A system for preparing high-purity inositol using corn steep liquor

Abstract

The utility model relates to a system for preparing high-purity inositol using corn slurry, the system comprising a precipitation tank, a first plate-frame filter, a fitin dissolving tank, an enzymolysis tank, a neutralization tank, a second plate-frame filter, a nanofiltration system, a first evaporator, a decolorizing tank, an ion exchange column, a second evaporator, a first crystallization kettle, a first centrifuge, a crude product dissolving tank, a second crystallization kettle, a second centrifuge, a hot air drying tank and a cold air fluidized bed connected sequentially by pipelines, a feed inlet of corn supernatant and a feed inlet of lime milk suspension are respectively arranged on the precipitation tank, a feed inlet of dilute hydrochloric acid solution is arranged on the fitin dissolving tank, and the material coming out of the discharge end of the cold air fluidized bed is the required inositol crystal product. The utility model can quickly obtain enzymolysis raw material liquid phytic acid, and compared with calcium phytate suspension, the homogeneity of the liquid phytic acid enzymolysis process system is improved, the enzymolysis conversion rate is increased to more than 98%, and the purity of the inositol crystal product is increased to more than 99.5%.

Description

Technical Field

[0001] The utility model belongs to the technical field of sugar alcohol preparation, and particularly relates to a system for preparing high-purity inositol by utilizing corn steep liquor. Background Art

[0002] Inositol, molecular formula is C6H 12 O6, as a water-soluble vitamin, is white crystal or crystalline powder, odorless, slightly sweet, relatively stable in the air, but easy to absorb moisture; inositol is widely present in animals, plants, and microorganisms, has many physiological functions, and is a growth factor for animals and microorganisms. The most commonly used ino-inositol preparation process in industry is generally to use corn soaking water as raw material, obtain calcium phytate (i.e., phytin) through resin adsorption-elution method or lime milk precipitation method, and then after beating phytin, hydrolyze it under high temperature and high pressure to obtain inositol, and finally remove phosphate, and then refine and crystallize to obtain inositol products.

[0003] The traditional phytin extraction process is as follows: lime milk is directly added to the corn soaking water to neutralize phytic acid, so that phytic acid reacts with calcium hydroxide to form phytin, and then solid phytin is obtained by plate and frame filtration. Phytin is hydrolyzed to obtain inositol and phosphate, and the phosphate reacts with calcium hydroxide to form calcium phosphate precipitate, which is separated by plate and frame, and the remaining liquid is refined and purified, cooled and crystallized to obtain inositol products. Although this method has been applied industrially for a long time, it still has disadvantages such as complicated process, low product quality, high labor intensity, serious pollution, and strong odor.

[0004] The patent with publication number CN106986749A discloses a method for preparing crystalline inositol, which comprises first adsorbing phytic acid with an ion exchange resin column, then eluting the adsorbed phytic acid with a desorbent, adding calcium hydroxide to the eluent to precipitate the phytic acid into phytin, and then hydrolyzing at high temperature and high pressure, neutralizing and filtering, and cooling and crystallizing to obtain inositol. The resin adsorption-elution method can obtain phytate with high purity, but the flow rate during adsorption and elution is generally 1-1.5 BV / h, which requires a high resin filling amount, and the eluted phytic acid generally still needs to be pulped into phytin for hydrolysis, so the processing efficiency is relatively slow. Utility Model Content

[0005] The technical problem to be solved by the utility model is to provide a system for preparing high-purity inositol by using corn steep liquor, which has the characteristics of fast phytic acid extraction efficiency, high enzymatic hydrolysis conversion rate, high purity of final inositol product, etc.

[0006] The utility model is implemented in this way, providing a system for preparing high-purity inositol by using corn slurry, comprising a precipitation tank, a first plate-frame filter, a fitin dissolving tank, an enzymolysis tank, a neutralization tank, a second plate-frame filter, a nanofiltration system, a first evaporator, a decolorization tank, an ion exchange column, a second evaporator, a first crystallization kettle, a first centrifuge, a crude product dissolving tank, a second crystallization kettle, a second centrifuge, a hot air drying tank and a cold air fluidized bed, wherein a feed port for corn supernatant and a feed port for lime milk suspension are respectively arranged on the precipitation tank, a discharge end of a phytate filter cake is arranged on the first plate-frame filter, a feed port for a dilute hydrochloric acid solution is arranged on the fitin dissolving tank, and the feed end of the fitin dissolving tank is connected to the discharge end of the phytate filter cake. A feed port for phytase is provided on the enzymolysis tank, a feed port for lime milk suspension is provided on the neutralization tank, a discharge end for filtrate is provided on the second plate and frame filter, a feed end of the nanofiltration system is connected with a discharge end of the filtrate through a pipeline, a discharge end for permeate is provided on the nanofiltration system, the discharge end of the permeate is connected with a feed end of the first evaporator, a discharge end for primary crystallized massecuite is provided on the first centrifuge, a feed port for purified water is provided on the crude product dissolution tank, the feed end of the crude product dissolution tank is connected with a discharge end of primary crystallized massecuite, a discharge end for recrystallized massecuite is provided on the second centrifuge, a feed end of the hot air drying tank is connected with a discharge end of the recrystallized massecuite, and the material discharged from the discharge end of the cold air fluidized bed is the desired inositol crystal product.

[0007] Furthermore, a filtrate discharge end is provided on the first plate and frame filter, and the filtrate discharge end is connected to a feed port of the sedimentation tank through a pipeline.

[0008] Furthermore, a discharge port for the first mother liquid is provided on the first centrifuge, and the discharge port for the first mother liquid is connected to a feed port of the second evaporator through a pipeline.

[0009] Furthermore, a discharge port for the second mother liquor is provided on the second centrifuge, and the discharge port for the second mother liquor is connected with a feed port of the crude product dissolving tank through a pipeline.

[0010] Compared with the prior art, the utility model discloses a system for preparing high-purity inositol by using corn slurry. The system for preparing high-purity inositol by using corn slurry comprises a precipitation tank, a first plate-frame filter, a fitin dissolving tank, an enzymolysis tank, a neutralization tank, a second plate-frame filter, a nanofiltration system, a first evaporator, a decolorizing tank, an ion exchange column, a second evaporator, a first crystallization kettle, a first centrifuge, a crude product dissolving tank, a second crystallization kettle, a second centrifuge, a hot air drying tank and a cold air fluidized bed, which are sequentially connected through pipelines. Feed ports for corn supernatant and lime milk suspension are respectively arranged on the precipitation tank, a feed port for dilute hydrochloric acid solution is arranged on the fitin dissolving tank, purified water for dissolving is contained in the crude product dissolving tank, and the material discharged from the discharge end of the cold air fluidized bed is the required inositol crystal product. The method of the utility model can quickly obtain liquid phytic acid as an enzymatic hydrolysis raw material. Compared with calcium phytate suspension, the uniformity of the liquid phytic acid enzymatic hydrolysis process system is improved, and the enzymatic hydrolysis conversion rate is increased to more than 98%. At the same time, the use of a nanofiltration system for impurity removal reduces the large amount of activated carbon used in the decolorization process, and the purity of the inositol crystal product is increased to more than 99.5%. BRIEF DESCRIPTION OF THE DRAWINGS

[0011] Figure 1 The utility model is a schematic diagram of the principle of a preferred embodiment of a system for preparing high-purity inositol using corn steep liquor. DETAILED DESCRIPTION

[0012] In order to make the technical problems, technical solutions and beneficial effects to be solved by the present invention more clearly understood, the present invention is further described in detail below in conjunction with the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not used to limit the present invention.

[0013] Please refer to Figure 1 As shown, the preferred embodiment of the system for preparing high-purity inositol using corn steep liquor in the utility model, the arrowed line segments in the figure illustrate the flow direction of each material in the system. The system comprises a precipitation tank 1, a first plate-frame filter 2, a fitin dissolving tank 3, an enzymolysis tank 4, a neutralization tank 5, a second plate-frame filter 6, a nanofiltration system 7, a first evaporator 8, a decolorizing tank 9, an ion exchange column 10, a second evaporator 11, a first crystallization kettle 12, a first centrifuge 13, a crude product dissolving tank 14, a second crystallization kettle 15, a second centrifuge 16, a hot air drying tank 17 and a cold air fluidized bed 18 connected sequentially by pipelines.

[0014] A feed port 101 for corn supernatant A and a feed port 102 for lime milk suspension B are respectively arranged on the precipitation tank 1, a discharge end 21 for calcium phytate filter cake is arranged on the first plate and frame filter 2, a feed port 31 for dilute hydrochloric acid solution C is arranged on the Fiting dissolution tank 3, and the feed end of the Fiting dissolution tank 3 is connected to the discharge end of the calcium phytate filter cake.

[0015] The first plate-frame filter 2 is provided with a filtrate discharge end 22, which is connected to a feed port of the sedimentation tank 1 through a pipeline. The filtrate obtained by filtering the first plate-frame filter 2 is returned to the sedimentation tank 1 through a pipeline for reuse.

[0016] The enzymolysis tank 4 is provided with a feed port 41 for phytase D, and the neutralization tank 5 is provided with a feed port 51 for lime milk suspension B.

[0017] The second plate-frame filter 6 is provided with a discharge end for the filtrate, and the feed end of the nanofiltration system 7 is connected to the discharge end for the filtrate through a pipeline. The nanofiltration system 7 is provided with a discharge end for the permeate, and the discharge end for the permeate is connected to the feed end of the first evaporator 8.

[0018] The first centrifuge 13 is provided with a discharge end of the primary crystallized massecuite, and the crude product dissolving tank 14 is provided with a feed port 141 of purified water E, and the feed end of the crude product dissolving tank 14 is connected to the discharge end of the primary crystallized massecuite. The second centrifuge 16 is provided with a discharge end of the recrystallized massecuite, and the feed end of the hot air drying tank 17 is connected to the discharge end of the recrystallized massecuite. The material discharged from the discharge end of the cold air fluidized bed 18 is the desired inositol crystal F product.

[0019] The first centrifuge 13 is provided with a first mother liquid discharge port 131, which is connected to a feed port of the second evaporator 11 through a pipeline. The first mother liquid separated by the first centrifuge 13 is returned to the second evaporator 11 through a pipeline for reuse.

[0020] The second centrifuge 16 is provided with a discharge port 161 of the second mother liquor, which is connected to a feed port of the crude product dissolving tank 14 through a pipeline. The second mother liquor separated by the second centrifuge 16 is returned to the crude product dissolving tank 14 through a pipeline for reuse.

[0021] The utility model also discloses a method for preparing high-purity inositol by using corn steep liquor, wherein the method uses the system for preparing high-purity inositol by using corn steep liquor as described above, and the method comprises the following steps:

[0022] The first step is to pre-treat the corn slurry to extract liquid phytic acid, add an appropriate amount of lime milk suspension B to the corn slurry supernatant A in the precipitation tank 1 to precipitate phytic acid, and after the precipitation is complete, filter it through the first plate and frame filter 2 to obtain a calcium phytate filter cake; then put the obtained calcium phytate filter cake into the Fiting dissolving tank 3, add dilute hydrochloric acid solution C to the Fiting dissolving tank 3 to dissolve the calcium phytate filter cake, and obtain liquid phytic acid after complete dissolution; in this step, the refractive index of the corn slurry supernatant A raw material is 40-50%, and the lime milk suspension B is added for precipitation to control the pH of the feed liquid in the precipitation tank 1 to be greater than 5, and the dilute hydrochloric acid solution C is added to dissolve the liquid phytic acid in the Fiting dissolving tank 3 to control the pH of the liquid phytic acid to be less than 2.

[0023] The second step is to hydrolyze the liquid phytic acid, pass the obtained liquid phytic acid into the enzymolysis tank 4, add phytase D according to 1-10wt% of the mass of the liquid phytic acid in the enzymolysis tank 4, start the enzymolysis reaction, and reach equilibrium after 6-12h of enzymolysis to obtain inositol enzymolysis solution; in this step, the pH of the inositol enzymolysis solution in the enzymolysis tank 4 is controlled to be 2.0-3.0 and the temperature is 55-75°C.

[0024] The third step is to purify the inositol hydrolyzate. The inositol hydrolyzate is passed into a neutralization tank 5, and an appropriate amount of lime milk suspension B is added to the inositol hydrolyzate for neutralization treatment. The pH of the feed solution in the neutralization tank 5 is controlled to be greater than 9 to precipitate phosphate. After the neutralization treatment is completed, the second plate and frame filter 6 is used for filtering to remove the phosphate precipitation, and then the filtered hydrolyzate is sequentially passed through a nanofiltration system 7, a first evaporator 8, a decolorization tank 9, an ion exchange column 10, and a second evaporator 11 to obtain an inositol concentrated solution. In this step, the refractive index of the discharge from the first evaporator 8 is 40-50%, the conductivity of the discharge from the ion exchange column 10 is less than 50 μs / cm, and the refractive index of the discharge from the second evaporator 11 is 50-70%.

[0025] The fourth step is to crystallize and dry the inositol concentrated solution. The obtained inositol concentrated solution is passed into the first crystallization kettle 12, and the temperature is reduced and crystallized at a rate of 0.5-3.0°C / h. The obtained primary crystallized sugar paste is separated by the first centrifuge 13, and then an appropriate amount of purified water is added to the crude product dissolution tank 14 to dissolve at 60°C to obtain an inositol solution with a refractive index of 60-70%; then the solution is poured into the second crystallization kettle 15, and recrystallized at a temperature reduction rate of 1.5-2.0°C / h. The obtained recrystallized sugar paste is successively separated by the second centrifuge 16, dried by the hot air drying tank 17, and dried by the cold air fluidized bed 18 to obtain the inositol crystal F product.

[0026] Among them, in the third step, the nanofiltration system 7 is used to remove large molecular weight impurities in the inositol hydrolyzate that are difficult to remove by activated carbon adsorption, and the size of the nanofiltration membrane is 300~800Da.

[0027] Wherein, in the fourth step, the first crystallization kettle 12 and the second crystallization kettle 15 respectively adopt a cooling crystallization method for crystallization, and the crystallization end point temperature is 40-50°C.

[0028] The system and method for preparing high-purity inositol using corn steep liquor of the present invention are further described below by means of specific examples. Example 1

[0029] The first embodiment of the method for preparing high-purity inositol using corn steep liquor of the present invention comprises the following steps:

[0030] Step 11, adding an appropriate amount of lime milk suspension B to the corn steep liquor supernatant A with a refractive index of 45% in the precipitation tank 1, adjusting the pH of the feed liquid in the precipitation tank 1 to 5.38 to precipitate calcium phytate, and filtering through the first plate and frame filter 2 after complete precipitation to obtain a calcium phytate filter cake; then completely dissolving the obtained calcium phytate filter cake in the Fiting dissolution tank 3, completely dissolving to obtain liquid phytic acid, adding dilute hydrochloric acid solution C to adjust the pH of the liquid phytic acid in the Fiting dissolution tank 3 to 1.94, and determining the concentration of the liquid phytic acid by colorimetry to be 50.95 g / L.

[0031] Step 12, the obtained liquid phytic acid is passed into the enzymolysis tank 4, phytase is added in an amount of 7wt%, the system temperature T=55°C and pH=2.8 are adjusted, and the enzymolysis is performed for 8h to obtain an inositol enzymolysis solution. The inositol concentration in the enzymolysis solution is determined by high performance liquid chromatography to be 13.63g / L, and the phytic acid enzymolysis conversion rate in this step is calculated to be 98.1%.

[0032] Step 13, passing the inositol hydrolyzate into the neutralization tank 5, adding an appropriate amount of lime milk suspension B to the inositol hydrolyzate in the neutralization tank 5 to precipitate phosphate, filtering through the second plate and frame filter 6 to remove the phosphate precipitate, and then passing the filtered hydrolyzate through the nanofiltration system 7, the first evaporator 8, the decolorization tank 9, the ion exchange column 10, and the second evaporator 11 in sequence to obtain an inositol concentrate with a conductivity of 22.84 μs / cm and a refractive index of 70%; then the obtained inositol concentrate is placed in the first crystallization kettle 12 and heated to 2°C. / h and cooled to 40°C for crystallization. The primary crystallized sugar paste is centrifuged in the first centrifuge 13 to obtain crude inositol. The crude inositol enters the crude product dissolving tank 14 and is further dissolved into an inositol solution with a refractive index of 70%. Then, the crude inositol is recrystallized to 40°C in the second crystallizing kettle 15 at a cooling rate of 2°C / h. The recrystallized sugar paste is sequentially centrifuged in the second centrifuge 16, dried at 80°C in the hot air drying tank 17, and dried at 30°C in the cold air fluidized bed 18 to obtain the desired inositol crystal F product.

[0033] According to the method in GB1903.42-2020, the purity of inositol crystal F product was measured to be 99.82%, and the other indicators all met the national standard requirements. Example 2

[0034] A second embodiment of the system and method for preparing high-purity inositol using corn steep liquor of the present invention comprises the following steps:

[0035] Step 21, add an appropriate amount of lime milk suspension B to the corn syrup supernatant A with a refractive index of 40% in the precipitation tank 1, adjust the pH of the liquid in the precipitation tank 1 to 5.25 to precipitate calcium phytate, and after complete precipitation, filter through the first plate and frame filter 2 to obtain a calcium phytate filter cake; then dissolve the obtained calcium phytate filter cake in the fitin dissolution tank 3, completely dissolve to obtain liquid phytic acid, add dilute hydrochloric acid solution C to adjust the pH of the liquid phytic acid in the fitin dissolution tank 3 to 1.92, and determine the concentration of the liquid phytic acid by colorimetry to be 48.33 g / L.

[0036] Step 22, the obtained liquid phytic acid is passed into the enzymolysis tank 4, phytase is added in an amount of 5wt%, the system temperature T=55°C and pH=2.8 are adjusted, and the enzymolysis is performed for 8h to obtain an inositol hydrolyzate. The inositol concentration in the hydrolyzate is determined by high performance liquid chromatography to be 12.84g / L, and the phytic acid enzymolysis conversion rate of this step is calculated to be 97.4%.

[0037] Step 23, passing the inositol hydrolyzate into the neutralization tank 5, adding an appropriate amount of lime milk suspension B to the inositol hydrolyzate in the neutralization tank 5 to precipitate phosphate, filtering through the second plate and frame filter 6 to remove the phosphate precipitate, and then passing the filtered hydrolyzate through the nanofiltration system 7, the first evaporator 8, the decolorization tank 9, the ion exchange column 10, and the second evaporator 11 in sequence to obtain an inositol concentrate with a conductivity of 19.25 μs / cm and a refractive index of 70%; then the obtained inositol concentrate is passed into the first crystallization kettle 12 and heated at 2°C. / h and cooled to 40°C for crystallization. The primary crystallized sugar paste is centrifuged in the first centrifuge 13 to obtain crude inositol. The crude inositol enters the crude product dissolving tank 14 and is further dissolved into an inositol solution with a refractive index of 70%. Then, the crude inositol is recrystallized to 40°C in the second crystallizing kettle 15 at a cooling rate of 2°C / h. The recrystallized sugar paste is sequentially centrifuged in the second centrifuge 16, dried at 80°C in the hot air drying tank 17, and dried at 30°C in the cold air fluidized bed 18 to obtain the desired inositol crystal F product.

[0038] According to the method in GB1903.42-2020, the purity of inositol crystal F product was measured to be 99.75%, and the other indicators all met the national standard requirements. Example 3

[0039] The third embodiment of the method for preparing high-purity inositol by using corn steep liquor of the utility model comprises the following steps:

[0040] Step 31, adding an appropriate amount of lime milk suspension B to the corn syrup supernatant A with a refractive index of 50% in the precipitation tank 1, adjusting the pH of the liquid in the precipitation tank 1 to 5.38 to precipitate calcium phytate, and filtering through the first plate and frame filter 2 after complete precipitation to obtain a calcium phytate filter cake; then dissolving the obtained calcium phytate filter cake in the Fiting dissolution tank 3, completely dissolving to obtain liquid phytic acid, adding dilute hydrochloric acid solution C to adjust the pH of the liquid phytic acid in the Fiting dissolution tank 3 to 1.88, and determining the concentration of the liquid phytic acid by colorimetry to be 49.37 g / L.

[0041] Step 32, the obtained liquid phytic acid is passed into the enzymolysis tank 4, phytase is added in an amount of 1wt%, the system temperature T=75°C and pH=2.0 are adjusted, and the enzymolysis is performed for 12 hours to obtain an inositol hydrolyzate. The inositol concentration in the hydrolyzate is determined by high performance liquid chromatography to be 13.17 g / L, and the phytic acid enzymolysis conversion rate of this step is calculated to be 97.8%.

[0042] Step 33, the inositol hydrolyzate is passed into the neutralization tank 5, an appropriate amount of lime milk suspension B is added to the inositol hydrolyzate in the neutralization tank 5 to precipitate phosphate, and the inositol hydrolyzate is filtered through the second plate and frame filter 6 to remove the phosphate precipitate, and then the filtered hydrolyzate is sequentially passed through the nanofiltration system 7, the first evaporator 8, the decolorization tank 9, the ion exchange column 10, and the second evaporator 11 to obtain an inositol concentrate with a conductivity of 18.44 μs / cm and a refractive index of 60%; and the obtained inositol concentrate is then passed into the first crystallization kettle 12 and heated to 3.0 ℃ / h and crystallize to 40℃. The primary crystallized sugar paste is centrifuged in the first centrifuge 13 to obtain crude inositol. The crude inositol enters the crude product dissolving tank 14 and is further dissolved into an inositol solution with a refractive index of 70%. Then, the crude inositol is recrystallized to 50℃ in the second crystallizing kettle 15 at a cooling rate of 2℃ / h. The recrystallized sugar paste is sequentially centrifuged in the second centrifuge 16, hot-air dried at 80℃ in the hot-air drying tank 17, and cold-air dried at 30℃ in the cold-air fluidized bed 18 to obtain the desired inositol crystal F product.

[0043] According to the method in GB1903.42-2020, the purity of inositol crystal F product was measured to be 99.68%, and the other indicators all met the national standard requirements. Example 4

[0044] The fourth embodiment of the method for preparing high-purity inositol using corn steep liquor of the utility model comprises the following steps:

[0045] Step 41, adding an appropriate amount of lime milk suspension B to the corn syrup supernatant A with a refractive index of 45% in the precipitation tank 1, adjusting the pH of the liquid in the precipitation tank 1 to 5.34 to precipitate calcium phytate, and filtering through the first plate and frame filter 2 after the precipitation is complete to obtain a calcium phytate filter cake; then completely dissolving the obtained calcium phytate filter cake in the fitin dissolution tank 3 to obtain liquid phytic acid after complete dissolution, adding dilute hydrochloric acid solution C to adjust the pH of the liquid phytic acid in the fitin dissolution tank 3 to 1.83, and determining the concentration of the liquid phytic acid by colorimetry to be 52.08 g / L.

[0046] Step 42, the obtained liquid phytic acid is passed into the enzymolysis tank 4, phytase is added in an amount of 10wt%, the system temperature T=55°C and pH=3.0 are adjusted, and enzymolysis is performed for 6h to obtain inositol enzymolysis solution. The inositol concentration in the enzymolysis solution is determined by high performance liquid chromatography to be 14.03g / L, and the phytic acid enzymolysis conversion rate of this step is calculated to be 98.8%.

[0047] Step 43, passing the inositol hydrolyzate into the neutralization tank 5, adding an appropriate amount of lime milk suspension B to the inositol hydrolyzate in the neutralization tank 5 to precipitate phosphate, filtering through the second plate and frame filter 6 to remove the phosphate precipitate, and then passing the filtered hydrolyzate through the nanofiltration system 7, the first evaporator 8, the decolorization tank 9, the ion exchange column 10, and the second evaporator 11 in sequence to obtain an inositol concentrate with a conductivity of 16.55 μs / cm and a refractive index of 70%; then the obtained inositol concentrate is passed into the first crystallization kettle 12 and heated at 0.5°C. / h and cooled to 45°C for crystallization. The obtained primary crystallized sugar paste is centrifuged in the first centrifuge 13 to obtain crude inositol. The crude inositol enters the crude product dissolving tank 14 and is further dissolved into an inositol solution with a refractive index of 70%. Then, it is recrystallized to 40°C in the second crystallizing kettle 15 at a cooling rate of 1.5°C / h. The obtained recrystallized sugar paste is sequentially centrifuged in the second centrifuge 16, hot-air dried at 80°C in the hot-air drying tank 17, and cold-air dried at 30°C in the cold-air fluidized bed 18 to obtain the desired inositol crystal F product.

[0048] According to the method in GB1903.42-2020, the purity of the inositol crystal F product was measured to be 99.95%, and the other indicators all met the national standard requirements. The test results of the above examples were compared to obtain Table 1.

[0049] Table 1 Comparison of test results of Example 1 to Example 4

[0050] category Phytate enzymatic conversion rate / % Purity of inositol crystal product / % Example 1 98.1 99.82 Example 2 97.4 99.75 Example 3 97.8 99.68 Example 4 98.8 99.95

[0051] Through the analysis of the above examples, it can be seen that after the corn steep liquor is treated by the method of the present invention, not only can liquid phytic acid be quickly obtained, but also an enzymatic hydrolysis conversion rate of >98% can be achieved, and the purity of the prepared inositol specific product is >99.5%.

[0052] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions and improvements made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. A system for preparing high-purity inositol using corn steep liquor, characterized in that: The invention comprises a precipitation tank, a first plate-frame filter, a fitin dissolving tank, an enzymolysis tank, a neutralization tank, a second plate-frame filter, a nanofiltration system, a first evaporator, a decolorization tank, an ion exchange column, a second evaporator, a first crystallization kettle, a first centrifuge, a crude product dissolving tank, a second crystallization kettle, a second centrifuge, a hot air drying tank and a cold air fluidized bed, which are sequentially connected through pipelines; a feed port for corn supernatant and a feed port for lime milk suspension are respectively arranged on the precipitation tank; a discharge end of a calcium phytate filter cake is arranged on the first plate-frame filter; a feed port for a dilute hydrochloric acid solution is arranged on the fitin dissolving tank; the feed end of the fitin dissolving tank is connected to the discharge end of the calcium phytate filter cake; and a feed port for phytase is arranged on the enzymolysis tank. A feed port for lime milk suspension is provided on the neutralization tank, a discharge end for filtrate is provided on the second plate and frame filter, the feed end of the nanofiltration system is connected with the discharge end of the filtrate through a pipeline, a discharge end for permeate is provided on the nanofiltration system, the discharge end for permeate is connected with the feed end of the first evaporator, a discharge end for primary crystallized massecuite is provided on the first centrifuge, a feed port for purified water is provided on the crude product dissolving tank, the feed end of the crude product dissolving tank is connected with the discharge end of primary crystallized massecuite, a discharge end for recrystallized massecuite is provided on the second centrifuge, the feed end of the hot air drying tank is connected with the discharge end of the recrystallized massecuite, and the material discharged from the discharge end of the cold air fluidized bed is the desired inositol crystal product.

2. The system for preparing high-purity inositol using corn steep liquor as claimed in claim 1, characterized in that: The first plate-and-frame filter is provided with a filtrate discharge end, and the filtrate discharge end is connected with a feed port of the sedimentation tank through a pipeline.

3. The system for preparing high-purity inositol using corn steep liquor as claimed in claim 1, characterized in that: The first centrifuge is provided with a discharge port for the first mother liquid, and the discharge port for the first mother liquid is connected with a feed port of the second evaporator through a pipeline.

4. The system for preparing high-purity inositol using corn steep liquor as claimed in claim 1, characterized in that: The second centrifuge is provided with a discharge port for the second mother liquor, and the discharge port for the second mother liquor is connected with a feed port of the crude product dissolving tank through a pipeline.

Images