the liquefaction tank into a second plate heat exchanger and a circulating water heat exchanger in sequence after no blue reaction of iodine test, sending the feed liquid after heat exchange into a fourth mixer, simultaneously adding dilute acid into the fourth mixer through a dilute acid tank, sending the mixture into a buffer tank after the mixture in the fourth mixer, and stirring for a period of time;
and 6) refluxing the material liquid stirred by the buffer tank into a fifth mixer through a branch, controlling the addition amount of the dilute acid through feedback of a second pH meter arranged in the fifth mixer, simultaneously adding the glucoamylase into the fifth mixer through a glucoamylase tank, mixing the material liquid by the fifth mixer, feeding the material liquid into the buffer tank, and discharging the material liquid when the pH value of the material liquid reaches a set value.
As a further limitation of the present invention, stirring in step 1) is carried out for 15min; step 2), heating to 52-58 ℃ through a first plate heat exchanger, wherein the concentration of dilute alkali is 2%; in the step 3), the flow of the liquefying enzyme is 0.51-0.68kg/t starch dry matter, and the set value range of the pH value is as follows: 5.3-5.6; the temperature of the discharged material liquid in the step 4) is as follows: 122-128 ℃, the flow rate of the liquefying enzyme is as follows: 0.64-0.85 kg/t starch dry matter; the set values of the liquefaction tank in the step 5) are as follows: 90 percent; step 6) adding the saccharifying enzyme into the mixture: 1.02-1.36kg/t starch dry matter, the setting range of pH value is: 4.2-4.5.
As a further limitation of the present invention, stirring in step 1) is carried out for 15min; step 2), heating to 54 ℃ through a first plate heat exchanger, wherein the concentration of dilute alkali is 2%; the flow rate of the liquefying enzyme in the step 3) is 0.57g/h, and the set value of the pH value is as follows: 5.4; the temperature of the discharged material liquid in the step 4) is as follows: at 125 ℃, the flow rate of the liquefying enzyme is as follows: 0.72kg/t starch dry matter; the set values of the liquefaction tank in the step 5) are as follows: 90 percent; and step 6), adding the saccharifying enzyme in the following amount: 1.18kg/t dry starch, the pH value being set: 4.3.
compared with the prior art, the invention has the beneficial effects that: the invention uses few storage tanks, pH adjustment and enzyme addition are carried out in the same storage tank, acid, alkali and enzyme are added in a gravity flow manner, the pH is positioned in a mixer for feed liquid backflow, and the correction of a pH electrode is convenient; the method adopts one-time injection to 120-130 ℃, and adds enzyme in the liquefaction reaction tank for 2 times before injection, thereby not only ensuring that starch is fully gelatinized and hydrolyzed in advance during liquefaction, but also ensuring that the post-enzyme addition is completely hydrolyzed, and the total enzyme addition amount is the same as that during conventional 105 ℃ injection liquefaction, the liquefied liquid protein and the sugar solution are obviously layered, and the filtering speed of the sugar solution is high; after the heat after the liquefaction reaction is utilized by water, the utilized heat is used for preheating the starch milk, the temperature of the preheated starch milk is controlled below the starch gelatinization temperature (60 ℃), and the steam consumption of a liquefaction ejector is reduced; the invention has high automation degree, does not need secondary injection, saves the investment of acid-base and enzyme metering pumps, has low investment cost, fully utilizes heat energy, and has important practical significance for saving steam consumption of power plants and improving liquefaction effect.
Drawings
Fig. 1 is a schematic diagram of the system principle employed in the present invention.
The system comprises a first starch milk tank 1, a first plate heat exchanger 2, a first mixer 3, a dilute alkali tank 4, a first liquefying enzyme tank 5, a first pH meter 6, a second mixer 7, a second starch milk tank 8, a liquefying injector 9, a liquefying maintaining pipe 10, a flash tank 11, a second liquefying enzyme tank 12, a third mixer 13, a liquefying tank 14, a second plate heat exchanger 15, a circulating water heat exchanger 16, a fourth mixer 17, a dilute acid tank 18, a saccharifying enzyme tank 19, a second pH meter 20, a fifth mixer 21 and a buffer tank 22.
Detailed Description
Example 1
As shown in fig. 1, the starch milk mixing and liquefying method adopts a starch milk mixing and liquefying system comprising a first starch milk tank 1, a first plate heat exchanger 2, a second starch milk tank 8, a liquefying maintaining pipe 10, a liquefying flash tank 11, a liquefying tank 14, a second plate heat exchanger 15, a circulating water heat exchanger 16 and a buffer tank 22, wherein an outlet of the first starch milk tank 1 is connected with an inlet of the first plate heat exchanger 2, an outlet of the first plate heat exchanger 2 and an outlet of a dilute alkali tank 4 are connected with an inlet of the second starch milk tank 8 through a first mixer 3, an outlet of the second starch milk tank 8 is connected with a liquefying ejector 9, an outlet of the second starch milk tank 8 is also connected with an outlet of a first liquefying enzyme tank 5 through a branch pipe and another inlet of the second starch milk tank 8 through a second mixer 7, a first pH meter 6 is arranged on the second mixer 7, the liquefying ejector 9 is connected with the liquefying maintaining pipe 10, the outlet of the liquefaction maintaining pipe 10 is connected with a liquefaction flash tank 11, the outlet of the liquefaction flash tank 11 and the outlet of a second liquefaction enzyme tank 12 are connected with the inlet of a liquefaction tank 14 through a third mixer 13, the outlet of the liquefaction tank 14 is connected with the inlet of a second plate heat exchanger 15, the outlet of the second plate heat exchanger 15 is connected with the inlet of a circulating water heat exchanger 16, the outlet of the circulating water heat exchanger 16 and the outlet of a dilute acid tank 18 are connected with the inlet of a buffer tank 22 through a fourth mixer 17, the outlet of the buffer tank 22 is connected with a saccharification tank, the outlet of the buffer tank 22 is also connected with the outlet of a saccharification enzyme tank 19 through a branch pipe and a fifth mixer 21 to be connected with the other inlet of the buffer tank 22, a second pH meter 20 is arranged on the buffer tank 22, three groups of liquefaction tanks 14 are arranged and are sequentially connected with each other, the first plate heat exchanger 2, the second plate heat exchanger 15 and the circulating water heat exchanger 16 are all water-material heat exchangers, a first mixer 3, the feeding pipelines in the second mixer 7, the third mixer 13, the fourth mixer 17 and the fifth mixer 21 are all inclined pipelines with an inclination angle of 30 degrees, and the inclined pipelines are correspondingly connected with the dilute alkali tank 4, the first liquefying enzyme tank 5, the second liquefying enzyme tank 12, the dilute acid tank 18 and the saccharifying enzyme tank 19, and the liquefying flash tank 11 is communicated with the atmosphere; the method comprises the following steps:
step 1) adding 7 tons of water into a first starch milk tank 1, adding 3 tons of starch, stirring for 15min, and feeding the stirred starch milk into a first plate heat exchanger 2 for heating;
step 2), heating the starch milk to 52 ℃ through a first plate heat exchanger 2, sending the starch milk into a first mixer 3, adding 2% dilute alkali into the first mixer 3 through a dilute alkali tank 4, mixing the starch milk in the first mixer 3, sending the starch milk into a second starch milk tank 8, and stirring for a period of time;
step 3) feeding the material liquid stirred by the second starch milk tank 8 back into the second mixer 7 through a branch, controlling the addition amount of dilute alkali through the feedback of a first pH meter 6 arranged in the second mixer 7, simultaneously adding liquefying enzyme into the second mixer 7 through a first liquefying enzyme tank 5, wherein the flow rate of the liquefying enzyme is 0.51kg/t of dry starch, feeding the mixed material liquid into the second starch milk tank 8 after the second mixer 7 is mixed, and feeding the material liquid into a liquefying ejector 9 when the pH value of the material liquid reaches 5.3;
and 4) adjusting the temperature of the discharged material liquid by adding steam into the liquefaction ejector 9: 122 ℃, when the temperature reaches a set value, the feed liquid is fed into the flash tank 11, the flash tank 11 is communicated with the atmosphere, the feed liquid in the flash tank 11 is fed into the third mixer 13, meanwhile, the liquefying enzyme is added into the third mixer 13 through the second liquefying enzyme tank 12, and the flow of the liquefying enzyme is as follows: 0.64kg/t starch dry matter, and the third mixer 13 is mixed and then sent into a liquefaction tank 14;
step 5) after 90% of the previous liquefaction tank 14 is filled, tangentially pressing feed liquid into the next liquefaction tank 14, finally sending the feed liquid into a second plate heat exchanger 15 and a circulating water heat exchanger 16 in sequence after the iodine in the feed liquid in the liquefaction tank 14 does not react blue, sending the feed liquid after heat exchange into a fourth mixer 17, simultaneously adding dilute acid into the fourth mixer 17 through a dilute acid tank 18, sending the mixture into a buffer tank 22 after the mixture in the fourth mixer 17 is mixed, and stirring for a period of time;
and step 6) refluxing the material liquid stirred by the buffer tank 22 into the fifth mixer 21 through a branch, controlling the addition amount of the dilute acid through feedback of a second pH meter 20 arranged in the fifth mixer 21, and simultaneously adding the saccharifying enzyme into the fifth mixer 21 through a saccharifying enzyme tank 19, wherein the addition amount of the saccharifying enzyme is as follows: 1.02kg/t dry starch, mixed in a fifth mixer 21 and sent into a buffer tank 22, and when the pH value of the feed liquid reaches 4.2, the feed liquid is sent out.
Example 2
As shown in fig. 1, the starch milk mixing and liquefying method adopts a starch milk mixing and liquefying system comprising a first starch milk tank 1, a first plate heat exchanger 2, a second starch milk tank 8, a liquefying maintaining pipe 10, a liquefying flash tank 11, a liquefying tank 14, a second plate heat exchanger 15, a circulating water heat exchanger 16 and a buffer tank 22, wherein an outlet of the first starch milk tank 1 is connected with an inlet of the first plate heat exchanger 2, an outlet of the first plate heat exchanger 2 and an outlet of a dilute alkali tank 4 are connected with an inlet of the second starch milk tank 8 through a first mixer 3, an outlet of the second starch milk tank 8 is connected with a liquefying ejector 9, an outlet of the second starch milk tank 8 is also connected with an outlet of a first liquefying enzyme tank 5 through a branch pipe and another inlet of the second starch milk tank 8 through a second mixer 7, a first pH meter 6 is arranged on the second mixer 7, the liquefying ejector 9 is connected with the liquefying maintaining pipe 10, the outlet of the liquefaction maintaining pipe 10 is connected with a liquefaction flash tank 11, the outlet of the liquefaction flash tank 11 and the outlet of a second liquefaction enzyme tank 12 are connected with the inlet of a liquefaction tank 14 through a third mixer 13, the outlet of the liquefaction tank 14 is connected with the inlet of a second plate heat exchanger 15, the outlet of the second plate heat exchanger 15 is connected with the inlet of a circulating water heat exchanger 16, the outlet of the circulating water heat exchanger 16 and the outlet of a dilute acid tank 18 are connected with the inlet of a buffer tank 22 through a fourth mixer 17, the outlet of the buffer tank 22 is connected with a saccharification tank, the outlet of the buffer tank 22 is also connected with the outlet of a saccharification enzyme tank 19 through a branch pipe and a fifth mixer 21 to be connected with the other inlet of the buffer tank 22, a second pH meter 20 is arranged on the buffer tank 22, three groups of liquefaction tanks 14 are arranged and are sequentially connected with each other, the first plate heat exchanger 2, the second plate heat exchanger 15 and the circulating water heat exchanger 16 are all water-material heat exchangers, a first mixer 3, the feeding pipelines in the second mixer 7, the third mixer 13, the fourth mixer 17 and the fifth mixer 21 are all inclined pipelines with an inclination angle of 45 degrees, and the inclined pipelines are correspondingly connected with the dilute alkali tank 4, the first liquefying enzyme tank 5, the second liquefying enzyme tank 12, the dilute acid tank 18 and the saccharifying enzyme tank 19, and the liquefying flash tank 11 is communicated with the atmosphere; the method comprises the following steps:
step 1) adding 7 tons of water into a first starch milk tank 1, adding 3 tons of starch, stirring for 15min, and feeding the stirred starch milk into a first plate heat exchanger 2 for heating;
step 2) heating the starch milk to 54 ℃ through a first plate heat exchanger 2, then sending the starch milk into a first mixer 3, meanwhile, adding 2% diluted alkali into the first mixer 3 through a diluted alkali tank 4, sending the starch milk into a second starch milk tank 8 after mixing in the first mixer 3, and stirring for a period of time;
step 3) feeding the material liquid stirred by the second starch milk tank 8 back into the second mixer 7 through a branch, controlling the addition amount of dilute alkali through the feedback of a first pH meter 6 arranged in the second mixer 7, simultaneously adding liquefying enzyme into the second mixer 7 through a first liquefying enzyme tank 5, wherein the flow rate of the liquefying enzyme is 0.57kg/t of dry starch, feeding the mixed material liquid into the second starch milk tank 8 after the second mixer 7 is mixed, and feeding the material liquid into a liquefying ejector 9 when the pH value of the material liquid reaches 5.4;
and 4) adjusting the temperature of the discharged material liquid by adding steam into the liquefaction ejector 9: 125 ℃, when the temperature reaches the set value, send the feed liquid into flash tank 11, flash tank 11 is linked together with the atmosphere, send the feed liquid in flash tank 11 into third blender 13, simultaneously, still add the liquefaction enzyme in third blender 13 through second liquefaction enzyme jar 12, the flow of liquefaction enzyme is: 0.72kg/t of dry starch, and the mixture is sent into a liquefaction tank 14 after being mixed by a third mixer 13;
step 5) after 90% of the previous liquefaction tank 14 is filled, tangentially pressing feed liquid into the next liquefaction tank 14, finally sending the feed liquid into a second plate heat exchanger 15 and a circulating water heat exchanger 16 in sequence after the iodine in the feed liquid in the liquefaction tank 14 does not react blue, sending the feed liquid after heat exchange into a fourth mixer 17, simultaneously adding dilute acid into the fourth mixer 17 through a dilute acid tank 18, sending the mixture into a buffer tank 22 after the mixture in the fourth mixer 17 is mixed, and stirring for a period of time;
and step 6) refluxing the material liquid stirred by the buffer tank 22 into the fifth mixer 21 through a branch, controlling the addition amount of the dilute acid through feedback of a second pH meter 20 arranged in the fifth mixer 21, and simultaneously adding the saccharifying enzyme into the fifth mixer 21 through a saccharifying enzyme tank 19, wherein the addition amount of the saccharifying enzyme is as follows: 1.18kg/t dry starch, mixed in a fifth mixer 21 and fed into a buffer tank 22, and when the pH value of the feed liquid reaches 4.3, the feed liquid is discharged.
Example 3
As shown in fig. 1, the starch milk mixing and liquefying method adopts a starch milk mixing and liquefying system comprising a first starch milk tank 1, a first plate heat exchanger 2, a second starch milk tank 8, a liquefying maintaining pipe 10, a liquefying flash tank 11, a liquefying tank 14, a second plate heat exchanger 15, a circulating water heat exchanger 16 and a buffer tank 22, wherein an outlet of the first starch milk tank 1 is connected with an inlet of the first plate heat exchanger 2, an outlet of the first plate heat exchanger 2 and an outlet of a dilute alkali tank 4 are connected with an inlet of the second starch milk tank 8 through a first mixer 3, an outlet of the second starch milk tank 8 is connected with a liquefying ejector 9, an outlet of the second starch milk tank 8 is also connected with an outlet of a first liquefying enzyme tank 5 through a branch pipe and another inlet of the second starch milk tank 8 through a second mixer 7, a first pH meter 6 is arranged on the second mixer 7, the liquefying ejector 9 is connected with the liquefying maintaining pipe 10, the outlet of the liquefaction maintaining pipe 10 is connected with a liquefaction flash tank 11, the outlet of the liquefaction flash tank 11 and the outlet of a second liquefaction enzyme tank 12 are connected with the inlet of a liquefaction tank 14 through a third mixer 13, the outlet of the liquefaction tank 14 is connected with the inlet of a second plate heat exchanger 15, the outlet of the second plate heat exchanger 15 is connected with the inlet of a circulating water heat exchanger 16, the outlet of the circulating water heat exchanger 16 and the outlet of a dilute acid tank 18 are connected with the inlet of a buffer tank 22 through a fourth mixer 17, the outlet of the buffer tank 22 is connected with a saccharification tank, the outlet of the buffer tank 22 is also connected with the outlet of a saccharification enzyme tank 19 through a branch pipe and a fifth mixer 21 to be connected with the other inlet of the buffer tank 22, a second pH meter 20 is arranged on the buffer tank 22, three groups of liquefaction tanks 14 are arranged and are sequentially connected with each other, the first plate heat exchanger 2, the second plate heat exchanger 15 and the circulating water heat exchanger 16 are all water-material heat exchangers, a first mixer 3, the feeding pipelines in the second mixer 7, the third mixer 13, the fourth mixer 17 and the fifth mixer 21 are all inclined pipelines with an inclination angle of 60 degrees, and the inclined pipelines are correspondingly connected with the dilute alkali tank 4, the first liquefying enzyme tank 5, the second liquefying enzyme tank 12, the dilute acid tank 18 and the saccharifying enzyme tank 19, and the liquefying flash tank 11 is communicated with the atmosphere; the method comprises the following steps:
step 1) adding 7 tons of water into a first starch milk tank 1, adding 3 tons of starch, stirring for 15min, and feeding the stirred starch milk into a first plate heat exchanger 2 for heating;
step 2), heating the starch milk to 58 ℃ through a first plate heat exchanger 2, sending the starch milk into a first mixer 3, adding 2% dilute alkali into the first mixer 3 through a dilute alkali tank 4, mixing the starch milk in the first mixer 3, sending the starch milk into a second starch milk tank 8, and stirring for a period of time;
step 3) feeding the material liquid stirred by the second starch milk tank 8 back into the second mixer 7 through a branch, controlling the addition amount of dilute alkali through the feedback of a first pH meter 6 arranged in the second mixer 7, simultaneously adding liquefying enzyme into the second mixer 7 through a first liquefying enzyme tank 5, wherein the flow rate of the liquefying enzyme is 0.68kg/t of dry starch, feeding the mixed material liquid into the second starch milk tank 8 after the second mixer 7 is mixed, and feeding the material liquid into a liquefying ejector 9 when the pH value of the material liquid reaches 5.6;
and 4) adjusting the temperature of the discharged material liquid by adding steam into the liquefaction ejector 9: and the temperature of 128 ℃, when the temperature reaches a set value, the feed liquid is fed into the flash tank 11, the flash tank 11 is communicated with the atmosphere, the feed liquid in the flash tank 11 is fed into the third mixer 13, meanwhile, the liquefying enzyme is added into the third mixer 13 through the second liquefying enzyme tank 12, and the flow of the liquefying enzyme is as follows: 0.85 kg/t dry starch, mixed by a third mixer 13 and sent into a liquefaction tank 14;
step 5) after 90% of the previous liquefaction tank 14 is filled, tangentially pressing feed liquid into the next liquefaction tank 14, finally sending the feed liquid into a second plate heat exchanger 15 and a circulating water heat exchanger 16 in sequence after the iodine in the feed liquid in the liquefaction tank 14 does not react blue, sending the feed liquid after heat exchange into a fourth mixer 17, simultaneously adding dilute acid into the fourth mixer 17 through a dilute acid tank 18, sending the mixture into a buffer tank 22 after the mixture in the fourth mixer 17 is mixed, and stirring for a period of time;
and step 6) refluxing the material liquid stirred by the buffer tank 22 into the fifth mixer 21 through a branch, controlling the addition amount of the dilute acid through feedback of a second pH meter 20 arranged in the fifth mixer 21, and simultaneously adding the saccharifying enzyme into the fifth mixer 21 through a saccharifying enzyme tank 19, wherein the addition amount of the saccharifying enzyme is as follows: 1.36kg/t dry starch, mixed in the fifth mixer 21 and sent to the buffer tank 22, when the pH value of the feed liquid reaches 4.5, the feed liquid is sent out.
The performance of the liquefied liquid obtained in the three embodiments is tested, and qualitative filter paper is adopted for filtration detection; the filtering speed of the liquefied liquid in example 1 is 60ml/min, the filtering speed of the liquefied liquid in example 2 is 75ml/min, the filtering speed of the liquefied liquid in example 3 is 70ml/min, and the filtering speed of the conventional liquefied liquid at 105 ℃ is 30ml/min in the comparative example; from the above results, it can be seen that the speed of the liquefied liquid of example 1 is increased by 1 time, the speed of the liquefied liquid of example 21 is increased by 1.5 times, the speed of the liquefied liquid of example 3 is increased by 1.3 times, the above 3 examples are superior to the comparative example, and of these, example 2 is the best; in conclusion, the liquefied liquid obtained by the method is convenient for filtering the saccharified liquid in the later period, and simultaneously, the investment of a metering pump and a storage tank is saved.
The present invention is not limited to the above-mentioned embodiments, and based on the technical solutions disclosed in the present invention, those skilled in the art can make some substitutions and modifications to some technical features without creative efforts according to the disclosed technical contents, and these substitutions and modifications are all within the protection scope of the present invention.
Claims (3)
1. A starch milk mixing and liquefying method, the adopted starch milk mixing and liquefying system comprises a first starch milk tank, a first plate heat exchanger, a second starch milk tank, a liquefying maintaining pipe, a liquefying flash tank, a liquefying tank, a second plate heat exchanger, a circulating water heat exchanger and a buffer tank, wherein an outlet of the first starch milk tank is connected with an inlet of the first plate heat exchanger, an outlet of the first plate heat exchanger and an outlet of a dilute alkali tank are connected with an inlet of the second starch milk tank through a first mixer, an outlet of the second starch milk tank is connected with a liquefying ejector, an outlet of the second starch milk tank is also connected with an outlet of a first liquefying enzyme tank through a branch pipe and another inlet of the second starch milk tank through a second mixer, the second mixer is provided with a first pH meter, the liquefying ejector is connected with the liquefying maintaining pipe, an outlet of the liquefying maintaining pipe is connected with the liquefying flash tank, the outlet of the liquefaction flash tank and the outlet of the second liquefaction enzyme tank are connected with the inlet of the liquefaction tank through a third mixer, the outlet of the liquefaction tank is connected with the inlet of a second plate heat exchanger, the outlet of the second plate heat exchanger is connected with the inlet of a circulating water heat exchanger, the outlet of the circulating water heat exchanger and the outlet of the dilute acid tank are connected with the inlet of a buffer tank through a fourth mixer, the outlet of the buffer tank is connected with a desugaring tank, the outlet of the buffer tank is also connected with the outlet of the saccharification enzyme tank through a branch pipe and the other inlet of the buffer tank through a fifth mixer, a second pH meter is arranged on the buffer tank, three groups of the liquefaction tanks are arranged and are sequentially connected with each other, the first plate heat exchanger, the second plate heat exchanger and the circulating water heat exchanger are water-material heat exchangers, the feeding pipelines in the first mixer, the second mixer, the third mixer, the fourth mixer and the fifth mixer are all inclined pipelines, the inclined pipelines are inclined pipelines, the inclined angles are 30-60 degrees, and are correspondingly connected with the dilute alkali tank, the system comprises a first liquefying enzyme tank, a second liquefying enzyme tank, a dilute acid tank and a saccharifying enzyme tank, wherein the liquefying flash tank is communicated with the atmosphere; characterized in that the method comprises the following steps:
step 1) adding water into a first starch milk tank, adding starch, stirring for a period of time, and feeding the stirred starch milk into a first plate heat exchanger for heating;
step 2) heating the starch milk by a first plate heat exchanger, feeding the starch milk into a first mixer, adding dilute alkali into the first mixer by a dilute alkali tank, mixing the starch milk in the first mixer, feeding the starch milk into a second starch milk tank, and stirring the starch milk for a period of time;
step 3) feeding the material liquid stirred by the second starch milk tank into a second mixer through a branch, controlling the addition amount of dilute alkali through feedback of a first pH meter arranged in the second mixer, simultaneously adding liquefied enzyme into the second mixer through a first liquefied enzyme tank, feeding the material liquid into the second starch milk tank after the second mixer is mixed, and feeding the material liquid into a liquefaction ejector after the pH value of the material liquid reaches a set value;
step 4) adjusting the temperature of the discharged material liquid by adding steam into the liquefaction ejector, when the temperature reaches a set value, feeding the material liquid into a flash tank, wherein the flash tank is communicated with the atmosphere, feeding the material liquid in the flash tank into a third mixer, simultaneously, adding a liquefaction enzyme into the third mixer through a second liquefaction enzyme tank, and feeding the mixture into a liquefaction tank after mixing by the third mixer;
step 5) after the previous liquefaction tank is filled with the set value, the feed liquid is tangentially pressed into the next liquefaction tank, finally, the feed liquid in the liquefaction tank is sequentially sent into a second plate heat exchanger and a circulating water heat exchanger after no blue reaction exists, the feed liquid after heat exchange is sent into a fourth mixer, meanwhile, dilute acid is added into the fourth mixer through a dilute acid tank, the feed liquid is sent into a buffer tank after being mixed in the fourth mixer, and the mixture is stirred for a period of time;
and 6) refluxing the material liquid stirred by the buffer tank into a fifth mixer through a branch, controlling the addition amount of the dilute acid through feedback of a second pH meter arranged in the fifth mixer, simultaneously adding the glucoamylase into the fifth mixer through a glucoamylase tank, mixing the material liquid by the fifth mixer, feeding the material liquid into the buffer tank, and discharging the material liquid when the pH value of the material liquid reaches a set value.
2. The method according to claim 1, wherein stirring is carried out for 15min in step 1); step 2), heating to 52-58 ℃ through a first plate heat exchanger, wherein the concentration of dilute alkali is 2%; the flow of the liquefying enzyme in the step 3) is 0.51-0.68kg/t of starch dry matter, and the set value range of the pH value is as follows: 5.3-5.6; the temperature of the discharged material liquid in the step 4) is as follows: the flow rate of the liquefying enzyme is as follows: 0.64-0.85 kg/t starch dry matter; the set values of the liquefaction tank in the step 5) are as follows: 90 percent; and step 6), adding the saccharifying enzyme in the following amount: 1.02-1.36kg/t starch dry matter, the setting range of pH value is: 4.2-4.5.
3. The method according to claim 2, wherein stirring is carried out for 15min in step 1); step 2), heating to 54 ℃ through a first plate heat exchanger, wherein the concentration of dilute alkali is 2%; the flow of the liquefying enzyme in the step 3) is 0.57g/t of starch dry matter, and the set value of the pH value is as follows: 5.4; the temperature of the discharged material liquid in the step 4) is as follows: at 125 ℃, the flow rate of the liquefying enzyme is as follows: 0.72kg/t starch dry matter; the set values of the liquefaction tank in the step 5) are as follows: 90 percent; and step 6), adding the saccharifying enzyme in the following amount: 1.18kg/t dry starch, the pH value being set: 4.3.
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Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR1450301A (en) * | 1964-10-26 | 1966-05-06 | Process for converting starch and other polysaccharides into products containing dextrose and maltose | |
| US3337414A (en) * | 1963-12-31 | 1967-08-22 | Corn Products Co | Saccharification of starch |
| CN101348816A (en) * | 2008-09-13 | 2009-01-21 | 天明（沈阳）酒精有限公司 | Use of low temperature boiling technology in alcohol production |
| CN102220395A (en) * | 2011-05-23 | 2011-10-19 | 北京坡华生化技术有限公司 | Biological sugaring process by using wheat starch |
| CN105238829A (en) * | 2014-07-11 | 2016-01-13 | 武汉中粮食品科技有限公司 | Enzymolysis method for starchy material |
| CN205616903U (en) * | 2016-05-18 | 2016-10-05 | 昆山品青生物科技有限公司 | Starch milk liquefaction system |
| CN206783696U (en) * | 2017-01-13 | 2017-12-22 | 内蒙古融成玉米开发有限公司 | Glucose production system |
| CN107653135A (en) * | 2017-10-18 | 2018-02-02 | 天津大学 | A kind of production method to brew alcohol |
| CN108486194A (en) * | 2018-03-22 | 2018-09-04 | 吉林省农业科学院 | A kind of method that corn flour prepares solid high fructose corn |
| CN208182999U (en) * | 2018-04-02 | 2018-12-04 | 中粮融氏生物科技有限公司 | A kind of fructose process units |
-
2020
- 2020-08-25 CN CN202010862653.6A patent/CN111925933B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3337414A (en) * | 1963-12-31 | 1967-08-22 | Corn Products Co | Saccharification of starch |
| FR1450301A (en) * | 1964-10-26 | 1966-05-06 | Process for converting starch and other polysaccharides into products containing dextrose and maltose | |
| CN101348816A (en) * | 2008-09-13 | 2009-01-21 | 天明（沈阳）酒精有限公司 | Use of low temperature boiling technology in alcohol production |
| CN102220395A (en) * | 2011-05-23 | 2011-10-19 | 北京坡华生化技术有限公司 | Biological sugaring process by using wheat starch |
| CN105238829A (en) * | 2014-07-11 | 2016-01-13 | 武汉中粮食品科技有限公司 | Enzymolysis method for starchy material |
| CN205616903U (en) * | 2016-05-18 | 2016-10-05 | 昆山品青生物科技有限公司 | Starch milk liquefaction system |
| CN206783696U (en) * | 2017-01-13 | 2017-12-22 | 内蒙古融成玉米开发有限公司 | Glucose production system |
| CN107653135A (en) * | 2017-10-18 | 2018-02-02 | 天津大学 | A kind of production method to brew alcohol |
| CN108486194A (en) * | 2018-03-22 | 2018-09-04 | 吉林省农业科学院 | A kind of method that corn flour prepares solid high fructose corn |
| CN208182999U (en) * | 2018-04-02 | 2018-12-04 | 中粮融氏生物科技有限公司 | A kind of fructose process units |
Non-Patent Citations (1)
| Title |
|---|
| 官雪薇 ; 江招财 ; .淀粉液糖生产过程控制系统.食品安全导刊.(第21期),全文. * |
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