CN116750870B - Method for removing total nitrogen from wastewater - Google Patents
Method for removing total nitrogen from wastewater Download PDFInfo
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- CN116750870B CN116750870B CN202311028879.6A CN202311028879A CN116750870B CN 116750870 B CN116750870 B CN 116750870B CN 202311028879 A CN202311028879 A CN 202311028879A CN 116750870 B CN116750870 B CN 116750870B
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 74
- 239000002351 wastewater Substances 0.000 title claims abstract description 60
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 38
- 238000006243 chemical reaction Methods 0.000 claims abstract description 33
- 239000000725 suspension Substances 0.000 claims abstract description 24
- 238000005273 aeration Methods 0.000 claims abstract description 4
- 238000010438 heat treatment Methods 0.000 claims description 93
- 239000000284 extract Substances 0.000 claims description 39
- 241001632052 Haloxylon ammodendron Species 0.000 claims description 38
- 239000007788 liquid Substances 0.000 claims description 28
- 238000010494 dissociation reaction Methods 0.000 claims description 19
- 238000004880 explosion Methods 0.000 claims description 16
- 230000005593 dissociations Effects 0.000 claims description 15
- 238000002360 preparation method Methods 0.000 claims description 12
- 239000000084 colloidal system Substances 0.000 claims description 11
- 238000005507 spraying Methods 0.000 claims description 10
- 101001065065 Aspergillus awamori Feruloyl esterase A Proteins 0.000 claims description 9
- 108090000317 Chymotrypsin Proteins 0.000 claims description 9
- 108090000526 Papain Proteins 0.000 claims description 9
- 239000004365 Protease Substances 0.000 claims description 9
- 108090000787 Subtilisin Proteins 0.000 claims description 9
- 229960002376 chymotrypsin Drugs 0.000 claims description 9
- 239000002131 composite material Substances 0.000 claims description 9
- 238000004821 distillation Methods 0.000 claims description 9
- 229940055729 papain Drugs 0.000 claims description 9
- 235000019834 papain Nutrition 0.000 claims description 9
- 230000001079 digestive effect Effects 0.000 claims description 8
- 235000011389 fruit/vegetable juice Nutrition 0.000 claims description 8
- 238000012423 maintenance Methods 0.000 claims description 8
- 241000186660 Lactobacillus Species 0.000 claims description 6
- 241000235342 Saccharomycetes Species 0.000 claims description 6
- 238000000227 grinding Methods 0.000 claims description 6
- 229940039696 lactobacillus Drugs 0.000 claims description 6
- 108090000790 Enzymes Proteins 0.000 claims description 5
- 102000004190 Enzymes Human genes 0.000 claims description 5
- 229940088598 enzyme Drugs 0.000 claims description 5
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 22
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 8
- 230000035484 reaction time Effects 0.000 abstract description 8
- 230000007613 environmental effect Effects 0.000 abstract description 6
- 230000001105 regulatory effect Effects 0.000 abstract description 5
- 229910021529 ammonia Inorganic materials 0.000 abstract description 4
- 230000001276 controlling effect Effects 0.000 abstract description 4
- 230000000052 comparative effect Effects 0.000 description 63
- JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical compound CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 description 20
- 241000894006 Bacteria Species 0.000 description 16
- 230000008859 change Effects 0.000 description 11
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 10
- 235000014655 lactic acid Nutrition 0.000 description 10
- 239000004310 lactic acid Substances 0.000 description 10
- 230000001546 nitrifying effect Effects 0.000 description 4
- 238000011056 performance test Methods 0.000 description 4
- 239000010865 sewage Substances 0.000 description 4
- 241001632080 Haloxylon Species 0.000 description 3
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 description 3
- 239000000969 carrier Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000003801 milling Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 235000016709 nutrition Nutrition 0.000 description 2
- 230000035764 nutrition Effects 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 241000234653 Cyperus Species 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- 241000908878 Halosiphon Species 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010170 biological method Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000006911 enzymatic reaction Methods 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000006396 nitration reaction Methods 0.000 description 1
- 235000006408 oxalic acid Nutrition 0.000 description 1
- 229920005749 polyurethane resin Polymers 0.000 description 1
- 108090000765 processed proteins & peptides Proteins 0.000 description 1
- 238000013102 re-test Methods 0.000 description 1
- 230000001850 reproductive effect Effects 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/10—Packings; Fillings; Grids
- C02F3/105—Characterized by the chemical composition
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/10—Packings; Fillings; Grids
- C02F3/105—Characterized by the chemical composition
- C02F3/106—Carbonaceous materials
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
- C02F3/303—Nitrification and denitrification treatment characterised by the nitrification
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
- C02F3/305—Nitrification and denitrification treatment characterised by the denitrification
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
- C02F3/347—Use of yeasts or fungi
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/38—Organic compounds containing nitrogen
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Life Sciences & Earth Sciences (AREA)
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- Biodiversity & Conservation Biology (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
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Abstract
The invention relates to the technical field of wastewater denitrification, and in particular provides a method for removing total nitrogen from wastewater, which comprises the following steps: step one: introducing the wastewater into a pre-reaction tank, regulating ph of the wastewater to 7.5 at 25 ℃, adding an SN-1F rapid ammonia remover with the concentration of 500ppm, and reacting for 80 minutes to obtain pre-treated wastewater; step two: introducing the pretreated wastewater into a biological reaction tank, adding a suspension carrier with the volume of 0.6-0.8% of the pretreated wastewater, and controlling the air-water ratio to be (10-12) by using an aeration hose: and (3) reacting for 6-8 hours at the temperature of 1, 25 ℃ to finish the total nitrogen removal. The specific suspension carrier proportion, gas-water ratio and reaction time of the invention are matched with the suspension carrier of the invention to form a good biological reaction environment, and the denitrification endurance and denitrification effect after environmental changes such as wastewater ph, temperature and the like are improved.
Description
Technical Field
The invention relates to the field of wastewater denitrification, in particular to a method for removing total nitrogen from wastewater.
Background
Nitrogen is one of the main causes of eutrophication of water, and denitrification treatment is necessary before sewage discharge. The sewage denitrification is realized mainly by a biological method, and the core of the sewage denitrification is two biological enzymatic reactions which are related to each other. In the nitration reaction, the oxygen oxidizes ammonia nitrogen into nitrate nitrogen under the catalysis of biological enzyme secreted by nitrifying bacteria; in the denitrification reaction, the carbon source reduces nitrate nitrogen into nitrogen under the catalysis of biological enzymes secreted by denitrifying bacteria, and the nitrogen escapes from water to realize the aim of sewage denitrification.
The existing advanced denitrification process principle is to add a certain amount of suspended carriers into a reaction environment to improve biomass and biological types in the reaction environment, so that the treatment efficiency of the reaction is improved, the suspended carriers are required to be higher, the existing used total nitrogen removal method for wastewater excessively pays attention to the high specific surface area of the carriers, and the problems of poor biocompatibility, insufficient denitrification endurance, suddenly reduced denitrification rate after environmental changes such as wastewater ph and temperature and the like exist.
Aiming at the existing problems, development of a novel wastewater total nitrogen removal method for wastewater denitrification, which has high biological affinity, strong denitrification endurance and better denitrification effect after changes of ph, temperature and the like, is urgently needed.
Disclosure of Invention
In order to solve the problems, the invention aims to provide a method for removing total nitrogen from wastewater, which comprises the following steps:
step one: introducing the wastewater into a pre-reaction tank, regulating ph of the wastewater to 7.5 at 25 ℃, adding an SN-1F rapid ammonia remover with the concentration of 500ppm, and reacting for 80 minutes to obtain pre-treated wastewater;
step two: introducing the pretreated wastewater into a biological reaction tank, adding a suspension carrier with the volume of 0.6-0.8% of the pretreated wastewater, and controlling the air-water ratio to be (10-12) by using an aeration hose: the reaction is carried out for 6 to 8 hours at the temperature of 1, 25 ℃ to finish the total nitrogen removal;
the preparation method of the suspension carrier comprises the following steps:
step one: taking 10kg of fresh whole haloxylon ammodendron herb with the leaf height of 20-30 cm and coarse tubers, immersing the root and stem parts of the haloxylon ammodendron herb into a dissociation liquid for 4-7 h at 45 ℃, wherein the dissociation liquid comprises 16-20% of feruloyl esterase by mass, 10-15% of eduction enzyme R-10 by mass and pure water for the balance to obtain primary dissociation haloxylon ammodendron herb;
step two: performing steam explosion on the primary-dissociation haloxylon ammodendron, wherein the steam pressure is 2.0-2.5 MPa, and the maintenance pressure time is 90-120 s, so that secondary-dissociation haloxylon ammodendron is obtained;
step three: placing the secondary dissociated haloxylon ammodendron into a high-temperature blast drier, and returning air at 70-90 ℃ for 40-60 m 3 Heating for 70-90 min per min, and then returning air for 130-170 m at 300-350 DEG C 3 Heating for 30-50 min to obtain a semi-carbonized carrier;
step four: spraying itself onto the surface of the semi-carbonized carrier3-5% by mass of a sea-iris extract, and returning air at 120-140 ℃ for 60-80 m 3 Heating for 20-30 min, spraying a composite liquid with the mass of 2-4% on the surface of the semi-carbonized carrier again, wherein the composite liquid comprises 70-75% of a sea-iris extract, 3-5% of lactobacillus, 6-8% of saccharomycetes and the balance of pure water, and returning air for 70-90 m at 60-80 DEG C 3 Heating for 10-20 min to obtain the suspension carrier;
the preparation method of the sea iris extract comprises the following steps:
step one: adding the sea iris into a digestive juice with twice mass per se, wherein the digestive juice comprises chymotrypsin with the mass fraction of 5-7%, subtilisin with the mass fraction of 10-12%, papain with the mass fraction of 7-9% and pure water with the balance being the rest, shaking the sea iris for 3 hours at 40 ℃, pouring the sea iris into a colloid mill together, and circularly grinding the sea iris for 2 times at the temperature of 4-6 ℃ at 2000-2500 r/min to obtain sea iris homogenate;
step two: and (3) distilling the sea-iris homogenate under reduced pressure at the temperature of 40-50 ℃ and the vacuum degree of 500-700 mbar until no liquid continuously flows out, and collecting distillate to obtain the sea-iris extract.
Further, the mass fraction of the feruloyl esterase is 18%, and the mass fraction of the eductase R-10 is 13%.
Further, the steam pressure of the steam explosion is 2.2MPa, and the maintenance time is 110s.
Further, the step three is to put the secondary dissociated haloxylon ammodendron into a high-temperature blast drier for air return at 84 ℃ for 50m 3 Heating for 80min, and returning air at 330 ℃ for 140m 3 Heating for 40min to obtain semi-carbonized carrier.
Further, spraying the sea-iris extract accounting for 4% of the mass of the sea-iris extract onto the surface of the semi-carbonized carrier, and returning air at 130 ℃ for 70m 3 Heating for 26min, spraying a composite liquid with the mass percent of 3% on the surface of the semi-carbonized carrier again, wherein the composite liquid comprises the sea-iris extract with the mass percent of 73%, lactobacillus with the mass percent of 4%, saccharomycetes with the mass percent of 7% and pure water with the balance being complemented, and returning air at 72 ℃ for 80m 3 Heating for 14min to obtain the suspension carrier.
Further, in the preparation method of the sea iris extract, the digestive juice comprises chymotrypsin with the mass fraction of 6%, subtilisin with the mass fraction of 11%, papain with the mass fraction of 8% and pure water with the balance being the rest.
Further, in the preparation method of the sea iris extract, the colloid mill is operated for 2400r/min circulation grinding for 2 times at 5 ℃.
Further, in the preparation method of the sea iris extract, the reduced pressure distillation is to continuously flow out the sea iris homogenate after the sea iris homogenate is distilled under the reduced pressure of 650mbar under the vacuum degree at 47 ℃.
The haloxylon ammopips of the Cyperus genus have long creeping root stems, oval tubers, slightly thin and weak stalks, 15-95 cm high, sharp triangular prism shapes, smooth base parts and tuber shapes, have striking reproductive capacity and are commonly used for constructing artificial wetlands.
The invention has the following beneficial effects:
1. the specific suspension carrier proportion, gas-water ratio and reaction time of the invention are matched with the suspension carrier of the invention, thus forming a good biological reaction environment and improving denitrification endurance and denitrification effect after environmental changes such as wastewater ph, temperature and the like;
2. the special dissociation solution and the component proportion thereof are matched with the dissociation temperature and time, so that the root tissue of the haloxylon ammodendron is loosened, and steam moisture is assisted to be absorbed into the root tissue during the next steam explosion, thereby improving the effect of the steam explosion on the root tissue of the haloxylon ammodendron;
3. the special condition steam explosion of the invention can loosen the haloxylon ammodendron, especially the rhizome tissue of the haloxylon ammodendron, and simultaneously avoid the breaking and separating of the haloxylon ammodendron, especially the leaves of the haloxylon ammodendron, thereby obtaining the complete, loose and multi-gap secondary dissociation haloxylon ammodendron;
4. the invention has the advantages that the special conditions of high-temperature blast drying are provided, four heating processes with different functions are provided, the first time is mainly to dry the secondary dissociation haloxylon ammodendron, the gap of the secondary dissociation haloxylon ammodendron is further enlarged, the second time is mainly to partially carbonize the surface of the haloxylon ammodendron, the adsorption effect is improved, the toughness of the halosiphon extract is maintained, the third time is mainly to fix the haloxylon ammodendron on the surface of the haloxylon ammodendron, adhesion and nutrition matrixes are provided for the subsequent fixing of strains, the fourth time is mainly to fix lactobacillus and saccharomycetes on the surface of the haloxylon ammodendron, and the wastewater treatment environment with specific suspension carrier proportion, gas-water ratio and reaction time is matched to eliminate the strains harmful to nitrifying bacteria and expand the growth space of nitrifying bacteria, and the finally obtained carrier can be suspended in the wastewater through multiple-round quality change, each carrier simultaneously has oxygen and anaerobic environment, so that nitrifying bacteria and denitrifying bacteria grow simultaneously;
5. the specific method of the invention extracts the sea-iris extract, on the basis of decomposing sea-iris tissues by multi-strain cooperation, combines with the grinding condition of a colloid mill, separates out the nutrition components of sea-iris as far as possible, and combines with reduced pressure distillation to reduce the damage to the activity of the sea-iris extract;
6. according to the invention, the components and the steps are matched with each other, a suspension carrier with a high specific surface area is physically obtained, and after the leaves and roots of the natural multi-branch structure of the haloxylon ammodendron are processed, the water flow motion can be more fully stirred in the wastewater treatment environment with the specific suspension carrier proportion, the air-water ratio and the reaction time to improve the denitrification effect, and the plant skeleton of the haloxylon ammodendron chemically matched with the sea-iris extract develops the biological affinity of the haloxylon ammodendron, so that compared with other materials, the haloxylon ammodendron is more suitable for the attachment growth of microorganisms, and the denitrification endurance and the denitrification effect after the environmental changes such as wastewater ph and temperature are improved.
Detailed Description
In order to more clearly illustrate the overall concept of the present invention, the following describes the overall scheme of the present invention in detail by way of examples; in the following description, numerous specific details are set forth in order to provide a more thorough understanding of the present invention; it will be apparent, however, to one skilled in the art that the invention may be practiced without one or more of these details; in other instances, well-known features have not been described in detail in order to avoid obscuring the invention.
The colloid mill of the invention is purchased from Guangzhou city blue mechanical equipment Co., ltd, and the product number is split colloid mill 200; the steam explosion machine is purchased from the manufacturing plant of the agricultural machinery of the serious of the oil filling riser market, and the goods number LB-X; the high temperature blast drier is purchased from Jiangsu Xingtai electric appliances Inc., model number XTDQ-102; the eductase R-10 is available from Shanghai Chemie Co., ltd; feruloyl esterase was purchased from Shanghai screening quasi-biotechnology Co., ltd, cat# ZME-E-FAERU; chymotrypsin is purchased from su-state day trade company, cat# KC90242; subtilisin was purchased from Shanxi North Biotechnology Inc., under the designation XNSW-0323-052; papain was purchased from Shaanxi Hejian peptide bioengineering Co., ltd, cat# D-03; lactic acid bacteria were purchased from Shanxi Xinyu Biotechnology Inc., product number XY-0414-161; yeast was purchased from Shanxi cloisonne Biotechnology Inc., cat# JTSW-0802-491; SN-1F quick ammonia remover was purchased from Guangzhou Hi-Jie environmental protection technologies Co.
Unless otherwise specified, the starting components in the examples below are commercially available, and the laboratory apparatus used is a laboratory conventional laboratory apparatus, and the performance test methods are known in the art.
The preferred embodiment is as follows:
example 1:
the method for removing total nitrogen from the wastewater comprises the following steps:
step one: introducing the wastewater into a pre-reaction tank, regulating ph of the wastewater to 7.5 at 25 ℃, adding an SN-1F rapid ammonia remover with the concentration of 500ppm, and reacting for 80 minutes to obtain pre-treated wastewater;
step two: introducing the pretreated wastewater into a biological reaction tank, adding a suspension carrier with the volume of 0.7% of the pretreated wastewater, and controlling the gas-water ratio to be 11 by using an aeration hose: the reaction is carried out for 7 hours at the temperature of 1, 25 ℃ to complete the total nitrogen removal;
the suspension carrier is prepared by the following method:
step one: taking 10kg of fresh whole haloxylon ammodendron herb with the leaf height of 20-30 cm and coarse tubers, immersing the root and stem parts of the haloxylon ammodendron herb into dissociation liquid for 4-7 h at 45 ℃, wherein the dissociation liquid comprises 18% of feruloyl esterase by mass, 13% of educing enzyme R-10 by mass and the balance of pure water, taking out the haloxylon herb, and controlling water until no dissociation liquid drops within 2s to obtain primary dissociation haloxylon herb;
step two: putting the primary dissociated haloxylon ammodendron into a steam explosion machine for steam explosion, wherein the steam pressure is 2.2MPa, and the maintenance time is 110s, so as to obtain secondary dissociated haloxylon ammodendron;
step three: putting the secondary dissociated haloxylon ammodendron into a high-temperature blast drier, and returning air at 84 ℃ for 50m 3 Heating for 80min, and returning air at 330 ℃ for 140m 3 Heating for 40min to obtain semi-carbonized carrier;
step four: spraying its natural siphon extract with mass of 4% onto semi-carbonized carrier surface, and placing into high temperature blast drier for air return at 130deg.C for 70m 3 Heating for 26min, spraying 3% of its composite liquid comprising 73% of sea iridescent extract, 4% of lactobacillus, 7% of saccharomycetes and the balance of pure water on the surface of semi-carbonized carrier, and returning air at 72deg.C for 80m 3 Heating for 14min to obtain suspension carrier;
the preparation method of the sea-iris extract comprises the following steps:
step one: weighing 1kg of fresh sea iris, cutting into pieces with the length of 1cm, adding two times of digestive juice, wherein the digestive juice comprises chymotrypsin with the mass fraction of 6%, subtilisin with the mass fraction of 11%, papain with the mass fraction of 8% and pure water with the balance being complemented, shaking at 40 ℃ for 3 hours, pouring the pieces into a colloid mill together, and circularly grinding for 2 times at 5 ℃ at 2400r/min to obtain sea iris homogenate;
step two: distilling the sea-iris homogenate at 47 ℃ under reduced pressure of 650mbar until no liquid continuously flows out, and collecting distillate to obtain sea-iris extract.
Examples 2 to 57:
example 2 differs from example 1 only in that the mass fraction of feruloyl esterase of example 2 is 16%;
example 3 differs from example 1 only in that the mass fraction of feruloyl esterase of example 3 is 20%;
example 4 differs from example 1 only in that the mass fraction of the eductase R-10 of example 4 is 10%;
example 5 differs from example 1 only in that the mass fraction of the eductase R-10 of example 5 is 15%;
example 6 differs from example 1 only in that the steam pressure of the steam explosion of example 6 is 2.0MPa;
example 7 differs from example 1 only in that the steam pressure of the steam explosion of example 7 is 2.5MPa;
example 8 differs from example 1 only in that the maintenance time of the steam explosion of example 8 is 90s;
example 9 differs from example 1 only in that the maintenance time of the steam explosion of example 9 is 120s;
example 10 differs from example 1 only in that the first heating of the high temperature forced air dryer of example 10 was 50m return air at 70℃ 3 Heating for 80min;
example 11 differs from example 1 only in that the first heating of the high temperature forced air dryer of example 11 was 50m return air at 90℃ 3 Heating for 80min;
example 12 differs from example 1 only in that the first heating of the high temperature forced air dryer of example 12 is 40m return air at 84℃ 3 Heating for 80min;
example 13 differs from example 1 only in that the first heating of the high temperature forced air dryer of example 13 is a return air at 84℃of 60m 3 Heating for 80min;
example 14 differs from example 1 only in that the first heating of the high temperature forced air dryer of example 14 was 50m return air at 84℃ 3 Heating for 70min;
example 15 differs from example 1 only in that the first heating of the high temperature forced air dryer of example 15 was 50m return air at 84℃ 3 Heating for 90min;
example 16 differs from example 1 only in that the second heating of the high temperature forced air dryer of example 16 was 140m return air at 300℃ 3 Heating for 40min;
example 17 differs from example 1 only in that the second heating of the high temperature forced air dryer of example 17 was 140m return air at 350℃ 3 Heating for 40min;
example 18 differs from example 1 only in that the second heating of the high temperature forced air dryer of example 18 was 130m return air at 330 c 3 Heating for 40min;
example 19 differs from example 1 only in that the second heating of the high temperature forced air dryer of example 19 was 170m return air at 330 c 3 Heating for 40min;
example 20 differs from example 1 only in that the second heating of the high temperature forced air dryer of example 20 was 140m return air at 330 c 3 Heating for 30min;
example 21 differs from example 1 only in that the second heating of the high temperature forced air dryer of example 21 was 140m return air at 330 c 3 Heating for 50min;
example 22 differs from example 1 only in that the third heating of the high temperature forced air dryer of example 22 was 70m return air at 120℃ 3 Heating for 26min;
example 23 differs from example 1 only in that the third heating of the high temperature forced air dryer of example 23 was 70m return air at 140℃ 3 Heating for 26min;
example 24 differs from example 1 only in that the third heating of the high temperature forced air dryer of example 24 was a return air at 130℃of 60m 3 Heating for 26min;
example 25 differs from example 1 only in that the third heating of the high temperature forced air dryer of example 25 was 80m return air at 130℃ 3 Heating for 26min;
example 26 differs from example 1 only in that the third heating of the high temperature forced air dryer of example 26 was 70m return air at 130 c 3 Heating for 20min;
example 27 differs from example 1 only in that the third heating of the high temperature forced air dryer of example 27 was 70m return air at 130 c 3 Heating for 30min;
example 28 differ from example 1 only in that the fourth heating of the high temperature forced air dryer of example 28 was 80m return air at 60℃ 3 Heating for 14min;
example 29 differs from example 1 only in that the fourth heating of the high temperature forced air dryer of example 29 was 80℃return air 80m 3 Heating for 14min;
example 30 differs from example 1 only in that the fourth heating of the high temperature forced air dryer of example 30 was 70m return air at 72℃ 3 Heating for 14min;
example 31 differs from example 1 only in that the fourth heating of the high temperature forced air dryer of example 31 was 90m return air at 72℃ 3 Heating for 14min;
example 32 differs from example 1 only in that the fourth heating of the high temperature forced air dryer of example 32 was 80m return air at 72℃ 3 Heating for 10min;
example 33 differs from example 1 only in that the fourth heating of the high temperature forced air dryer of example 33 was 80m return air at 72℃ 3 Heating for 20min;
example 34 differs from example 1 only in that the mass fraction of chymotrypsin of example 34 is 5%;
example 35 differs from example 1 only in that the mass fraction of chymotrypsin of example 35 is 7%;
example 36 differs from example 1 only in that the mass fraction of subtilisin of example 36 is 10%;
example 37 differs from example 1 only in that the mass fraction of subtilisin of example 37 is 12%;
example 38 differs from example 1 only in that the mass fraction of papain of example 38 is 7%;
example 39 differs from example 1 only in that the mass fraction of papain of example 39 is 9%;
example 40 differs from example 1 only in that the colloid mill of example 40 has a milling speed of 2000r/min;
example 41 differs from example 1 only in that the grinding speed of the colloid mill of example 41 is 2500r/min;
example 42 differs from example 1 only in that the temperature of the reduced pressure distillation of example 42 is 40 ℃;
example 43 differs from example 1 only in that the temperature of the reduced pressure distillation of example 43 is 50 ℃;
example 44 differs from example 1 only in that the vacuum of the reduced pressure distillation of example 44 is 500mbar;
example 45 differs from example 1 only in that the vacuum of the reduced pressure distillation of example 45 is 700mbar;
example 46 differs from example 1 only in that the complex liquid of example 46 comprises 70% by mass of a sea iris extract, 4% by mass of lactic acid bacteria, 7% by mass of yeasts and the balance of pure water;
example 47 differs from example 1 only in that the complex liquid of example 47 comprises a mass fraction of 75% of a sea iris extract, a mass fraction of 4% of lactic acid bacteria, a mass fraction of 7% of yeasts and the balance of pure water;
example 48 differs from example 1 only in that the complex liquid of example 48 comprises a sea iris extract with a mass fraction of 73%, lactic acid bacteria with a mass fraction of 3%, yeast with a mass fraction of 7% and pure water with the balance being made up;
example 49 differs from example 1 only in that the complex liquid of example 49 comprises a sea iris extract with a mass fraction of 73%, lactic acid bacteria with a mass fraction of 5%, yeast with a mass fraction of 7% and pure water with the balance being made up;
example 50 differs from example 1 only in that the complex liquid of example 50 comprises a sea iris extract with a mass fraction of 73%, lactic acid bacteria with a mass fraction of 4%, yeast with a mass fraction of 6% and pure water with the balance being made up;
example 51 differs from example 1 only in that the complex liquid of example 51 comprises a sea iris extract with a mass fraction of 73%, lactic acid bacteria with a mass fraction of 4%, yeast with a mass fraction of 8% and pure water with the balance being made up;
example 52 differs from example 1 only in that the biological reaction tank of example 52 is charged with suspended carrier in an amount of 0.6% of the pretreated wastewater;
example 53 differs from example 1 only in that the biological reaction tank of example 53 is charged with suspended carrier in an amount of 0.8% of the pretreated wastewater;
example 54 differs from example 1 only in that the gas-water ratio in the biological reaction tank of example 54 is 10:1, a step of;
example 55 differs from example 1 only in that the gas-water ratio in the biological reaction tank of example 55 is 12:1, a step of;
example 56 differs from example 1 only in that the reaction time in the biological reaction tank of example 56 is 6 hours;
example 57 differs from example 1 only in that the reaction time in the bioreactor of example 57 is 8 hours.
Comparative examples 1 to 31:
comparative example 1 differs from example 1 only in that the mass fraction of feruloyl esterase of comparative example 1 is 26%;
comparative example 2 differs from example 1 only in that the mass fraction of the eductase R-10 of comparative example 2 is 20%;
comparative example 3 differs from example 1 only in that the steam pressure of the steam explosion of comparative example 3 is 3.0MPa;
comparative example 4 differs from example 1 only in that the maintenance time of the steam explosion of comparative example 4 is 150s;
comparative example 5 differs from example 1 only in that the first heating of the high temperature forced air dryer of comparative example 5 was 50m return air at 100℃ 3 Heating for 80min;
comparative example 6 differs from example 1 only in that the first heating of the high temperature forced air dryer of comparative example 6 was 80m return air at 84 deg.c 3 Heating for 80min;
comparative example 7 differs from example 1 only in that the first heating of the high temperature forced air dryer of comparative example 7 was 50m return air at 84 deg.c 3 Heating for 100min;
comparative example 8 and example 1The only difference is that the second heating of the high temperature blast dryer of comparative example 8 was 140m return air at 400℃ 3 Heating for 40min;
comparative example 9 differs from example 1 only in that the second heating of the high temperature forced air dryer of comparative example 9 was a return air at 330℃of 200m 3 Heating for 40min;
comparative example 10 differs from example 1 only in that the second heating of the high temperature forced air dryer of comparative example 10 was 140m return air at 330 c 3 Heating for 60min;
comparative example 11 differs from example 1 only in that the third heating of the high temperature forced air dryer of comparative example 11 was 70m return air at 160 c 3 Heating for 26min;
comparative example 12 differs from example 1 only in that the third heating of the high temperature forced air dryer of comparative example 12 was 100m return air at 130 c 3 Heating for 26min;
comparative example 13 differs from example 1 only in that the third heating of the high temperature forced air dryer of comparative example 13 was 70m return air at 130 c 3 Heating for 40min;
comparative example 14 differs from example 1 only in that the fourth heating of the high temperature forced air dryer of comparative example 14 was 80m return air at 90 deg.c 3 Heating for 14min;
comparative example 15 differs from example 1 only in that the fourth heating of the high temperature forced air dryer of comparative example 15 was 110m return air at 72 c 3 Heating for 14min;
comparative example 16 differs from example 1 only in that the fourth heating of the high temperature forced air dryer of comparative example 16 was 80m return air at 72℃ 3 Heating for 30min;
comparative example 17 differs from example 1 only in that the mass fraction of chymotrypsin of comparative example 17 is 9%;
comparative example 18 differs from example 1 only in that the mass fraction of subtilisin of comparative example 18 is 15%;
comparative example 19 differs from example 1 only in that the mass fraction of papain of comparative example 19 is 12%;
comparative example 20 differs from example 1 only in that the colloid mill of comparative example 20 had a milling speed of 3000r/min;
comparative example 21 differs from example 1 only in that the temperature of reduced pressure distillation of comparative example 21 is 60 ℃;
comparative example 22 differs from example 1 only in that comparative example 22 has a vacuum of 900mbar by distillation under reduced pressure;
comparative example 23 differs from example 1 only in that the complex liquid of comparative example 23 comprises 80% by mass of a sea iris extract, 4% by mass of lactic acid bacteria, 7% by mass of yeast and the balance of pure water;
comparative example 24 differs from example 1 only in that the complex liquid of comparative example 24 comprises a sea iris extract of 73% by mass, lactic acid bacteria of 8% by mass, yeast of 7% by mass and pure water of the balance;
comparative example 25 differs from example 1 only in that the complex liquid of comparative example 25 includes a sea iris extract of 73% by mass, lactic acid bacteria of 4% by mass, yeast of 10% by mass, and pure water of the balance;
comparative example 26 differs from example 1 only in that comparative example 26 replaces the haloxylon ammodendron herb with Gui Zhuzhu pieces 10 to 15cm long of the same weight;
comparative example 27 differs from example 1 only in that comparative example 27 replaces the sea-iris extract with the same weight of 600R polyurethane resin of hefeihua new materials science and technology limited;
comparative example 28 without the use of the method for preparing a suspension vehicle of the present invention, suspension balls of the same weight of su jing environmental protection new materials limited were directly used as suspension vehicles;
comparative example 29 differs from example 1 only in that the biological reaction tank of comparative example 29 was charged with suspended carrier in an amount of 1.2% by volume of the pretreated wastewater;
comparative example 30 differs from example 1 only in that the gas-water ratio in the biological reaction tank of comparative example 30 is 15:1, a step of;
comparative example 31 differs from example 1 only in that the reaction time in the biological reaction tank of comparative example 31 was 10 hours.
The total nitrogen removal method of wastewater of each example was subjected to performance test of denitrification endurance, performance test of denitrification effect after ph change, and performance test of denitrification effect after temperature change.
Test preparation: the total nitrogen concentration of the pretreated wastewater in each example is controlled to be 500mg/l, the pretreated wastewater is introduced into a biological reaction tank, the total nitrogen concentration of the effluent of the biological reaction tank is measured after the reaction is finished, and the first wastewater is used for microbial growth and is not counted for comparison.
The denitrification endurance effect of the total nitrogen removal method of the wastewater is represented by the value of the total nitrogen concentration of the effluent of the tenth batch of biological reaction tanks, and the total nitrogen concentration is reserved to an integer position.
Cleaning equipment and carrying out test preparation again, regulating the ph of the second batch of wastewater to 6.5 by using oxalic acid before the second batch of wastewater enters the biological reaction tank, and representing the denitrification effect of the total nitrogen removal method of the wastewater after ph change by using the value of the total nitrogen concentration of the effluent of the second batch of biological reaction tank, wherein the total nitrogen concentration is kept to an integer position.
Cleaning equipment and re-testing preparation, regulating the temperature of the second batch of wastewater to 10 ℃ before the second batch of wastewater enters the biological reaction tank, and representing the denitrification effect of the wastewater total nitrogen removal method after temperature change by using the value of the total nitrogen concentration of the effluent of the second batch of biological reaction tank, wherein the total nitrogen concentration is kept to an integer position.
The test results of each example are shown in Table 1.
As can be seen from the data in table 1, the total nitrogen removal method for wastewater of the example of the present invention has a better denitrification endurance effect, a denitrification effect after ph change and a denitrification effect after temperature change than the total nitrogen removal method for wastewater of each comparative example. Further, the denitrification endurance effect, the denitrification effect after ph change and the denitrification effect after temperature change of the embodiment 1 of the present invention are the best embodiments of the present invention, and the adjustment of parameters is accidental, and the present invention uses the haloxylon ammodendron and the sea-iris extract to prepare the suspension carrier suitable for the specific suspension carrier proportion, the air-water ratio and the reaction time of the present invention in the wastewater treatment environment through the specific process of the present invention, and combines the denitrification endurance effect, the denitrification effect after ph change and the denitrification effect after temperature change pursued by the present invention to form the specific technical scheme of the present invention.
The foregoing is merely exemplary of the present invention and is not intended to limit the present invention; various modifications and variations of the present invention will be apparent to those skilled in the art; any modification, equivalent replacement, improvement, etc. which come within the spirit and principles of the invention are to be included in the scope of the claims of the present invention.
Claims (8)
1. The method for removing total nitrogen from wastewater is characterized by comprising the following steps of:
step one: introducing the wastewater into a pre-reaction tank, adjusting the pH of the wastewater to 7.5 at 25 ℃, adding an SN-1F rapid ammonia nitrogen remover with the concentration of 500ppm, and reacting for 80 minutes to obtain pre-treated wastewater;
step two: introducing the pretreated wastewater into a biological reaction tank, adding a suspension carrier with the volume of 0.6-0.8% of the pretreated wastewater, and controlling the air-water ratio to be (10-12) by using an aeration hose: the reaction is carried out for 6 to 8 hours at the temperature of 1, 25 ℃ to finish the total nitrogen removal;
the preparation method of the suspension carrier comprises the following steps:
step one: taking 10kg of fresh whole haloxylon ammodendron, immersing the root and stem parts of the haloxylon ammodendron in a dissociation liquid for 4-7 h at 45 ℃, wherein the dissociation liquid comprises 16-20% of feruloyl esterase by mass, 10-15% of educing enzyme R-10 by mass and the balance of pure water to obtain primary dissociation haloxylon ammodendron;
step two: performing steam explosion on the primary-dissociation haloxylon ammodendron, wherein the steam pressure is 2.0-2.5 MPa, and the maintenance pressure time is 90-120 s, so that secondary-dissociation haloxylon ammodendron is obtained;
step three: will beThe secondary dissociated haloxylon ammodendron is put into a high-temperature blast drier, and air return is carried out at 70-90 ℃ for 40-60 m 3 Heating for 70-90 min per min, and then returning air for 130-170 m at 300-350 DEG C 3 Heating for 30-50 min to obtain a semi-carbonized carrier;
step four: spraying a sea-iris extract with the mass of 3-5% on the surface of the semi-carbonized carrier, and returning air at 120-140 ℃ for 60-80 m 3 Heating for 20-30 min, spraying a composite liquid with the mass of 2-4% on the surface of the semi-carbonized carrier again, wherein the composite liquid comprises 70-75% of a sea-iris extract, 3-5% of lactobacillus, 6-8% of saccharomycetes and the balance of pure water, and returning air for 70-90 m at 60-80 DEG C 3 Heating for 10-20 min to obtain the suspension carrier;
the preparation method of the sea iris extract comprises the following steps:
step one: adding the sea iris into a digestive juice with twice mass per se, wherein the digestive juice comprises chymotrypsin with the mass fraction of 5-7%, subtilisin with the mass fraction of 10-12%, papain with the mass fraction of 7-9% and pure water with the balance being the rest, shaking the sea iris for 3 hours at 40 ℃, pouring the sea iris into a colloid mill together, and circularly grinding the sea iris for 2 times at the temperature of 4-6 ℃ at 2000-2500 r/min to obtain sea iris homogenate;
step two: and (3) distilling the sea-iris homogenate under reduced pressure at the temperature of 40-50 ℃ and the vacuum degree of 500-700 mbar until no liquid continuously flows out, and collecting distillate to obtain the sea-iris extract.
2. The method for removing total nitrogen from wastewater according to claim 1, wherein the mass fraction of feruloyl esterase is 18% and the mass fraction of eductase R-10 is 13%.
3. The method for removing total nitrogen from wastewater according to claim 1, wherein the steam pressure of the steam explosion is 2.2MPa and the maintenance time is 110s.
4. The method for removing total nitrogen from wastewater according to claim 1, wherein said step three is to put said secondary dissociated haloxylon ammodendron into a high temperature blast drier and return air at 84 ℃50m 3 Heating for 80min, and returning air at 330 ℃ for 140m 3 Heating for 40min to obtain semi-carbonized carrier.
5. The method for removing total nitrogen from wastewater according to claim 1, wherein said step four is spraying the surface of said semi-carbonized carrier with its own mass of 4% of the extract of sea-iris, and returning air at 130 ℃ for 70m 3 Heating for 26min, spraying a composite liquid with the mass percent of 3% on the surface of the semi-carbonized carrier again, wherein the composite liquid comprises the sea-iris extract with the mass percent of 73%, lactobacillus with the mass percent of 4%, saccharomycetes with the mass percent of 7% and pure water with the balance being complemented, and returning air at 72 ℃ for 80m 3 Heating for 14min to obtain the suspension carrier.
6. The method for removing total nitrogen from wastewater according to claim 1, wherein the digestive juice comprises chymotrypsin with a mass fraction of 6%, subtilisin with a mass fraction of 11%, papain with a mass fraction of 8% and pure water with the balance being the same.
7. The method for removing total nitrogen from wastewater according to claim 1, wherein said colloid mill is operated at 5 ℃ for 2400r/min for 2 times in the preparation of said sea iris extract.
8. The method for removing total nitrogen from wastewater according to claim 1, wherein in the method for producing the sea-iris extract, the reduced pressure distillation is to continuously flow out the sea-iris homogenate from the sea-iris extract under a vacuum of 650mbar at 47 ℃.
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