CN113773407A - Clean production method of tremella polysaccharide - Google Patents
Clean production method of tremella polysaccharide Download PDFInfo
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- 241001506047 Tremella Species 0.000 title claims abstract description 60
- 150000004676 glycans Chemical class 0.000 title claims abstract description 39
- 229920001282 polysaccharide Polymers 0.000 title claims abstract description 39
- 239000005017 polysaccharide Substances 0.000 title claims abstract description 39
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 37
- 238000001704 evaporation Methods 0.000 claims abstract description 80
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 65
- 238000000034 method Methods 0.000 claims abstract description 39
- 230000008569 process Effects 0.000 claims abstract description 33
- 239000002699 waste material Substances 0.000 claims abstract description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 31
- 239000002351 wastewater Substances 0.000 claims abstract description 29
- 239000012528 membrane Substances 0.000 claims abstract description 23
- 238000001728 nano-filtration Methods 0.000 claims abstract description 23
- 238000004064 recycling Methods 0.000 claims abstract description 20
- 150000003839 salts Chemical class 0.000 claims abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract description 12
- 238000004821 distillation Methods 0.000 claims abstract description 11
- 239000012267 brine Substances 0.000 claims abstract description 9
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 9
- 230000001376 precipitating effect Effects 0.000 claims abstract description 8
- 238000004062 sedimentation Methods 0.000 claims description 44
- 239000010802 sludge Substances 0.000 claims description 34
- 239000000243 solution Substances 0.000 claims description 24
- 241001148470 aerobic bacillus Species 0.000 claims description 17
- 241001148471 unidentified anaerobic bacterium Species 0.000 claims description 17
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 16
- 239000010865 sewage Substances 0.000 claims description 15
- 238000001556 precipitation Methods 0.000 claims description 13
- 238000011084 recovery Methods 0.000 claims description 11
- 238000000926 separation method Methods 0.000 claims description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 9
- 238000000605 extraction Methods 0.000 claims description 9
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 9
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 9
- 239000001301 oxygen Substances 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
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- 238000006731 degradation reaction Methods 0.000 claims description 5
- 230000007062 hydrolysis Effects 0.000 claims description 5
- 238000006460 hydrolysis reaction Methods 0.000 claims description 5
- 239000012466 permeate Substances 0.000 claims description 5
- 239000011148 porous material Substances 0.000 claims description 5
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- MCMNRKCIXSYSNV-UHFFFAOYSA-N ZrO2 Inorganic materials O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 claims description 4
- 229910009474 Y2O3—ZrO2 Inorganic materials 0.000 claims description 3
- 230000007613 environmental effect Effects 0.000 claims description 2
- 230000003301 hydrolyzing effect Effects 0.000 claims description 2
- 241000894006 Bacteria Species 0.000 claims 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims 1
- 239000005416 organic matter Substances 0.000 claims 1
- 239000000126 substance Substances 0.000 claims 1
- 230000008020 evaporation Effects 0.000 abstract description 79
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 14
- 239000007787 solid Substances 0.000 abstract description 9
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 7
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 abstract description 7
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- 238000005265 energy consumption Methods 0.000 description 2
- 241000233866 Fungi Species 0.000 description 1
- 206010028980 Neoplasm Diseases 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08B—POLYSACCHARIDES; DERIVATIVES THEREOF
- C08B37/00—Preparation of polysaccharides not provided for in groups C08B1/00 - C08B35/00; Derivatives thereof
- C08B37/0003—General processes for their isolation or fractionation, e.g. purification or extraction from biomass
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Abstract
A clean production method of Tremella polysaccharide comprises extracting, separating solid and liquid, recycling waste residue, precipitating, recovering ethanol, and post-treating; the post-treatment is to carry out the post-treatment on the waste water with high salt content which is not evaporated, firstly, the high-salt waste water is filtered by a nanofiltration membrane, salt and water penetrate through the waste water, the trapped organic matters are further treated by an AO treatment process, and the brine passing through the nanofiltration membrane is concentrated and crystallized by reduced pressure distillation; the steam evaporated under reduced pressure is subjected to reboiling treatment for cyclic utilization; through the filtering technology of the nanofiltration membrane, the AO treatment process and the method of reduced pressure evaporation concentration crystallization, the produced wastewater can be autonomously treated to reach the discharge standard, the discharged COD is 170-177mg/L, the total nitrogen is 50-54mg/L, the total phosphorus is 1.1-1.6mg/L, the ammonia nitrogen is 1.0-1.8mg/L, and the pH is 7.70-7.75.
Description
Technical Field
The invention belongs to the technical field of edible fungus processing, and particularly relates to a clean production method of tremella polysaccharide.
Background
Tremella, also known as Tremella, is a traditional tonic in our country, and has multiple effects of promoting fluid production, invigorating qi, nourishing yin, nourishing brain, strengthening heart, etc. The tremella polysaccharide is heteropolysaccharide extracted and purified from the fruiting body, deep fermented spore liquid and other parts of tremella, has excellent physiological functions of improving human body's immunity, eliminating free radical, resisting tumor, lowering blood fat, lowering blood sugar, lowering cholesterol, etc. and possesses powerful water maintaining property and filming property, and may be used widely in health food, cosmetics, biomedicine and other industries.
The traditional production method of the tremella polysaccharide has the advantages of single energy utilization, low utilization rate and high consumption, and the produced wastewater is directly delivered to a sewage treatment plant for treatment, so that the water resource is wasted, and the production cost is also increased. The competition is also increasingly intense with the rise of more and more tremella polysaccharide producers. Therefore, it is very necessary to develop a production method of tremella polysaccharide which can fully utilize energy, reduce energy consumption and reduce wastewater discharge.
Disclosure of Invention
Aiming at the defects in the prior art, the invention aims to provide a clean production method of tremella polysaccharide, which can not only fully utilize energy and reduce energy consumption, but also protect the environment and reduce the discharge of waste water.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows:
a clean production method of tremella polysaccharide comprises the steps of extracting, carrying out solid-liquid separation, recycling waste residues, precipitating, recycling alcohol and carrying out post-treatment.
The extraction comprises the steps of firstly putting edible tremella without roots into water, then heating to 90-100 ℃ through steam, and then extracting for 40-60min to obtain extracted tremella and extracting solution.
Wherein the mass ratio of the tremella to the water is 1: 100-200.
Performing solid-liquid separation, namely performing solid-liquid separation on the extracted tremella and the extracting solution through a horizontal spiral centrifuge, and centrifuging to obtain solid waste residues and a precipitation solution;
the rotating speed of the horizontal spiral centrifuge is 3800-.
And (3) recycling the waste residues, heating the solid waste residues to 95-105 ℃ through steam, extracting for 4.5-5.5h, and spray drying to obtain the food-grade tremella polysaccharide.
And (4) recycling the waste residues, and crushing the solid waste residues to obtain the feed-grade tremella polysaccharide.
And precipitating, namely precipitating the extracting solution by using alcohol to obtain a precipitated material, then dehydrating the precipitated material for three times in a precipitation tank, recovering waste alcohol after the three-time dehydration is finished, then transferring the dehydrated material to a centrifugal machine for centrifugal treatment, and drying the material after the centrifugal treatment is finished to obtain a finished product.
The volume ratio of the extracting solution to the alcohol is 1:2.5-3.5, and the alcohol content of the alcohol is 55-60 degrees.
The alcohol content of the precipitated material is 68-72 degrees after the first dehydration, the alcohol content is 78-82 degrees after the second dehydration, and the alcohol content is 85-90 degrees after the third dehydration.
The centrifugation rate of the centrifugation treatment is 4800-5200rpm, and the water content after centrifugation is 45-50%.
And recovering the alcohol, namely centrifuging the waste alcohol after the three-time dehydration by using a disk centrifuge, separating the centrifuged solid particles from the waste alcohol, mixing the solid particles with a finished product, introducing the separated waste alcohol into a multi-effect evaporation tower for evaporation and purification to obtain the alcohol with the purity of 92-97 ℃, and performing post-treatment on the waste water with high salt content which is not evaporated.
The rotating speed of the disk centrifuge is 4800-5200 r/min.
The multiple-effect evaporation tower divide into a effect malleation evaporation tower, two effect atmospheric evaporation towers and three effect negative pressure evaporation towers, and the temperature of three evaporation towers reduces in proper order, and two effect atmospheric evaporation towers utilize the wine gas that a effect malleation evaporation tower evaporated to carry out the heating, and one effect malleation evaporation tower wine gas cooling condensation simultaneously, preheating of three effect negative pressure evaporation towers when advancing alcohol also goes on through the heat transfer.
The top temperature of the one-effect positive pressure evaporation tower is 127-129 ℃, and the bottom temperature of the one-effect positive pressure evaporation tower is 148.8-150 ℃; the tower top temperature of the two-effect normal pressure evaporation tower is 90-98 ℃, and the tower bottom temperature is 108-112 ℃; the tower top temperature of the triple-effect negative pressure evaporation tower is 50-55 ℃, and the tower bottom temperature is 60-65 ℃; the preheating temperature of the triple-effect negative pressure evaporation tower is 40-45 ℃.
And a part of the wine gas evaporated by the one-effect positive pressure evaporation tower is recycled, a part of the wine gas is reboiled, and the volume ratio of the wine gas for recycling to the wine gas for reboiling is 2: 2.8-3.2.
The temperature during the evaporation purification is 71-75 ℃.
The post-treatment is to carry out the post-treatment on the waste water with high salt content which is not evaporated, firstly, the high-salt waste water is filtered by a nanofiltration membrane, salt and water penetrate through the waste water, the trapped organic matters are further treated by an AO treatment process, and the brine passing through the nanofiltration membrane is concentrated and crystallized by reduced pressure distillation; the steam evaporated under reduced pressure is subjected to reboiling treatment for recycling.
The temperature in the reduced pressure distillation process is 71-75 ℃, and the pressure is 30-35 KPa.
The nanofiltration membrane is made of Y2O3-ZrO2And TiO2-ZrO2Of which the pore diameter is 4.5-5.5 nm.
The AO treatment process is to remove organic matters in sewage through anaerobic bacteria and aerobic bacteria, and reaches the discharge standard.
The AO treatment process comprises the following steps: introducing the trapped organic matters into a sewage tank, then introducing the organic matters into an adjusting tank to adjust the pH value to 6.8-7.2, hydrolyzing macromolecular organic matters into micromolecules in an anaerobic tower through anaerobic bacteria, wherein the hydrolysis time is 3-5h, then introducing the organic matters into an oxygen tank to degrade through aerobic bacteria, the degradation time is 3-5h, then introducing the organic matters into a sedimentation tank, the sedimentation time is 1-1.5h, the precipitator is polymeric ferric sulfate, and the purified water is discharged after sedimentation in the sedimentation tank.
In the AO treatment process, the trapped organic matters slowly flow in a sewage tank, an anaerobic tower, an oxygen tank and a sedimentation tank, and the daily treatment capacity of the organic matters is 200-220m3。
The dosage of the polymeric ferric sulfate is 100-110 kg/day.
The anaerobic bacteria are granular sludge strains, the aerobic bacteria are activated sludge, and the granular sludge strains and the activated sludge are purchased from Jiangxi water, environmental protection and science and technology Limited.
The sedimentation ratio of the granular activated sludge and the activated sludge is more than 20%, the sedimentation ratio needs to be detected periodically in the treatment process, and if the sedimentation ratio is lower than 20%, the granular activated sludge or the activated sludge needs to be supplemented until the sedimentation ratio is more than 20%.
The concentration of the saline water passing through the nanofiltration membrane is 20-25 g/L.
The clean production method of the tremella polysaccharide has the advantages that natural gas used in the method can be reused after being boiled again, the utilization rate of the natural gas is improved by 52.8%, and the recovery utilization rate of alcohol is 94.8%.
A clean production method of tremella polysaccharide is provided, wherein the AO treatment process in the method removes organic matters in water through anaerobic bacteria and aerobic bacteria to reach the discharge standard, the discharged COD is 170-177mg/L, the total nitrogen is 50-54mg/L, the total phosphorus is 1.1-1.6mg/L, the ammonia nitrogen is 1.0-1.8mg/L, and the pH is 7.70-7.75.
Compared with the prior art, the invention has the beneficial effects that:
(1) according to the clean production method of the tremella polysaccharide, the extracted solution of tremella is separated from the waste residues through the horizontal spiral centrifugal machine, the waste residues are further processed and can be used as feed after being crushed, the comprehensive conversion rate of raw materials is improved, and waste is avoided;
(2) according to the clean production method of the tremella polysaccharide, the alcohol and the materials are separated through centrifugation, the materials are recovered, the material loss is reduced, the conversion rate is improved, the alcohol recovery utilization rate is 94.8% after the separated waste alcohol is subjected to multiple times of evaporation and purification, and the continuous utilization of resources is realized;
(3) according to the clean production method of the tremella polysaccharide, the produced wastewater can be automatically treated by a filtering technology of a nanofiltration membrane, an AO treatment process and a method of reduced pressure evaporation concentration crystallization, so that the discharge standard is reached, the discharged COD is 177mg/L, the total nitrogen is 50-54mg/L, the total phosphorus is 1.1-1.6mg/L, the ammonia nitrogen is 1.0-1.8mg/L, and the pH is 7.70-7.75;
(4) according to the clean production method of the tremella polysaccharide, steam used for reduced pressure evaporation concentration can be fully utilized through steam reboiling, the reboiled steam is used for tremella extraction, a multiple-effect evaporation tower and reduced pressure evaporation concentration, the purpose of waste heat recycling is achieved, unnecessary energy loss is avoided, and the production cost is reduced;
(5) according to the clean production method of the tremella polysaccharide, disclosed by the invention, zero emission is achieved by treating and comprehensively utilizing waste residues, waste water and waste gas, and the method is an environment-friendly clean production method of the tremella polysaccharide; the recycling of alcohol and steam is realized, the excessive loss of resources and energy is avoided, the production cost is reduced, the enterprise can continuously produce, and the productivity is improved.
Drawings
Fig. 1 is a process flow diagram of a clean production method of tremella polysaccharide according to the present application.
Detailed Description
In order to more clearly understand the technical features, objects, and effects of the present invention, specific embodiments of the present invention will now be described.
Example 1
As shown in fig. 1, a clean production method of tremella polysaccharide comprises the following specific processes:
1. extraction: firstly, 75kg of edible tremella without roots is put into 8t of water, and then the tremella and the extracting solution are extracted for 40min after the temperature is raised to 90 ℃ through steam, so that the extracted tremella and the extracting solution are obtained.
2. Solid-liquid separation: performing solid-liquid separation on the extracted tremella and the extracting solution through a horizontal spiral centrifuge, and centrifuging to obtain solid waste residues and a precipitation solution;
the rotating speed of the horizontal spiral centrifuge is 4000 r/min.
3. And (3) recycling waste residues: and (3) heating the centrifuged solid waste residue to 100 ℃ by steam in a re-extraction mode, and extracting for 5 hours to obtain the food-grade tremella polysaccharide.
4. And (3) precipitation: precipitating the extracting solution with alcohol to obtain a precipitated material, wherein the volume ratio of the extracting solution to the alcohol is 1:3, the alcoholic strength of the alcohol is 55 degrees, then dehydrating the precipitated material in a precipitation tank for three times, recovering waste alcohol after the three times of dehydration, then transferring the dehydrated material into a centrifuge for centrifugal treatment, and drying the material after the centrifugal treatment to obtain a finished product.
The alcohol content of the precipitated material is 70 degrees after the first dehydration, 80 degrees after the second dehydration and 85 degrees after the third dehydration;
the centrifugation rate of the centrifugation treatment was 5000rpm, and the water content after centrifugation was 45%.
5. Alcohol recovery: centrifuging the waste alcohol after the third dehydration by using a disc centrifuge, separating the centrifuged solid particles from the waste alcohol, and mixing the solid particles with a finished product;
the rotating speed of the disc centrifuge is 5000 r/min.
Introducing the separated waste alcohol into a multi-effect evaporation tower for evaporation recovery to obtain alcohol with the purity of 95 degrees, and then carrying out post-treatment on the waste water with high salt content which is not evaporated;
the multiple-effect evaporation tower divide into a effect malleation evaporation tower, two effect atmospheric evaporation towers and three effect negative pressure evaporation towers, and the temperature of three evaporation towers reduces in proper order, and two effect atmospheric evaporation towers utilize the wine gas that a effect malleation evaporation tower evaporated to carry out the heating, and one effect malleation evaporation tower wine gas cooling condensation simultaneously, preheating of three effect negative pressure evaporation towers when advancing alcohol also goes on through the heat transfer.
The top temperature of the one-effect positive pressure evaporation tower is 127-129 ℃, and the bottom temperature of the one-effect positive pressure evaporation tower is 148.8-150 ℃; the tower top temperature of the two-effect normal pressure evaporation tower is 90-98 ℃, and the tower bottom temperature is 108-112 ℃; the tower top temperature of the triple-effect negative pressure evaporation tower is 50-55 ℃, and the tower bottom temperature is 60-65 ℃; the preheating temperature of the triple-effect negative pressure evaporation tower is 40 ℃.
And a part of the wine gas evaporated by the one-effect positive pressure evaporation tower is recycled, a part of the wine gas is reboiled, and the volume ratio of the wine gas for recycling to the wine gas for reboiling is 2: 3.
The temperature during the evaporation purification was 71 ℃.
6. And (3) post-treatment: when the waste water with high salt content which is not evaporated is subjected to post-treatment, the high-salt waste water is filtered by a nanofiltration membrane, salt and water permeate through the waste water, the trapped organic matters are further treated by an AO treatment process, and the brine passing through the nanofiltration membrane is subjected to concentration and crystallization treatment by reduced pressure distillation; the steam evaporated under reduced pressure is subjected to reboiling treatment for recycling.
The temperature in the reduced pressure distillation process is 71 ℃, and the pressure is 32 KPa.
The nanofiltration membrane is made of Y2O3-ZrO2The pore diameter is 5 nm.
The AO treatment process is to remove organic matters in sewage through anaerobic bacteria and aerobic bacteria, and reaches the discharge standard.
The AO treatment process comprises the following steps: the trapped organic matters are introduced into a sewage tank, then enter an adjusting tank to adjust the pH value to 7.0, then are hydrolyzed by anaerobic bacteria in an anaerobic tower to hydrolyze macromolecular organic matters into small molecules, the hydrolysis time is 3 hours, then the large molecular organic matters enter an oxygen tank to degrade the organic matters by aerobic bacteria, the degradation time is 3 hours, then the large molecular organic matters enter a sedimentation tank, the sedimentation time is 1 hour, a precipitator is polymeric ferric sulfate, and purified water is discharged after sedimentation in the sedimentation tank.
In the AO treatment process, the trapped organic matters slowly flow in a sewage tank, an anaerobic tower, an oxygen tank and a sedimentation tank, and the daily treatment capacity of the organic matters is 200m3。
The dosage of the polymeric ferric sulfate is 100 kg/day.
The anaerobic bacteria are granular sludge strains, and the aerobic bacteria are activated sludge.
The sedimentation ratio of the granular activated sludge and the activated sludge is 20%, the sedimentation ratio needs to be detected periodically in the treatment process, and if the sedimentation ratio is lower than 20%, the granular activated sludge or the activated sludge needs to be supplemented until the sedimentation ratio is more than 20%.
The concentration of the brine passing through the nanofiltration membrane is 20 g/L.
The COD of the purified water is 177mg/L, the total nitrogen is 54mg/L, the total phosphorus is 1.6mg/L, the ammonia nitrogen is 1.8mg/L, and the pH value is 7.75.
Example 2
As shown in fig. 1, a clean production method of tremella polysaccharide comprises the following specific processes:
1. extraction: firstly, 75kg of edible tremella without roots is put into 8t of water, and then the tremella and the extracting solution are obtained after the temperature is raised to 95 ℃ through steam and extracted for 50 min.
2. Solid-liquid separation: performing solid-liquid separation on the extracted tremella and the extracting solution through a horizontal spiral centrifuge, and centrifuging to obtain solid waste residues and a precipitation solution;
the rotating speed of the horizontal spiral centrifuge is 4000 r/min.
3. And (3) recycling waste residues: and crushing the solid waste residue after centrifugation in a re-extraction mode to obtain the feed-grade tremella polysaccharide.
4. And (3) precipitation: precipitating the extracting solution with alcohol to obtain a precipitated material, wherein the volume ratio of the extracting solution to the alcohol is 1:3, the alcoholic strength of the alcohol is 57 degrees, then dehydrating the precipitated material in a precipitation tank for three times, recovering waste alcohol after the three times of dehydration, then transferring the dehydrated material into a centrifuge for centrifugal treatment, and drying the material after the centrifugation to obtain a finished product.
The alcohol content of the precipitated material is 70 degrees after the first dehydration, 80 degrees after the second dehydration and 88 degrees after the third dehydration;
the centrifugation time of the centrifugation treatment is 30min, the centrifugation speed of the centrifuge is 5000rpm, and the water content after centrifugation is 45%.
5. Alcohol recovery: centrifuging the waste alcohol after the third dehydration by using a disc centrifuge, separating the centrifuged solid particles from the waste alcohol, and mixing the solid particles with a finished product;
the rotating speed of the disc centrifuge is 5000 r/min.
Introducing the separated waste alcohol into a multi-effect evaporation tower for evaporation recovery to obtain alcohol with the purity of 95 degrees, and then carrying out post-treatment on the waste water with high salt content which is not evaporated;
the multiple-effect evaporation tower divide into a effect malleation evaporation tower, two effect atmospheric evaporation towers and three effect negative pressure evaporation towers, and the temperature of three evaporation towers reduces in proper order, and two effect atmospheric evaporation towers utilize the wine gas that a effect malleation evaporation tower evaporated to carry out the heating, and one effect malleation evaporation tower wine gas cooling condensation simultaneously, preheating of three effect negative pressure evaporation towers when advancing alcohol also goes on through the heat transfer.
The top temperature of the one-effect positive pressure evaporation tower is 127-129 ℃, and the bottom temperature of the one-effect positive pressure evaporation tower is 148.8-150 ℃; the tower top temperature of the two-effect normal pressure evaporation tower is 90-98 ℃, and the tower bottom temperature is 108-112 ℃; the tower top temperature of the triple-effect negative pressure evaporation tower is 50-55 ℃, and the tower bottom temperature is 60-65 ℃; the preheating temperature of the triple-effect negative pressure evaporation tower is 43 ℃.
And a part of the wine gas evaporated by the one-effect positive pressure evaporation tower is recycled, a part of the wine gas is reboiled, and the volume ratio of the wine gas for recycling to the wine gas for reboiling is 2: 3.
The temperature during the evaporation purification was 73 ℃.
6. And (3) post-treatment: when the waste water with high salt content which is not evaporated is subjected to post-treatment, the high-salt waste water is filtered by a nanofiltration membrane, salt and water permeate through the waste water, the trapped organic matters are further treated by an AO treatment process, and the brine passing through the nanofiltration membrane is subjected to concentration and crystallization treatment by reduced pressure distillation; the steam evaporated under reduced pressure is subjected to reboiling treatment for recycling.
The temperature in the reduced pressure distillation process is 73 ℃, and the pressure is 32 KPa.
The nanofiltration membrane is made of TiO2-ZrO2The pore diameter is 5 nm.
The AO treatment process is to remove organic matters in sewage through anaerobic bacteria and aerobic bacteria, and reaches the discharge standard.
The AO treatment process comprises the following steps: the trapped organic matters are introduced into a sewage tank, then enter an adjusting tank to adjust the pH value to 7.3, then are hydrolyzed by anaerobic bacteria in an anaerobic tower to hydrolyze macromolecular organic matters into small molecules, the hydrolysis time is 4 hours, then the large molecular organic matters enter an oxygen tank to degrade the organic matters by aerobic bacteria, the degradation time is 4 hours, then the large molecular organic matters enter a sedimentation tank, the sedimentation time is 1.2 hours, a precipitator is polymeric ferric sulfate, and purified water is discharged after sedimentation in the sedimentation tank.
In the AO treatment process, the trapped organic matters slowly flow in a sewage tank, an anaerobic tower, an oxygen tank and a sedimentation tank, and the daily treatment capacity of the organic matters is 210m3。
The dosage of the polymeric ferric sulfate is 105 kg/day.
The anaerobic bacteria are granular sludge strains, and the aerobic bacteria are activated sludge.
The sedimentation ratio of the granular activated sludge and the activated sludge is 22%, the sedimentation ratio needs to be detected periodically in the treatment process, and if the sedimentation ratio is lower than 22%, the granular activated sludge or the activated sludge needs to be supplemented until the sedimentation ratio is higher than 22%.
The concentration of the brine passing through the nanofiltration membrane is 23 g/L.
The COD of the purified water is 173mg/L, the total nitrogen is 52mg/L, the total phosphorus is 1.4mg/L, the ammonia nitrogen is 1.2mg/L, and the pH value is 7.72.
Example 3
As shown in fig. 1, a clean production method of tremella polysaccharide comprises the following specific processes:
1. extraction: firstly, 75kg of edible tremella without roots is put into 8t of water, and then the tremella and the extracting solution are extracted for 60min after the temperature is raised to 100 ℃ through steam, so that the extracted tremella and the extracting solution are obtained.
2. Solid-liquid separation: performing solid-liquid separation on the extracted tremella and the extracting solution through a horizontal spiral centrifuge, and centrifuging to obtain solid waste residues and a precipitation solution;
the rotating speed of the horizontal spiral centrifuge is 4000 r/min.
3. And (3) recycling waste residues: and crushing the solid waste residue after centrifugation in a re-extraction mode to obtain the feed-grade tremella polysaccharide.
4. And (3) precipitation: precipitating the extracting solution with alcohol to obtain a precipitated material, wherein the volume ratio of the extracting solution to the alcohol is 1:3, the alcoholic strength of the alcohol is 60 degrees, then dehydrating the precipitated material in a precipitation tank for three times, recovering waste alcohol after the three times of dehydration, then transferring the dehydrated material into a centrifuge for centrifugal treatment, and drying the material after the centrifugal treatment to obtain a finished product.
The alcohol content of the precipitated material is 70 degrees after the first dehydration, 80 degrees after the second dehydration and 88 degrees after the third dehydration;
the centrifugation rate of the centrifugation treatment was 5000rpm, and the water content after centrifugation was 50%.
5. Alcohol recovery: centrifuging the waste alcohol after the third dehydration by using a disc centrifuge, separating the centrifuged solid particles from the waste alcohol, and mixing the solid particles with a finished product;
the rotating speed of the disc centrifuge is 5000 r/min.
Introducing the separated waste alcohol into a multi-effect evaporation tower for evaporation recovery to obtain alcohol with the purity of 95 degrees, and then carrying out post-treatment on the waste water with high salt content which is not evaporated;
the multiple-effect evaporation tower divide into a effect malleation evaporation tower, two effect atmospheric evaporation towers and three effect negative pressure evaporation towers, and the temperature of three evaporation towers reduces in proper order, and two effect atmospheric evaporation towers utilize the wine gas that a effect malleation evaporation tower evaporated to carry out the heating, and one effect malleation evaporation tower wine gas cooling condensation simultaneously, preheating of three effect negative pressure evaporation towers when advancing alcohol also goes on through the heat transfer.
The top temperature of the one-effect positive pressure evaporation tower is 127-129 ℃, and the bottom temperature of the one-effect positive pressure evaporation tower is 148.8-150 ℃; the tower top temperature of the two-effect normal pressure evaporation tower is 90-98 ℃, and the tower bottom temperature is 108-112 ℃; the tower top temperature of the triple-effect negative pressure evaporation tower is 50-55 ℃, and the tower bottom temperature is 60-65 ℃; the preheating temperature of the triple-effect negative pressure evaporation tower is 45 ℃.
And a part of the wine gas evaporated by the one-effect positive pressure evaporation tower is recycled, a part of the wine gas is reboiled, and the volume ratio of the wine gas for recycling to the wine gas for reboiling is 2: 3.
The temperature during the evaporation purification was 75 ℃.
6. And (3) post-treatment: when the waste water with high salt content which is not evaporated is subjected to post-treatment, the high-salt waste water is filtered by a nanofiltration membrane, salt and water permeate through the waste water, the trapped organic matters are further treated by an AO treatment process, and the brine passing through the nanofiltration membrane is subjected to concentration and crystallization treatment by reduced pressure distillation; the steam evaporated under reduced pressure is subjected to reboiling treatment for recycling.
The temperature in the reduced pressure distillation process is 75 ℃, and the pressure is 32 KPa.
The nanofiltration membrane is made of TiO2-ZrO2The pore diameter is 5 nm.
The AO treatment process is to remove organic matters in sewage through anaerobic bacteria and aerobic bacteria, and reaches the discharge standard.
The AO treatment process comprises the following steps: the trapped organic matters are introduced into a sewage tank, then enter an adjusting tank to adjust the pH value to 7.5, then are hydrolyzed by anaerobic bacteria in an anaerobic tower to hydrolyze macromolecular organic matters into small molecules, the hydrolysis time is 5 hours, then the large molecular organic matters enter an oxygen tank to degrade the organic matters by aerobic bacteria, the degradation time is 5 hours, then the large molecular organic matters enter a sedimentation tank, the sedimentation time is 1.5 hours, a precipitator is polymeric ferric sulfate, and purified water is discharged after sedimentation in the sedimentation tank.
In the AO treatment process, the trapped organic matters slowly flow in a sewage tank, an anaerobic tower, an oxygen tank and a sedimentation tank, and the daily treatment capacity of the organic matters is 220m3。
The dosage of the polymeric ferric sulfate is 110 kg/day.
The anaerobic bacteria are granular sludge strains, and the aerobic bacteria are activated sludge.
The sedimentation ratio of the granular activated sludge and the activated sludge is 25%, the sedimentation ratio needs to be detected periodically in the treatment process, and if the sedimentation ratio is lower than 25%, the granular activated sludge or the activated sludge needs to be supplemented until the sedimentation ratio is more than 25%.
The concentration of the brine passing through the nanofiltration membrane is 25 g/L.
The COD of the purified water is 170mg/L, the total nitrogen is 50mg/L, the total phosphorus is 1.1mg/L, the ammonia nitrogen is 1.0mg/L, and the pH value is 7.70.
Example 4
According to the clean production method of tremella polysaccharide described in embodiment 2, alcohol and heat used in production are counted by specific production examples:
adding 75kg edible Tremella with root removed into 8t water, and heating and maintaining at 360m3The heat released by natural gas combustion requires 25t of alcohol for centrifugate precipitation and 450m for alcohol evaporation3The heat released by the combustion of natural gas can recover 23.7t of alcohol, can produce 15t of high-salt waste water, can permeate 14.5t of waste water with salt content, and can be reduced pressure evaporated and concentrated to obtain 1085m3The heat released by the combustion of the natural gas is reboiled by a reboiler, thus saving 1000m3The utilization rate of the natural gas is improved by 52.8%, the recovery utilization rate of alcohol is 94.8%, the AO treatment process is to remove organic matters in water through anaerobic bacteria and aerobic bacteria, the emission standard is reached, the discharged COD is 173mg/L, the total nitrogen is 52mg/L, the total phosphorus is 1.4mg/L, the ammonia nitrogen is 1.2mg/L, and the pH value is 7.72.
All percentages used in the present invention are mass percentages unless otherwise indicated.
Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that changes may be made in the embodiments and/or equivalents thereof without departing from the spirit and scope of the invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A clean production method of tremella polysaccharide is characterized by comprising the steps of extraction, solid-liquid separation, waste residue recycling, precipitation, alcohol recovery and post-treatment.
2. The clean production method of tremella polysaccharide as claimed in claim 1, wherein the post-treatment comprises precipitating the extracted solution of tremella polysaccharide with alcohol, centrifuging the precipitated waste alcohol, evaporating and recovering, and performing post-treatment on the waste water with high salt content which is not evaporated in the waste alcohol, wherein the high-salt waste water is filtered by a nanofiltration membrane to permeate salt and water, the trapped organic matter is further treated by AO treatment process, and the brine passing through the nanofiltration membrane is concentrated and crystallized by reduced pressure distillation; the steam evaporated under reduced pressure is subjected to reboiling treatment for recycling.
3. The clean production method of tremella polysaccharide as claimed in claim 2, wherein the temperature during the reduced pressure distillation is 71-75 ℃ and the pressure is 30-35 KPa.
4. The clean production method of tremella polysaccharide as claimed in claim 2, wherein the nanofiltration membrane is made of Y2O3-ZrO2And TiO2-ZrO2Of which the pore diameter is 4.5-5.5 nm.
5. The clean production method of tremella polysaccharide as claimed in claim 2, wherein said AO treatment process is to remove organic substances in the sewage by anaerobic bacteria and aerobic bacteria to reach the discharge standard.
6. The clean production method of tremella polysaccharide as claimed in claim 5, wherein the AO treatment process comprises: introducing the trapped organic matters into a sewage tank, then introducing the organic matters into an adjusting tank to adjust the pH value to 6.8-7.2, hydrolyzing macromolecular organic matters into micromolecules in an anaerobic tower through anaerobic bacteria, wherein the hydrolysis time is 3-5h, then introducing the organic matters into an oxygen tank to degrade through aerobic bacteria, the degradation time is 3-5h, then introducing the organic matters into a sedimentation tank, the sedimentation time is 1-1.5h, the precipitator is polymeric ferric sulfate, and the purified water is discharged after sedimentation in the sedimentation tank.
7. The clean production method of tremella polysaccharide as claimed in claim 6, wherein the amount of said polyferric sulfate is 90-110 kg/day.
8. The clean production method of tremella polysaccharide as claimed in claim 6, wherein said anaerobic bacteria are granular sludge bacteria, said aerobic bacteria are activated sludge, and said granular sludge bacteria and activated sludge are both purchased from Jiangxi water environmental protection science and technology Co.
9. The clean production method of tremella polysaccharide as claimed in claim 1, wherein the sedimentation ratio of the granular activated sludge to the activated sludge is above 20%, the sedimentation ratio needs to be periodically detected during the treatment process, and if the sedimentation ratio is below 20%, granular activated sludge or activated sludge needs to be supplemented until the sedimentation ratio is above 20%.
10. The clean production method of tremella polysaccharide as claimed in claim 1, wherein the natural gas used in the method is reboiled and reused, which improves the utilization rate of natural gas by 52.8% and the recovery rate of alcohol is 94.8%.
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