CN215975863U - Dephosphorization and denitrification system for kitchen garbage - Google Patents
Dephosphorization and denitrification system for kitchen garbage Download PDFInfo
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- CN215975863U CN215975863U CN202120725452.1U CN202120725452U CN215975863U CN 215975863 U CN215975863 U CN 215975863U CN 202120725452 U CN202120725452 U CN 202120725452U CN 215975863 U CN215975863 U CN 215975863U
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Abstract
The utility model discloses a system for dephosphorizing and denitriding kitchen waste, which is characterized in that anaerobic acid production is carried out after the kitchen waste is pretreated, and an alkaline substance is added in the process to adjust the pH value (the pH value is more than 8.0) so as to obtain fermentation liquor (the mass concentration of organic acid/organic acid salt is more than 5%) containing organic acid/organic acid salt; and carrying out steam evaporation on the fermentation liquor to remove ammonia nitrogen. The organic acid/organic acid salt in the fermentation liquor is used as a carbon source in the denitrification process, so that the high-efficiency denitrification is realized. In the anaerobic acid production process, the alkaline substance is added, so that the yield of the organic acid/organic acid salt is improved, and the organic acid/organic acid salt can be used as a carbon source in the subsequent denitrification process. On the other hand, the method adopts a steam evaporation method to remove ammonia nitrogen, so that the ammonia nitrogen removal efficiency can be effectively improved.
Description
Technical Field
The utility model belongs to the technical field of organic waste disposal of kitchen waste treatment, and particularly relates to a kitchen waste dephosphorization and denitrification system.
Background
Kitchen waste, also known as kitchen waste, refers to waste generated in activities such as daily life, food processing, food service, unit meal supply and the like of residents, and comprises discarded vegetable leaves, leftovers, fruit peels, egg shells, tea leaves, bones and the like, and the main sources of the kitchen waste are household kitchens, restaurants, mess halls, markets and other industries related to food processing.
The kitchen waste contains extremely high moisture and organic matters, is easy to rot and generates stink. Illegal collection and recycling of kitchen waste can pose a threat to the environment and the health of residents. The kitchen garbage is separately collected, the amount of organic matters entering a landfill can be reduced, the generation of odor and garbage leachate is reduced, the adverse effect of excessive moisture on garbage incineration treatment can be avoided, and the corrosion to equipment is reduced. The kitchen garbage can be converted into new resources through proper treatment and processing, the characteristic of high organic matter content enables the kitchen garbage to be used as fertilizer and feed after strict treatment, methane can be generated 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 the kitchen waste is that the kitchen waste is firstly sorted, is ground and then is subjected to wet heat treatment, and is centrifuged to carry out three-phase separation of waste oil, slurry and solid residues; esterifying the separated waste oil to prepare biodiesel; the slurry is firstly subjected to anaerobic fermentation to produce methane, then aerobic treatment is carried out, and finally the slurry is discharged after reaching the standard; composting or insect absorption is carried out on the kitchen solid residues.
The main problems of the prior art include long process flow, low added value of biogas, difficult standard discharge of slurry and the like, in particular to the problems of high ammonia nitrogen concentration in wastewater, difficult treatment, difficult product sale after solid slag composting and the like. The problems need to be solved effectively, so that effective treatment of kitchen garbage is realized better, and environment-friendly resource recycling is realized.
SUMMERY OF THE UTILITY MODEL
Utility model purpose: in order to overcome the defects in the prior art, the utility model provides a system for removing phosphorus and nitrogen from kitchen waste, which is an efficient, energy-saving and environment-friendly kitchen waste denitrification method, and adopts the mode of adding alkaline substances, improving the pH value of a fermentation system, prolonging the acid production time of fermentation, and effectively removing phosphorus and ammonia nitrogen in the kitchen waste wastewater by combining a steam evaporation denitrification mode.
The technical scheme is as follows: in order to achieve the purpose, the technical scheme adopted by the utility model is mainly summarized as the following 2 steps:
1. an anaerobic alkaline acid production technology for kitchen garbage. Organic matters in the kitchen garbage are converted into organic acid through the metabolism of anaerobic acid-producing microorganisms, and the pH value (pH) of the system is reduced in the acid-producing process, so that acidification inhibition is generated, and continuous acid production is not facilitated. The technique adopts the addition of alkaline substances, such as Ca (OH)2The pH value of the fermentation system is increased, the reaction process is favorably and smoothly carried out, and the acid production time of the fermentation is prolonged. Meanwhile, phosphoric acid is generated in the anaerobic acid production process of kitchen wastes, and the phosphoric acid and calcium ions form precipitates, so that phosphorus in the wastewater is removed.
2. A steam evaporation technology of high-concentration ammonia nitrogen. Because the kitchen waste contains a large amount of protein, a large amount of ammonia nitrogen is generated in the anaerobic acid production process, and the purity of subsequent organic acid is not high due to the existence of the ammonia nitrogen, so that the organic acid is used as a high-quality carbon source. By adopting the steam evaporation technology, under the condition that the temperature is not very high, ammonia nitrogen is removed from the wastewater, and the generated ammonia gas can be recycled into ammonium bicarbonate, so that the problems of high energy consumption and high cost of the traditional ammonia nitrogen treatment are solved.
The utility model aims to provide a system for dephosphorizing and denitriding kitchen waste, 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; kitchen waste enters from the water inlet end of the anaerobic acid-producing system, the water outlet end of the anaerobic acid-producing 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-phase ammonia nitrogen is discharged from the steam outlet end of the denitrification system;
the anaerobic acidogenic 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 value 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;
a steam inlet of the secondary negative pressure low-temperature deamination device is connected with a steam system, and a secondary steam outlet end of the secondary negative pressure low-temperature deamination device is connected with a steam inlet end of the primary negative pressure low-temperature deamination device;
the outlet end of the deamination fermentation liquor of the primary negative pressure low-temperature deamination device is connected with the inlet end of the deamination fermentation liquor of the secondary negative pressure low-temperature deamination device, the outlet end of the deamination fermentation liquor of the secondary negative pressure low-temperature deamination device is connected with the return inlet end of the deamination fermentation liquor of the preheater, and the deamination fermentation liquor is discharged from the outlet end of the deamination fermentation liquor at the bottom of the preheater;
a 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 recovery reaction device, and carbon dioxide and water are arranged in the recovery reaction device; and the outlet of the recovery reaction device is connected with the crystallizing tank.
Optionally, an intermediate filter 1 is arranged between the outlet end of the deamination fermentation broth of the primary negative pressure low-temperature deamination device and the inlet end of the deamination fermentation broth of the secondary negative pressure low-temperature deamination device, and after the deamination fermentation broth is filtered by the intermediate filter 1, the concentration of suspended matters is 10-500 mg/L.
Optionally, the condensation purification device includes steam outlet end and vapour phase ammonia nitrogen outlet end, wherein, is located the vapour phase ammonia nitrogen outlet end on condensation purification device's upper portion with retrieve reaction unit and connect, be located the steam outlet end of condensation purification device's bottom with the gaseous phase entry end of one-level negative pressure low temperature deamination device is connected.
Optionally, a bottom discharge port of the crystallization tank is connected with a centrifuge, a liquid phase outlet of the centrifuge is connected with a mother liquor tank, and a bottom outlet of the mother liquor tank is connected with a water inlet end of the recovery reaction device located at the upper part.
Optionally, a mother liquor filter is arranged between the bottom outlet of the mother liquor tank and the recovery reaction device.
Optionally, the alkali addition system ii further comprises a pH probe, a PLC control system, and an alkali addition pump, wherein the pH probe is located 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 addition pump, and the alkali addition pump is in pipeline connection with the alkali tank;
and when the detection signal of the pH probe reaches a set value of pH 8-10, the PLC control system controls the alkali adding pump to be started, and the alkaline substances in the alkali tank are conveyed to the alkaline substances in the anaerobic fermentation tank.
Optionally, the anaerobic acid production 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 component, 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 component are sequentially connected by a pipeline, and fermentation liquor containing the organic acid/organic acid salt generated by the anaerobic acid production system is discharged from the water outlet end of the external tubular membrane component; the external tubular membrane component is formed by connecting a plurality of membrane tubes through elbows.
Optionally, the membrane anaerobic system further comprises a drum 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 component are sequentially connected through pipelines.
Optionally, a concentrated solution outlet end of the external tubular membrane module is connected with a backflow water inlet end of the intermediate cache tank, a backflow water outlet end of the intermediate cache tank is connected with a backflow water inlet end of the anaerobic fermentation tank, and the external tubular membrane module, the intermediate cache tank and the anaerobic fermentation tank form a concentrated solution backflow circulation system; the inlet end of the external tubular membrane component is connected with a circulating pump, and the cross flow rate of the inlet end of the external tubular membrane component is controlled to be 4-6 m/s.
Optionally, the alkaline substance is NaOH and Ca (OH)2Wherein, Ca (OH)2The dosage of the compound is enough to form calcium phosphate sediment with phosphate radical, and the rest 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 100-300 mg/L.
Optionally, when the kitchen waste is a mixture of kitchen waste organic solid residues and kitchen waste water, the weight ratio of the kitchen waste organic solid residues to the kitchen waste water is (5-10): (70-90); when the kitchen waste is organic solid kitchen waste, the organic solid kitchen waste is diluted by adding water, and the mass concentration of the organic solid kitchen waste is 10%.
The kitchen waste is pretreated and then enters an anaerobic acid production system to carry out anaerobic acid production reaction, an alkaline substance is added into the anaerobic acid production system through an alkaline addition system, the pH is regulated to be more than or equal to 8.0, metal ions in the alkaline substance react with phosphorus to precipitate, and dephosphorized fermentation liquor containing organic acid/organic acid salt is obtained; and (4) the fermentation liquor enters a denitrification system for denitrification treatment, and finally the dephosphorization and denitrification fermentation liquor is obtained.
Optionally, the denitrification system is a steam evaporation denitrification system, and has a three-stage cyclic denitrification process:
2.1) primary denitrification: transferring heat and mass of the fermentation liquor with a heat supply device of a preheater and a secondary deamination fermentation liquor in a reflux self-secondary negative-pressure low-temperature deamination device, converting part of the fermentation liquor into vapor-phase ammonia nitrogen and deamination fermentation liquor at 50-65 ℃, and allowing the vapor-phase ammonia nitrogen and the residual fermentation liquor to enter a primary negative-pressure low-temperature deamination device;
2.2) secondary denitrification: introducing fresh steam into the secondary negative pressure low-temperature deamination device;
after the vapor-phase ammonia nitrogen and the residual fermentation liquor enter the primary negative pressure low temperature deamination device, performing secondary denitrification by mass transfer and heat transfer with fresh steam from the 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 recovery reaction device in the ammonia absorption unit, the ammonium bicarbonate recovery reaction device reacts with ammonia-containing steam to generate an ammonium bicarbonate solution, crystals are precipitated after the ammonium bicarbonate solution is supersaturated, and solid ammonium bicarbonate is obtained through centrifugal dehydration;
2.3) three times of denitrification: and the secondary deamination fermentation liquor enters a secondary negative pressure low-temperature deamination device, is subjected to mass and heat transfer with fresh steam to perform 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 together, the tertiary denitrification fermentation liquor flows back to the preheater, and after mass and heat transfer, the deamination fermentation liquor obtained in the step 2.1) is obtained, and is discharged from a water outlet end of the deamination fermentation liquor at the bottom of the preheater.
Optionally, the anaerobic acidogenic reaction comprises the following steps:
1.1) filtering the kitchen garbage, then feeding the filtered kitchen garbage into an anaerobic fermentation tank, adding alkaline substances to control the pH to be more than or equal to 8.0, carrying out anaerobic acid production reaction at the temperature of 30-57 ℃, and decomposing the kitchen garbage into hydrogen and CO2And an initial fermentation broth;
1.2) collecting the hydrogen and CO by a gas-liquid separator2；
1.3) 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 production amount of the anaerobic acid production process is more than 30 g/L.
Optionally, the product of the anaerobic acidogenic reaction further comprises a gaseous product H2And CO2，H2The mass concentration of the carbon dioxide is 40-70%, and the balance is CO2。
Has the advantages that: compared with the prior art, the method for dephosphorizing and denitriding kitchen garbage has the following advantages,
(1) the process flow is shorter, and the cost is saved compared with the traditional kitchen waste 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 the removal efficiency of ammonia nitrogen is improved.
(4) The product of anaerobic alkaline acidogenesis is H2And CO2Gaseous product of which H2Can be recycled as clean energy, and is an environment-friendly kitchen waste treatment mode;
(5) calcium phosphate precipitation and ammonia nitrogen steam evaporation are adopted, the effect is better than that of the traditional struvite precipitation of phosphorus and ammonia nitrogen, and the problems of difficult struvite precipitation and the like caused by the inconsistent proportion of phosphorus and ammonia nitrogen in fermentation liquor are solved.
Drawings
FIG. 1 is a schematic view of a system for dephosphorization and denitrogenation of kitchen waste.
FIG. 2 is a flow chart of a process for dephosphorizing and denitriding kitchen waste.
FIG. 3 is a schematic diagram of a membrane anaerobic system;
FIG. 4 is a schematic view of a steam evaporative denitrification processing system;
reference numerals: an anaerobic acid production system I, an alkali addition system II, a denitrification system III, a concentration 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 (programmable logic controller) control system 303, an alkali adding pump 304, a gas-liquid separator 4, a water outlet device 5, an intermediate cache tank 6, an intermediate cache tank reflux pump 7, a sludge inlet pump 8, a sludge filter 9, a circulating pump 10, a membrane component 11, a drum screening machine 12, a drum screening machine water outlet 13, a drum screening machine slag 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 deamination device 502, a second-stage low-temperature deamination device 503, Intermediate filter 5031, condensation purification apparatus 504, recovery reaction apparatus 505, condenser 5051, crystallizer 5052, centrifuge 5053, mother liquor tank 5054, transfer 5056, and packaging 5057.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
As shown in fig. 1, a system for dephosphorization and denitrogenation of kitchen waste comprises an anaerobic acid production system i, an alkali addition system ii, and a denitrification system iii, wherein the kitchen waste enters from a water inlet end of the anaerobic acid production system i, a water outlet end of the anaerobic acid production system i is connected with a water inlet end of the denitrification system iii, a fermentation liquid containing organic acid/organic acid salt is discharged from a water outlet end of the denitrification system iii, and vapor-phase ammonia nitrogen is discharged from a 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 value of the water body is stored in the alkali tank 302;
the alkali tank 302 is connected with the anaerobic fermentation tank 3;
and the denitrification system III is a steam evaporation denitrification system.
As an alternative, the set value is pH 8-10.
FIG. 2 shows a flow chart of the process for removing phosphorus and nitrogen from kitchen garbage. The method can be divided into the following two steps:
1. anaerobic alkaline acid production technology for kitchen garbage
The utility model relates to kitchen waste, which is a treatment object and comprises filtered kitchen waste organic solid residues and/or kitchen waste water, wherein the protein content of the kitchen waste organic solid residues (dry matters) 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 100-300 mg/L. Wherein when the kitchen waste is a mixture of kitchen waste organic solid residues and kitchen waste water, the weight ratio of the kitchen waste organic solid residues to the kitchen waste water is (5-10): (70-90); when the kitchen waste is organic solid kitchen waste, the organic solid kitchen waste is diluted by adding water, and the mass concentration of the organic solid kitchen waste is 10%.
Optionally, the anaerobic acid production process of the present invention may 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 sieving machine 12, an intermediate buffer tank 6, a sludge inlet pump 8, a sludge filter 9, a circulation pump 10, and a water inlet end and a water outlet end of an external tubular membrane module 11 of the membrane anaerobic system are sequentially connected by a pipeline, and a fermentation liquid containing the organic acid/organic acid salt generated by the anaerobic acid production system is discharged from the water outlet end of the external tubular membrane module 11;
optionally, the membrane pipes of the external tubular membrane module 11 are connected together by an elbow 16, so as to conveniently draw out fibers deposited at the membrane sludge inlet end by hand, and a hand hole is formed in the elbow 16.
Optionally, the concentrated solution outlet end of the external tubular membrane module 11 is connected to the backflow water inlet end of the intermediate buffer tank 6, the backflow water outlet end of the intermediate buffer tank 6 is connected to the backflow water inlet end of the anaerobic fermentation tank 3 through the intermediate buffer tank reflux pump 7, and the external tubular membrane module 11, the intermediate buffer tank 6 and the anaerobic fermentation tank 3 form a concentrated solution backflow circulation system.
Wherein, drum screen extension 12 is equipped with drum screen extension and produces mouth of a river 13 and drum screen extension and produce slag hole 14, and drum screen extension produces the mouth of a river 13 and is connected to middle buffer tank 6, and drum screen extension produces slag hole 14 and is connected to 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 value 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 embodiment, the alkali addition system ii further includes a pH probe 301, a PLC control system 303 and an alkali adding pump 304, wherein 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, and conveys 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) high-concentration kitchen waste wastewater enters from a first pipeline Q1, impurities are removed through a water inlet pump 1 and a raw water filter 2, the 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 alkali addition system to control the pH value to be more than or equal to 8.0; the alkali addition system is used for adding Ca (OH)2NaOH, the alkali adding system comprises a pH probe 301, an alkali tank 302, a PLC control system 303, an alkali adding pump 304, Ca (OH)2Mixing with NaOH and storing in the alkali tank 302; wherein, a 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, a PLC control system 303 controls an alkali adding pump 304 to automatically add alkali into the anaerobic fermentation tank 3 from an alkali tank 302 through a thirteenth pipeline Q13, the set value is pH 8-9, and the pH in the tank is maintained at about 9; the kitchen waste is firstly hydrolyzed into micromolecular substances by macromolecular large-particle substances under hydrolytic acidification bacteria, and then is further degraded into volatile fatty acid and hydrogen under hydrogen-producing acetogenic bacteria, in the prior art, the volatile fatty acid is decomposed into methane under methanogenic bacteria, wherein the optimal pH value of the methanogenic bacteria is 6.8-7.5; the utility model controls the pH value to be more than 8.0 by adding alkali, preferably 8-9, thereby inhibiting the activity of methanogens, blocking the methanogenesis process, controlling the reactor process to be in the stage of producing hydrogen and acetic acid, further decomposing acetic acid into CO2；
1.2) gaseous products (hydrogen, CO) produced after anaerobic fermentation2) Collected and utilized after passing through a gas-liquid separator 4;
1.3) the initial fermentation liquor after fermentation 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 from a water producing port 13 of the drum screening machine for buffer storage 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, the separated liquid and the separated residues are respectively discharged from an eleventh pipeline Q11 and a twelfth pipeline Q12 and enter the next treatment link;
1.4) filtering and filtering the initial fermentation liquor after the buffer storage from a third pipeline Q3 through a sludge inlet pump 8 and a sludge filter 9 from a fourth pipeline Q4 to an external tubular membrane module 11 to obtain fermentation liquor after anaerobic acidogenesis, and discharging the fermentation liquor through a fifth pipeline Q5; the membrane concentrated solution sequentially flows back to the intermediate cache tank 6 through a sixth pipeline Q6 and an eighth pipeline Q8, and then flows back to the anaerobic fermentation tank 3 from a second pipeline Q2 through an intermediate cache tank reflux pump 7; the circulation pump 10 provides a cross flow rate of 4-6m/s to the external tubular membrane module 11 to slow down membrane fouling.
Optionally, the membrane used in the utility model is a tubular membrane, the material used is a PVDF membrane, and the pure water flux of the PVDF membrane is 700L/m2h, bubble point 0.03, burst strength 4.2 MPa.
And (3) anaerobic fermentation results:
after 5-10 days of fermentation, the acid yield of the kitchen garbage is more than 30g/L, and the pH value of the obtained acidified fermentation liquor is 8-10;
the calcium phosphate precipitated in the reaction system is about 200mg/L, and the removal efficiency of the phosphorus reaches about 90 percent.
And the mass concentration of the organic acid/organic acid salt in the obtained dephosphorized fermentation liquor containing the organic acid/organic acid salt is more than 3 percent. Gaseous product H2And CO2In (H)2The mass concentration of the carbon dioxide is 40-70%, and the balance is CO2。
2. Steam evaporation technology of high-concentration ammonia nitrogen
Performing denitrification treatment on the acidified fermentation liquor by using a steam evaporation denitrification treatment system, wherein the steam evaporation denitrification treatment 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, as shown in fig. 4;
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;
a steam inlet of the secondary negative pressure low temperature deamination device 503 is connected with a steam system, and a secondary steam outlet end of the secondary negative pressure low temperature deamination device 503 is connected with a steam inlet end of the primary negative pressure low temperature deamination device 502;
the outlet end of deamination fermentation liquor of the primary negative pressure low-temperature deamination device 502 is connected with the inlet end of deamination fermentation liquor of the secondary negative pressure low-temperature deamination device 503, the outlet end of deamination fermentation liquor of the secondary negative pressure low-temperature deamination device 503 is connected with the return inlet end of deamination fermentation liquor of the preheater 501, and deamination fermentation liquor is discharged from the outlet end of deamination fermentation liquor at the bottom of the preheater 501;
a 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 recovery reaction device 505, and carbon dioxide and water are arranged in the recovery reaction device 505; the outlet of the recovery reaction apparatus 505 is connected to a crystallizer 5052.
Optionally, the condensation purification device 504 includes a steam outlet end and a vapor-phase ammonia nitrogen outlet end, wherein, the vapor-phase ammonia nitrogen outlet end located on the upper portion of the condensation purification device 504 is connected with the recovery reaction device 505, and the steam outlet end located at the bottom of the condensation purification device 504 is connected with the vapor-phase inlet end of the primary negative pressure low-temperature deamination device 502.
Optionally, the bottom discharge port of the crystallization tank 5052 is connected to a centrifuge 5053, the liquid phase outlet of the centrifuge 5053 is connected to a mother liquor tank 5054, and the bottom outlet of the mother liquor tank 5054 is connected to the water inlet port of the recovery reaction apparatus 505 located 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 reaction device 505.
The steam evaporation denitrification treatment system has a three-stage circular denitrification process, and the process principle and the process are as follows:
2.1) primary denitrification: the fermentation liquor transfers heat with a heat supply device of a preheater 501 and the secondary deamination fermentation liquor in a reflux self-secondary negative-pressure low-temperature deamination device 503, 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 residual fermentation liquor enter a 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 the vapor-phase ammonia nitrogen and the residual fermentation liquor enter a primary negative pressure low temperature deamination device 502, performing secondary denitrification by mass transfer and heat transfer with fresh steam from a 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 condensation purification device 504 for condensation, purification and recovery; carbon dioxide and water are introduced into a recovery reaction device 505 arranged in the condensation purification device 504 and react with ammonia-containing steam to generate an ammonium bicarbonate solution, crystals are precipitated after the ammonium bicarbonate solution is supersaturated, and solid ammonium bicarbonate is obtained through centrifugal dehydration;
2.3) three times of denitrification: the secondary deamination fermentation liquor enters a secondary negative pressure low-temperature deamination device 503 and transfers heat with fresh steam in a mass transfer manner to perform 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 denitrification fermentation liquor flows back to the preheater 501 to obtain the deamination fermentation liquor obtained in the step 2.1) after the mass transfer and the heat transfer, and the deamination fermentation liquor is discharged from a water outlet end of the deamination fermentation liquor at the bottom of the preheater 501.
Optionally, conveying the secondary deamination fermentation liquor discharged by the primary negative-pressure low-temperature deamination device to an intermediate filter by a pump to reduce SS to 10-500mg/L, and then feeding the secondary deamination fermentation liquor into the secondary negative-pressure low-temperature deamination device;
the first-stage negative pressure low-temperature deamination device and the second-stage negative pressure low-temperature deamination device adopt a direct heating mode, fresh steam firstly enters the second-stage negative pressure low-temperature deamination device and vertically moves from bottom to top in the second-stage negative pressure low-temperature deamination device, the vertically moving steam enters the bottom of the first-stage negative pressure low-temperature deamination device through a pipeline at the top of the second-stage negative pressure low-temperature deamination device and vertically moves from bottom to top in the first-stage negative pressure low-temperature deamination device, and the vertically moving steam finally forms vapor-phase steam containing ammonia gas at the top of the first-stage negative pressure low-temperature deamination device; and the mass transfer and heat transfer of the gas-liquid phase are realized by the fermentation liquor and the steam in the primary negative pressure low-temperature deamination device and the secondary negative pressure low-temperature deamination device respectively, so that the transfer of carbon dioxide and ammonia gas in the fermentation liquor to the steam is completed, and the mass concentration of ammonia nitrogen in the fermentation liquor subjected to the two-stage negative pressure low-temperature deamination is reduced to be below 400mg/L from 4000 mg/L.
Vapor phase steam containing ammonia enters a condensation and purification device from the top of a primary negative pressure low temperature deamination device, the steam is condensed and reflows, and only gas phase containing ammonia and carbon dioxide enters a subsequent ammonium bicarbonate recovery reaction device; and reacting ammonia gas and carbon dioxide in a gas phase with water in the reaction device in an ammonium bicarbonate recovery reaction device to form ammonium bicarbonate, continuously saturating to form a crystallization liquid, and finally separating solid from liquid to obtain an ammonium bicarbonate saturated liquid and ammonium bicarbonate crystals.
And (3) denitrification results of the steam evaporation denitrification treatment system:
after steam evaporation, the residual ammonia nitrogen in the acidified fermentation liquor is lower than 200mg/L, and the removal efficiency of the ammonia nitrogen reaches about 90%; the evaporated ammonia gas is recovered into ammonium bicarbonate. The steam evaporation process keeps the loss of organic acids low and thus helps to increase the C: N ratio in the acidified fermentation broth.
The present invention will be further described with reference to the following examples. The present invention will be better understood from the following examples. However, those skilled in the art will readily appreciate that the specific material ratios, process conditions and results thereof described in the examples are illustrative only and should not be taken as limiting the utility model as detailed in the claims.
Example 1
The process for preparing nitrogen and phosphorus removal by using kitchen garbage comprises the following steps:
1) anaerobic alkaline acid production technology for kitchen garbage
The processing object of the embodiment is kitchen waste, which is a mixture of filtered kitchen waste organic solid residue and kitchen waste water, and the weight ratio of the kitchen waste organic solid residue to the kitchen waste water is 8: 80. wherein the protein content of the organic solid residue (dry matter) of the kitchen residue is 19.6%; the COD of the kitchen waste water is 108480mg/L, the total nitrogen is 2156mg/L, and the total phosphorus is 227 mg/L.
The kitchen garbage is in a membrane anaerobic system, and NaOH and Ca (OH) are intermittently added through an alkali adding system2And fermenting to produce acid, wherein the pH value is maintained between 8.0 and 9.0 in the reaction process.
And (3) anaerobic fermentation results:
after 10 days of retention time, the acid yield of the kitchen garbage after fermentation is 60g/L, the pH of the obtained fermentation liquor is about 9, the concentration of total phosphorus is 10mg/L, and the concentration of ammonia nitrogen is 1154 mg/L;
gaseous product H2And CO2In (H)2Has a mass concentration of 64% and the balance of CO2。
2) Steam evaporation technology of high-concentration ammonia nitrogen
After steam evaporation, the residual ammonia nitrogen in the fermentation liquor is 200mg/L, and the removal efficiency of the ammonia nitrogen reaches 90.7%; the evaporated ammonia gas is recovered into ammonium bicarbonate.
Example 2
The process for preparing nitrogen and phosphorus removal by using kitchen garbage comprises the following steps:
1) anaerobic alkaline acid production technology for kitchen garbage
The object to be treated in this example was kitchen waste, which was centrifugally filtered, and had a COD of 108480mg/L, a total nitrogen of 2156mg/L and a total phosphorus of 227 mg/L.
The kitchen garbage is in a membrane anaerobic system, and NaOH and Ca (OH) are intermittently added through an alkali adding system2And fermenting to produce acid, wherein the pH value is maintained between 8.0 and 9.0 in the reaction process.
And (3) anaerobic fermentation results:
after 10 days of retention time, the acid yield of the kitchen garbage after fermentation is 50g/L, the pH of the obtained fermentation liquor is about 9, the concentration of total phosphorus is 9mg/L, and the concentration of ammonia nitrogen is 958 mg/L;
gaseous product H2And CO2In (H)2Has a mass concentration of 55% and the balance of CO2。
2) Steam evaporation technology of high-concentration ammonia nitrogen
After steam evaporation, the residual ammonia nitrogen in the fermentation liquor is 150mg/L, and the removal efficiency of the ammonia nitrogen reaches 93 percent; the evaporated ammonia gas is recovered into ammonium bicarbonate.
Example 3
The process for preparing nitrogen and phosphorus removal by using kitchen garbage comprises the following steps:
1) anaerobic alkaline acid production technology for kitchen garbage
The object to be treated in this example is kitchen waste, including filtered organic solid kitchen waste, wherein the protein content of the organic solid kitchen waste (dry matter) is 19.6%.
Before anaerobic fermentation, water is added to dilute and ferment the kitchen residue organic solid residue to make the mass concentration of the kitchen residue organic solid residue reach 10%.
The kitchen garbage is in a membrane anaerobic system, and Ca (OH) is intermittently added through an alkali adding system2And fermenting to produce acid, wherein the pH value is maintained between 8.0 and 9.0 in the reaction process.
And (3) anaerobic fermentation results:
after 10 days of retention time, the acid production of the kitchen garbage after fermentation is 45g/L, the pH of the obtained fermentation liquor is about 9, the concentration of total phosphorus is 7mg/L, and the concentration of ammonia nitrogen is 820 mg/L;
gaseous product H2And CO2In (H)2Has a mass concentration of 50% and the balance of CO2。
2) Steam evaporation technology of high-concentration ammonia nitrogen
After steam evaporation, the residual ammonia nitrogen in the fermentation liquor is 105mg/L, and the removal efficiency of the ammonia nitrogen reaches 87.2%; the evaporated ammonia gas is recovered into ammonium bicarbonate.
The above description is only of the preferred embodiments of the present invention, and it should be 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 utility model and these are intended to be within the scope of the utility model.
Claims (10)
1. The system for dephosphorization and denitrification of kitchen waste is characterized by comprising an anaerobic acid production system (I), an alkali addition system (II) and a denitrification 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 denitrification 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-phase ammonia nitrogen is discharged from the steam outlet end of the denitrification system (III);
the anaerobic acidogenic 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 value 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.
2. The dephosphorization and denitrification system for kitchen waste according to claim 1, wherein 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);
a steam inlet of the secondary negative pressure low-temperature deamination device (503) is connected with a steam system, and a secondary steam outlet end of the secondary negative pressure low-temperature deamination device (503) is connected with a steam inlet end of the primary negative pressure low-temperature deamination device (502);
the outlet end of deamination fermentation liquor of the primary negative pressure low-temperature deamination device (502) is connected with the inlet end of deamination fermentation liquor of the secondary negative pressure low-temperature deamination device (503), the outlet end of deamination fermentation liquor of the secondary negative pressure low-temperature deamination device (503) is connected with the reflux inlet end of deamination fermentation liquor of the preheater (501), and deamination fermentation liquor is discharged from the water outlet end of deamination fermentation liquor at the bottom of the preheater (501);
a 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 recovery reaction device (505), and carbon dioxide and water are contained in the recovery reaction device (505); the outlet of the recovery reaction device (505) is connected with a crystallizing tank (5052).
3. The system for dephosphorization and denitrogenation of kitchen waste according to claim 2, wherein said condensing and purifying device (504) comprises a steam outlet end and a vapor phase ammonia nitrogen outlet end, wherein the vapor phase ammonia nitrogen outlet end located at the upper part of said condensing and purifying device (504) is connected with said recovery reaction device (505), and the steam outlet end located at the bottom of said condensing and purifying device (504) is connected with the vapor phase inlet end of said primary negative pressure low temperature deamination device (502).
4. The system for dephosphorization and denitrogenation of kitchen waste according to claim 2, characterized in that the bottom outlet of said crystallizer tank (5052) is connected to a centrifuge (5053), the liquid outlet of said centrifuge (5053) is connected to a mother liquor tank (5054), and the bottom outlet of said mother liquor tank (5054) is connected to the water inlet of said recovery reactor (505) located at the upper part.
5. The dephosphorization and denitrification system for kitchen waste according to claim 4, wherein a mother liquor filter (5055) is provided between the bottom outlet of said mother liquor tank (5054) and said recycling reactor (505).
6. The system for dephosphorization and denitrogenation of kitchen waste according to claim 1, wherein said alkali addition system (II) further comprises a pH probe (301), a PLC control system (303) and an alkali addition pump (304), wherein said pH probe (301) is located in said anaerobic fermentation tank (3), said pH probe (301) is in signal connection with said PLC control system (303), said PLC control system (303) is in control connection with said alkali addition pump (304), and said alkali addition pump (304) is in pipe connection with said alkali tank (302);
when the detection signal of the pH probe (301) reaches a set value pH of 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 the alkaline substances in the anaerobic fermentation tank (3).
7. The system for dephosphorization and denitrogenation of kitchen waste according to claim 1, wherein said anaerobic acid production system (i) is a membrane anaerobic system, said membrane anaerobic system comprises an anaerobic fermentation tank (3), a water outlet device (5), a middle buffer tank (6) and an external tubular membrane module (11), said anaerobic fermentation tank (3), said water outlet device (5), said middle buffer tank (6) and said external tubular membrane module (11) are connected by pipes in sequence at their water inlet and outlet ends, and the fermentation broth containing said organic acid/salt produced by said anaerobic acid production system is discharged from the water outlet end of said external tubular membrane module (11); the external tubular membrane component (11) is formed by connecting a plurality of membrane tubes through elbows (16).
8. The dephosphorization and denitrification system for kitchen waste according to claim 7, wherein said membrane anaerobic system further comprises a drum screen (12), a sludge filter (9);
the water inlet end and the water outlet end of the water outlet device (5), the drum screening machine (12), the middle buffer tank (6), the sludge filter (9) and the tubular membrane component (11) are sequentially connected through pipelines.
9. The dephosphorization and denitrification system for kitchen waste according to claim 7, wherein the concentrated solution outlet end of the external tubular membrane module (11) is connected with the water inlet and return end of the intermediate buffer tank (6), the water outlet and return end of the intermediate buffer tank (6) is connected with the water inlet and return end of the anaerobic fermentation tank (3), and the external tubular membrane module (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 component (11) is connected with a circulating pump (10), and the cross flow rate of the inlet end of the external tubular membrane component (11) is controlled to be 4-6 m/s.
10. According to any one of claims 1-9The system for dephosphorization and denitrogenation of kitchen garbage is characterized in that the alkaline substances are NaOH and Ca (OH)2Wherein, Ca (OH)2The dosage of the compound is enough to form calcium phosphate sediment with phosphate radical, and the rest is NaOH.
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| CN115072946A (en) * | 2022-08-03 | 2022-09-20 | 福安药业集团烟台只楚药业有限公司 | Method for preparing high-concentration ammonia water by extracting ammonia gas from gentamicin fermentation wastewater |
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