阅读说明：本技术 一种用于医药洛伐他汀的糖浆制备方法 (Preparation method of syrup for medical lovastatin ) 是由 周春海 于 2020-11-27 设计创作，主要内容包括：本发明公开了一种用于医药洛伐他汀的糖浆制备方法,包括以下步骤,(1)淀粉开浆、(2)调浆、(3)喷射液化、(4)维持柱保温、(5)糖化、(6)陶瓷膜过滤、(7)中转罐调PH、(8)MVR蒸发浓缩和(9)出料,采用本方案设计的一种用于医药洛伐他汀的糖浆制备方法生产的糖浆纯度高,糖浆中的油脂和蛋白质杂质含量低。(The invention discloses a preparation method of syrup for medical lovastatin, which comprises the following steps of (1) starch pulping, (2) size mixing, (3) jet liquefaction, (4) column heat preservation maintenance, (5) saccharification, (6) ceramic membrane filtration, (7) pH adjustment in a transfer tank, (8) MVR evaporation concentration and (9) discharging.)

1. A preparation method of syrup for medical lovastatin is characterized by comprising the following steps:

(1) starch slurry

a. Adding water with the water temperature of 60-66 ℃ into the corn starch raw material to prepare starch slurry, wherein the mass ratio of the corn starch: 1: 1-1.8 of water to obtain starch slurry;

(2) size mixing

b. Adding water into the starch slurry for size mixing, and mixing the concentration of the starch slurry into 14-20 DEG Be';

c. adjusting the pH of the starch slurry to 5.4-6.5;

d. adding high-temperature resistant amylase into the starch slurry, wherein the addition amount of the high-temperature resistant amylase is 0.1L/t of starch, and then filtering;

(3) jet liquefaction

e. Preheating an ejector to 115 ℃ by using steam with the pressure of 3.8-5 bar, and then spraying the starch slurry, wherein the spraying temperature is controlled to be 115-125 ℃;

f. adding high-temperature resistant amylase into the starch slurry, wherein the addition amount of the high-temperature resistant amylase is 0.045-0.2L enzyme/t starch;

(4) maintaining column thermal insulation

g. Starch slurry enters a maintaining column for laminar flow maintenance;

(5) saccharification

h. Maintaining laminar flow to reduce the temperature of the discharged starch slurry to 58-64 ℃ through a heat exchanger;

i. adjusting the pH value of the starch slurry to 4.2-4.6;

j. adding saccharifying enzyme into the starch slurry to obtain a saccharified solution;

k. carrying out enzyme deactivation treatment on the saccharified liquid, and then separating and filtering;

(6) ceramic membrane filtration

l, filtering the saccharified liquid by a ceramic membrane to obtain a filtered sugar liquid, wherein the transmittance of the filtered sugar liquid after filtering is required to be more than or equal to 97 percent;

(7) PH adjustment of transfer tank

m, transferring the filtered sugar solution into a transfer tank to adjust the pH value, and ensuring the normal operation of the subsequent processes;

(8) MVR evaporative concentration

n, evaporating and concentrating the filtered sugar solution in MVR, wherein the discharge concentration is required to be controlled to be 65.0-66.0%, the pH is required to be controlled to be 5.0-6.0, and the temperature is required to be 60-65 ℃ to obtain concentrated syrup;

(9) discharging

And o, transferring the concentrated syrup to an empty syrup storage tank.

2. The method for preparing syrup for medicinal lovastatin according to claim 1, wherein: in the step c, 4% food-grade dilute caustic soda is used for adjusting the pH value of the starch slurry to be 5.4-6.5.

3. The method for preparing syrup for medicinal lovastatin according to claim 1, wherein: in the step d, the high-temperature resistant amylase is alpha-amylase.

4. The method for preparing syrup for medicinal lovastatin according to claim 1, wherein: in the step g, the laminar flow maintaining time is 2.0-2.4 h.

5. The method for preparing syrup for medicinal lovastatin according to claim 1, wherein: in the step h, the laminar flow keeps the discharged material DE controlled at 18-20, and the iodine color reaction of starch slurry discharged by the laminar flow is purple to mauve.

6. The method for preparing syrup for medicinal lovastatin according to claim 1, wherein: in the step i, 5% diluted hydrochloric acid is used for adjusting the pH value to 4.2-4.6.

7. The method for preparing syrup for medicinal lovastatin according to claim 1, wherein: in the step j, the saccharifying enzyme is glucoamylase and composite saccharifying enzyme, and the adding amount is 13L of glucoamylase +5L of composite saccharifying enzyme/130 m³And (4) saccharifying liquid.

8. The method for preparing syrup for medicinal lovastatin according to claim 1, wherein: in the step I, the saccharification liquid is filtered by a ceramic membrane with the aperture of 0.1 micron.

9. The method for preparing syrup for medicinal lovastatin according to claim 1, wherein: in the step m, sodium carbonate and citric acid are used for adjusting the pH value, and the qualified pH value is adjusted to ensure that the pH value of the subsequent MVR evaporation, concentration and discharge material is 5.0-6.0.

10. The method for preparing syrup for medicinal lovastatin according to claim 1, wherein: and in the step o, the hollow syrup storage tank is sterilized by steam before sugar is put into the hollow syrup storage tank, the sterilization temperature is more than or equal to 82 ℃ and is maintained for more than 45 minutes, and after the hollow syrup storage tank is sterilized, the hollow syrup storage tank is naturally cooled to 60-65 ℃, and then concentrated syrup can be added.

Technical Field

The invention relates to a preparation method of syrup, in particular to a preparation method of syrup for medical lovastatin.

Background

The lovastatin is a lipid regulating drug, and is fermented by monascus fungi, starch dextrin is adopted as a fermentation substrate in conventional fermentation, dextrin is a starch primary hydrolysate, molecular chains of dextrin are different in length and larger in difference on a microscopic level, and for microbial fermentation, the molecules with different molecular chains cause different conversion and utilization periods, so that the lovastatin is not beneficial to stable industrial microbial culture. And the dextrin directly converted from the starch contains impurities such as grease, protein, particles and the like brought by the raw material starch, the impurities influence the purity of the system and are not beneficial to microbial metabolism, metabolic byproducts are easy to generate in the metabolic process, the content of soluble impurities in the system is increased, the yield of lovastatin is reduced, and the separation difficulty is increased.

Therefore, those skilled in the art have been devoted to the development of a process for the preparation of a syrup for the pharmaceutical lovastatin having a low content of impurities.

Disclosure of Invention

In view of the above defects in the prior art, the technical problem to be solved by the present invention is to provide a method for preparing a syrup for medical lovastatin, so as to solve the problems that the components in starch syrup in the prior art cannot satisfy the requirement for producing medical lovastatin by fermenting monascus, and the impurities such as oil, protein and the like in the syrup produced in the production process of starch syrup purification cannot satisfy the requirement for producing lovastatin by fermenting monascus.

The preparation method of the syrup for medical lovastatin is characterized by comprising the following steps of (1) starch pulping: a. adding water with the water temperature of 60-66 ℃ into the corn starch raw material to prepare starch slurry, wherein the mass ratio of the corn starch: 1: 1-1.8 of water to obtain starch slurry; (2) size mixing: b. adding water into the starch slurry for size mixing, and mixing the concentration of the starch slurry into 14-20 DEG Be'; c. adjusting the pH of the starch slurry to 5.4-6.5; d. adding high-temperature resistant amylase into the starch slurry, wherein the addition amount of the high-temperature resistant amylase is 0.1L/t of starch, and then filtering; (3) injection liquefaction: e. preheating an ejector to 115 ℃ by using steam with the pressure of 3.8-5 bar, and then spraying the starch slurry, wherein the spraying temperature is controlled to be 115-125 ℃; f. adding high-temperature resistant amylase into the starch slurry, wherein the addition amount of the high-temperature resistant amylase is 0.045-0.2L enzyme/t starch; (4) maintaining the column for heat preservation: g. starch slurry enters a maintaining column for laminar flow maintenance; (5) saccharification: h. maintaining laminar flow to reduce the temperature of the discharged starch slurry to 58-64 ℃ through a heat exchanger; i. adjusting the pH value of the starch slurry to 4.2-4.6; j. adding saccharifying enzyme into the starch slurry to obtain a saccharified solution; k. carrying out enzyme deactivation treatment on the saccharified liquid, and then separating and filtering; (6) ceramic membrane filtration: l, filtering the saccharified liquid by a ceramic membrane to obtain a filtered sugar liquid, wherein the transmittance of the filtered sugar liquid after filtering is required to be more than or equal to 97 percent; (7) adjusting the pH value in a transfer tank: m, transferring the filtered sugar solution into a transfer tank to adjust the pH value, and ensuring the normal operation of subsequent processes; (8) MVR evaporation and concentration: n, evaporating and concentrating the filtered sugar solution in MVR, wherein the discharge concentration is required to be controlled to be 65.0-66.0%, the pH is required to be controlled to be 5.0-6.0, and the temperature is required to be 60-65 ℃ to obtain concentrated syrup; (9) discharging: and o, transferring the concentrated syrup to an empty syrup storage tank.

Further, in the step c, 4% food-grade dilute caustic soda is used for adjusting the pH value of the starch slurry to be 5.4-6.5.

Further, in the step d, the high temperature resistant amylase is alpha-amylase.

Further, in the step g, the laminar flow maintaining time is 2.0-2.4 h.

Further, in the step h, the laminar flow keeps the discharging DE controlled at 18-20, and the iodine color reaction of the starch slurry discharged by the laminar flow is purple to mauve.

Further, in the step i, the pH is adjusted to be 4.2-4.6 by using 5% dilute hydrochloric acid.

Further, in the step j, the glucoamylase and the composite glucoamylase are used as the saccharifying enzyme, and the adding amount is 13L of glucoamylase +5L of composite glucoamylase/130 m³And (4) saccharifying liquid.

Further, in the step k, the enzyme deactivation treatment mode is to add hydrochloric acid to adjust the pH value to 3.2-3.8.

Further, in the step k, the enzyme deactivation treatment mode is to heat the saccharification liquid to 82-86 ℃ and keep the temperature for 1 hour or more to deactivate the enzyme.

Further, in the step l, the saccharification liquid is filtered by a ceramic membrane with the aperture of 0.1 micron.

Further, in the step m, sodium carbonate and citric acid are used for adjusting the pH value, and the qualified pH value is adjusted to ensure that the pH value of the subsequent MVR evaporation, concentration and discharge material is 5.0-6.0.

Further, in the step o, the hollow syrup storage tank is sterilized by steam before sugar is put into the hollow syrup storage tank, the sterilization temperature is more than or equal to 82 ℃ and is maintained for more than 45 minutes, and after the hollow syrup storage tank is sterilized, the hollow syrup storage tank is naturally cooled to 60-65 ℃, and then concentrated sugar liquor can be added.

The invention has the beneficial effects that: the syrup produced by the method has high purity, has low content of oil and protein impurities, and can meet the requirement of producing lovastatin by fermenting monascus.

Detailed Description

Example one

A preparation method of syrup for medical lovastatin is characterized by comprising the following steps:

(1) starch slurry

a. Adding water with the water temperature of 60 ℃ into the corn starch raw material to prepare starch slurry, wherein the mass ratio of the corn starch: and (3) obtaining starch slurry by using water as 1:1, filtering the starch slurry by using a 2mm screen filter, and removing ferromagnetic pollutants by using a strong magnetic iron removal filter.

(2) Size mixing

b. Adding water into the starch slurry for size mixing, and adjusting the concentration of the starch slurry to 14 degrees Be';

c. adjusting the pH value of the starch slurry to 5.4 by using 4% food-grade dilute caustic soda;

d. adding high-temperature resistant alpha-amylase into the starch slurry, wherein the addition amount of the high-temperature resistant alpha-amylase is 0.1L/t of starch, and then filtering.

(3) Jet liquefaction

e. Preheating the ejector to 115 ℃ by using steam with the pressure of 3.8bar, and then spraying the starch slurry, wherein the spraying temperature is controlled to be 115 ℃;

f. high temperature resistant amylase was added to the starch slurry at an amount of 0.045 enzyme/t starch.

(4) Maintaining column thermal insulation

g. And (4) allowing the starch slurry to enter a maintaining column for maintaining laminar flow, wherein the laminar flow maintaining time is 2.0 h.

(5) Saccharification

h. Controlling the discharging DE at 18 by laminar flow, cooling the discharged starch slurry to 58 ℃ by a heat exchanger, and requiring the iodine color reaction of the starch slurry discharged by the laminar flow to be purple to purple;

i. adjusting the pH value of the starch slurry to 4.2 by using 5% dilute hydrochloric acid;

j. adding saccharifying enzyme (glucoamylase and composite saccharifying enzyme) into starch slurry at an amount of 130m³Adding 13L of glucoamylase and 5L of compound glucoamylase into the saccharification liquid to obtain the saccharification liquid, wherein the saccharification liquid is qualified when the monosaccharide is more than or equal to 94%;

k. and (3) carrying out enzyme deactivation treatment on the saccharified liquid, wherein the enzyme deactivation treatment mode is that hydrochloric acid is added to adjust the pH value to 3.2 or the saccharified liquid is heated to 82 ℃ and is kept for 1 hour or more to deactivate enzyme, then cyclone separation and scraper filtration are carried out, and ferromagnetic pollutants are removed through a strong magnetic iron removal filter.

(6) Ceramic membrane filtration

And l, filtering the saccharified liquid by a 0.1-micron ceramic membrane to obtain a filtered sugar liquid, wherein the transmittance of the filtered sugar liquid after filtering is required to be more than or equal to 97 percent, and the filtered sugar liquid is clear and transparent and has no visible impurities.

(7) PH adjustment of transfer tank

And m, transferring the filtered sugar solution into a transfer tank to adjust the pH, adjusting the pH by using sodium carbonate and citric acid, adjusting the qualified pH value to ensure that the pH of the subsequent MVR evaporation concentration discharge is 5.0, and filtering by using 350-mesh spun silk.

(8) MVR evaporative concentration

n, evaporating and concentrating the filtered sugar solution in MVR, wherein the discharge concentration is required to be controlled to be 65.0%, the pH is required to be controlled to be 5.0, and the temperature is required to be 60 ℃ to obtain concentrated syrup;

(9) discharging

And (o) sterilizing the empty syrup storage tank by using steam before adding sugar, wherein the sterilization temperature is more than or equal to 82 ℃ and is kept for more than 45 minutes, naturally cooling the empty storage tank to 60 ℃ after the sterilization of the empty storage tank is finished, and then adding concentrated syrup.

Example two

A preparation method of syrup for medical lovastatin is characterized by comprising the following steps:

(1) starch slurry

a. Adding water with the water temperature of 66 ℃ into the corn starch raw material to prepare starch slurry, wherein the mass ratio of the corn starch: obtaining starch slurry by using water 1.8, filtering the starch slurry by using a 2mm screen filter, and removing ferromagnetic pollutants by using a strong magnetic iron removal filter.

(2) Size mixing

b. Adding water into the starch slurry for size mixing, and adjusting the concentration of the starch slurry to 20-degree Be';

c. adjusting the pH value of the starch slurry to 6.5 by using 4% food-grade dilute caustic soda;

d. adding high-temperature resistant alpha-amylase into the starch slurry, wherein the addition amount of the high-temperature resistant alpha-amylase is 0.1L/t of starch, and then filtering.

(3) Jet liquefaction

e. Preheating the ejector to 115 ℃ by using steam with the pressure of 5bar, and then spraying the starch slurry, wherein the spraying temperature is controlled at 125 ℃;

f. high temperature resistant amylase is added into the starch slurry, and the addition amount is 0.2L of enzyme/t of starch.

(4) Maintaining column thermal insulation

g. And (4) allowing the starch slurry to enter a maintaining column for maintaining laminar flow, wherein the laminar flow maintaining time is 2.4 h.

(5) Saccharification

h. Controlling the discharging DE at 20 by laminar flow, cooling the discharged starch slurry to 64 ℃ by a heat exchanger, and requiring the iodine color reaction of the starch slurry discharged by the laminar flow to be purple to purple;

i. adjusting the pH value of the starch slurry to 4.6 by using 5% dilute hydrochloric acid;

j. adding saccharifying enzyme (glucoamylase and composite saccharifying enzyme) into starch slurry at an amount of 130m³Adding 13L of glucoamylase and 5L of compound glucoamylase into the saccharification liquid to obtain the saccharification liquid, wherein the saccharification liquid is qualified when the monosaccharide is more than or equal to 94%;

k. and (3) carrying out enzyme deactivation treatment on the saccharified liquid, wherein the enzyme deactivation treatment mode is that hydrochloric acid is added to adjust the pH value to 3.8 or the saccharified liquid is heated to 86 ℃ and is kept for 1 hour or more to deactivate enzyme, then cyclone separation and scraper filtration are carried out, and ferromagnetic pollutants are removed through a strong magnetic iron removal filter.

(6) Ceramic membrane filtration

And l, filtering the saccharified liquid by a 0.1-micron ceramic membrane to obtain a filtered sugar liquid, wherein the transmittance of the filtered sugar liquid after filtering is required to be more than or equal to 97 percent, and the filtered sugar liquid is clear and transparent and has no visible impurities.

(7) PH adjustment of transfer tank

And m, transferring the filtered sugar solution into a transfer tank to adjust the pH, adjusting the pH by using sodium carbonate and citric acid, adjusting the qualified pH value to ensure that the pH of the subsequent MVR evaporation concentration discharge is 6.0, and filtering by using 350-mesh spun silk.

(8) MVR evaporative concentration

And n, evaporating and concentrating the filtered sugar solution in MVR, wherein the discharge concentration is required to be controlled to be 66.0%, the pH is required to be controlled to be 6.0, and the temperature is required to be 65 ℃, so that the concentrated syrup is obtained.

(9) Discharging

And (3) sterilizing the empty syrup storage tank by using steam before adding sugar, wherein the sterilization temperature is more than or equal to 82 ℃ and is kept for more than 45 minutes, naturally cooling the empty storage tank to 65 ℃ after the sterilization of the empty storage tank is finished, and then adding concentrated syrup.

EXAMPLE III

A preparation method of syrup for medical lovastatin is characterized by comprising the following steps:

(1) starch slurry

a. Adding water with the water temperature of 63 ℃ into the corn starch raw material to prepare starch slurry, wherein the mass ratio of the corn starch: and (3) obtaining starch slurry by adding water in a ratio of 1:5, filtering the starch slurry by using a 2mm screen filter, and removing ferromagnetic pollutants by using a strong magnetic iron removal filter.

(2) Size mixing

b. Adding water into the starch slurry for size mixing, and adjusting the concentration of the starch slurry to 17-degree Be';

c. adjusting the pH value of the starch slurry to 5.9 by using 4% food-grade dilute caustic soda;

d. adding high-temperature resistant alpha-amylase into the starch slurry, wherein the addition amount of the high-temperature resistant alpha-amylase is 0.1L/t of starch, and then filtering.

(3) Jet liquefaction

e. Preheating the ejector to 115 ℃ by using steam with the pressure of 4.4bar, and then spraying the starch slurry, wherein the spraying temperature is controlled at 110 ℃;

f. high temperature resistant amylase was added to the starch slurry at an amount of 0.145L enzyme/t starch.

(4) Maintaining column thermal insulation

g. And (4) allowing the starch slurry to enter a maintaining column for maintaining laminar flow, wherein the laminar flow maintaining time is 2.2 h.

(5) Saccharification

h. Controlling the discharging DE at 19 by laminar flow, cooling the discharged starch slurry to 61 ℃ by a heat exchanger, and requiring the iodine color reaction of the starch slurry discharged by laminar flow to be purple to purple red;

i. adjusting the pH value of the starch slurry to 4.4 by using 5% dilute hydrochloric acid;

j. adding saccharifying enzyme (glucoamylase and composite saccharifying enzyme) into starch slurry at an amount of 130m³Adding 13L glucoamylase and 5L composite glucoamylase into the saccharified solution to obtain saccharified solution, wherein monosaccharide in the saccharified solution is not less than 94% is qualified as saccharification;

k. and (3) carrying out enzyme deactivation treatment on the saccharified liquid, wherein the enzyme deactivation treatment mode is that hydrochloric acid is added to adjust the pH value to 3.5 or the saccharified liquid is heated to 84 ℃ and is kept for 1 hour or more to deactivate enzyme, then cyclone separation and scraper filtration are carried out, and ferromagnetic pollutants are removed through a strong magnetic iron removal filter.

(6) Ceramic membrane filtration

And l, filtering the saccharified liquid by a 0.1-micron ceramic membrane to obtain a filtered sugar liquid, wherein the transmittance of the filtered sugar liquid after filtering is required to be more than or equal to 97 percent, and the filtered sugar liquid is clear and transparent and has no visible impurities.

(7) PH adjustment of transfer tank

And m, transferring the filtered sugar solution into a transfer tank to adjust the pH, adjusting the pH by using sodium carbonate and citric acid, adjusting the qualified pH value to ensure that the pH of the subsequent MVR evaporation concentration discharge is 5.5, and filtering by using 350-mesh spun silk.

(8) MVR evaporative concentration

n, evaporating and concentrating the filtered sugar solution in MVR, wherein the discharge concentration is required to be controlled to be 65.5%, the pH is required to be controlled to be 5.5, and the temperature is required to be 63 ℃ to obtain concentrated syrup;

(9) discharging

And (3) sterilizing the empty syrup storage tank by using steam before adding sugar, wherein the sterilization temperature is more than or equal to 82 ℃ and is kept for more than 45 minutes, naturally cooling the empty storage tank to 63 ℃ after the sterilization of the empty storage tank is finished, and then adding concentrated syrup.

Example four

A preparation method of syrup for medical lovastatin is characterized by comprising the following steps:

(1) starch slurry

a. Adding water with the water temperature of 61 ℃ into the corn starch raw material to prepare starch slurry, wherein the mass ratio of the corn starch: and (3) obtaining starch slurry by adding water in a ratio of 1:2, filtering the starch slurry by using a 2mm screen filter, and removing ferromagnetic pollutants by using a strong magnetic iron removal filter.

(2) Size mixing

b. Adding water into the starch slurry for size mixing, and mixing the concentration of the starch slurry into 15-degree Be';

c. adjusting the pH value of the starch slurry to 5.5 by using 4% food-grade dilute caustic soda;

d. adding high-temperature resistant alpha-amylase into the starch slurry, wherein the addition amount of the high-temperature resistant alpha-amylase is 0.1L/t of starch, and then filtering.

(3) Jet liquefaction

e. Preheating the ejector to 115 ℃ by using steam with the pressure of 4bar, and then spraying the starch slurry, wherein the spraying temperature is controlled at 120 ℃;

f. high temperature resistant amylase is added into the starch slurry, and the addition amount is 0.08L enzyme/t starch.

(4) Maintaining column thermal insulation

g. And (4) allowing the starch slurry to enter a maintaining column for maintaining laminar flow, wherein the laminar flow maintaining time is 2.0 h.

(5) Saccharification

h. Controlling the discharging DE at 18 by laminar flow, cooling the discharged starch slurry to 60 ℃ by a heat exchanger, and requiring the iodine color reaction of the starch slurry discharged by the laminar flow to be purple to purple;

i. adjusting the pH value of the starch slurry to 4.5 by using 5% dilute hydrochloric acid;

j. adding saccharifying enzyme (glucoamylase and composite saccharifying enzyme) into starch slurry at an amount of 130m³Adding 13L of glucoamylase and 5L of compound glucoamylase into the saccharification liquid to obtain the saccharification liquid, wherein the saccharification liquid is qualified when the monosaccharide is more than or equal to 94%;

k. and (3) carrying out enzyme deactivation treatment on the saccharified liquid, wherein the enzyme deactivation treatment mode is that hydrochloric acid is added to adjust the pH value to 3.5 or the saccharified liquid is heated to 85 ℃ and is kept for 1 hour or more to deactivate enzyme, then cyclone separation and scraper filtration are carried out, and ferromagnetic pollutants are removed through a strong magnetic iron removal filter.

(6) Ceramic membrane filtration

And l, filtering the saccharified liquid by a 0.1-micron ceramic membrane to obtain a filtered sugar liquid, wherein the transmittance of the filtered sugar liquid after filtering is required to be more than or equal to 97 percent, and the filtered sugar liquid is clear and transparent and has no visible impurities.

(7) PH adjustment of transfer tank

And m, transferring the filtered sugar solution into a transfer tank to adjust the pH, adjusting the pH by using sodium carbonate and citric acid, adjusting the qualified pH value to ensure that the pH of the subsequent MVR evaporation concentration discharge is 5.5, and filtering by using 350-mesh spun silk.

(8) MVR evaporative concentration

n, evaporating and concentrating the filtered sugar solution in MVR, wherein the discharge concentration is required to be controlled to be 65.0%, the pH is required to be controlled to be 5.5, and the temperature is required to be 60 ℃ to obtain concentrated syrup;

(9) discharging

And (o) sterilizing the empty syrup storage tank by using steam before adding sugar, wherein the sterilization temperature is more than or equal to 82 ℃ and is kept for more than 45 minutes, naturally cooling the empty storage tank to 60 ℃ after the sterilization of the empty storage tank is finished, and then adding concentrated syrup.

EXAMPLE five

A preparation method of syrup for medical lovastatin is characterized by comprising the following steps:

(1) starch slurry

a. Adding water with the water temperature of 65 ℃ into the corn starch raw material to prepare starch slurry, wherein the mass ratio of the corn starch: and (3) obtaining starch slurry by adding water in a ratio of 1:6, filtering the starch slurry by using a 2mm screen filter, and removing ferromagnetic pollutants by using a strong magnetic iron removal filter.

(2) Size mixing

b. Adding water into the starch slurry for size mixing, and adjusting the concentration of the starch slurry to 18-degree Be';

c. adjusting the pH value of the starch slurry to 6 by using 4% food-grade dilute caustic soda;

d. adding high-temperature resistant alpha-amylase into the starch slurry, wherein the addition amount of the high-temperature resistant alpha-amylase is 0.1L/t of starch, and then filtering.

(3) Jet liquefaction

e. Preheating the ejector to 115 ℃ by using steam with the pressure of 4.5bar, and then spraying the starch slurry, wherein the spraying temperature is controlled at 120 ℃;

f. high temperature resistant amylase was added to the starch slurry at an amount of 0.145L enzyme/t starch.

(4) Maintaining column thermal insulation

g. And (4) allowing the starch slurry to enter a maintaining column for maintaining laminar flow, wherein the laminar flow maintaining time is 2.4 h.

(5) Saccharification

h. Controlling the discharging DE at 19 by laminar flow, cooling the discharged starch slurry to 63 ℃ by a heat exchanger, and requiring the iodine color reaction of the starch slurry discharged by laminar flow to be purple to purple;

i. adjusting the pH value of the starch slurry to 4.5 by using 5% dilute hydrochloric acid;

j. adding saccharifying enzyme (glucoamylase and composite saccharifying enzyme) into starch slurry at an amount of 130m³Adding 13L of glucoamylase and 5L of compound glucoamylase into the saccharification liquid to obtain the saccharification liquid, wherein the saccharification liquid is qualified when the monosaccharide is more than or equal to 94%;

k. and (3) carrying out enzyme deactivation treatment on the saccharified liquid, wherein the enzyme deactivation treatment mode is that hydrochloric acid is added to adjust the pH value to 3.6 or the saccharified liquid is heated to 85 ℃ and is kept for 1 hour or more to deactivate enzyme, then cyclone separation and scraper filtration are carried out, and ferromagnetic pollutants are removed through a strong magnetic iron removal filter.

(6) Ceramic membrane filtration

And l, filtering the saccharified liquid by a 0.1-micron ceramic membrane to obtain a filtered sugar liquid, wherein the transmittance of the filtered sugar liquid after filtering is required to be more than or equal to 97 percent, and the filtered sugar liquid is clear and transparent and has no visible impurities.

(7) PH adjustment of transfer tank

And m, transferring the filtered sugar solution into a transfer tank to adjust the pH, adjusting the pH by using sodium carbonate and citric acid, adjusting the qualified pH value to ensure that the pH of the subsequent MVR evaporation concentration discharge is 5.8, and filtering by using 350-mesh spun silk.

(8) MVR evaporative concentration

n, evaporating and concentrating the filtered sugar solution in MVR, wherein the discharge concentration is required to be controlled to be 66.0%, the pH is controlled to be 6, and the temperature is 65 ℃ to obtain concentrated syrup;

(9) discharging

And (3) sterilizing the empty syrup storage tank by using steam before adding sugar, wherein the sterilization temperature is more than or equal to 82 ℃ and is kept for more than 45 minutes, naturally cooling the empty storage tank to 65 ℃ after the sterilization of the empty storage tank is finished, and then adding concentrated syrup.

Table 1 shows the results of the tests of the different examples

The foregoing detailed description of the preferred embodiments of the invention has been presented. It should be understood that numerous modifications and variations could be devised by those skilled in the art in light of the present teachings without departing from the inventive concepts. Therefore, the technical solutions available to those skilled in the art through logic analysis, reasoning and limited experiments based on the prior art according to the concept of the present invention should be within the scope of protection defined by the claims.