CN112176004A - Production method of citric acid - Google Patents
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Abstract
The invention relates to the field of microbial fermentation, and discloses a production method of citric acid. The method comprises the following steps: (1) pretreating raw materials; (2) mixing slurry; (3) liquefying; (4) fermenting; (5) separating and purifying the citric acid; wherein titanium dioxide is added in any one or more of steps (1) to (4). The method provided by the invention is characterized in that titanium dioxide is added in a certain proportion in the process of producing citric acid by fermenting biomass serving as a raw material, aspergillus niger bacteria balls are reduced and the specific surface area is increased in the stirring process, and meanwhile, the toxin contained in a culture medium is adsorbed, so that the mass transfer performance of the culture medium is improved, the cell activity is enhanced, and the speed of the material entering and exiting cells is increased, thereby achieving the purpose of accelerating the metabolic cycle of aspergillus niger, further shortening the fermentation period, saving the energy consumption, improving the productivity and reducing the production cost.
Description
Technical Field
The invention relates to the field of microbial fermentation, in particular to a method for accelerating the metabolism of aspergillus niger in the production process of citric acid by taking titanium dioxide as a dispersion grinding accelerator.
Background
Citric acid (also known as citric acid) is a tricarboxylic acid compound, is easily soluble in water, non-toxic, odorless, has strong sour taste, is an important multifunctional organic acid, and is widely applied to the fields of food, medicine, chemical industry and the like. Citric acid is also the edible organic acid with the greatest yield and consumption in the world today, with its demand increasing at a rate of 5% per year, with widespread use in emerging industrial fields. With the increasing demand year by year, the improvement of citric acid fermentation efficiency becomes a new research subject, and the factor for limiting the increase of citric acid is analyzed from the perspective of fermentation period, and the influence brought by the change of thallus volume is elaborated.
Aspergillus niger is one of the safest species identified by FDA in the United states and is GRAS qualified, and its colony gradually changes from white to brown, the spore area is black, and the colony is villous and has irregular edges. The hyphae have septum and branch, are multicellular mycelium, are colorless or colored, have podocytes, grow one or two layers of small peduncles from the apical sac, and grow a string of conidia at the apical of the small peduncles.
The production process of the citric acid mainly comprises the steps of crushing raw materials, mixing pulp, liquefying, fermenting, extracting and drying, and the final product is the citric acid. In the citric acid fermentation process, the metabolism speed of thalli is gradually reduced along with the accumulation of acidity and the aggregation of colonies, the consumption of a culture medium is slower and slower, and the fermentation period is longer. Therefore, in the normal citric acid fermentation process, the later metabolic speed is very slow, and only the fermentation period can be prolonged in order to improve the utilization rate of the culture medium.
According to investigation, the currently common metabolism accelerating method has the advantages that a culture medium is optimized or a fermentation process is adjusted, but the metabolism of Aspergillus niger is accelerated, the acid production is reduced or the cost is increased, in addition, a new strain is developed, and the method has poor stability and certain risks.
Disclosure of Invention
The invention aims to solve the problems of reduction of thallus metabolism speed and lengthening of fermentation period along with acidity accumulation and colony aggregation in the citric acid fermentation process, and provides a citric acid production method.
The invention provides a production method of citric acid, which comprises the following steps:
(1) pretreating raw materials;
(2) mixing slurry;
(3) liquefying;
(4) fermenting;
(5) separating and purifying the citric acid;
wherein titanium dioxide is added in any one or more of steps (1) to (4).
Preferably, the titanium dioxide has a particle size of 1 μm to 2000. mu.m, preferably 10 μm to 1000. mu.m.
Preferably, the titanium dioxide is added in an amount of 5 to 50kg/t dry basis, preferably 10 to 40kg/t dry basis.
Preferably, titanium dioxide is added in any one or more of said steps (2) to (4), preferably at least in step (2).
The method for accelerating the metabolism of the aspergillus niger in the citric acid production process by taking the titanium dioxide as the dispersion grinding accelerator can reduce the bacterial balls, increase the specific surface area, improve the mass transfer performance of a culture medium and accelerate the speed of material entering and exiting cells, thereby achieving the purpose of accelerating the metabolism cycle of the aspergillus niger, further shortening the fermentation period, saving the energy consumption, improving the productivity and reducing the production cost.
Detailed Description
The following describes in detail specific embodiments of the present invention. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
In the present invention, the particle size or particle size range of the material means that the material in the particle size range accounts for more than 90% of the total mass of the material, for example, the particle size of the treated material is 1000 μm to 2000 μm, the particle size in the treated material is more than 90% of the particle size in the range, and the particle size of the material can be determined by sieving.
The production method of citric acid provided by the invention comprises the following steps:
(1) pretreating raw materials;
(2) mixing slurry;
(3) liquefying;
(4) fermenting;
(5) separating and purifying the citric acid;
wherein titanium dioxide is added in any one or more of steps (1) to (4).
In the invention, in the citric acid production process, titanium dioxide in a certain proportion is added as an accelerator for catalytic adsorption, so that hypha winding can be reduced, the bacteria balls can be reduced, the specific surface area can be increased, harmful toxins can be adsorbed, the environment of a culture medium can be improved, the mass transfer performance of the culture medium can be improved, the speed of the material entering and exiting cells can be accelerated, and the aim of accelerating the metabolic cycle of Aspergillus niger can be realized.
In the present invention, the particle size of the titanium dioxide can be selected from a wide range, and may be 1 μm to 2000. mu.m, for example, 1 μm, 6.5. mu.m, 10. mu.m, 23. mu.m, 38. mu.m, 48. mu.m, 58. mu.m, 75. mu.m, 90. mu.m, 106. mu.m, 120. mu.m, 150. mu.m, 180. mu.m, 250. mu.m, 300. mu.m, 550. mu.m, 600. mu.m, 1000. mu.m, 1700. mu.m, 2000. mu.m, or any range between two points, preferably 10 μm to 1000. mu.m, and more preferably 75. mu.m to 250. mu.
The inventor of the invention finds that the titanium dioxide with larger grain diameter can cause the bacterial balls and the bacteria to be excessively damaged to influence the bacteria reproduction, the equipment is seriously abraded, and the titanium dioxide can be coupled to form a complex compound when the grain diameter is smaller, so that the bacteria growth and reproduction are not utilized.
In the present invention, the amount of the titanium dioxide to be added may be selected from a wide range, and specifically may be 5 to 50kg/t of dry raw material, for example, 5kg/t of dry raw material, 10kg/t of dry raw material, 15kg/t of dry raw material, 20kg/t of dry raw material, 25kg/t of dry raw material, 30kg/t of dry raw material, 35kg/t of dry raw material, 40kg/t of dry raw material, 45kg/t of dry raw material, 50kg/t of dry raw material, or any value therebetween, preferably 10 to 40kg/t of dry raw material.
The inventor of the present invention found that when the amount of titanium dioxide added is larger or smaller than the above range, the osmotic pressure of the culture medium is too high, which may cause abnormal metabolism of the bacterial cells or cause no desired effect.
In the present invention, titanium dioxide of different particle sizes can be obtained by conventional technical means such as pulverization, sieving, and the like.
In the present invention, the dry-based raw material is dry matter contained in the raw material, and the dry-based raw material mass can be obtained by a routine experiment means, for example, the dry-based raw material mass ratio of the raw material can be determined by drying the raw material, and then the dry-based raw material mass is calculated according to the raw material mass. Specifically, the raw material may be dried in an oven at 105 ℃ until a constant weight, which is the weight of dry matter.
In the present invention, titanium dioxide may be added in any one or several of the steps (2) to (4), preferably at least in step (2). The inventors of the present application found in experiments that the beneficial effects, for example, acceleration of metabolic rate, shortening of fermentation period, increase of acidity and conversion rate, etc., can be further improved by adding titanium dioxide in step (2).
In the present invention, the raw material may be one or more of a starch raw material, a saccharide raw material, and a cellulosic raw material; preferably, the starch raw material is one or more of corn, rice, wheat, sorghum, potato, sweet potato, jerusalem artichoke and cassava, the saccharide raw material is one or more of sugarcane juice, molasses, sweet sorghum juice, beet juice and syrup, and the fiber raw material is one or more of wheat straw, rice straw, corn straw and energy grass. Wherein the energy grass can be sweet sorghum, switchgrass, miscanthus crops, and the like. The starch raw material is subjected to crushing treatment, the cellulose raw material is subjected to crushing, steam explosion or cooking and acid-base neutralization treatment, and the saccharide raw material is subjected to dilution or acid-base neutralization treatment.
In the present invention, none of the steps (1) to (5) is particularly limited, and any conventional method in the art is applicable to the present invention.
In the present invention, the purpose of the pretreatment of the raw material is to treat the raw material so that the raw material is in a form easily utilized by microorganisms, thereby promoting the progress of the fermentation process. Therefore, the methods conventionally used in the art for the purpose of the pretreatment of the above-mentioned raw materials are all applicable to the present invention. Generally, the feedstock pretreatment may include dilution, comminution, steam explosion, cooking, or acid-base neutralization; the granularity of the pretreated material can be 1.25-4000 micrometers; preferably 500 μm to 3000 μm, more preferably 1000 μm to 2500 μm. When the granularity of the processed raw material is larger than the range, the liquefaction time can be prolonged, and when the granularity of the processed raw material is smaller than the range, the viscosity of the material is too high, so that the liquefaction and fermentation processes are influenced.
In the present invention, the process of size mixing may include: adding water to the product obtained by the raw material pretreatment and mixing with slurry; wherein the material-water ratio is 1:1-1:20, preferably 1:2-1: 10; the temperature is 25 to 80 ℃, preferably 30 to 75 ℃, and more preferably 40 to 65 ℃. Wherein, the size mixing process can also comprise a step of adjusting pH, and the adjusted pH is 3-8, preferably 4-7, and more preferably 5-7.
In the invention, the material-water ratio involved in the slurry mixing process is the mass ratio of the raw materials to the water.
In the present invention, the purpose of the liquefaction is to convert the pretreated material into fermentable sugars, resulting in a mash. Therefore, any method conventionally used in the art to achieve the purpose of the liquefaction treatment of the present invention is applicable to the present invention. Specifically, the process of liquefying may include: adding amylase into the product obtained by size mixing for liquefaction, wherein the addition amount of the amylase is 10-80U/g of dry base raw material, and preferably 15-60U/g of dry base raw material; the liquefaction temperature is 55-120 ℃, preferably 70-105 ℃, and the liquefaction pH is 3-8, preferably 4-7; the liquefaction time is 0.1 to 16 hours, preferably 0.2 to 10 hours, and more preferably 0.5 to 5 hours.
In the present invention, the fermentation step is intended to produce citric acid by fermenting the mash obtained after the liquefaction treatment described above with Aspergillus niger. Therefore, methods conventionally used in the art to achieve the fermentation object of the present invention are applicable to the present invention. Specifically, the process of fermentation may include: inoculating a strain into a product obtained in the liquefaction process for fermentation; the amount of the inoculated strain can be selected within a wide range, and may be, for example, 0.1 to 5kg/t dry basis material, preferably 0.5 to 4kg/t dry basis material, and more preferably 0.1 to 3kg/t dry basis material. The bacterial species may be present in the form of a spore powder. The pH may be 2 to 7, preferably 3 to 6, the temperature may be 10 to 60 ℃, preferably 25 to 40 ℃ and the time may be 0.1 to 10 days, preferably 1 to 8 days, and more preferably 2 to 5 days.
In the present invention, the fermentation process may be one of batch fermentation, continuous fermentation, and semi-continuous fermentation.
In the present invention, the purpose of the separation and purification process of citric acid is to extract citric acid from the citric acid mother liquor obtained by fermentation. Therefore, any method conventionally used in the art which can achieve the object of the separation and purification treatment of the present invention is suitable for the present invention. Specifically, the separation and purification process of the citric acid may include: and sequentially neutralizing, acidolyzing, decolorizing, concentrating, crystallizing and centrifugally drying the product obtained by fermentation to obtain the anhydrous citric acid.
The present invention will be described in detail below by way of examples.
In the following examples, the titanium dioxide is available from Shanghai William industries, Inc.
The Aspergillus niger is purchased from national standard product net, and the model is Aspergillus niger 98003.
DE value%: reducing sugars (calculated as glucose) are a percentage of the dry matter of the syrup.
Acidity: the number of milligrams of potassium hydroxide (KOH) required to neutralize 1 gram of chemical was determined by the method of GB 1987-2007 food additive citric acid.
Conversion rate: namely, the conversion rate of citric acid (%) (concentration of citric acid fermentation broth x volume of citric acid fermentation broth/weight of total sugar) × 100%, wherein the concentration of citric acid fermentation broth is acidity.
Yield of citric acid (yield of citric acid actually obtained/theoretical amount obtained) × 100%.
In the following examples, three replicates were performed and the results obtained were averaged.
Example 1
This example illustrates the method of accelerating Aspergillus niger metabolism in the citric acid production process provided by the present invention
(1) Weighing 1kg of corn flour, wherein the particle size of the corn flour is 1000-2000 mu m.
(2) Mixing corn flour and 5kg of water, and then carrying out size mixing in a circulating water bath, wherein the size mixing temperature is 60 ℃, and the size mixing time is 40 min.
(3) Adjusting pH of the product obtained by size mixing to about 6 with sodium hydroxide, adding amylase for enzymolysis and liquefaction, wherein the addition amount of the amylase is 20U/g dry base corn flour, the enzymolysis temperature is 90 ℃, and the time is 1 h.
(4) And mixing the liquefied product with a certain proportion of water to obtain a fermentation medium with a DE value of 18%. Inoculating the Aspergillus niger seed liquid into a fermentation culture medium, wherein the inoculation amount is 0.2g, the fermentation pH is 6, the temperature is 35 ℃, and the fermentation is finished when the reducing sugar concentration of the fermentation culture medium is lower than 0.5%.
(5) Extracting, neutralizing, acidolyzing, decolorizing, concentrating, crystallizing, centrifuging, and oven drying to obtain anhydrous citric acid.
Titanium dioxide with the particle size of 75-250 mu m is added in the step (2), and the addition amount is 30 g.
The changes in the parameters during liquefaction and fermentation were recorded and the results are shown in table 1.
Example 2
This example illustrates the method of accelerating Aspergillus niger metabolism in the citric acid production process provided by the present invention
(1) 1kg of dried potato powder is crushed and sieved to obtain a material with the particle size of 1000-2000 mu m.
(2) Adding 2kg water into the pulverized powder, and adjusting pH to about 4.5 at 50 deg.C in a circulating water bath for 1 hr.
(3) Adding amylase for enzymolysis and liquefaction, wherein the addition amount of the amylase is 30U/g of dried basic potatoes, the temperature is 80 ℃, the pH value is about 4.5, and the time is 40 min.
(4) And mixing the liquefied product with a certain proportion of water to obtain a fermentation medium with a DE value of 18%. Inoculating the Aspergillus niger seed liquid into a fermentation culture medium, wherein the inoculation amount is 1g, the fermentation pH is 4.5, the temperature is 35 ℃, and the fermentation is finished when the reducing sugar concentration of the fermentation culture medium is lower than 0.5%.
(5) Extracting, neutralizing, acidolyzing, decolorizing, concentrating, crystallizing, centrifuging, and oven drying to obtain anhydrous citric acid.
Titanium dioxide powder having a particle size of 75 μm to 250 μm was added in an amount of 35g in step (4).
The changes in the parameters during liquefaction and fermentation were recorded and the results are shown in table 1.
Example 3
This example illustrates the method of accelerating Aspergillus niger metabolism in the citric acid production process provided by the present invention
(1) 1kg of corn straws are taken and crushed, the granularity of the crushed material is required to be 1200-2000 mu m, and then the crushed material is subjected to steam explosion treatment.
(2) Adding 10kg of water into the treated material, and carrying out size mixing in a circulating water bath for 1h, wherein the size mixing temperature is 75 ℃, and the pH value is 5.
(3) Adding amylase for enzymolysis and liquefaction, wherein the addition amount of the amylase is 50U/g dry basis corn straw, the temperature is 90 ℃, the pH value is about 5, and the time is 4 hours.
(4) And mixing the liquefied product with a certain proportion of water to obtain a fermentation medium with a DE value of 18%. Inoculating the Aspergillus niger seed liquid into a fermentation culture medium, wherein the inoculation amount is 0.5g, the fermentation pH is 6, the temperature is 35 ℃, and the fermentation is finished when the reducing sugar concentration of the fermentation culture medium is lower than 0.5%.
(5) Extracting, neutralizing, acidolyzing, decolorizing, concentrating, crystallizing, centrifuging, and oven drying to obtain anhydrous citric acid.
Titanium dioxide powder with the particle size of 75-250 mu m is respectively added in the steps (2) and (4), and the addition amount is 10 g.
The changes in the parameters during liquefaction and fermentation were recorded and the results are shown in table 1.
Example 4
This example illustrates the effect of different steps of titanium dioxide addition
4-1, all the steps are the same as in example 1 except that the titanium dioxide addition step is the (3) th step.
4-2, all the steps are the same as in example 1 except that the titanium dioxide addition step is the (4) th step.
4-3, all the steps are the same as in example 1, except that the titanium dioxide addition step is the steps (2) and (4), and the amount of addition in both steps is 15 g.
The changes in the parameters during liquefaction and fermentation were recorded and the results are shown in table 1.
Example 5
This example is intended to illustrate the effect of adding titanium dioxide of different particle sizes
5-1, all the steps are the same as in example 1 except that the added particle size of titanium dioxide is 1 μm to 10 μm.
5-2, all the steps are the same as in example 1, except that the added particle size of titanium dioxide is 10 μm to 75 μm.
5-3, all the steps are the same as in example 1, except that the added particle size of titanium dioxide is 250 μm to 1000. mu.m.
5 to 4, all the steps are the same as in example 1 except that the added particle size of titanium dioxide is 1000 μm to 2000. mu.m.
The changes in the parameters during liquefaction and fermentation were recorded and the results are shown in table 1.
Example 6
This example is intended to illustrate the effect of different amounts of titanium dioxide
6-1, all the steps were the same as in example 1 except that the amount of titanium dioxide added was 5 g.
6-2, all the steps were the same as in example 1 except that the amount of titanium dioxide added was 10 g.
6-3, all the steps were the same as in example 1 except that the amount of titanium dioxide added was 40 g.
6-4, all the steps were the same as in example 1 except that the amount of titanium dioxide added was 50 g.
The changes in the parameters during liquefaction and fermentation were recorded and the results are shown in table 1.
Comparative example 1
All steps were the same as in example 1 except that no titanium dioxide was added.
The changes in the parameters during liquefaction and fermentation were recorded and the results are shown in table 1.
Comparative example 2
All the steps were the same as in example 1, except that the additive was montmorillonite having the same mass and the same particle size.
The changes in the parameters during liquefaction and fermentation were recorded and the results are shown in table 1.
Comparative example 3
All steps are the same as example 1, and the different additives are graphene with the same mass and the same particle size.
The changes in the parameters during liquefaction and fermentation were recorded and the results are shown in table 1.
Comparative example 4
All steps are the same as example 1, except that the additive is alumina with the same mass and the same particle size.
The changes in the parameters during liquefaction and fermentation were recorded and the results are shown in table 1.
TABLE 1
Comparing the data of examples 1 to 6 and comparative examples 1 to 4, it can be seen that the method of the present invention can shorten the fermentation period, increase the acidity, and increase the conversion rate, which indicates that the method of the present invention has the effect of accelerating the metabolic rate after adding titanium dioxide, and does not adversely affect the extraction and separation of citric acid.
As can be seen by comparing the data of the embodiment 1 with the data of the embodiment 4-1 to 3, the titanium dioxide is added in different steps to catalyze the fermentation process to cause different influences, the titanium dioxide is added in the liquefaction in the step (2) to further shorten the fermentation period, improve the acidity and improve the conversion rate, and the adverse influence on the extraction and separation of the citric acid is avoided.
Examples 1 and 5 demonstrate that the effect obtained when the particle diameter of titanium dioxide is in the range of 75 to 250 μm is superior to the effect obtained in the other range of 10 to 1000 μm, and further superior to the other range.
Examples 1 and 6 demonstrate that the best technical effect is obtained when the addition amount of titanium dioxide is 10-40kg/t dry base raw material, which is better than the technical effect which can be achieved by the ranges of 5-10kg/t dry base raw material and 40-50kg/t dry base raw material.
From the data in table 1, it can be seen that the addition of a proper amount of titanium dioxide with a proper particle size in the aspergillus niger fermentation process can accelerate the aspergillus niger metabolic rate, shorten the fermentation period, and improve the acidity and the citric acid conversion rate. The content of residual sugar can be reduced by adding titanium dioxide, and the adverse effect on the subsequent extraction and separation process of citric acid is avoided, so that the beneficial technical effect is achieved.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention. Including each of the specific features, are combined in any suitable manner. The invention is not described in detail in order to avoid unnecessary repetition. Such simple modifications and combinations should be considered within the scope of the present disclosure as well.
Claims (10)
1. A method of producing citric acid, the method comprising:
(1) pretreating raw materials;
(2) mixing slurry;
(3) liquefying;
(4) fermenting;
(5) separating and purifying the citric acid;
wherein titanium dioxide is added in any one or more of steps (1) to (4).
2. A process according to claim 1, wherein the titanium dioxide has a particle size of 1 μm to 2000 μm, preferably 10 μm to 1000 μm.
3. A process according to claim 1 or 2, wherein the titanium dioxide is added in an amount of 5-50kg/t dry basis, preferably 10-40kg/t dry basis.
4. The method according to claim 1, wherein titanium dioxide is added in any one or several of the steps (2) to (4), preferably at least in step (2).
5. The method of claim 1, wherein the feedstock is one or more of a starch feedstock, a saccharide feedstock, and a cellulosic feedstock;
preferably, the starch raw material is one or more of corn, rice, wheat, sorghum, potato, sweet potato, jerusalem artichoke and cassava, the saccharide raw material is one or more of sugarcane juice, molasses, sweet sorghum juice, beet juice and syrup, and the fiber raw material is one or more of wheat straw, rice straw, corn straw and energy grass.
6. The method of claim 1, wherein the process of sizing comprises: adding water into the product obtained in the step (1) and stirring the mixture; wherein the material-water ratio is 1:1-1:20, preferably 1:2-1: 10; the size mixing temperature is 25-80 ℃, preferably 30-75 ℃.
7. The method of claim 1, wherein the liquefying comprises: adding amylase into the product obtained in the step (2) for liquefaction; the addition amount of the amylase is 10-80U/g dry base raw material, preferably 15-60U/g dry base raw material.
8. The method according to claim 7, wherein the liquefaction temperature is 55-120 ℃, preferably 70-105 ℃; the liquefaction pH is between 3 and 8, preferably between 4 and 7; the liquefaction time is 0.1-16h, preferably 0.1-10 h.
9. The method of claim 1, wherein the process of fermenting comprises: inoculating a strain into the product obtained in the step (3) for fermentation; the strain inoculation amount is 0.1-5kg/t dry basis raw material, preferably 0.5-kg/t dry basis raw material; the pH value is 2-7, preferably 3-6; the temperature is 10-60 deg.C, preferably 25-40 deg.C.
10. The method of claim 1, wherein the separation and purification process of the citric acid comprises: and (4) sequentially neutralizing, acidolyzing, decoloring, concentrating, crystallizing, centrifuging and drying the product obtained in the step (4) to obtain the anhydrous citric acid.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2010115013A2 (en) * | 2009-04-02 | 2010-10-07 | University Of Florida Research Foundation Inc. | Functionalized fullerenes as antifungal agents |
| CN103074314A (en) * | 2012-12-31 | 2013-05-01 | 浙江大学 | Method for producing feruloyl esterase through Aspergillus niger fermentation |
| CN102876738B (en) * | 2012-09-14 | 2014-05-14 | 日照金禾博源生化有限公司 | Method for producing citric acid by using high-strength fermentation technology |
| EP3119900A2 (en) * | 2014-03-20 | 2017-01-25 | Technische Universität Berlin | Method for obtaining microbial secondary metabolites or derivatives thereof by heterologous expression of at least one synthetase of said secondary metabolites in filamentous fungi |
| CN106591399A (en) * | 2016-11-29 | 2017-04-26 | 浙江工商大学 | Biological preparation method of fermentation medium and rhamnolipid |
| CN107022582A (en) * | 2017-05-23 | 2017-08-08 | 山东大学 | A kind of Application way of sugar residue |
-
2019
- 2019-07-05 CN CN201910606002.8A patent/CN112176004B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2010115013A2 (en) * | 2009-04-02 | 2010-10-07 | University Of Florida Research Foundation Inc. | Functionalized fullerenes as antifungal agents |
| CN102876738B (en) * | 2012-09-14 | 2014-05-14 | 日照金禾博源生化有限公司 | Method for producing citric acid by using high-strength fermentation technology |
| CN103074314A (en) * | 2012-12-31 | 2013-05-01 | 浙江大学 | Method for producing feruloyl esterase through Aspergillus niger fermentation |
| EP3119900A2 (en) * | 2014-03-20 | 2017-01-25 | Technische Universität Berlin | Method for obtaining microbial secondary metabolites or derivatives thereof by heterologous expression of at least one synthetase of said secondary metabolites in filamentous fungi |
| CN106591399A (en) * | 2016-11-29 | 2017-04-26 | 浙江工商大学 | Biological preparation method of fermentation medium and rhamnolipid |
| CN107022582A (en) * | 2017-05-23 | 2017-08-08 | 山东大学 | A kind of Application way of sugar residue |
Non-Patent Citations (3)
| Title |
|---|
| CHONLADAPOKHUM 等: "New insight into the disinfection mechanism of Fusarium monoliforme and Aspergillus niger by TiO2 photocatalyst under low intensity UVA light", 《JOURNAL OF PHOTOCHEMISTRY AND PHOTOBIOLOGY B: BIOLOGY》 * |
| 李志啸 等: "纳米包装材料对双孢菇细胞壁代谢及品质的影响", 《食品科学》 * |
| 特里姆 等: "《工业催化剂的设计》", 31 May 1984, 化学工业出版社 * |
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