CN111205338A - Method for recovering arabinose from arabinose mother liquor - Google Patents
Method for recovering arabinose from arabinose mother liquor Download PDFInfo
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Abstract
The invention relates to a method for recovering arabinose from arabinose mother liquor, which comprises the following steps: and (2) sequentially carrying out alkali injection, primary decolorization, ion exchange, concentration crystallization, centrifugal separation and redissolution, secondary decolorization, vacuum crystallization, secondary centrifugation and drying and packaging processes on the arabinose mother liquor to finally obtain an arabinose finished product, wherein the pH of the arabinose mother liquor after the alkali injection process is stabilized at 5.0-6.0, the decolorization temperature in the primary decolorization and secondary decolorization processes is controlled at 60-65 ℃, and the pH of the discharged material after the ion exchange process is controlled at more than 4.0. The invention reduces the rate of converting the arabinose into other miscellaneous sugars in the arabinose mother liquor purification process and improves the purity and recovery rate of the finished arabinose; the acidic substances are neutralized before the arabinose mother liquor enters the ion exchange, so that the load of the ion exchange anion column is reduced, and the exchange capacity of the ion exchange column is improved.
Description
Technical Field
The invention belongs to the technical field of arabinose mother liquor recycling, and particularly relates to a method for recycling arabinose from arabinose mother liquor.
Background
The arabinose mother liquor refers to mother liquor generated by centrifugal separation in the arabinose refining process, and nearly 2 tons of arabinose mother liquor are generated when every 1 ton of arabinose is generated in the arabinose production process. In the current industry, arabinose mother liquor can only be sold at a lower price, and the added value is lower. The arabinose content in the arabinose mother liquor is still high and reaches 50-65%, so that a large recycling space exists, and arabinose can be recovered and extracted again through process treatment. For example, patent publication No. CN104892688A discloses a method for recovering L-arabinose from a mother liquor of L-arabinose crystallization, and describes a method for obtaining arabinose with a purity of more than 98% by subjecting the mother liquor of the crystallization to steps of decolorization, purification, concentration, crystallization, recrystallization and the like. However, this technique has the following drawbacks: in the process of preparing the arabinose, a large amount of acidic substances exist in the arabinose mother liquor due to the influences of arabinose sources, extraction processes, microbial fermentation, acidic substance enrichment and the like.
Disclosure of Invention
The technical problem to be solved by the invention is to provide a method for recovering arabinose from arabinose mother liquor, which can prevent the conversion of arabinose at high temperature and improve the yield of the arabinose mother liquor.
The invention is realized by providing a method for recovering arabinose from arabinose mother liquor, which comprises the following steps: and (2) sequentially carrying out alkali injection, primary decolorization, ion exchange, concentration crystallization, centrifugal separation and redissolution, secondary decolorization, vacuum crystallization, secondary centrifugation and drying and packaging processes on the arabinose mother liquor to finally obtain an arabinose finished product, wherein the pH of the arabinose mother liquor after the alkali injection process is stabilized at 5.0-6.0, the decolorization temperature in the primary decolorization and secondary decolorization processes is controlled at 60-65 ℃, and the pH of the discharged material after the ion exchange process is controlled at more than 4.0.
Further, the method comprises the steps of:
step one, alkali injection: injecting the centrifugally separated arabinose mother liquor into an alkali injection tank, adding a sodium carbonate solution, and adjusting the pH of the arabinose mother liquor to 5-6;
step two, primary decoloring: the sugar liquid obtained in the first step enters a primary decoloring tank through a pipeline, activated carbon is added into the primary decoloring tank for primary decoloring, and the decoloring temperature is 60-65 ℃;
step three, ion exchange: the sugar solution treated in the second step enters an ion exchange column to remove impurity ions in the sugar solution, and the pH of the discharged material of the anion column is controlled to be more than 4.0;
step four, concentration and crystallization: concentrating the sugar solution after ion exchange by an evaporator, and then feeding the concentrated sugar solution into a crystallization cylinder for cooling and crystallization;
step five, centrifugal separation and redissolution: centrifugally separating the material treated in the step four to obtain crystals with the arabinose concentration of 85-90%, and adding deionized water into the crystals for redissolving;
step six, secondary decoloring: feeding the arabinose heavy solution treated in the fifth step into a secondary decoloring tank for secondary decoloring, wherein the decoloring temperature is 60-65 ℃;
step seven, vacuum crystallization: concentrating the decolorized material liquid treated in the sixth step by using an evaporator, then feeding the concentrated material liquid into a vacuum sugar boiling system, and adding 100-200 g of seed crystal for vacuum crystallization;
step eight: secondary centrifugation, drying and packaging: and (4) centrifuging the material treated in the step seven for the second time, drying the material in a hot air drying system to obtain arabinose crystals with the content of more than 98%, and packaging the arabinose crystals to obtain an arabinose finished product.
Compared with the prior art, the method for recovering the arabinose from the arabinose mother liquor has the following characteristics:
1. the rate of converting arabinose into other miscellaneous sugars in the arabinose mother liquor purification process is reduced, and the purity and recovery rate of finished arabinose are improved;
2. the process is simple, excessive equipment is not required to be added, the investment cost is low, and the arabinose mother liquor can be recycled only by processing the arabinose mother liquor in the centralized time of the existing arabinose production line;
3. the acidic substances are neutralized before the arabinose mother liquor enters the ion exchange, so that the load of the ion exchange anion column is reduced, and the exchange capacity of the ion exchange column is improved.
Detailed Description
In order to make the technical problems, technical solutions and advantageous effects to be solved by the present invention more apparent, the present invention is further described in detail below with reference to the following embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
The preferred embodiment of the method for recovering the arabinose from the arabinose mother liquor comprises the following steps: and (2) sequentially carrying out alkali injection, primary decolorization, ion exchange, concentration crystallization, centrifugal separation and redissolution, secondary decolorization, vacuum crystallization, secondary centrifugation and drying and packaging processes on the arabinose mother liquor to finally obtain an arabinose finished product, wherein the pH of the arabinose mother liquor after the alkali injection process is stabilized at 5.0-6.0, the decolorization temperature in the primary decolorization and secondary decolorization processes is controlled at 60-65 ℃, and the pH of the discharged material after the ion exchange process is controlled at more than 4.0.
Specifically, the method for recovering the arabinose from the arabinose mother liquor comprises the following steps:
step one, alkali injection: injecting the centrifugally separated arabinose mother liquor into an alkali injection tank, adding a sodium carbonate solution, and adjusting the pH of the arabinose mother liquor to 5-6.
Step two, primary decoloring: and (3) introducing the sugar liquor obtained in the first step into a primary decoloring tank through a pipeline, and adding activated carbon into the primary decoloring tank to perform primary decoloring at the decoloring temperature of 60-65 ℃.
Step three, ion exchange: and (4) introducing the sugar solution treated in the step (II) into an ion exchange column to remove impurity ions in the sugar solution, and controlling the pH of the discharged material of the anion column to be more than 4.0.
Step four, concentration and crystallization: and concentrating the sugar solution after ion exchange to reach a concentration of 80% by an evaporator, and then feeding the sugar solution into a crystallization cylinder for cooling and crystallization.
Step five, centrifugal separation and redissolution: and (4) centrifugally separating the material treated in the fourth step to obtain crystals with the arabinose concentration of 85-90%, and adding deionized water into the crystals for redissolving.
Step six, secondary decoloring: and (4) allowing the arabinose re-dissolved material liquid treated in the fifth step to enter a secondary decoloring tank for secondary decoloring, wherein the decoloring temperature is 60-65 ℃, and the light transmittance of the decoloring material liquid is controlled to be more than 95%.
Step seven, vacuum crystallization: concentrating the decolorized feed liquid treated in the sixth step to 76% of concentration by an evaporator, then feeding the concentrated decolorized feed liquid into a vacuum sugar boiling system, and adding 100-200 g of seed crystal for vacuum crystallization.
Step eight: secondary centrifugation, drying and packaging: and (4) centrifuging the material treated in the step seven for the second time, drying the material in a hot air drying system to obtain arabinose crystals with the content of more than 98%, and packaging the arabinose crystals to obtain an arabinose finished product.
The method for recovering arabinose from arabinose mother liquor of the present invention is further illustrated below with reference to specific examples.
Example 1
An embodiment of the first method for recovering arabinose from arabinose mother liquor of the invention comprises the following steps:
and 11, conveying the arabinose mother liquor after centrifugal separation to an alkali injection tank through a pump, adding a food-grade sodium carbonate solution with the concentration of 4%, adjusting the pH of the arabinose mother liquor to 5.5, uniformly mixing, and then feeding into a pre-decoloring tank. Wherein the refractive index of the arabinose mother liquor is 55 percent, the arabinose content is 75 percent, and the pH value is 2.7.
And (3) introducing the sugar liquor obtained in the steps (12) and (11) into a primary decoloring tank from a pre-decoloring tank through a pipeline, starting steam for heating when the liquid level of the primary decoloring tank reaches 30%, raising the temperature to 62 ℃, simultaneously adding 1.25Kg/h of activated carbon for decoloring, and controlling the light transmission of the sugar liquor discharged from the primary decoloring tank to be more than 90%.
And (3) treating the sugar solution decolorized in the steps (13) and (12) by using an anion column and a cation column of an ion exchange column in sequence to remove impurity ions in the sugar solution, controlling the ion exchange temperature at 45 ℃ and controlling the pH of the discharged material of the anion column at 4.4.
And step 14, concentrating the sugar solution subjected to ion exchange in an evaporator until the refractive index is 80%, discharging at the temperature of 80 ℃, and crystallizing in a cooling crystallization cylinder, wherein the cooling speed is controlled at 1 ℃/h.
And step 15, after the temperature is reduced to 35-40 ℃, performing centrifugal separation on the material treated in the step 14 to obtain crystals with the arabinose concentration of 87%, and adding deionized water into the crystals to redissolve the crystals until the refraction is 66%.
And (3) allowing the arabinose heavy solution treated in the step (16) and the step (15) to enter a secondary decoloring tank for secondary decoloring, wherein the decoloring temperature is 62 ℃, and the light transmittance of the decoloring solution is controlled to be more than 95%.
And (5) feeding the secondarily decolorized feed liquid obtained in the steps (17) and (16) into an evaporator for secondary concentration through a precision filter, feeding the material concentrated by the evaporator until the refraction reaches 77%, into a vacuum crystallization system, controlling the vacuum to be more than-0.096 MPa, and adding 200g of seed crystal for vacuum crystallization.
Step 18, blanking the material subjected to vacuum crystallization in the step 17 to a crystallization assisting groove for centrifugation, and keeping the temperature of the crystallization assisting groove at 55-60 ℃; and (3) allowing the materials in the crystallization assisting groove to enter a secondary centrifuge for secondary centrifugation, allowing the centrifuged materials to enter a hot air drying tank for drying at the air temperature of 85 ℃ to obtain arabinose crystals with the content of 98.4%, controlling the water content of the crystals to be within 0.15%, and packaging the arabinose crystals to obtain arabinose finished products.
The arabinose recovery rate in the arabinose mother liquor of the embodiment was calculated to be 25.4%.
Example 2
An embodiment of the second method for recovering arabinose from the arabinose mother liquor of the present invention comprises the following steps:
and step 21, conveying the arabinose mother liquor after centrifugal separation to an alkali injection tank through a pump, adding a food-grade sodium carbonate solution with the concentration of 4%, adjusting the pH value of the arabinose mother liquor to 5, uniformly mixing, and then feeding into a pre-decoloring tank. Wherein the refractive index of the arabinose mother liquor is 55 percent, the arabinose content is 75 percent, and the pH value is 2.7.
And (3) introducing the sugar liquor obtained in the step (22) and the step (21) into a primary decoloring tank from a pre-decoloring tank through a pipeline, starting steam for heating when the liquid level of the primary decoloring tank reaches 30%, raising the temperature to 60 ℃, simultaneously adding 1.25Kg/h of activated carbon for decoloring, and controlling the light transmission of the sugar liquor discharged from the primary decoloring tank to be more than 90%.
And (3) treating the sugar solution decolorized in the steps (23) and (22) by using an anion column and a cation column of an ion exchange column in sequence to remove impurity ions in the sugar solution, controlling the ion exchange temperature at 45 ℃ and controlling the pH of the discharged material of the anion column at 4.1.
And 24, concentrating the sugar solution subjected to ion exchange in an evaporator until the refractive index is 80%, discharging at the temperature of 80 ℃, and crystallizing in a cooling crystallization cylinder, wherein the cooling speed is controlled at 1 ℃/h.
And 25, after the temperature is reduced to 35-40 ℃, performing centrifugal separation on the material treated in the step 24 to obtain crystals with the arabinose concentration of 85%, and adding deionized water into the crystals to redissolve the crystals until the refraction is 66%.
And (3) allowing the arabinose heavy solution treated in the step (26) and the step (25) to enter a secondary decoloring tank for secondary decoloring, wherein the decoloring temperature is 60 ℃, and the light transmittance of the decoloring solution is controlled to be more than 95%.
And (3) feeding the secondarily decolorized feed liquid obtained in the steps (27) and (26) into an evaporator for secondary concentration through a precision filter, feeding the material concentrated by the evaporator until the refraction reaches 77%, into a vacuum crystallization system, controlling the vacuum to be more than-0.096 MPa, and adding 150g of seed crystal for vacuum crystallization.
Step 28, blanking the material subjected to vacuum crystallization in the step 27 to a crystallization assisting groove for centrifugation, and keeping the temperature of the crystallization assisting groove at 55-60 ℃; and (3) allowing the materials in the crystallization assisting groove to enter a secondary centrifuge for secondary centrifugation, allowing the centrifuged materials to enter a hot air drying tank for drying at the air temperature of 85 ℃ to obtain arabinose crystals with the content of 98.0%, controlling the water content of the crystals to be within 0.15%, and packaging the arabinose crystals to obtain arabinose finished products.
The arabinose recovery rate in the arabinose mother liquor of the embodiment is 25.1 percent by calculation.
Example 3
An embodiment of the third method for recovering arabinose from the arabinose mother liquor of the present invention comprises the following steps:
and 31, conveying the arabinose mother liquor after centrifugal separation to an alkali injection tank through a pump, adding a food-grade sodium carbonate solution with the concentration of 4%, adjusting the pH value of the arabinose mother liquor to 6, uniformly mixing, and then feeding into a pre-decoloring tank. Wherein the refractive index of the arabinose mother liquor is 55 percent, the arabinose content is 75 percent, and the pH value is 2.7.
And 32, introducing the sugar liquor obtained in the step 31 from the pre-decoloring tank into a primary decoloring tank through a pipeline, starting steam for heating when the liquid level of the primary decoloring tank reaches 30%, raising the temperature to 65 ℃, simultaneously adding 1.25Kg/h of activated carbon for decoloring, and controlling the light transmission of the sugar liquor discharged from the primary decoloring tank to be more than 90%.
And (3) treating the sugar solution decolorized in the steps 33 and 32 by using an anion column and a cation column of an ion exchange column in sequence to remove impurity ions in the sugar solution, controlling the ion exchange temperature at 45 ℃ and controlling the pH of the discharged sugar solution from the anion column at 4.8.
And step 34, concentrating the sugar solution subjected to ion exchange in an evaporator until the refractive index is 80%, discharging at the temperature of 80 ℃, and crystallizing in a cooling crystallization cylinder, wherein the cooling speed is controlled at 1 ℃/h.
And step 35, after the temperature is reduced to 35-40 ℃, performing centrifugal separation on the material treated in the step 34 to obtain crystals with the arabinose concentration of 90%, and adding deionized water into the crystals to redissolve the crystals until the refraction is 66%.
And (4) allowing the arabinose heavy solution treated in the step (36) and the step (35) to enter a secondary decoloring tank for secondary decoloring, wherein the decoloring temperature is 65 ℃, and the light transmittance of the decoloring solution is controlled to be more than 95%.
And (4) feeding the secondarily decolored feed liquid obtained in the steps (37) and (36) into an evaporator for secondary concentration through a precision filter, feeding the material concentrated by the evaporator until the refractive index is 77% into a vacuum crystallization system, controlling the vacuum to be more than-0.096 MPa, and adding 100g of seed crystal for vacuum crystallization.
Step 38, blanking the material subjected to vacuum crystallization in the step 37 to a crystallization assisting groove for centrifugation, and keeping the temperature of the crystallization assisting groove at 55-60 ℃; and (3) allowing the materials in the crystallization assisting groove to enter a secondary centrifuge for secondary centrifugation, allowing the centrifuged materials to enter a hot air drying tank for drying at the air temperature of 85 ℃ to obtain arabinose crystals with the content of 98.8%, controlling the water content of the crystals to be within 0.15%, and packaging the arabinose crystals to obtain arabinose finished products.
According to measurement, the arabinose recovery rate in the arabinose mother liquor of the embodiment is 25.8%.
Comparative example
To illustrate the effect of the process of the present invention, the following comparative examples were conducted. The comparative example comprises the following steps:
injecting the centrifugally separated arabinose mother liquor into a primary decoloring tank, starting steam for heating when the liquid level of the primary decoloring tank reaches 30%, heating to 75-80 ℃, simultaneously adding 1.25Kg/h of activated carbon for decoloring, and controlling the light transmission of sugar liquor discharged from the primary decoloring tank to be more than 90%. Wherein the refractive index of the arabinose mother liquor is 55 percent, the arabinose content is 75 percent, and the pH value is 2.7.
And the second step and the first step of decolorizing sugar solution are treated successively with positive column and negative column of ion exchange column to eliminate impurity ion from sugar solution, the ion exchange temperature is controlled at 45 deg.c and the pH value of the discharged material from the negative column is controlled over 3.5.
And thirdly, concentrating the sugar solution after ion exchange to reach the concentration of 80% through an evaporator, discharging at the temperature of 80 ℃, and feeding the sugar solution into a cooling crystallization cylinder for crystallization, wherein the cooling speed is controlled at 1 ℃/h.
And fourthly, after the temperature is reduced to 35-40 ℃, centrifugally separating the material treated in the third step to obtain arabinose crystals, adding deionized water to redissolve the arabinose crystals until the refraction is 66%.
And (5) allowing the arabinose heavy solution treated in the fifth step and the fourth step to enter a secondary decoloring tank for secondary decoloring, wherein the light transmittance of the decoloring solution is controlled to be more than 95%.
And (3) feeding the secondarily decolorized feed liquid in the sixth step and the fifth step into an evaporator for secondary concentration through a precision filter, feeding the material concentrated by the evaporator until the refractive index is 77% into a vacuum crystallization system, controlling the vacuum to be more than-0.096 Mpa, and adding 200g of seed crystal for vacuum crystallization.
The seventh step: sixthly, blanking the material subjected to vacuum crystallization to a crystallization assisting groove for centrifugation, and keeping the temperature of the crystallization assisting groove at 55-60 ℃; and (3) allowing the materials in the crystallization assisting groove to enter a secondary centrifuge for secondary centrifugation, allowing the centrifuged materials to enter a hot air drying tank for drying at the air temperature of 85 ℃ to obtain arabinose crystals with the content of more than 98%, controlling the water content of the crystals to be within 0.15%, and packaging the arabinose crystals to obtain arabinose finished products.
According to measurement and calculation, the recovery rate of the arabinose in the arabinose mother liquor of the comparative example is 23.6%.
The main parameters and results of example 1 and comparative example were compared to give the following table.
As is obvious from the comparison of the data, the method of the invention can prevent the conversion of the arabinose and improve the recovery rate of the arabinose by increasing the pH of the arabinose mother liquor, reducing the temperature of the decoloring procedure and controlling the pH of the ion exchange material to be more than 4.0.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents and improvements made within the spirit and principle of the present invention are intended to be included within the scope of the present invention.
Claims (5)
1. A method for recovering arabinose from arabinose mother liquor is characterized by comprising the following steps: and (2) sequentially carrying out alkali injection, primary decolorization, ion exchange, concentration crystallization, centrifugal separation and redissolution, secondary decolorization, vacuum crystallization, secondary centrifugation and drying and packaging processes on the arabinose mother liquor to finally obtain an arabinose finished product, wherein the pH of the arabinose mother liquor after the alkali injection process is stabilized at 5.0-6.0, the decolorization temperature in the primary decolorization and secondary decolorization processes is controlled at 60-65 ℃, and the pH of the discharged material after the ion exchange process is controlled at more than 4.0.
2. The method for recovering arabinose from the arabinose mother liquor as claimed in claim 1, which comprises the steps of:
step one, alkali injection: injecting the centrifugally separated arabinose mother liquor into an alkali injection tank, adding a sodium carbonate solution, and adjusting the pH of the arabinose mother liquor to 5-6;
step two, primary decoloring: the sugar liquid obtained in the first step enters a primary decoloring tank through a pipeline, activated carbon is added into the primary decoloring tank for primary decoloring, and the decoloring temperature is 60-65 ℃;
step three, ion exchange: the sugar solution treated in the second step enters an ion exchange column to remove impurity ions in the sugar solution, and the pH of the discharged material of the anion column is controlled to be more than 4.0;
step four, concentration and crystallization: concentrating the sugar solution after ion exchange by an evaporator, and then feeding the concentrated sugar solution into a crystallization cylinder for cooling and crystallization;
step five, centrifugal separation and redissolution: centrifugally separating the material treated in the step four to obtain crystals with the arabinose concentration of 85-90%, and adding deionized water into the crystals for redissolving;
step six, secondary decoloring: feeding the arabinose heavy solution treated in the fifth step into a secondary decoloring tank for secondary decoloring, wherein the decoloring temperature is 60-65 ℃;
step seven, vacuum crystallization: concentrating the decolorized material liquid treated in the sixth step by using an evaporator, then feeding the concentrated material liquid into a vacuum sugar boiling system, and adding 100-200 g of seed crystal for vacuum crystallization;
step eight: secondary centrifugation, drying and packaging: and (4) centrifuging the material treated in the step seven for the second time, drying the material in a hot air drying system to obtain arabinose crystals with the content of more than 98%, and packaging the arabinose crystals to obtain an arabinose finished product.
3. The method for recovering arabinose from the arabinose mother liquor as claimed in claim 2, which comprises the steps of:
step 11, conveying the arabinose mother liquor after centrifugal separation to an alkali injection tank through a pump, adding a sodium carbonate solution, adjusting the pH of the arabinose mother liquor to 5.5, uniformly mixing, and then feeding into a pre-decoloring tank;
step 12, the sugar liquor in the step 11 enters a primary decoloring tank from a pre-decoloring tank through a pipeline, when the liquid level of the primary decoloring tank reaches 30%, steam is started to heat, the temperature is raised to 62 ℃, meanwhile, activated carbon is added according to 1.25Kg/h for decoloring, and the light transmission of the sugar liquor discharged from the primary decoloring tank is controlled to be more than 90%;
step 13, the sugar solution decolorized in step 12 is treated by an anion column and a cation column of an ion exchange column in sequence to remove impurity ions in the sugar solution, the ion exchange temperature is controlled at 45 ℃, and the pH of the discharged material of the anion column is controlled at 4.4;
step 14, feeding the sugar solution after ion exchange into an evaporator for concentration until the refractive index is 80%, discharging the sugar solution at the temperature of 80 ℃, feeding the sugar solution into a cooling crystallization cylinder for crystallization, and controlling the cooling speed at 1 ℃/h;
step 15, after the temperature is reduced to 35-40 ℃, performing centrifugal separation on the material treated in the step 14 to obtain arabinose crystals, and adding deionized water into the arabinose crystals to redissolve the arabinose crystals until the refractive index is 66%;
step 16, allowing the arabinose heavy solution treated in the step 15 to enter a secondary decoloring tank for secondary decoloring, wherein the decoloring temperature is 62 ℃;
the feed liquid of the secondary decolorization in the step 17 and the step 16 passes through a precision filter and enters an evaporator for secondary concentration, the material concentrated by the evaporator until the refraction reaches 77 percent enters a vacuum crystallization system, the vacuum is controlled to be more than-0.096 Mpa, and 200g of seed crystal is added for vacuum crystallization;
step 18, blanking the material subjected to vacuum crystallization in the step 17 to a crystallization assisting groove for centrifugation, and keeping the temperature of the crystallization assisting groove at 55-60 ℃; and (3) allowing the materials in the crystallization assisting groove to enter a secondary centrifuge for secondary centrifugation, allowing the centrifuged materials to enter a hot air drying tank for drying at the air temperature of 85 ℃ to obtain arabinose crystals with the content of 98.4%, controlling the water content of the crystals to be within 0.15%, and packaging the arabinose crystals to obtain arabinose finished products.
4. The method for recovering arabinose from the arabinose mother liquor as claimed in claim 2, which comprises the steps of:
step 21, conveying the arabinose mother liquor after centrifugal separation to an alkali injection tank through a pump, adding a sodium carbonate solution, adjusting the pH of the arabinose mother liquor to 5, uniformly mixing, and then feeding into a pre-decoloring tank;
step 22, the sugar liquor in the step 21 enters a primary decoloring tank from a pre-decoloring tank through a pipeline, when the liquid level of the primary decoloring tank reaches 30%, steam is started to heat, the temperature is raised to 60 ℃, meanwhile, activated carbon is added according to 1.25Kg/h for decoloring, and the light transmission of the sugar liquor discharged from the primary decoloring tank is controlled to be more than 90%;
the sugar solution decolorized in the steps 23 and 22 is treated by an anode column and an anion column of an ion exchange column in sequence to remove impurity ions in the sugar solution, the ion exchange temperature is controlled at 45 ℃, and the pH of the discharged material of the anion column is controlled at 4.1;
step 24, concentrating the sugar solution subjected to ion exchange in an evaporator until the refractive index is 80%, discharging at the temperature of 80 ℃, and crystallizing in a cooling crystallization cylinder, wherein the cooling speed is controlled at 1 ℃/h;
step 25, after the temperature is reduced to 35-40 ℃, performing centrifugal separation on the material treated in the step 24 to obtain arabinose crystals, and adding deionized water into the arabinose crystals to redissolve the arabinose crystals until the refractive index is 66%;
step 26, allowing the arabinose heavy solution treated in the step 25 to enter a secondary decoloring tank for secondary decoloring, wherein the decoloring temperature is 60 ℃;
feeding the material liquid obtained in the step 27 and the step 26 after secondary decolorization into an evaporator for secondary concentration through a precision filter, feeding the material concentrated by the evaporator until the refractive index is 77% into a vacuum crystallization system, controlling the vacuum to be more than-0.096 Mpa, and adding 150g of seed crystal for vacuum crystallization;
step 28, blanking the material subjected to vacuum crystallization in the step 27 to a crystallization assisting groove for centrifugation, and keeping the temperature of the crystallization assisting groove at 55-60 ℃; and (3) allowing the materials in the crystallization assisting groove to enter a secondary centrifuge for secondary centrifugation, allowing the centrifuged materials to enter a hot air drying tank for drying at the air temperature of 85 ℃ to obtain arabinose crystals with the content of 98.0%, controlling the water content of the crystals to be within 0.15%, and packaging the arabinose crystals to obtain arabinose finished products.
5. The method for recovering arabinose from the arabinose mother liquor as claimed in claim 2, which comprises the steps of:
31, conveying the arabinose mother liquor after centrifugal separation to an alkali injection tank through a pump, adding a sodium carbonate solution, adjusting the pH of the arabinose mother liquor to 6, uniformly mixing, and then feeding into a pre-decoloring tank;
32, the sugar liquor obtained in the step 31 enters a primary decoloring tank from a pre-decoloring tank through a pipeline, when the liquid level of the primary decoloring tank reaches 30%, steam is started to heat, the temperature is raised to 65 ℃, meanwhile, activated carbon is added according to 1.25Kg/h for decoloring, and the light transmission of the sugar liquor discharged from the primary decoloring tank is controlled to be more than 90%;
the sugar solution decolorized in the steps 33 and 32 is treated by an anion column and a cation column of an ion exchange column to remove impurity ions in the sugar solution, the ion exchange temperature is controlled at 45 ℃, and the pH of the discharged sugar solution from the anion column is controlled at 4.8;
step 34, concentrating the sugar solution subjected to ion exchange in an evaporator until the refractive index is 80%, discharging at the temperature of 80 ℃, and crystallizing in a cooling crystallization cylinder, wherein the cooling speed is controlled at 1 ℃/h;
step 35, after the temperature is reduced to 35-40 ℃, performing centrifugal separation on the material treated in the step 34 to obtain arabinose crystals, and adding deionized water into the arabinose crystals to redissolve the arabinose crystals until the refractive index is 66%;
step 36, allowing the arabinose heavy solution treated in the step 35 to enter a secondary decoloring tank for secondary decoloring, wherein the decoloring temperature is 65 ℃;
feeding the material liquid subjected to secondary decolorization in the steps 37 and 36 into an evaporator for secondary concentration through a precision filter, feeding the material concentrated by the evaporator until the refractive index is 77% into a vacuum crystallization system, controlling the vacuum to be more than-0.096 Mpa, and adding 100g of seed crystal for vacuum crystallization;
step 38, blanking the material subjected to vacuum crystallization in the step 37 to a crystallization assisting groove for centrifugation, and keeping the temperature of the crystallization assisting groove at 55-60 ℃; and (3) allowing the materials in the crystallization assisting groove to enter a secondary centrifuge for secondary centrifugation, allowing the centrifuged materials to enter a hot air drying tank for drying at the air temperature of 85 ℃ to obtain arabinose crystals with the content of 98.8%, controlling the water content of the crystals to be within 0.15%, and packaging the arabinose crystals to obtain arabinose finished products.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113979839A (en) * | 2021-11-25 | 2022-01-28 | 浙江华康药业股份有限公司 | Method for improving utilization rate of xylitol mother liquor |
| CN113976186A (en) * | 2021-11-25 | 2022-01-28 | 浙江华康药业股份有限公司 | Xylose mother liquor ion exchange system and method |
| CN115253364A (en) * | 2022-08-10 | 2022-11-01 | 安徽海蓝生物科技有限公司 | Centrifugation process and centrifugation equipment for tartaric acid solution |
| CN115785174A (en) * | 2022-12-17 | 2023-03-14 | 浙江华康药业股份有限公司 | Preparation method of high-purity arabinose crystal |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101538589A (en) * | 2009-05-07 | 2009-09-23 | 张兰波 | New clean method for producing xylitol and arabinose |
| CN101824055A (en) * | 2009-12-30 | 2010-09-08 | 山东福田药业有限公司 | Method for preparing L-arabinose by taking corn bran as material |
| CN102286571A (en) * | 2011-06-16 | 2011-12-21 | 北京化工大学 | Clean and high-efficiency production process for preparing xylose and L-arabinose |
| CN104892688A (en) * | 2015-06-05 | 2015-09-09 | 山东福田药业有限公司 | Method for recycling L-arabinose by using L-arabinose crystallization mother liquor |
| CN110468169A (en) * | 2019-09-04 | 2019-11-19 | 吉林省农业科学院 | A kind of method of corncob production L-arabinose |
-
2020
- 2020-02-11 CN CN202010087310.7A patent/CN111205338A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101538589A (en) * | 2009-05-07 | 2009-09-23 | 张兰波 | New clean method for producing xylitol and arabinose |
| CN101824055A (en) * | 2009-12-30 | 2010-09-08 | 山东福田药业有限公司 | Method for preparing L-arabinose by taking corn bran as material |
| CN102286571A (en) * | 2011-06-16 | 2011-12-21 | 北京化工大学 | Clean and high-efficiency production process for preparing xylose and L-arabinose |
| CN104892688A (en) * | 2015-06-05 | 2015-09-09 | 山东福田药业有限公司 | Method for recycling L-arabinose by using L-arabinose crystallization mother liquor |
| CN110468169A (en) * | 2019-09-04 | 2019-11-19 | 吉林省农业科学院 | A kind of method of corncob production L-arabinose |
Non-Patent Citations (2)
| Title |
|---|
| 苏会波，等: "新资源食品L-阿拉伯糖的制备、功能、应用和市场现状", 《食品工业科技》 * |
| 黄伟红，等: "利用L- 阿拉伯糖结晶母液回收L-阿拉伯糖的研究", 《中国食品添加剂》 * |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113979839A (en) * | 2021-11-25 | 2022-01-28 | 浙江华康药业股份有限公司 | Method for improving utilization rate of xylitol mother liquor |
| CN113976186A (en) * | 2021-11-25 | 2022-01-28 | 浙江华康药业股份有限公司 | Xylose mother liquor ion exchange system and method |
| CN113976186B (en) * | 2021-11-25 | 2023-08-15 | 浙江华康药业股份有限公司 | Xylose mother liquor ion exchange system and method |
| CN113979839B (en) * | 2021-11-25 | 2024-02-09 | 浙江华康药业股份有限公司 | Method for improving utilization rate of xylitol mother liquor |
| CN115253364A (en) * | 2022-08-10 | 2022-11-01 | 安徽海蓝生物科技有限公司 | Centrifugation process and centrifugation equipment for tartaric acid solution |
| CN115253364B (en) * | 2022-08-10 | 2023-10-31 | 安徽海蓝生物科技有限公司 | Centrifugal process and centrifugal equipment for tartaric acid solution |
| CN115785174A (en) * | 2022-12-17 | 2023-03-14 | 浙江华康药业股份有限公司 | Preparation method of high-purity arabinose crystal |
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