CN112980896B - Kitchen waste dephosphorization and nitrogen removal system and method - Google Patents
Kitchen waste dephosphorization and nitrogen removal system and method Download PDFInfo
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- CN112980896B CN112980896B CN202110383562.9A CN202110383562A CN112980896B CN 112980896 B CN112980896 B CN 112980896B CN 202110383562 A CN202110383562 A CN 202110383562A CN 112980896 B CN112980896 B CN 112980896B
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- 239000010806 kitchen waste Substances 0.000 title claims abstract description 118
- 238000000034 method Methods 0.000 title claims abstract description 30
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims description 54
- 229910052757 nitrogen Inorganic materials 0.000 title claims description 27
- 238000000855 fermentation Methods 0.000 claims abstract description 165
- 230000004151 fermentation Effects 0.000 claims abstract description 118
- 239000002253 acid Substances 0.000 claims abstract description 62
- 238000004519 manufacturing process Methods 0.000 claims abstract description 55
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 51
- 238000001704 evaporation Methods 0.000 claims abstract description 27
- 239000000126 substance Substances 0.000 claims abstract description 25
- 150000007524 organic acids Chemical class 0.000 claims abstract description 19
- 230000008569 process Effects 0.000 claims abstract description 18
- -1 organic acid salt Chemical class 0.000 claims abstract description 15
- 230000009615 deamination Effects 0.000 claims description 132
- 238000006481 deamination reaction Methods 0.000 claims description 132
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 103
- 239000003513 alkali Substances 0.000 claims description 58
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 49
- 239000012528 membrane Substances 0.000 claims description 46
- 238000006243 chemical reaction Methods 0.000 claims description 39
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- 238000009833 condensation Methods 0.000 claims description 23
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- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 claims description 20
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 20
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 claims description 19
- 235000012538 ammonium bicarbonate Nutrition 0.000 claims description 19
- 239000001099 ammonium carbonate Substances 0.000 claims description 19
- 238000010992 reflux Methods 0.000 claims description 19
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 18
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 15
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- 238000012216 screening Methods 0.000 claims description 7
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 6
- 239000013078 crystal Substances 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 4
- QORWJWZARLRLPR-UHFFFAOYSA-H tricalcium bis(phosphate) Chemical compound [Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O QORWJWZARLRLPR-UHFFFAOYSA-H 0.000 claims description 4
- 230000002053 acidogenic effect Effects 0.000 claims description 3
- 239000001506 calcium phosphate Substances 0.000 claims description 3
- 229910000389 calcium phosphate Inorganic materials 0.000 claims description 3
- 235000011010 calcium phosphates Nutrition 0.000 claims description 3
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- 229910019142 PO4 Inorganic materials 0.000 claims description 2
- 150000002431 hydrogen Chemical class 0.000 claims description 2
- 229910021645 metal ion Inorganic materials 0.000 claims description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 2
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- 230000001276 controlling effect Effects 0.000 claims 1
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- 238000005516 engineering process Methods 0.000 description 13
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- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 6
- 239000002351 wastewater Substances 0.000 description 5
- 241000894006 Bacteria Species 0.000 description 4
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000001556 precipitation Methods 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
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- 229910000147 aluminium phosphate Inorganic materials 0.000 description 2
- CKMXBZGNNVIXHC-UHFFFAOYSA-L ammonium magnesium phosphate hexahydrate Chemical compound [NH4+].O.O.O.O.O.O.[Mg+2].[O-]P([O-])([O-])=O CKMXBZGNNVIXHC-UHFFFAOYSA-L 0.000 description 2
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
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- 238000000926 separation method Methods 0.000 description 2
- 229910052567 struvite Inorganic materials 0.000 description 2
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- 241000238631 Hexapoda Species 0.000 description 1
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- 230000000789 acetogenic effect Effects 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/40—Preparation of oxygen-containing organic compounds containing a carboxyl group including Peroxycarboxylic acids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/26—Carbonates or bicarbonates of ammonium
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P3/00—Preparation of elements or inorganic compounds except carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- 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
- C02F2101/105—Phosphorus compounds
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- 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
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/005—Processes using a programmable logic controller [PLC]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- Processing Of Solid Wastes (AREA)
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Abstract
The invention discloses a system and a method for dephosphorizing and denitriding kitchen waste, which specifically comprises the steps of carrying out anaerobic acid production after pretreatment of the kitchen waste, and adding alkaline substances to adjust pH (pH is more than 8.0) in the process to obtain fermentation liquor (the mass concentration of organic acid/organic acid salt is more than 5%) with high content of organic acid/organic acid salt; and (3) evaporating the fermentation liquor by steam to remove ammonia nitrogen. The organic acid/organic acid salt in the fermentation broth is used as a carbon source in the denitrification process, so that high-efficiency denitrification is realized. In the anaerobic acid production process, the alkaline substance is added, so that the output of the organic acid/organic acid salt is improved, and the method can be used as a carbon source in the subsequent denitrification process. On the other hand, the ammonia nitrogen is removed by adopting a steam evaporation method, so that the ammonia nitrogen removal efficiency can be effectively improved.
Description
Technical Field
The invention belongs to the technical field of organic waste disposal in kitchen waste treatment, and particularly relates to a system and a method for dephosphorizing and denitriding kitchen waste.
Background
Kitchen waste, also called kitchen waste, refers to waste generated in activities such as daily living and food processing, food service, unit meal supply and the like of residents, and comprises discarded unused vegetable leaves, leftovers, fruit peel, eggshells, tea residues, bones and the like, and is mainly sourced from household kitchens, restaurants, dining halls, markets and other industries related to food processing.
Kitchen waste contains extremely high moisture and organic matters, is easy to spoil and generates malodor. Illegal collection and recycling of kitchen waste can cause threat to environment and resident health. The kitchen garbage is singly collected, so that the amount of organic matters entering a landfill site can be reduced, odor and garbage percolate are reduced, adverse effects on garbage incineration caused by excessive water can be avoided, and corrosion to equipment is reduced. After proper treatment and processing, kitchen garbage can be converted into new resources, and the kitchen garbage can be used as fertilizer and feed after being strictly treated due to the characteristic of high organic matter content, biogas can be produced to be used as fuel or power generation, and the grease part can be used for preparing biofuel.
At present, the main technology for treating kitchen waste is that the kitchen waste is firstly separated, crushed, subjected to wet heat treatment and centrifuged, and subjected to three-phase separation of waste oil, slurry and solid slag; esterifying the separated waste oil to prepare biodiesel; anaerobic fermentation is carried out on the slurry to produce biogas, then aerobic treatment is carried out, and finally the biogas is discharged after reaching the standard; composting or insect digestion is carried out on kitchen solid residues.
The main problems of the prior art include long process flow, low biogas added value, difficult standard discharge of slurry, and the like, and particularly the problems of high ammonia nitrogen concentration in wastewater, difficult treatment, difficult product sales after slag solidification and fertilizer piling, and the like. These problems are needed to be effectively solved, so that the kitchen waste can be effectively treated and the environment-friendly resource recycling can be achieved.
Disclosure of Invention
The invention aims to: in order to overcome the defects in the prior art, the invention provides a kitchen waste dephosphorization and nitrogen removal system and method, which adopt the mode of adding alkaline substances, improving the pH value of a fermentation system, prolonging the fermentation acid production time and combining steam evaporation denitrification to effectively remove phosphorus and ammonia nitrogen in kitchen waste water, thereby being an efficient, energy-saving and environment-friendly kitchen waste denitrification method.
The technical scheme is as follows: in order to achieve the above purpose, the technical scheme adopted by the invention is mainly summarized as the following 2 steps:
1. Anaerobic alkaline acid production technology for kitchen waste. Organic matters in kitchen waste are converted into organic acids through the metabolism of anaerobic acidogenic microorganisms, and the pH value (pH) of a system is reduced in the acidogenic process, so that acidification inhibition is generated, and continuous acidogenesis is not facilitated. The technology adopts the addition of alkaline substances such as Ca (OH) 2 to improve the pH value of a fermentation system, thereby being beneficial to the smooth proceeding of the reaction process and prolonging the fermentation acid production time. Meanwhile, phosphoric acid can be generated in the anaerobic acid production process of kitchen residues, and the phosphoric acid and calcium ions can form precipitation, so that phosphorus in the wastewater is removed.
2. Vapor evaporation technology of high concentration ammonia nitrogen. Because kitchen waste contains a large amount of proteins, a large amount of ammonia nitrogen is generated in the anaerobic acid production process, and the existence of the ammonia nitrogen can cause low purity of subsequent organic acid, so that the subsequent organic acid is influenced to be used as a high-quality carbon source. By adopting the steam evaporation technology, ammonia nitrogen is removed from the wastewater under the condition that the temperature is not very high, and the generated ammonia can be recovered into ammonium bicarbonate, so that the problems of high energy consumption and high cost of the traditional ammonia nitrogen treatment are reduced.
The invention aims to provide a kitchen waste dephosphorization and denitrification system, which comprises an anaerobic acid production system, an alkali addition system and a denitrification system, wherein the alkali addition system is connected with the anaerobic acid production system, and the anaerobic acid production system is connected with the denitrification system; kitchen waste enters from the water inlet end of the anaerobic acid production system, the water outlet end of the anaerobic acid production system is connected with the water inlet end of the denitrification system, fermentation liquor containing organic acid/organic acid salt is discharged from the water outlet end of the denitrification system, and vapor ammonia nitrogen is discharged from the steam outlet end of the denitrification system;
the anaerobic acid production system comprises an anaerobic fermentation tank, and a gas-liquid separator is arranged at the top of the anaerobic fermentation tank;
the alkali adding system comprises an alkali tank, wherein an alkaline substance for adjusting the pH of the water body is stored in the alkali tank;
the alkali tank is connected with the anaerobic fermentation tank;
The denitrification system is a steam evaporation denitrification system.
Optionally, the steam evaporation denitrification system comprises a preheater, a primary negative pressure low-temperature deamination device, a secondary negative pressure low-temperature deamination device, a condensation purification device and a recovery reaction device;
The water inlet end of the preheater is connected with the water outlet end of the anaerobic acid production system, and the vapor-liquid outlet end of the preheater is connected with the vapor-liquid inlet end of the primary negative pressure low temperature deamination device;
The steam inlet of the secondary negative pressure low temperature deamination device is connected with a steam system, and the secondary steam outlet end of the secondary negative pressure low temperature deamination device is connected with the steam inlet end of the primary negative pressure low temperature deamination device;
The deamination fermentation liquor outlet end of the primary negative pressure low-temperature deamination device is connected with the deamination fermentation liquor inlet end of the secondary negative pressure low-temperature deamination device, the deamination fermentation liquor outlet end of the secondary negative pressure low-temperature deamination device is connected with the deamination fermentation liquor reflux inlet end of the preheater, and the deamination fermentation liquor is discharged from the deamination fermentation liquor outlet end at the bottom of the preheater;
The vapor-phase ammonia nitrogen recovery end positioned at the top of the primary negative pressure low temperature deamination device is connected with the condensation purification device, the condensation purification device is connected with a reaction recovery device, and carbon dioxide and water are arranged in the reaction recovery device; the outlet of the reaction recovery device is connected with the crystallization tank.
Optionally, an intermediate filter 1 is arranged between the deamination fermentation liquor outlet end of the primary negative pressure low-temperature deamination device and the deamination fermentation liquor inlet end of the secondary negative pressure low-temperature deamination device, and the concentration of suspended matters is 10-500mg/L after the deamination fermentation liquor is filtered by the intermediate filter 1.
Optionally, the condensation purification device comprises a steam outlet end and a vapor ammonia nitrogen outlet end, wherein the vapor ammonia nitrogen outlet end positioned at the upper part of the condensation purification device is connected with the recovery reaction device, and the steam outlet end positioned at the bottom of the condensation purification device is connected with the vapor inlet end of the primary negative pressure low temperature deamination device.
Optionally, the bottom discharge gate of crystallization jar is connected with centrifuge, centrifuge liquid phase export is connected with the mother liquor jar, the bottom export of mother liquor jar with retrieve the water inlet that reaction unit is located upper portion is connected.
Optionally, a mother liquor filter is arranged between the bottom outlet of the mother liquor tank and the recovery reaction device.
Optionally, the alkali adding system II further comprises a pH probe, a PLC control system and an alkali adding pump, wherein the pH probe is positioned in the anaerobic fermentation tank, the pH probe is in signal connection with the PLC control system, the PLC control system is in control connection with the alkali adding pump, and the alkali adding pump is in pipeline connection with the alkali tank;
when the detection signal of the pH probe reaches the set value pH 8-10, the PLC control system controls the alkali adding pump to be started, and alkaline substances in the alkali tank are conveyed to alkaline substances in the anaerobic fermentation tank.
Optionally, the anaerobic acid producing system is a membrane anaerobic system, the membrane anaerobic system comprises an anaerobic fermentation tank, a water outlet device, a middle buffer tank and an external tubular membrane assembly, the anaerobic fermentation tank, the water outlet device, the middle buffer tank and the water inlet end and the water outlet end of the external tubular membrane assembly are connected in sequence through pipelines, and fermentation liquor containing the organic acid/organic acid salt produced by the anaerobic acid producing system is discharged from the water outlet end of the external tubular membrane assembly; the external tubular membrane assembly is formed by connecting a plurality of membrane tubes through elbows.
Optionally, the membrane anaerobic system further comprises a roller screening machine and a sludge filter;
the water outlet device, the roller screening machine, the middle buffer tank, the sludge filter and the water inlet end and the water outlet end of the tubular membrane assembly are connected in sequence through pipelines.
Optionally, the concentrated solution outlet end of the external tubular membrane assembly is connected with the reflux water inlet end of the intermediate buffer tank, the reflux water outlet end of the intermediate buffer tank is connected with the reflux water inlet end of the anaerobic fermentation tank, and the external tubular membrane assembly, the intermediate buffer tank and the anaerobic fermentation tank form a concentrated solution reflux circulation system; the inlet end of the external tubular membrane assembly is connected with a circulating pump, and the cross flow rate of the inlet end of the external tubular membrane assembly is controlled to be 4-6m/s.
The invention further aims to provide an operation method of the kitchen waste dephosphorization and nitrogen removal system, wherein kitchen waste enters an anaerobic acid production system to carry out anaerobic acid production reaction after being pretreated, alkaline substances are added into the anaerobic acid production system through an alkali adding system, the pH value is more than or equal to 8.0, metal ions in the alkaline substances react with phosphorus to precipitate, and dephosphorization fermentation liquor containing organic acid/organic acid salt is obtained; and (3) introducing the fermentation liquor into a denitrification system for denitrification treatment to finally obtain dephosphorized and denitrified fermentation liquor.
Optionally, the alkaline substances are NaOH and Ca (OH) 2, wherein the amount of Ca (OH) 2 is such that calcium phosphate precipitate is formed with phosphate, and the balance is NaOH.
Optionally, the kitchen waste comprises kitchen waste organic solid residues and/or kitchen waste water after centrifugal filtration, wherein the protein content of the kitchen waste organic solid residues is 10% -30%; the COD of the kitchen waste water is 90000-120000mg/L, the total nitrogen is 1000-3000mg/L, and the total phosphorus is 100-300mg/L.
Optionally, when the kitchen waste is a mixture of kitchen waste organic solid slag and kitchen waste water, the weight ratio of the kitchen waste organic solid slag to the kitchen waste water is (5-10): (70-90); when the kitchen waste is kitchen waste organic solid slag, the kitchen waste organic solid slag is diluted by adding water, and the mass concentration of the kitchen waste organic solid slag is 10%.
Optionally, the denitrification system is a steam evaporation denitrification system, and has a three-stage circulation denitrification process:
2.1 Primary denitrification: the fermentation liquor and a heat supply device of a preheater and the secondary deamination fermentation liquor in the secondary negative pressure low-temperature deamination device are subjected to mass transfer and heat transfer in a backflow manner, part of fermentation liquor is converted into vapor-phase ammonia nitrogen and deamination fermentation liquor at 50-65 ℃, and the vapor-phase ammonia nitrogen and the residual fermentation liquor enter the primary negative pressure low-temperature deamination device;
2.2 Secondary denitrification): fresh steam is introduced into the secondary negative pressure low-temperature deamination device;
after entering a primary negative pressure low temperature deamination device, the vapor ammonia nitrogen and the residual fermentation liquor carry out secondary denitrification with the mass transfer and heat transfer of fresh steam from a secondary negative pressure low temperature deamination device to obtain ammonia-containing steam and secondary deamination fermentation liquor; the secondary deamination fermentation liquor enters a secondary negative pressure low-temperature deamination device;
The ammonia-containing steam is discharged from the top and enters an ammonia absorption unit for condensation, purification and recovery; carbon dioxide and water are introduced into an ammonium bicarbonate reaction recovery device in the ammonia absorption unit, and react with ammonia-containing steam to generate ammonium bicarbonate solution, crystals are separated out after the ammonium bicarbonate solution is supersaturated, and solid ammonium bicarbonate is obtained through centrifugal dehydration;
2.3 Three denitrification: the secondary deamination fermentation liquor enters a secondary negative pressure low-temperature deamination device, mass transfer and heat transfer are carried out on the secondary deamination fermentation liquor and fresh steam, tertiary denitrification is carried out on the secondary deamination fermentation liquor to obtain ammonia-containing steam and tertiary deamination fermentation liquor, the ammonia-containing steam and the fresh steam enter a primary negative pressure low-temperature deamination device together, the tertiary deamination fermentation liquor flows back to the preheater, the step 2.1) is obtained after mass transfer and heat transfer, and the deamination fermentation liquor is discharged from a deamination fermentation liquor water outlet end at the bottom of the preheater.
Optionally, the anaerobic acidogenesis reaction comprises the following steps:
1.1 Filtering kitchen waste, then entering an anaerobic fermentation tank, adding alkaline substances to control the pH to be more than or equal to 8.0, and performing anaerobic acid production reaction at 30-57 ℃, wherein the kitchen waste is decomposed into hydrogen, CO 2 and initial fermentation liquor;
1.2 Collecting the hydrogen and the CO 2 through a gas-liquid separator;
1.3 And (3) discharging the initial fermentation liquor from the water outlet end of the anaerobic fermentation tank, filtering to obtain fermentation liquor after anaerobic acid production, and discharging for later use.
Optionally, the acid yield of the anaerobic acid production process is greater than 30g/L.
Optionally, the products of the anaerobic acidogenesis reaction further comprise gaseous products H 2 and CO 2,H2, wherein the mass concentration of the gaseous products H 2 and CO 2 is 40-70%.
The beneficial effects are that: compared with the prior art, the dephosphorization and nitrogen removal method for kitchen waste has the following advantages,
(1) The process flow is shorter, and the cost is saved compared with the traditional kitchen garbage treatment;
(2) The high-concentration organic acid/organic acid salt obtained in the alkaline fermentation acid production process can be used as a carbon source in the subsequent denitrification process, and is beneficial to improving the ammonia nitrogen removal efficiency.
(4) The anaerobic alkaline acid-producing products are H 2 and CO 2 gaseous products, wherein H 2 can be recycled as clean energy, and the method is an environment-friendly kitchen waste treatment mode;
(5) The method has the advantages that the effect is better than that of the traditional struvite precipitation of phosphorus and ammonia nitrogen by adopting calcium phosphate precipitation and ammonia nitrogen steam evaporation, and meanwhile, the problems of difficult struvite precipitation and the like caused by uncoordinated proportion of phosphorus and ammonia nitrogen in fermentation liquor are solved.
Drawings
Fig. 1 is a schematic diagram of a dephosphorization and nitrogen removal system for kitchen waste.
Fig. 2 is a process flow chart of dephosphorization and nitrogen removal of kitchen waste.
FIG. 3 is a schematic diagram of a membrane anaerobic system;
FIG. 4 is a schematic diagram of a steam evaporation denitrification treatment system;
Reference numerals: an anaerobic acid producing system I, an alkali adding system II, a denitrification system III, a concentrating system IV, a water inlet pump 1, a raw water filter 2, an anaerobic fermentation tank 3, a pH probe 301, an alkali tank 302, a PLC control system 303, an alkali adding pump 304, a gas-liquid separator 4, a water outlet 5, an intermediate buffer tank 6, an intermediate buffer tank reflux pump 7, a mud inlet pump 8, a sludge filter 9, a circulating pump 10, a membrane module 11, a drum separator 12, a drum separator water outlet 13, a drum separator water outlet 14, an extruder 15, an elbow 16, a first pipeline Q1, a second pipeline Q2, a third pipeline Q3, a fourth pipeline Q4, a fifth pipeline Q5, a sixth pipeline Q6, a seventh pipeline Q7, an eighth pipeline Q8, a ninth pipeline Q9, a tenth pipeline Q10, an eleventh pipeline Q11, a twelfth pipeline Q12, a preheater 501, a first-stage negative pressure low-temperature deamination device 502, a second-stage negative pressure low-temperature deamination device 504, an intermediate filter 5031, a condensation purification device 504, a condenser 505, a crystallizer 5053, a 5052, and a recovery system 5056.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
The system comprises an anaerobic acid production system I, an alkali addition system II and a denitrification system III, wherein kitchen waste enters from the water inlet end of the anaerobic acid production system I, the water outlet end of the anaerobic acid production system I is connected with the water inlet end of the denitrification system III, fermentation liquor containing organic acid/organic acid salt is discharged from the water outlet end of the denitrification system III, and vapor ammonia nitrogen is discharged from the steam outlet end of the denitrification system III;
the anaerobic acid production system I comprises an anaerobic fermentation tank 3, and a gas-liquid separator 4 is arranged at the top of the anaerobic fermentation tank 3;
The alkali adding system II comprises an alkali tank 302, wherein an alkaline substance for adjusting the pH of the water body is stored in the alkali tank 302;
The alkali tank 302 is connected with the anaerobic fermentation tank 3;
The denitrification system III is a steam evaporation denitrification system.
As an alternative embodiment, the set point is pH 8-10.
Fig. 2 shows a process flow chart of dephosphorization and nitrogen removal of kitchen waste. The method can be divided into the following two steps:
1. Anaerobic alkaline acid production technology for kitchen waste
The treatment object of the invention is kitchen waste, comprising filtered kitchen waste organic solid slag and/or kitchen waste water, wherein the protein content of the kitchen waste organic solid slag (dry matter) is 10% -30%; COD of the kitchen waste water is 90000-120000mg/L, total nitrogen is 1000-3000mg/L, and total phosphorus is 100-300mg/L. Wherein, when the kitchen waste is a mixture of kitchen waste organic solid slag and kitchen waste water, the weight ratio of the kitchen waste organic solid slag to the kitchen waste water is (5-10): (70-90); when the kitchen waste is kitchen waste organic solid slag, the kitchen waste organic solid slag is diluted by adding water, and the mass concentration of the kitchen waste organic solid slag is 10%.
Optionally, the anaerobic acid production process of the invention can be performed in a membrane anaerobic system, as shown in fig. 3, a water inlet pump 1, a raw water filter 2, an anaerobic fermentation tank 3, a gas-liquid separator 4, a water outlet device 5, a drum screening machine 12, an intermediate buffer tank 6, a mud inlet pump 8, a sludge filter 9, a circulating pump 10, a water inlet end and a water outlet end of an external tubular membrane assembly 11 are sequentially connected in a pipeline, and fermentation liquor containing the organic acid/organic acid salt produced by the anaerobic acid production system is discharged from the water outlet end of the external tubular membrane assembly 11;
optionally, each membrane tube of the external tubular membrane assembly 11 is connected together through an elbow 16, and in order to facilitate drawing out the fibers deposited at the membrane sludge inlet end by hand, a hand hole is formed in the elbow 16.
Optionally, the concentrated solution outlet end of the external tubular membrane assembly 11 is connected with the reflux water inlet end of the intermediate buffer tank 6, the reflux water outlet end of the intermediate buffer tank 6 is connected with the reflux water inlet end of the anaerobic fermentation tank 3 through the intermediate buffer tank reflux pump 7, and the external tubular membrane assembly 11, the intermediate buffer tank 6 and the anaerobic fermentation tank 3 form a concentrated solution reflux circulation system.
Wherein the drum screen 12 is provided with a drum screen water producing port 13 and a drum screen slag producing port 14, the drum screen water producing port 13 is connected to the intermediate buffer tank 6, and the drum screen slag producing port 14 is connected to the extruder 15.
As shown in fig. 3, the anaerobic acid production system i comprises an anaerobic fermentation tank 3, and a gas-liquid separator 4 is arranged at the top of the anaerobic fermentation tank 3; the alkali adding system II comprises an alkali tank 302, wherein an alkaline substance for adjusting the pH of the water body is stored in the alkali tank 302; the alkali tank 302 is connected with the anaerobic fermentation tank 3.
As an optional implementation manner, the alkali adding system ii further includes a pH probe 301, a PLC control system 303, and an alkali adding pump 304, where the pH probe 301 is located in the anaerobic fermentation tank 3, the pH probe 301 is in signal connection with the PLC control system 303, the PLC control system 303 is in control connection with the alkali adding pump 304, and the alkali adding pump 304 is in pipeline connection with the alkali tank 302;
When the detection signal of the pH probe 301 reaches a set value, the PLC control system 303 controls the alkali adding pump 304 to be turned on, so as to convey the alkaline substance in the alkali tank 302 to the alkaline substance in the anaerobic fermentation tank 3.
The anaerobic fermentation process of the membrane type anaerobic system is as follows:
1.1 The kitchen waste high-concentration wastewater enters from a first pipeline Q1, impurities are removed through a water inlet pump 1 and a raw water filter 2, and then the kitchen waste high-concentration wastewater is lifted to an anaerobic fermentation tank 3, the temperature in the anaerobic fermentation tank 3 is maintained at 35-40 ℃ or 50-55 ℃, and alkaline substances are added through an alkaline adding system to control the pH value to be more than or equal to 8.0; the alkali adding system is used for adding Ca (OH) 2 and NaOH, and comprises a pH probe 301, an alkali tank 302, a PLC control system 303 and an alkali adding pump 304, wherein Ca (OH) 2 and NaOH are stored in the alkali tank 302 after being mixed; wherein, the pH probe 301 in the anaerobic fermentation tank 3 monitors the pH in the anaerobic fermentation tank 3 in real time, when the pH is lower than a set value, the PLC control system 303 controls the alkali adding pump 304 to automatically add alkali from the alkali tank 302 to the anaerobic fermentation tank 3 through the thirteenth pipeline Q13, the set value is pH 8-9, and the pH in the tank is maintained at about 9; the kitchen garbage is firstly hydrolyzed into small molecular substances by macromolecular large particle substances under the condition of hydrolytic acidification bacteria, then is further degraded into volatile fatty acid and hydrogen under the condition of hydrogen-producing acetogenic bacteria, and in the prior art, the volatile fatty acid is decomposed into methane under the condition of methanogenic bacteria, wherein the optimal pH value of the methanogenic bacteria is 6.8-7.5; the pH is controlled to be above 8.0, preferably 8-9 by adding alkali, so that the activity of methanogen is inhibited, the methanogen process is blocked, and the reactor process is controlled to be in the stage of hydrogen production and acetic acid production, so that acetic acid is further decomposed into CO 2;
1.2 The gas products (hydrogen and CO 2) generated after anaerobic fermentation are collected and utilized after passing through a gas-liquid separator 4;
1.3 The fermented initial fermentation liquid enters a drum screening machine 12 from a ninth pipeline through a water outlet device 5 for filtration and then enters an intermediate buffer tank 6 for buffer storage from a water outlet 13 of the drum screening machine through a tenth pipeline Q10; after the residues discharged from the residue producing port 14 of the drum screening machine enter an extruder 15 for further solid-liquid separation treatment, separating liquid and separated residues are respectively discharged from an eleventh pipeline Q11 and a twelfth pipeline Q12 and enter the next treatment link;
1.4 The buffered initial fermentation liquor is filtered and filtered from the third pipeline Q3 to the external tubular membrane assembly 11 through the sludge inlet pump 8 and the sludge filter 9, and the fermentation liquor after anaerobic acidogenesis is discharged through the fifth pipeline Q5; the membrane concentrate flows back to the intermediate buffer tank 6 through a sixth pipeline Q6 and an eighth pipeline Q8 in sequence, and then flows back to the anaerobic fermentation tank 3 from the second pipeline Q2 through the intermediate buffer tank reflux pump 7; the circulation pump 10 provides a cross-flow rate of 4-6m/s for the external tubular membrane module 11 to slow down membrane fouling.
Alternatively, the membrane used in the invention is a tubular membrane, the material used is PVDF membrane, the pure water flux is 700L/m 2 h, the bubble point is 0.03, and the bursting strength is 4.2Mpa.
Anaerobic fermentation result:
The acid yield of kitchen waste after 5-10 days of fermentation is more than 30g/L, and the pH value of the obtained acidified fermentation liquor is 8-10;
The precipitated calcium phosphate in the reaction system is about 200mg/L, and the phosphorus removal efficiency reaches about 90%.
The dephosphorized fermentation liquor containing organic acid/organic acid salt is obtained, and the mass concentration of the organic acid/organic acid salt is more than 3%. The mass concentration of H 2 in the gaseous products H 2 and CO 2 is 40-70%, and the rest is CO 2.
2. Steam evaporation technology for high-concentration ammonia nitrogen
The acidified fermentation liquor is subjected to denitrification treatment by adopting a steam evaporation denitrification treatment system, as shown in fig. 4, the steam evaporation denitrification system comprises a preheater 501, a primary negative pressure low-temperature deamination device 502, a secondary negative pressure low-temperature deamination device 503, a condensation purification device 504 and a recovery reaction device 505;
The water inlet end of the preheater 501 is connected with the water outlet end of the anaerobic acid production system I, and the vapor-liquid outlet end of the preheater 501 is connected with the vapor-liquid inlet end of the primary negative pressure low temperature deamination device 502;
The steam inlet of the second-stage negative pressure low-temperature deamination device 503 is connected with a steam system, and the secondary steam outlet end of the second-stage negative pressure low-temperature deamination device 503 is connected with the steam inlet end of the first-stage negative pressure low-temperature deamination device 502;
The deamination fermentation liquor outlet end of the primary negative pressure low-temperature deamination device 502 is connected with the deamination fermentation liquor inlet end of the secondary negative pressure low-temperature deamination device 503, the deamination fermentation liquor outlet end of the secondary negative pressure low-temperature deamination device 503 is connected with the deamination fermentation liquor reflux inlet end of the preheater 501, and the deamination fermentation liquor is discharged from the deamination fermentation liquor outlet end at the bottom of the preheater 501;
The vapor ammonia nitrogen recovery end positioned at the top of the primary negative pressure low temperature deamination device 502 is connected with the condensation purification device 504, the condensation purification device 504 is connected with a reaction recovery device 505, and the reaction recovery device 505 is internally provided with carbon dioxide and water; the outlet of the reaction recovery device 505 is connected to a crystallization tank 5052.
Optionally, the condensation and purification device 504 includes a vapor outlet end and a vapor ammonia nitrogen outlet end, where the vapor ammonia nitrogen outlet end located at the upper part of the condensation and purification device 504 is connected to the recovery reaction device 505, and the vapor outlet end located at the bottom of the condensation and purification device 504 is connected to the vapor inlet end of the first-stage negative pressure low-temperature deamination device 502.
Optionally, the bottom outlet of the crystallization tank 5052 is connected with a centrifuge 5053, the liquid phase outlet of the centrifuge 5053 is connected with a mother liquor tank 5054, and the bottom outlet of the mother liquor tank 5054 is connected with a water inlet end of the recovery reaction device 505 at the upper part.
Optionally, a mother liquor filter 5055 is provided between the bottom outlet of the mother liquor tank 5054 and the recovery reactor 505.
The steam evaporation denitrification treatment system has a three-stage circulation denitrification process, and the process principle and the process are as follows:
2.1 Primary denitrification: the mass transfer and heat transfer of the fermentation liquor and the heat supply device of the preheater 501 and the secondary deamination fermentation liquor in the secondary negative pressure low temperature deamination device 503 are performed by reflux, part of the fermentation liquor is converted into vapor-phase ammonia nitrogen and deamination fermentation liquor at 50-65 ℃, and the vapor-phase ammonia nitrogen and the rest fermentation liquor enter the primary negative pressure low temperature deamination device 502;
2.2 Secondary denitrification): fresh steam is introduced into the secondary negative pressure low-temperature deamination device 503;
After entering the primary negative pressure low temperature deamination device 502, the vapor ammonia nitrogen and the residual fermentation liquor carry out secondary denitrification with the mass transfer and heat transfer of fresh steam from the secondary negative pressure low temperature deamination device 503 to obtain ammonia-containing steam and secondary deamination fermentation liquor; the secondary deamination fermentation liquor enters a secondary negative pressure low-temperature deamination device 503;
The ammonia-containing steam is discharged from the top and enters a condensing and purifying device 504 for condensing, purifying and recycling; carbon dioxide and water are introduced into a reaction recovery device 505 arranged in the condensation and purification device 504, and react with ammonia-containing steam to generate ammonium bicarbonate solution, crystals are separated out after the ammonium bicarbonate solution is supersaturated, and solid ammonium bicarbonate is obtained through centrifugal dehydration;
2.3 Three denitrification: the secondary deamination fermentation liquor enters a secondary negative pressure low-temperature deamination device 503, and is subjected to mass transfer and heat transfer with fresh steam, and is subjected to tertiary denitrification to obtain ammonia-containing steam and tertiary deamination fermentation liquor, the ammonia-containing steam and the fresh steam enter a primary negative pressure low-temperature deamination device 502 together, the tertiary deamination fermentation liquor flows back to the preheater 501, and after mass transfer and heat transfer, the deamination fermentation liquor is obtained in step 2.1), and is discharged from a deamination fermentation liquor water outlet end at the bottom of the preheater 501.
Optionally, the secondary deamination fermentation liquid discharged from the primary negative pressure low-temperature deamination device is conveyed to an intermediate filter through a pump to reduce SS to 10-500mg/L, and then enters the secondary negative pressure low-temperature deamination device;
The first-stage and second-stage negative pressure low-temperature deamination devices adopt a direct heating mode, fresh steam firstly enters the second-stage negative pressure low-temperature deamination devices and moves vertically from bottom to top in the second-stage negative pressure low-temperature deamination devices, vertically moving steam enters the bottoms of the first-stage negative pressure low-temperature deamination devices through pipelines at the tops of the second-stage negative pressure low-temperature deamination devices and moves vertically from bottom to top in the first-stage negative pressure low-temperature deamination devices, and vertically moving steam finally forms vapor phase steam containing ammonia at the tops of the first-stage negative pressure low-temperature deamination devices; the mass transfer and heat transfer of gas and liquid phases of the fermentation liquor and the steam are respectively realized in the primary negative pressure low-temperature deamination device and the secondary negative pressure low-temperature deamination device, and the transfer of carbon dioxide and ammonia in the fermentation liquor to the steam is completed, so that the mass concentration of ammonia nitrogen in the fermentation liquor subjected to the two-stage negative pressure low-temperature deamination is reduced from 4000mg/L to below 400 mg/L.
Vapor phase steam containing ammonia enters a condensation purification device from the top of the primary negative pressure low temperature deamination device, then the steam is condensed and flows back, and only the vapor phase containing ammonia and carbon dioxide enters a subsequent ammonium bicarbonate reaction recovery device; and (3) reacting ammonia gas in a gas phase, carbon dioxide and water in the reaction device in the ammonium bicarbonate reaction recovery device to form ammonium bicarbonate, continuously saturating to form crystallization liquid, and finally obtaining saturated ammonium bicarbonate liquid and ammonium bicarbonate crystals through solid-liquid separation.
Denitrification results of the steam evaporation denitrification treatment system:
After steam evaporation, the residual ammonia nitrogen in the acidified fermentation broth is lower than 200mg/L, and the ammonia nitrogen removal efficiency reaches about 90%; the evaporated ammonia gas is recovered into ammonium bicarbonate. The steam evaporation process maintains low losses of organic acid, thereby helping to increase the C: N ratio in the acidified fermentation broth.
The invention will be further illustrated with reference to examples. The invention will be better understood from the following examples. However, it will be readily understood by those skilled in the art that the specific material ratios, process conditions and results thereof described in the examples are illustrative of the present invention and should not be construed as limiting the invention described in detail in the claims.
Example 1
The process for preparing the denitrification and dephosphorization from the kitchen waste comprises the following steps:
1) Anaerobic alkaline acid production technology for kitchen waste
The treatment object of this embodiment is kitchen waste, which is a mixture of filtered kitchen waste organic solid slag and kitchen waste water, and the weight ratio of the kitchen waste organic solid slag to the kitchen waste water is 8:80. wherein the protein content of the kitchen waste organic solid residue (dry matter) is 19.6%; COD of the kitchen waste water is 108480mg/L, total nitrogen is 2156mg/L, and total phosphorus is 227mg/L.
In a membrane anaerobic system, naOH and Ca (OH) 2 are intermittently added through an alkali adding system to ferment and produce acid, and the pH value is maintained between 8.0 and 9.0 in the reaction process.
Anaerobic fermentation result:
After the residence time of 10 days, the acid yield of the kitchen waste after fermentation is 60g/L, the pH value of the obtained fermentation liquid is about 9, the total phosphorus concentration is 10mg/L, and the ammonia nitrogen concentration is 1154mg/L;
The mass concentration of H 2 in the gaseous products H 2 and CO 2 was 64% with the remainder being CO 2.
2) Steam evaporation technology for high-concentration ammonia nitrogen
After steam evaporation, the residual ammonia nitrogen in the fermentation broth is 200mg/L, and the ammonia nitrogen removal efficiency reaches 90.7%; the evaporated ammonia gas is recovered into ammonium bicarbonate.
Example 2
The process for preparing the denitrification and dephosphorization from the kitchen waste comprises the following steps:
1) Anaerobic alkaline acid production technology for kitchen waste
The treatment object of the embodiment is kitchen waste, which is kitchen waste water after centrifugal filtration, COD of the kitchen waste water is 108480mg/L, total nitrogen is 2156mg/L, and total phosphorus is 227mg/L.
In a membrane anaerobic system, naOH and Ca (OH) 2 are intermittently added through an alkali adding system to ferment and produce acid, and the pH value is maintained between 8.0 and 9.0 in the reaction process.
Anaerobic fermentation result:
after the residence time of 10 days, the acid yield of the kitchen waste after fermentation is 50g/L, the pH value of the obtained fermentation liquid is about 9, the total phosphorus concentration is 9mg/L, and the ammonia nitrogen concentration is 958mg/L;
The mass concentration of H 2 in the gaseous products H 2 and CO 2 was 55% with the remainder being CO 2.
2) Steam evaporation technology for high-concentration ammonia nitrogen
After steam evaporation, the residual ammonia nitrogen in the fermentation broth is 150mg/L, and the ammonia nitrogen removal efficiency reaches 93%; the evaporated ammonia gas is recovered into ammonium bicarbonate.
Example 3
The process for preparing the denitrification and dephosphorization from the kitchen waste comprises the following steps:
1) Anaerobic alkaline acid production technology for kitchen waste
The treatment object of this embodiment is kitchen waste, including filtered kitchen waste organic solid residue, wherein the protein content of the kitchen waste organic solid residue (dry matter) is 19.6%.
Before anaerobic fermentation, the organic solid residue of kitchen waste is diluted and fermented by adding water, so that the mass concentration of the organic solid residue reaches 10%.
The kitchen garbage is in a membrane anaerobic system, ca (OH) 2 is intermittently added by an alkali adding system, fermentation and acid production are carried out, and the pH value is maintained between 8.0 and 9.0 in the reaction process.
Anaerobic fermentation result:
After the residence time of 10 days, the acid yield of the kitchen waste after fermentation is 45g/L, the pH value of the obtained fermentation liquid is about 9, the total phosphorus concentration is 7mg/L, and the ammonia nitrogen concentration is 820mg/L;
The mass concentration of H 2 in the gaseous products H 2 and CO 2 was 50% with the remainder being CO 2.
2) Steam evaporation technology for high-concentration ammonia nitrogen
After steam evaporation, the residual ammonia nitrogen in the fermentation broth is 105mg/L, and the ammonia nitrogen removal efficiency reaches 87.2%; the evaporated ammonia gas is recovered into ammonium bicarbonate.
The foregoing is only a preferred embodiment of the invention, it being noted that: it will be apparent to those skilled in the art that various modifications and adaptations can be made without departing from the principles of the present invention, and such modifications and adaptations are intended to be comprehended within the scope of the invention.
Claims (14)
1. The kitchen waste dephosphorization and nitrogen removal system is characterized by comprising an anaerobic acid production system (I), an alkali addition system (II) and a nitrogen removal system (III), wherein the alkali addition system (II) is connected with the anaerobic acid production system (I), and the anaerobic acid production system (I) is connected with the nitrogen removal system (III); kitchen waste enters from the water inlet end of the anaerobic acid production system (I), the water outlet end of the anaerobic acid production system (I) is connected with the water inlet end of the denitrification system (III), fermentation liquor containing organic acid/organic acid salt is discharged from the water outlet end of the denitrification system (III), and vapor ammonia nitrogen is discharged from the steam outlet end of the denitrification system (III);
The anaerobic acid production system (I) comprises an anaerobic fermentation tank (3), and a gas-liquid separator (4) is arranged at the top of the anaerobic fermentation tank (3);
the alkali adding system (II) comprises an alkali tank (302), wherein an alkaline substance for adjusting the pH of the water body is stored in the alkali tank (302);
the alkali tank (302) is connected with the anaerobic fermentation tank (3);
the denitrification system (III) is a steam evaporation denitrification system;
The steam evaporation denitrification system comprises a preheater (501), a primary negative pressure low-temperature deamination device (502), a secondary negative pressure low-temperature deamination device (503), a condensation purification device (504) and a recovery reaction device (505);
The water inlet end of the preheater (501) is connected with the water outlet end of the anaerobic acid production system (I), and the vapor-liquid outlet end of the preheater (501) is connected with the vapor-liquid inlet end of the primary negative pressure low temperature deamination device (502);
the steam inlet of the secondary negative pressure low temperature deamination device (503) is connected with a steam system, and the secondary steam outlet end of the secondary negative pressure low temperature deamination device (503) is connected with the steam inlet end of the primary negative pressure low temperature deamination device (502);
The deamination fermentation liquor outlet end of the primary negative pressure low-temperature deamination device (502) is connected with the deamination fermentation liquor inlet end of the secondary negative pressure low-temperature deamination device (503), the deamination fermentation liquor outlet end of the secondary negative pressure low-temperature deamination device (503) is connected with the deamination fermentation liquor reflux inlet end of the preheater (501), and the deamination fermentation liquor is discharged from the deamination fermentation liquor outlet end at the bottom of the preheater (501);
The vapor-phase ammonia nitrogen recovery end positioned at the top of the primary negative pressure low-temperature deamination device (502) is connected with the condensation purification device (504), the condensation purification device (504) is connected with a reaction recovery device (505), and the reaction recovery device (505) is internally provided with carbon dioxide and water; the outlet of the reaction recovery device (505) is connected with a crystallization tank (5052);
pretreating kitchen waste, entering an anaerobic acid production system (I) for anaerobic acid production reaction, adding alkaline substances into the anaerobic acid production system (I) through an alkali addition system (II), and regulating the pH value to be more than or equal to 8.0, wherein metal ions in the alkaline substances react with phosphorus to precipitate, so as to obtain dephosphorized fermentation liquor containing organic acid/organic acid salt; the fermentation liquor enters a denitrification system (III) for denitrification treatment, and finally dephosphorization and denitrification fermentation liquor is obtained;
The alkaline substances are NaOH and Ca (OH) 2, wherein the dosage of Ca (OH) 2 is that calcium phosphate precipitate is formed by the Ca (OH) 2 and phosphate, and the rest is NaOH;
The denitrification system (III) is a steam evaporation denitrification system and comprises a three-stage circulation denitrification process:
2.1 Primary denitrification: the fermentation liquor and a heat supply device of a preheater and the secondary deamination fermentation liquor in the secondary negative pressure low-temperature deamination device are subjected to mass transfer and heat transfer in a backflow manner, part of fermentation liquor is converted into vapor-phase ammonia nitrogen and deamination fermentation liquor at 50-65 ℃, and the vapor-phase ammonia nitrogen and the residual fermentation liquor enter the primary negative pressure low-temperature deamination device;
2.2 Secondary denitrification): fresh steam is introduced into the secondary negative pressure low-temperature deamination device;
after entering a primary negative pressure low temperature deamination device, the vapor ammonia nitrogen and the residual fermentation liquor carry out secondary denitrification with the mass transfer and heat transfer of fresh steam from a secondary negative pressure low temperature deamination device to obtain ammonia-containing steam and secondary deamination fermentation liquor; the secondary deamination fermentation liquor enters a secondary negative pressure low-temperature deamination device;
The ammonia-containing steam is discharged from the top and enters a condensing and purifying device for condensing, purifying and recycling; carbon dioxide and water are introduced into a reaction recovery device arranged in the condensation purification device, and react with ammonia-containing steam to generate ammonium bicarbonate solution, crystals are separated out after the ammonium bicarbonate solution is supersaturated, and solid ammonium bicarbonate is obtained through centrifugal dehydration;
2.3 Three denitrification: the secondary deamination fermentation liquor enters a secondary negative pressure low-temperature deamination device, mass transfer and heat transfer are carried out on the secondary deamination fermentation liquor and fresh steam, tertiary denitrification is carried out on the secondary deamination fermentation liquor to obtain ammonia-containing steam and tertiary deamination fermentation liquor, the ammonia-containing steam and the fresh steam enter a primary negative pressure low-temperature deamination device together, the tertiary deamination fermentation liquor flows back to the preheater, the step 2.1) is obtained after mass transfer and heat transfer, and the deamination fermentation liquor is discharged from a deamination fermentation liquor water outlet end at the bottom of the preheater.
2. The dephosphorization and nitrogen removal system for kitchen waste according to claim 1, wherein an intermediate filter (5031) is arranged between the deamination fermentation liquor outlet end of the primary negative pressure low temperature deamination device (502) and the deamination fermentation liquor inlet end of the secondary negative pressure low temperature deamination device (503), and the suspended matter concentration is 10-500mg/L after the deamination fermentation liquor is filtered by the intermediate filter (5031).
3. The kitchen waste dephosphorization and nitrogen removal system according to claim 1, wherein the condensation and purification device (504) comprises a steam outlet end and a vapor ammonia nitrogen outlet end, wherein the vapor ammonia nitrogen outlet end positioned at the upper part of the condensation and purification device (504) is connected with the recovery reaction device (505), and the steam outlet end positioned at the bottom of the condensation and purification device (504) is connected with the vapor inlet end of the primary negative pressure low temperature deamination device (502).
4. The kitchen waste dephosphorization and nitrogen removal system according to claim 1, wherein a bottom discharge port of the crystallization tank (5052) is connected with a centrifuge (5053), a liquid phase outlet of the centrifuge (5053) is connected with a mother liquor tank (5054), and a bottom outlet of the mother liquor tank (5054) is connected with a water inlet end of the recovery reaction device (505) at the upper part.
5. The system for dephosphorization and nitrogen removal of kitchen waste according to claim 4, characterized in that a mother liquor filter (5055) is arranged between the bottom outlet of the mother liquor tank (5054) and the recovery reaction device (505).
6. The kitchen waste dephosphorization and nitrogen removal system according to claim 1, wherein the alkali adding system (ii) further comprises a pH probe (301), a PLC control system (303) and an alkali adding pump (304), wherein the pH probe (301) is positioned in the anaerobic fermentation tank (3), the pH probe (301) is in signal connection with the PLC control system (303), the PLC control system (303) is in control connection with the alkali adding pump (304), and the alkali adding pump (304) is in pipeline connection with the alkali tank (302);
When the detection signal of the pH probe (301) reaches a set value pH 8-10, the PLC control system (303) controls the alkali adding pump (304) to be started, and alkaline substances in the alkali tank (302) are conveyed to alkaline substances in the anaerobic fermentation tank (3).
7. The kitchen waste dephosphorization and nitrogen removal system according to claim 1, wherein the anaerobic acid production system (I) is a membrane type anaerobic system, the membrane type anaerobic system comprises an anaerobic fermentation tank (3), a water outlet device (5), an intermediate buffer tank (6) and an external tubular membrane assembly (11), the anaerobic fermentation tank (3), the water outlet device (5), the intermediate buffer tank (6) and the water inlet end and the water outlet end of the external tubular membrane assembly (11) are sequentially connected in a pipeline manner, and fermentation liquor containing the organic acid/organic acid salt produced by the anaerobic acid production system is discharged from the water outlet end of the external tubular membrane assembly (11); the external tubular membrane assembly (11) is formed by connecting a plurality of membrane tubes through elbows (16).
8. A kitchen waste dephosphorization and denitrification system according to claim 7, wherein the membrane anaerobic system further comprises a drum screen (12) and a sludge filter (9);
The water outlet device (5), the drum screening machine (12), the intermediate buffer tank (6), the sludge filter (9) and the water inlet end and the water outlet end of the tubular membrane assembly (11) are connected through pipelines in sequence.
9. The kitchen waste dephosphorization and nitrogen removal system according to claim 7, wherein a concentrated solution outlet end of the external tubular membrane assembly (11) is connected with a reflux water inlet end of the intermediate buffer tank (6), a reflux water outlet end of the intermediate buffer tank (6) is connected with a reflux water inlet end of the anaerobic fermentation tank (3), and the external tubular membrane assembly (11), the intermediate buffer tank (6) and the anaerobic fermentation tank (3) form a concentrated solution reflux circulation system; the inlet end of the external tubular membrane assembly (11) is connected with a circulating pump (10), and the cross flow rate of the inlet end of the external tubular membrane assembly (11) is controlled to be 4-6m/s.
10. The kitchen waste dephosphorization and nitrogen removal system according to claim 1, wherein the kitchen waste comprises centrifugally filtered kitchen waste organic solid slag and/or kitchen waste water, and the protein content of the kitchen waste organic solid slag is 10% -30%; the COD of the kitchen waste water is 90000-120000 mg/L, the total nitrogen is 1000-3000 mg/L, and the total phosphorus is 100-300 mg/L.
11. The system for dephosphorizing and denitriding kitchen waste according to claim 10, wherein when the kitchen waste is a mixture of kitchen waste organic solid slag and kitchen waste water, the weight ratio of the kitchen waste organic solid slag to the kitchen waste water is (5-10): (70-90); when the kitchen waste is kitchen waste organic solid slag, the kitchen waste organic solid slag is diluted by adding water, and the mass concentration of the kitchen waste organic solid slag is 10%.
12. The system for dephosphorization and nitrogen removal of kitchen waste according to claim 1, wherein the anaerobic acidogenic reaction comprises the following steps:
1.1 Filtering kitchen waste, then, entering an anaerobic fermentation tank (3), adding alkaline substances, controlling the pH to be more than or equal to 8.0, and performing anaerobic acid production reaction at 30-57 ℃, wherein the kitchen waste is decomposed into hydrogen, CO 2 and initial fermentation liquor;
1.2 Collecting the hydrogen and the CO 2 through a gas-liquid separator (4);
1.3 And (3) discharging the initial fermentation liquor from the water outlet end of the anaerobic fermentation tank (3), filtering to obtain fermentation liquor after anaerobic acid production, and discharging for later use.
13. The system for dephosphorization and nitrogen removal of kitchen waste according to claim 12, wherein the acid yield of the anaerobic acid production process is more than 30g/L.
14. The system for dephosphorization and nitrogen removal of kitchen waste according to claim 12, wherein the products of the anaerobic acid production reaction further comprise gaseous products H 2 and CO 2,H2, the mass concentration of which is 40-70%, and the balance of which is CO 2.
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