CN109455884B - A nitrogen resource thermal extraction and recovery system - Google Patents
A nitrogen resource thermal extraction and recovery system Download PDFInfo
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- CN109455884B CN109455884B CN201811573635.5A CN201811573635A CN109455884B CN 109455884 B CN109455884 B CN 109455884B CN 201811573635 A CN201811573635 A CN 201811573635A CN 109455884 B CN109455884 B CN 109455884B
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- C05—FERTILISERS; MANUFACTURE THEREOF
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- C02F1/02—Treatment of water, waste water, or sewage by heating
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Abstract
The invention discloses a nitrogen resource heat extraction and recovery system which comprises a pretreatment unit, a resolving unit, a deamination unit, an ammonia absorption unit, a crystallization dehydration unit and other auxiliary units such as steam preparation, tail gas purification, thick slag precipitation, acid washing and the like which are connected in sequence. The invention transfers ammonia nitrogen in liquid phase to vapor phase by physical method, and then by external applicationAnd (3) carrying out chemical reaction with ammonia nitrogen in a vapor phase in a liquid phase to generate ammonium bicarbonate solution, precipitating crystals after the ammonium bicarbonate solution is saturated in a transition mode, and obtaining solid ammonium bicarbonate through centrifugal dehydration. The system not only realizes the recovery of nitrogen resources in the leachate of the landfill and anaerobic fermentation biogas slurry of the kitchen sludge, but also greatly reduces the engineering investment and the operation cost of the subsequent sewage treatment system, and realizes the aims of energy conservation and consumption reduction. The system is also suitable for recycling nitrogen resources in other types of high ammonia nitrogen wastewater in coal chemical industry and the like.
Description
Technical Field
The invention relates to the technical field of garbage leachate and kitchen sludge anaerobic fermentation biogas slurry treatment, in particular to a nitrogen resource heat extraction and recovery system.
Background
Ammonia nitrogen is a long-term pollutant in landfill leachate, and as the landfill time increases, the ammonia nitrogen concentration gradually increases, and the ammonia nitrogen concentration of old leachate with the landfill time exceeding 10 years can reach more than 3000 mg/L. With the increase of the service time of landfill sites and the development of waste incineration power generation in recent 10 years, the aging of leachate of the landfill sites becomes a problem focus. The aged leachate has the characteristics of low COD Cr and high NH 3 -N, TN, the B/C ratio is generally lower than 0.3, the C/N ratio is less than or equal to 3 or even lower, and the biogas slurry obtained by anaerobic fermentation of the fresh leachate of the incineration plant and the anaerobic fermentation biogas slurry of the kitchen waste have similar water quality characteristics as the aged leachate of the landfill.
The landfill leachate and the anaerobic fermentation biogas slurry of the kitchen sludge generally need to be treated to reach relevant standards and then can be discharged into urban sewage or water. The discharge requirement of the standard of the pollutant discharge of the domestic refuse landfill (GB 16889-2008) table 2 on the pollutant discharge of the landfill leachate is NH 3 -N is less than or equal to 25mg/L, TN and less than or equal to 40mg/L, and the water quality standard of the sewage discharge into the urban sewer (GB) is NH 3 -N is less than or equal to 45mg/L, TN and less than or equal to 60mg/L. The high concentration ammonia nitrogen and low C/N ratio bring great difficulty to the standard treatment of leachate and anaerobic fermentation biogas slurry of kitchen sludge, the landfill aged leachate or anaerobic fermentation biogas slurry of kitchen sludge with the imbalance of the C/N ratio is treated by adopting a membrane bioreactor, the cost of adding a carbon source is often more than 50% of the running cost, and the system has poor water impact load resistance and unstable water quality. Therefore, development of a novel process system for pretreatment of landfill leachate or anaerobic fermentation biogas slurry of kitchen sludge is urgently needed, on one hand, nitrogen load of a subsequent biological treatment system is reduced, and meanwhile, nitrogen resource utilization is achieved.
Disclosure of Invention
Aiming at the characteristics of high NH 3 -N concentration, low COD and imbalance of C/N ratio in landfill leachate and kitchen sludge anaerobic fermentation biogas slurry and the treatment requirements thereof, the invention provides a complete nitrogen resource heat extraction recovery system, and the method of thermal analysis of bicarbonate ions, negative pressure stripping of free ammonia, CO 2 absorption of vapor phase ammonia, crystallization of ammonium bicarbonate solution, solid-liquid separation and the like is adopted to recover ammonia nitrogen in the landfill leachate and kitchen sludge anaerobic fermentation biogas slurry as ammonium bicarbonate products, and the ammonium bicarbonate products are sold as high-quality fertilizers, and simultaneously reduce the nitrogen load of a subsequent sewage treatment system, reduce engineering investment, save the amount of additional carbon sources, save operation cost, relieve the membrane scaling phenomenon of an MBR sewage treatment system, improve the operation stability of the sewage treatment system and reduce maintenance cost.
The technical scheme of the invention is as follows, and the nitrogen resource heat extraction and recovery system is characterized by comprising:
The pretreatment unit is used for pretreating landfill leachate and anaerobic fermentation biogas slurry of kitchen sludge to form ammonia-containing wastewater entering a subsequent unit, wherein COD (chemical oxygen demand) of the ammonia-containing wastewater is less than or equal to 10000mg/L, SS and less than or equal to 1000mg/L;
the analysis unit is connected with the pretreatment unit and comprises a preheater and an analysis reaction tower, the upper part of the analysis reaction tower is provided with a filler area, the lower part of the analysis reaction tower is provided with a water collecting area and a sludge hopper, ammonia-containing wastewater enters the analysis reaction tower after being preheated, the preheated ammonia-containing wastewater and ammonia-containing steam reflowed by the deamination unit are subjected to heat exchange reaction in the filler area, the temperature of the ammonia-containing wastewater is further increased, and bicarbonate ions in the ammonia-containing wastewater are analyzed to be The ions and the CO 2 are combined,The method comprises the steps of reacting ions with calcium and magnesium ions in ammonia-containing wastewater to generate carbonate precipitate for precipitation, collecting CO 2 together with ammonia-containing steam at the top of a desorption reaction tower, and conveying the ammonia-containing wastewater to an ammonia absorption unit through the top of the desorption reaction tower;
The ammonia-containing wastewater of the analytical reaction tower enters the deamination tower and then carries out stripping deamination reaction with external steam in the packing region, ammonia nitrogen in a liquid phase enters a vapor phase, and the ammonia-containing steam is collected at the top of the deamination tower and flows back to the analytical reaction tower of the analytical reaction unit from the top of the deamination tower;
The ammonia absorption unit is connected with an analysis reaction tower of the analysis unit, the ammonia absorption unit comprises a condenser, a gas-liquid separator, a reflux pump, an ammonia recovery tower, a circulating water pump, a cooler, an ammonia pumping mixing device, a discharging pump and a tail gas recovery and treatment device, ammonia-containing steam at the top of the analysis reaction tower of the analysis unit is condensed by the condenser and then is led to the ammonia recovery tower, the condensate flows back to the deamination tower or the ammonia recovery tower of the deamination unit, the ammonia recovery tower is filled with water, CO 2 is introduced into the ammonia recovery tower, ammonia and CO 2 in the ammonia-containing gas react in the ammonia recovery tower to generate ammonium bicarbonate solution, the generated transitional saturated ammonium bicarbonate solution of the ammonia recovery tower is pumped to the crystallization dehydration unit by a discharging pump, and the residual gas in the ammonia recovery tower is sent to the tail gas recovery and treatment device for tail gas treatment;
And the crystallization dehydration unit is connected with the ammonia absorption unit and is used for dehydrating the transition saturated ammonium bicarbonate solution to form ammonium bicarbonate solid, and the dehydrated filtrate is returned to the ammonia recovery tower.
Further, the pretreatment unit adopts different pretreatment processes according to different treatment objects, the pretreatment unit comprises a landfill leachate pretreatment unit and a kitchen sludge anaerobic fermentation biogas slurry pretreatment unit, the landfill leachate pretreatment unit adopts anaerobic+precipitation or filtration pretreatment or anaerobic MBR pretreatment on fresh leachate of a landfill or leachate of a garbage incineration plant, the old leachate in the landfill is subjected to precipitation or filtration pretreatment, and the kitchen sludge anaerobic fermentation biogas slurry pretreatment unit adopts centrifugation or plate frame dehydration on kitchen sludge anaerobic fermentation biogas slurry, and the dehydrated filtrate is subjected to air floatation pretreatment.
Further, the first input end of the preheater is connected with the balance water tank, the second input end of the preheater is connected with the water outlet end at the bottom of the deamination tower through a water pump, the first output end of the preheater is connected with the input end of the analysis reaction tower, the second output end of the preheater is connected with a water outlet pipe, high-temperature wastewater at the bottom of the deamination tower is pumped to the preheater of the analysis unit through the water pump, and ammonia-containing wastewater in the balance water tank flows into the analysis reaction tower after being preheated.
Further, the sludge hopper of the analysis reaction tower is connected with the thick slag sedimentation tank through a sludge pump, and the sludge in the waste water and the sludge generated in the analysis reaction process are accumulated in the sludge hopper and are periodically discharged to the thick slag sedimentation tank through the sludge pump.
Further, in the ammonia absorption unit, the input end of the condenser is connected with the analysis unit through a pipeline, the output end of the condenser is connected with the gas-liquid separator, the liquid outlet end of the gas-liquid separator is connected with the deamination tower of the deamination unit, and the gas outlet end of the gas-liquid separator is connected with the ammonia recovery tower.
Further, an air outlet is formed in the top of the ammonia recovery tower, the air outlet in the top of the ammonia recovery tower is connected with an air inlet of the tail gas recovery tower, a spray header is arranged on the upper portion of the tail gas recovery tower, the spray header is connected with a water inlet at the upper end of the tail gas recovery tower, a water outlet is formed in the lower end of the tail gas recovery tower, the water outlet is connected with a water inlet at the upper end of the ammonia recovery tower through a water pump, residual gas at the top of the ammonia recovery tower is introduced into the tail gas recovery tower, tap water is adopted for leaching, and leaching liquid flows back to the ammonia recovery tower.
Further, a circulating water outlet is formed in the bottom of the ammonia recovery tower, the circulating water outlet is connected with the upper portion of the ammonia recovery tower through a circulating water pump, a cooler and an ammonia extraction mixing device, the ammonia extraction mixing device is further connected with the air outlet end of the gas-liquid separator so as to perform preliminary cooling on the gas-liquid mixture in the ammonia recovery tower, the running water supplementing quantity of the ammonia recovery tower is controlled to enable the ammonium bicarbonate solution to reach a saturated state, a negative pressure environment is formed in the ammonia extraction mixing device, and the output gas of the air outlet end of the gas-liquid separator is introduced into the gas-liquid mixture of the circulating loop and then enters the ammonia recovery tower.
Further, a tail gas outlet is formed in the top of the tail gas recovery tower, the tail gas outlet is connected with the tail gas purification tower through a draught fan, a water inlet is formed in the upper end of the tail gas purification tower, pickling solution is injected into the water inlet of the tail gas purification tower, the gas outlet at the top of the tail gas purification tower is connected to the biological reaction tank through the draught fan, the leached tail gas in the tail gas recovery tower is introduced into the tail gas purification tower through the draught fan, and the leached tail gas is introduced into the aerobic zone of the biological reaction tank of the sewage treatment system for 1-3 m under the liquid after pickling.
Further, the crystallization dehydration unit comprises a crystal slurry tank, a stirrer is arranged in the crystal slurry tank, an outlet at the bottom of the crystal slurry tank is connected with a centrifugal dehydrator, the centrifugal dehydrator is used for dehydrating the generated transition saturated ammonium bicarbonate solution of the ammonia recovery tower, the dehydrated filtrate is stored in a mother liquor pond and pumped to the ammonia recovery tower by the mother liquor pump, and the dehydrated ammonium bicarbonate solid is conveyed to a packer by a conveyor.
Further, the ammonia recovery tower, the condenser, the desorption reaction tower and the deamination tower are in a negative pressure state through a negative pressure device, and the stripping reaction of the deamination tower is carried out in a negative pressure state (50000 Pa-70000 Pa).
According to the invention, nitrogen in garbage leachate and anaerobic fermentation biogas slurry of kitchen sludge can be converted into ecological ammonia fertilizer by a heat extraction technology and a physical and chemical method, so that the recycling of nitrogen is realized, the investment and operation cost of sewage treatment engineering are reduced, and the engineering economic benefit and the social benefit are very remarkable. The system is also suitable for recycling nitrogen resources in other types of high ammonia nitrogen wastewater in coal chemical industry and the like. Compared with the existing deamination technologies of air stripping, chemical precipitation, oxidation and the like, the invention has the following beneficial effects:
1. the system for extracting and recovering nitrogen resources in the landfill leachate and the anaerobic fermentation biogas slurry of the kitchen sludge converts nitrogen in the landfill leachate and the anaerobic fermentation biogas slurry of the kitchen sludge into a high-purity ammonium bicarbonate (NH 4HCO3) product, so that the recycling of nitrogen is realized;
2. The system for extracting and recovering nitrogen resources in the landfill leachate and the anaerobic fermentation biogas slurry of the kitchen sludge can greatly reduce the nitrogen load of a sewage biological treatment system, reduce the engineering investment of the sewage treatment system, improve the C/N ratio of the leachate (anaerobic fermentation biogas slurry), create good water quality conditions for the subsequent biological denitrification treatment, reduce the added carbon source amount of the biological denitrification and save the operation cost;
3. The system for extracting and recovering the nitrogen resources in the landfill leachate and the anaerobic fermentation biogas slurry of the kitchen sludge by heat can remove Ca 2+、Mg2+ in raw water of the leachate (biogas slurry) in the form of CaCO 3、MgCO3, and the leachate (biogas slurry) subjected to stripping deamination pretreatment has the characteristics of low calcium and magnesium ion concentration, low TN concentration, coordination of COD and TN ratio and the like, is beneficial to the operation of an MBR biological reaction tank and an ultrafiltration membrane component, can relieve the membrane scaling phenomenon, reduces the membrane cleaning frequency, prolongs the service life of the membrane, and further reduces the operation and maintenance cost.
Drawings
FIG. 1 is a schematic diagram of a system for stripping deamination of landfill leachate in accordance with an embodiment of the present invention.
Detailed Description
The invention is further described below in connection with specific examples.
Examples
Referring to fig. 1, fig. 1 shows a process flow for stripping deamination to treat aged landfill leachate, wherein:
The device comprises a pretreatment unit, a kitchen sludge anaerobic fermentation biogas slurry treatment unit and a kitchen sludge anaerobic fermentation biogas slurry treatment unit, wherein fresh leachate of a landfill or leachate of a garbage incineration plant adopts anaerobic+precipitation (or filtration) pretreatment or anaerobic MBR pretreatment, and the purpose of controlling COD (chemical oxygen demand) entering a subsequent unit to be less than or equal to 10000mg/L, SS to or less than or equal to 1000mg/L is achieved. The leachate or biogas slurry treated by the pretreatment unit is stored in the balance water tank 1 and is lifted to the analysis unit by the sewage pump.
The device comprises an analysis unit, an ammonia-containing wastewater treatment unit, a deamination unit, a pretreatment unit, a wastewater treatment unit and a wastewater treatment unit, wherein the analysis unit is connected with the pretreatment unit and comprises a preheater 2, an analysis reaction tower 3, a concentrated slag precipitation tank, a water pump and the like, the pretreated leachate or biogas slurry is preheated to enable the temperature of the leachate or biogas slurry to be increased to 55-65 ℃, ammonia-containing wastewater enters the analysis reaction tower 3 after being preheated, a filler area is arranged at the upper part of the analysis reaction tower 3, a water collecting area and a sludge bucket are arranged at the lower part of the analysis reaction tower, the preheated wastewater entering the analysis reaction tower and the refluxed ammonia-containing steam are subjected to heat exchange reaction in the filler area to enable the temperature of the wastewater to be further increased to 80-90 ℃, and sludge in the wastewater and sludge generated in the analysis reaction process are periodically discharged to the concentrated slag precipitation tank through the pump, and effluent of the analysis reaction tower is lifted to the deamination unit through the pump.
The ammonia removal unit is connected with the analysis unit and comprises an ammonia removal tower 4 and a water pump, wherein the upper part of the ammonia removal tower is provided with a filler area, and the lower part of the ammonia removal tower is provided with a water collecting area;
An ammonia absorption unit connected to the analysis reaction tower 3 of the analysis unit, wherein the ammonia absorption unit comprises a condenser 5, a gas-liquid separator 6, a reflux pump, an ammonia recovery tower 7, a circulating water pump, a cooler 8, an ammonia extraction mixing device 9, a discharge pump, and a tail gas recovery and treatment device (a tail gas recovery tower 10, a tail gas purification tower 11, an induced draft fan, etc.); the ammonia recovery tower is provided with a water injection end, a CO 2 inlet end, an exhaust gas input end, an exhaust gas output end and a liquid discharge end, the input end of the condenser is connected with the steam output end of the resolving unit, the output end of the condenser is connected with the gas-liquid separator, the liquid outlet end of the gas-liquid separator is connected with the deamination tower of the deamination unit through the reflux pump, the exhaust gas output end of the gas-liquid separator is connected with the exhaust gas input end of the ammonia recovery tower, the exhaust gas output end of the ammonia recovery tower 7 is connected with the crystallization dehydration unit through the discharge pump, the water injection end of the ammonia recovery tower is connected with the liquid reflux end of the crystallization dehydration unit, the ammonia-containing steam at the top of the resolving unit is led to the ammonia recovery tower 7 through the ammonia extraction mixing device 9, the condensate flows back to the deamination tower 4 of the deamination unit, the ammonia extraction mixing device adopts the venturi principle, the throat is arranged in the ammonia extraction mixing device, the mixed liquid in the ammonia recovery tower circulates through the water pump, the circulation pipe is provided with the cooler and the throat, the throat is simultaneously connected with the liquid output end of the condenser, the ammonia is led into the ammonia recovery tower through the venturi tube 7, the ammonia recovery tower is led into the ammonia recovery tower through the negative pressure side of the venturi effect 2, the ammonia recovery tower is formed by the ammonia recovery tower, the ammonia recovery tower is fed into the ammonia recovery tower through the air output end of the negative pressure of the condenser 7, the method comprises the steps of (1) absorbing water from a circulating water outlet at the bottom of an ammonia recovery tower 7 by a circulating water pump, cooling and returning to the ammonia recovery tower 7, wherein ammonia gas and CO 2 react in a liquid phase of the ammonia recovery tower 7 to generate ammonium bicarbonate, non-condensable gas at the top of the ammonia recovery tower enters a tail gas recovery tower 10, tap water is adopted for leaching, leaching solution flows back to the ammonia recovery tower 7, tail gas enters a purifying tower 11, and the tail gas is led to a biological reaction tank aerobic zone of a sewage treatment system for 1-3 m under the liquid after being subjected to acid cleaning, wherein the generated transition saturated ammonium bicarbonate solution of the ammonia recovery tower 7 is pumped to a crystallization dehydration unit;
The crystallization dehydration unit is connected with the ammonia absorption unit and comprises a crystal slurry tank 12, a centrifugal dehydrator 13, a mother liquor pool 14, a conveyor 15, a packer 16, a mother liquor pump and the like, wherein a stirrer is arranged in the crystal slurry tank 12, ammonium bicarbonate crystals grow up and reach a certain concentration, gravity flows to the centrifugal dehydrator 13, dehydrated filtrate is stored in the mother liquor pool 14 and is pumped to the ammonia recovery tower 7 by the mother liquor, and dehydrated ammonium bicarbonate solids are conveyed to the packer 16 by the conveyor 15.
The heat extraction and recovery system for nitrogen resources in landfill leachate and anaerobic fermentation biogas slurry of kitchen sludge sequentially comprises the following steps:
(1) Pretreating landfill leachate and anaerobic fermentation biogas slurry of kitchen sludge. Fresh percolate (landfill initial percolate or incineration plant percolate) is pretreated by adopting anaerobic+precipitation (or filtration) or anaerobic MBR, old percolate in a landfill is pretreated by adopting precipitation or filtration, anaerobic fermentation biogas slurry of kitchen sludge is dehydrated by adopting centrifugation or a plate frame, and dehydrated filtrate is pretreated by adopting air floatation.
(2) Preheating the pretreated percolate or biogas slurry to raise the temperature to 55-65 ℃.
(3) And pumping the preheated percolate or biogas slurry to a desorption reaction tower, introducing steam into the desorption reaction tower, and further raising the temperature of the percolate or biogas slurry to 80-90 ℃ in the desorption reaction tower. After preheating and heating, the ammonia-containing steam enters the upper part of the desorption reaction tower, and the ammonia-containing steam from the deamination tower enters the lower part of the desorption reaction tower. The percolate is fully contacted with the reflux ammonia-containing steam in the process of flowing through the tower plate and is subjected to heat exchange, the temperature of the percolate is further increased, and bicarbonate ions in the stock solution are resolved intoThe ions and the CO 2 are combined,The ions react with calcium and magnesium ions in the stock solution to generate calcium carbonate and magnesium carbonate precipitate to be separated out, the calcium carbonate and the magnesium carbonate precipitate are periodically discharged out of the analysis reaction tower by a pump, and CO 2 is collected at the top of the analysis reaction tower together with ammonia steam. The ratio of free ammonia nitrogen in the stock solution after temperature rising and analysis is greatly improved, and part of free ammonia in the stock solution diffuses to gas phase in the process of contact reaction with the reflux ammonia steam, so that high-concentration ammonia-containing steam is formed and collected at the top of the analysis reaction tower.
(4) Pumping the effluent of the analysis reaction tower to a deamination tower, introducing saturated steam into the deamination tower, and controlling the deamination tower to be in a negative pressure state through a negative pressure device to realize stripping deamination.
(5) The ammonia-containing steam formed by the deamination tower flows back to the desorption reaction tower, exchanges heat with percolate or biogas slurry entering the desorption reaction tower, introduces the ammonia-containing steam at the top of the desorption reaction tower into a condenser through an ammonia pumping mixing device, and flows back to the deamination tower or the ammonia recovery tower after condensed water and ammonia gas are introduced into the ammonia recovery tower.
(6) Tap water and CO 2 are introduced into the ammonia recovery tower, so that CO 2 reacts with ammonia gas in a liquid phase to generate ammonium bicarbonate and gradually reach saturation, and meanwhile, the temperature of a solution in the ammonia recovery tower is reduced by arranging a bypass cooling system, so that ammonia bicarbonate crystals are separated out.
(7) Periodically discharging ammonium bicarbonate crystal mixed liquid of the ammonia recovery tower to a crystal slurry tank, cooling the mixed liquid in the crystal slurry tank to further separate out ammonium bicarbonate, enabling the mixed liquid of the crystal slurry tank to flow to a centrifugal dehydrator by gravity for solid-liquid separation, returning dehydrated filtrate to the ammonia recovery tower, packaging and bagging the solid, and recycling.
The preferred embodiments of the invention disclosed above are intended only to assist in the explanation of the invention. The preferred embodiments are not exhaustive or to limit the invention to the precise form disclosed. Obviously, many modifications and variations are possible in light of the above teaching. The embodiments were chosen and described in order to best explain the principles of the invention and the practical application, to thereby enable others skilled in the art to best understand and utilize the invention. The invention is limited only by the claims and the full scope and equivalents thereof.
Claims (8)
1. A nitrogen resource heat extraction recovery system, the system comprising:
The pretreatment unit is used for pretreating landfill leachate and anaerobic fermentation biogas slurry of kitchen sludge to form ammonia-containing wastewater entering a subsequent unit, wherein COD (chemical oxygen demand) of the ammonia-containing wastewater is less than or equal to 10000mg/L, SS and less than or equal to 1000mg/L;
the analysis unit is connected with the pretreatment unit and comprises a preheater and an analysis reaction tower, the upper part of the analysis reaction tower is provided with a filler area, the lower part of the analysis reaction tower is provided with a water collecting area and a sludge hopper, ammonia-containing wastewater enters the analysis reaction tower after being preheated, the preheated ammonia-containing wastewater and ammonia-containing steam reflowed by the deamination unit are subjected to heat exchange reaction in the filler area, the temperature of the ammonia-containing wastewater is further increased, and bicarbonate ions in the ammonia-containing wastewater are analyzed to be The ions and the CO 2 are combined,The method comprises the steps of reacting ions with calcium and magnesium ions of ammonia-containing wastewater to generate carbonate precipitate for precipitation, collecting CO 2 together with ammonia-containing steam at the top of a desorption reaction tower, and conveying the ammonia-containing wastewater to an ammonia absorption unit through the top of the desorption reaction tower;
The ammonia-containing wastewater of the analytical reaction tower enters the deamination tower and then carries out stripping deamination reaction with external steam in the packing region, ammonia nitrogen in a liquid phase enters a vapor phase, and the ammonia-containing steam is collected at the top of the deamination tower and flows back to the analytical reaction tower of the analytical reaction unit from the top of the deamination tower;
The ammonia absorption unit is connected with the analysis reaction tower of the analysis unit, the ammonia absorption unit comprises a condenser, a gas-liquid separator, a reflux pump, an ammonia recovery tower, a circulating water pump, a cooler, an ammonia extraction mixing device, a discharging pump and a tail gas recovery and treatment device, ammonia-containing steam at the top of the analysis reaction tower of the analysis unit is condensed by the condenser and then is led to the ammonia recovery tower, condensate flows back to the deamination tower or the ammonia recovery tower of the deamination unit, the ammonia recovery tower is filled with water, CO 2 is introduced into the ammonia recovery tower, ammonia in the ammonia-containing gas and CO 2 react in the ammonia recovery tower to generate ammonium bicarbonate solution, the generated ammonium bicarbonate solution in the ammonia recovery tower is pumped into the crystallization dehydration unit by the discharging pump, the residual gas in the ammonia recovery tower is sent into the tail gas recovery and treatment device for tail gas treatment, the circulating water outlet is arranged at the bottom of the ammonia recovery tower, the circulating water outlet is connected with the upper part of the ammonia recovery tower through the circulating water pump, the cooler and the ammonia extraction mixing device, the ammonia extraction mixing device is also connected with the air outlet end of the gas-liquid separator so as to control the gas-liquid mixture in the ammonia recovery tower to make the ammonia recovery tower enter the ammonia recovery tower into the primary air-liquid recovery tower, and the ammonia recovery tower is saturated with the air-liquid mixture after the ammonia recovery tower reaches the air-liquid recovery tower, and the air-saturated air phase condition is discharged from the air recovery device, and the air mixture reaches the primary air recovery phase condition is saturated condition;
And the crystallization dehydration unit is connected with the ammonia absorption unit and is used for dehydrating the ammonium bicarbonate solution to form ammonium bicarbonate solid, and the dehydrated filtrate is returned to the ammonia recovery tower.
2. The nitrogen resource heat extraction and recovery system according to claim 1, wherein the pretreatment unit comprises a landfill leachate pretreatment unit and a kitchen sludge anaerobic fermentation biogas slurry pretreatment unit, wherein the landfill leachate pretreatment unit pretreats fresh leachate of a landfill site or leachate of a garbage incineration plant by adopting anaerobic+precipitation or filtration pretreatment or anaerobic MBR, old leachate in the landfill site is pretreated by adopting precipitation or filtration, and the kitchen sludge anaerobic fermentation biogas slurry pretreatment unit dehydrates kitchen sludge anaerobic fermentation biogas slurry by adopting centrifugation or a plate frame, and the dehydrated filtrate is pretreated by adopting air floatation.
3. The nitrogen resource heat extraction and recovery system according to claim 1, wherein a first input end of the preheater is connected with the balance water tank, a second input end of the preheater is connected with a water outlet end at the bottom of the deamination tower through a water pump, a first output end of the preheater is connected with an input end of the analysis reaction tower, a second output end of the preheater is connected with a water outlet pipe, high-temperature wastewater at the bottom of the deamination tower is pumped to the preheater of the analysis unit through the water pump, and ammonia-containing wastewater in the balance water tank flows into the analysis reaction tower after being preheated.
4. The nitrogen resource heat extraction and recovery system according to claim 1, wherein the sludge hopper of the resolution reaction tower is connected with the thick slag settling tank through a sludge pump, and sludge carried by the waste water and produced in the course of the resolution reaction are accumulated in the sludge hopper and are periodically discharged to the thick slag settling tank through the sludge pump.
5. The nitrogen resource heat extraction and recovery system as claimed in claim 1, wherein in the ammonia absorption unit, an input end of the condenser is connected with the analysis unit through a pipeline, an output end of the condenser is connected with the gas-liquid separator, a liquid outlet end of the gas-liquid separator is connected with the deamination tower of the deamination unit, and an air outlet end of the gas-liquid separator is connected with the ammonia recovery tower.
6. The nitrogen resource heat extraction and recovery system according to claim 1, wherein the top of the ammonia recovery tower is provided with an air outlet, the air outlet at the top of the ammonia recovery tower is connected with an air inlet of the tail gas recovery tower, the upper part of the tail gas recovery tower is provided with a spray header, the spray header is connected with a water inlet at the upper end of the tail gas recovery tower, the lower end of the tail gas recovery tower is provided with a water outlet, the water outlet is connected with a water inlet at the upper end of the ammonia recovery tower through a water pump, residual gas at the top of the ammonia recovery tower is introduced into the tail gas recovery tower, tap water is adopted for leaching, and leaching liquid flows back to the ammonia recovery tower.
7. The nitrogen resource heat extraction and recovery system according to claim 6, wherein a tail gas outlet is formed in the top of the tail gas recovery tower, the tail gas outlet is connected with a tail gas purification tower through a draught fan, a water inlet is formed in the upper end of the tail gas purification tower, pickling liquid is injected into the water inlet of the tail gas purification tower, the gas outlet at the top of the tail gas purification tower is connected to the biological reaction tank through the draught fan, the leached tail gas in the tail gas recovery tower is introduced into the tail gas purification tower through the draught fan, and the leached tail gas is introduced into the biological reaction tank of the sewage treatment system under the aerobic zone liquid of the biological reaction tank for 1-3 m after pickling.
8. The nitrogen resource heat extraction and recovery system according to claim 1, wherein the crystallization and dehydration unit comprises a crystal slurry tank, a stirrer is arranged in the crystal slurry tank, an outlet at the bottom of the crystal slurry tank is connected with a centrifugal dehydrator, the centrifugal dehydrator is used for dehydrating the generated transition saturated ammonium bicarbonate solution of the ammonia recovery tower, the dehydrated filtrate is stored in a mother liquor tank, the dehydrated filtrate is pumped into the ammonia recovery tower by a mother liquor pump, and the dehydrated ammonium bicarbonate solid is conveyed to a packer by a conveyor.
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| CN110372143A (en) * | 2019-07-19 | 2019-10-25 | 中节能工程技术研究院有限公司 | Landfill leachate physicochemical deamination pretreatment method and device |
| CN111960489A (en) * | 2020-08-07 | 2020-11-20 | 华夏碧水环保科技有限公司 | Garbage penetrating fluid resource recycling system |
| CN112142264B (en) * | 2020-09-28 | 2024-04-09 | 上海市政工程设计研究总院（集团）有限公司 | Treatment system and method for realizing zero emission of landfill leachate and fermented biogas slurry |
| CN112961770B (en) * | 2021-04-09 | 2024-04-16 | 江苏马盛生物科技股份有限公司 | System and method for preparing organic acid/organic acid salt from kitchen waste |
| CN112980896B (en) * | 2021-04-09 | 2024-06-07 | 江苏马盛生物科技股份有限公司 | Kitchen waste dephosphorization and nitrogen removal system and method |
| CN113816549A (en) * | 2021-08-27 | 2021-12-21 | 成都中能恒远环保科技有限公司 | Ammonia nitrogen recovery method in kitchen waste treatment process |
| CN114850170A (en) * | 2022-04-22 | 2022-08-05 | 北京交通大学 | A collaborative device for energy recovery and pollution reduction and carbon reduction of food waste resources |
| CN114871245A (en) * | 2022-04-24 | 2022-08-09 | 南京万德斯环保科技股份有限公司 | Method for recycling ammonia nitrogen in kitchen waste and preparing sewage treatment carbon source |
| CN116282698B (en) * | 2023-03-06 | 2025-02-11 | 武汉天源环保股份有限公司 | Sewage treatment system and method |
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