A high-temperature chemical environmental protection anaerobic system

Abstract

The present invention discloses a high-temperature chemical environmental protection anaerobic system, which is used in the field of organic waste treatment. The system includes a pretreatment device, an anaerobic device, a biogas slurry treatment device, a power generation device and a biogas residue recovery device. The pretreatment device includes a hydrolysis fluidization component, and the hydrolysis liquid outlet of the hydrolysis fluidization component leads to the inlet of the anaerobic device. The sludge outlet of the biogas slurry treatment device and the concentrated liquid outlet of the anaerobic device both lead to a solid-liquid separator. The biogas slurry outlet of the solid-liquid separator leads to the biogas slurry treatment device, and the biogas residue outlet of the solid-liquid separator leads to the biogas residue recovery device. The exhaust gas outlet of the anaerobic device and the biogas outlet of the biogas slurry treatment device lead to the power generation device. The present invention improves the biodegradability of organic matter and also makes the gas production rate of the process higher than that of the conventional process. In addition, the system achieves the purpose of environmental protection.

Description

Technical Field

[0001] The present invention relates to the field of organic waste treatment, and particularly to a high-temperature chemical environmental protection anaerobic system. Background Art

[0002] High-water-content organic wastes include pharmaceutical sludge, breeding manure, human feces, kitchen waste, municipal sludge, food industry sludge, etc. At present, the common method for treating them is anaerobic biochemical treatment. After anaerobic biochemical treatment, biogas slurry and biogas are produced. The substances such as NH3 and PO in the biogas slurry have the greatest impact on the environment. If discharged without treatment, these substances will cause pollution to the environmental water bodies, and directly discharging the biogas into the environment will also cause air pollution. Currently, there is a process of using anaerobic ammonium oxidation process to treat biogas slurry. However, the COD in the biogas slurry is generally high, and the anaerobic ammonium oxidation process system has certain requirements for the COD of the water quality, and the proliferation of ANAMMOX (red bacteria) in the system is also relatively sensitive to COD; the current anaerobic ammonium oxidation process less considers how to reduce the COD in the biogas slurry. Summary of the Invention

[0003] In order to solve the above problems, the present invention provides a high-temperature chemical environmental protection anaerobic system, which can environmentally protect the treatment of organic wastes.

[0004] The technical solution adopted by the present invention is as follows:

[0005] A high-temperature chemical environmental protection anaerobic system includes a pretreatment device, an anaerobic device, a biogas slurry treatment device, a power generation device, and a biogas residue recovery device. The pretreatment device includes a hydrolysis fluidization component. The hydrolysis liquid outlet of the hydrolysis fluidization component leads to the inlet of the anaerobic device. The sludge outlet of the biogas slurry treatment device and the concentrated liquid outlet of the anaerobic device both lead to a solid-liquid separator. The biogas slurry outlet of the solid-liquid separator leads to the biogas slurry treatment device, and the biogas residue outlet of the solid-liquid separator leads to the biogas residue recovery device. The exhaust port of the anaerobic device and the biogas outlet of the biogas slurry treatment device lead to the power generation device.

[0006] As a further improvement of the present invention, the biogas residue recovery device includes a drying kiln and a granulation and forming component. The biogas residue outlet of the solid-liquid separator leads to the drying kiln, and the outlet of the drying kiln leads to the granulation and forming component.

[0007] As a further improvement of the present invention, the hydrolysis fluidization component includes a fluidized bed body, a housing, and a steam distributor. The top of the fluidized bed body is provided with an overflow port. The pretreatment device is provided with an ammonia crystallizer and a slurry inlet leading to the inside of the fluidized bed body. The housing is sleeved outside the fluidized bed body, and an overflow chamber is formed between the housing and the fluidized bed body. The top of the housing is provided with an ammonia gas outlet communicating with the overflow chamber. The ammonia gas outlet leads to the ammonia crystallizer, and the ammonia crystallizer is connected to the drying kiln. The bottom of the housing is also provided with a hydrolysis liquid outlet leading to the overflow chamber. The steam distributor is arranged at the bottom of the fluidized bed body and is externally connected to a steam input pipe.

[0008] As a further improvement of the present invention, the power generation device includes a biogas purification component, a voltage stabilizing component and a generator connected in sequence. The exhaust port of the anaerobic device and the biogas outlet of the biogas slurry treatment device lead to the biogas purification component. The flue gas outlet of the generator is communicated into a flue gas regenerative boiler. The flue gas outlet of the flue gas regenerative boiler is connected to a drying kiln, and the steam outlet of the flue gas regenerative boiler is connected to a steam input pipe.

[0009] As a further improvement of the present invention, the biogas purification component includes a desulfurization module and a dehumidification module through which biogas passes respectively.

[0010] As a further improvement of the present invention, the pretreatment device further includes a homogenization component, which includes a homogenization tank and a homogenization tank. The outlet of the homogenization tank is provided with a cutting pump, the outlet of the cutting pump is provided with a feeding pump, the outlet of the feeding pump is connected to the homogenization tank through a pipeline, and the outlet of the homogenization tank is connected to the hydrolysis fluidization component through a pipeline.

[0011] As a further improvement of the present invention, the biogas slurry treatment device includes a deep anaerobic reactor, an aerobic nitrification reactor and an anaerobic ammonia oxidation reactor connected in sequence. The biogas slurry outlet of the solid-liquid separator leads to the inlet of the deep anaerobic reactor.

[0012] As a further improvement of the present invention, the deep anaerobic reactor has a liquid inlet, a biogas outlet, a liquid outlet and a liquid return port. An aeration component is arranged in the aerobic nitrification reactor. The liquid outlet of the deep anaerobic reactor leads to the inlet of the aerobic nitrification reactor. The liquid inlet of the anaerobic ammonia oxidation reactor communicates with the liquid outlet of the aerobic nitrification reactor. The liquid outlet of the anaerobic ammonia oxidation reactor leads to a transfer container, and the biogas outlet of the deep anaerobic reactor leads to the power generation device.

[0013] As a further improvement of the present invention, the biogas slurry treatment device further includes a biogas slurry tank. The solid-liquid separator has a biogas residue outlet, a biogas slurry outlet and a suction inlet leading to the biogas slurry tank. The concentrated liquid outlet of the anaerobic device is introduced into the biogas slurry tank through a pipeline, and the biogas slurry outlet of the solid-liquid separator communicates with the liquid inlet of the deep anaerobic reactor.

[0014] As a further improvement of the present invention, the deep anaerobic reactor is provided with a sludge discharge port. The sludge discharge port of the deep anaerobic reactor and the sludge discharge port of the aerobic nitrification reactor are connected in parallel through a pipeline and then lead to the biogas slurry tank.

[0015] The beneficial effects of the present invention are as follows: By setting up a hydrolysis fluidization component, the present invention significantly reduces the suspended solids (SS) of the waste, converts some insoluble COD under conventional processes into soluble COD that is easily biodegradable, improves the biodegradability of organic matter, and also makes the gas production rate of the process higher than that of conventional processes. In addition, the system is provided with a power generation device and a biogas residue recovery device. The biogas generated during the hydrolysis fluidization and biogas slurry treatment processes is utilized for energy through the power generation device, and the generated biogas residue is recovered and used for fertilizer production, thereby achieving the purpose of environmental protection. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] The present invention will be further described below in conjunction with the drawings and embodiments.

[0017] Figure 1 is the process schematic diagram of the present invention;

[0018] Figure 2 is the schematic diagram of the pretreatment device;

[0019] Figure 3 is the schematic diagram of the hydrolysis fluidization component;

[0020] Figure 4 is the schematic diagram of the biogas slurry treatment device;

[0021] Figure 5 is the schematic diagram of the biogas residue recovery device;

[0022] Figure 6 is the schematic diagram of the power generation device. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0023] Refer to Figures 1 to 6 the high-temperature chemical environmental protection anaerobic system shown, which includes a pretreatment device, an anaerobic device 2, a biogas slurry treatment device, a power generation device, and a biogas residue recovery device. The pretreatment device includes a hydrolysis fluidization component 1. The hydrolysis liquid outlet of the hydrolysis fluidization component 1 leads to the inlet of the anaerobic device 2. The sludge outlet of the biogas slurry treatment device and the concentrated liquid outlet of the anaerobic device 2 both lead to the solid-liquid separator 8. The biogas slurry outlet of the solid-liquid separator 8 leads to the biogas slurry treatment device, and the biogas residue outlet of the solid-liquid separator 8 leads to the biogas residue recovery device. The exhaust port of the anaerobic device and the biogas outlet of the biogas slurry treatment device lead to the power generation device.

[0024] The pretreatment device, the anaerobic device 2, the biogas slurry treatment device, the power generation device, and the biogas residue recovery device will be described in detail below.

[0025] The biogas residue recovery device includes a drying kiln 9 and a granulation and forming component 10.

[0026] The concentrated liquid outlet of the anaerobic device 2 leads to the solid-liquid separator 8. The solid-liquid separator 8 is provided with a biogas residue outlet and a biogas slurry outlet. The biogas slurry after solid-liquid separation is discharged from the biogas slurry outlet to the subsequent biogas slurry treatment device. The biogas residue after solid-liquid separation is led to the drying kiln 9 through the biogas residue outlet for drying and dehydration. The outlet of the drying kiln 9 is led to the granulation and forming component 10 through a conveying component. The dried biogas residue is transformed into solid fertilizer through the treatment of the granulation and forming component 10, and then is packaged and transported.

[0027] Reference Figure 5 , the biogas residue outlet is connected to the inlet of the screw conveyor 81 through a pipeline. The screw conveyor 81 is a horizontal screw and leads to the above-mentioned drying kiln 9. The outlet of the drying kiln 9 is located at the bottom and is provided with a lifting component 82. The lifting component 82 can be an inclined screw conveyor, and the outlet of the screw conveyor is located at the top and leads to the granulation and forming component 10.

[0028] The pretreatment device includes a hydrolysis fluidization component 1. The hydrolysis liquid outlet of the hydrolysis fluidization component 1 leads to the inlet of the anaerobic device 2. The function of the hydrolysis fluidization component 1 is to accelerate the decomposition of organic matter in organic waste, break the chemical bonds of organic matter, and change the organic matter with long molecular chains into organic matter with short molecular chains. Some substances that are difficult to decompose in traditional anaerobic reactors become biodegradable substances after passing through the hydrolysis fluidization component 1, greatly improving the biodegradability of organic waste. Thus, the liquid (hydrolysis liquid) discharged into the anaerobic device 2 is relatively easy to treat. The specific structure of the pretreatment device will be described below.

[0029] The above-mentioned biogas slurry treatment device includes a deep anaerobic reactor 3, an aerobic nitrification reactor 4, and an anaerobic ammonium oxidation reactor 5 connected in sequence. The concentrated liquid outlet of the anaerobic device 2 leads to the inlet of the deep anaerobic reactor 3, and the concentrated liquid (biogas slurry) is discharged into the deep anaerobic reactor 3. The function of the biogas slurry treatment device is to treat the biogas slurry generated by the system. In the embodiment, the deep anaerobic reactor 3 adopts medium-temperature anaerobic. After the biogas slurry is treated by the deep anaerobic reactor 3, it becomes thin biogas slurry, and the thin biogas slurry flows into the aerobic nitrification reactor 4 under the action of gravity. The deep anaerobic reactor 3 and the aerobic nitrification reactor 4 form an A / O process combination for phosphorus removal and continuous removal of organic matter in sewage, providing an electron acceptor for the subsequent anaerobic ammonium oxidation process; the biogas slurry after aerobic treatment flows into the anaerobic ammonium oxidation reactor 5. The advantage of using the anaerobic ammonium oxidation process to treat the biogas slurry is to remove TN and NH3 without using the carbon source of the biogas slurry.

[0030] The following describes the pretreatment device.

[0031] Combined with reference Figure 2 and Figure 3, the pretreatment device further includes a homogenization component 6, and the slurry outlet of the homogenization component 6 leads to the hydrolysis fluidization component 1. The homogenization component 6 is used to disperse the solid substances in the organic waste through stirring, cutting or other means, and mix them with water to form a slurry, which is convenient for subsequent treatment in the hydrolysis fluidization component 1.

[0032] The homogenization component 6 includes a homogenization tank 61 and a homogenization tank 62. A stirring paddle is provided inside the homogenization tank 61, and a cutting pump 63 is provided at the outlet of the homogenization tank 61. While a feed pump 64 is provided at the outlet of the cutting pump 63, it can also be refluxed to the homogenization tank 61 through a pipeline. The outlet of the feed pump 64 is connected to the homogenization tank 62 through a pipeline, and the outlet of the homogenization tank 62 is connected to the hydrolysis fluidization component 1 through a pipeline. The organic waste can be mixed with water in the homogenization tank 61, pre-mixed by the stirring paddle 65, and then output and homogenized after being transported and stirred by the cutting pump 63; during the stirring process, the organic waste circulates between the homogenization tank 61 and the cutting pump 63, and the impurities brought in by the organic waste are crushed under the repeated cutting of the cutting pump 63; the stirred and cut organic waste is diluted into a slurry, and the slurry continuously circulates, stirs and cuts until the homogenization tank 61 is filled with the slurry and the stirring ends, and then the slurry is pumped into the homogenization tank 62 by the slurry feed pump 64. A stirrer is also provided inside the homogenization tank 62 to keep the slurry uniform.

[0033] A feeding pressurization component is provided on the pipeline connecting the homogenization tank 62 and the hydrolysis fluidization component 1. The feeding pressurization component can input the slurry into the hydrolysis fluidization component 1, and at the same time boost the pressure of the slurry to a suitable pressure, so that the slurry and the hydrolysis fluidization component 1 have a suitable pressure value. The preferred feeding pressurization component is a high-pressure piston pump 66.

[0034] The above-mentioned hydrolysis fluidization component 1 has a hydrolysis liquid outlet, an ammonia gas outlet 121, a slurry inlet 122 and a steam inlet, wherein the slurry inlet is connected to the high-pressure piston pump 66 to input the homogenized slurry into the hydrolysis fluidization component 1. In the hydrolysis fluidization component 1, the slurry is heated so that the nutrients in the slurry are hydrolyzed into substances such as polysaccharides, organic acids, peptides and enzymes. When the protein is hydrolyzed, the nitrogen element NH4 + is decomposed into unstable free ammonia HN3·H2O (hydrated ammonia), and the unstable free ammonia further turns into ammonia gas and is discharged through the ammonia gas outlet 121 under the action of heat.

[0035] The pretreatment device further includes a heat exchanger 17. The heat exchanger 17 is a plate heat exchanger, which connects the hydrolysis liquid outlet of the hydrolysis fluidization component 1 to the subsequent process device, and at the same time connects the outlet of the homogenization component to the slurry inlet 122. The slurry entering the slurry inlet 122 can be heated by using the heat in the hydrolysis liquid, so that the system reasonably utilizes heat and saves costs.

[0036] The following describes the hydrolysis fluidization component 1.

[0037] The hydrolysis fluidization component 1 includes a fluidized bed body 11, a housing 12, and a steam distributor 13.

[0038] The fluidized bed body 11 is in the shape of a container, with an open top forming an overflow port 14. The hydrolyzed liquid that overflows in the fluidized bed body 11 can flow out to the outside from the overflow port 14. A sludge discharge port is provided at the bottom of the fluidized bed body 11, and a slurry inlet 122 leads to the inside of the fluidized bed body 11 and is externally connected to a feed pipe; the feed pipe is at a position higher than the sludge discharge port but also close to the bottom of the fluidized bed body 11.

[0039] The steam distributor 13 is arranged at the bottom of the fluidized bed body 11, and its steam injection direction is preferably upward and leads to the inside of the fluidized bed body 11, forming water vapor rising from bottom to top. The steam distributor 13 is externally connected to a water vapor input pipe 111 through a steam inlet, for introducing high-pressure and high-temperature water vapor into the inside of the fluidized bed body 11.

[0040] The housing 12 is sleeved outside the fluidized bed body 11 and makes the fluidized bed body 11 located in the middle. The top wall of the housing 12 is separated from the overflow port 14 by a certain distance in the height direction, and the outer wall of the housing 12 is separated from the outer wall of the fluidized bed body 11 by a certain distance to form an overflow chamber. The hydrolyzed liquid flowing out from the overflow port 14 can enter the overflow chamber. A hydrolyzed liquid outlet leading to the overflow chamber is also provided at the bottom of the housing 12, for discharging the hydrolyzed liquid in the overflow chamber out of the housing 12. An ammonia outlet 121 is arranged at the top of the housing 12 and communicates with the overflow chamber to discharge the ammonia generated during hydrolysis. The ammonia outlet 121 is connected with a discharge valve 123 for controlling the discharge of ammonia.

[0041] Then the process of hydrolysis fluidization using the hydrolysis fluidization component 1 is as follows:

[0042] The contaminated slurry is input into the fluidized bed body 11. At this time, the fluidized bed body 11 can be in a high-temperature and high-pressure state through preheating and pressurization, or the high-temperature and high-pressure contaminated slurry can be directly input into the closed fluidized bed body 11; the high-temperature water vapor enters the fluidized bed body 11 through the steam distributor 13 to further heat up the contaminated slurry; at this time, the organic matter in the contaminated slurry will decompose rapidly, the chemical bonds of the organic matter will break, and the organic matter with long molecular chains will become organic matter with short molecular chains. Some substances that are difficult to decompose in traditional anaerobic reactors will become biodegradable substances after passing through the fluidized bed body 11, and the biodegradability of the contaminated slurry is greatly improved; part of the decomposed hydrolysis liquid will bypass the fluidized bed body 11 and enter the overflow chamber. The substances that have not been decomposed will continue to stay in the fluidized bed body 11 for decomposition due to their relatively large specific gravity; due to being in a high-temperature and high-pressure state, part of the organic matter and ammonia in the hydrolysis liquid will become gas containing ammonia, which is discharged from the ammonia outlet 121, and the ammonia will be discharged to the ammonia crystallizer 16 described later for crystallization; after operating for a period of time, some organic matter (such as cellulose) and inorganic matter (such as fixed carbon, stone powder, etc.) that cannot be decomposed will remain in the fluidized bed body 11. In order to ensure the hydrolysis effect, the mud discharge port is opened for mud discharge in a certain production cycle.

[0043] The above process can also be simply summarized as: the contaminated slurry enters the fluidized bed body 11. The lighter suspended solids in it rise upward under the push of high-temperature and high-pressure steam, overflow the fluidized bed body 11, and flow to the mud discharge port at the bottom. The materials with larger particle size and heavier weight descend along the inner cavity wall and are washed and hydrolyzed by steam again, and so on; during the process of the contaminated slurry and steam rising, heat exchange occurs between the steam and the contaminated slurry, and the steam condenses into water and mixes into the contaminated slurry.

[0044] The principle of the above process is as follows: during the fluidization process of the contaminated slurry in the device, due to the action of heat, the nutrients in the contaminated slurry are hydrolyzed into substances such as polysaccharides, organic acids, peptides, and enzymes. When the protein is hydrolyzed, the nitrogen element NH4 + is decomposed into unstable free ammonia HN3·H2O (hydrated ammonia). Under the action of heat, the unstable free ammonia further becomes ammonia gas and is regularly released through the exhaust valve installed at the top of the tower. The reaction formulas related to hydrolysis and ammonia removal are as follows:

[0045] 1). NH4 + +OH - →NH3·H2O

[0046] 2). NH3·H2O→NH3↑+H2O

[0047] Through high-temperature hydrolysis, the organic matter is hydrolyzed and acidified into hydrolysis liquid. In this embodiment, the high-temperature water vapor can be used as the fluidizing gas for solid organic matter and the stripping gas for NH3, and at the same time, it is also the medium for providing the hydrolysis temperature. The high-temperature water vapor is also at high pressure to maintain the pressure in the fluidized bed body 11 and heat up the contaminated slurry in the fluidized bed body 11 to 120 - 190 °C.

[0048] The heat exchanger 17 described above has a cold inlet and a hot outlet that communicate with each other, and a hot inlet and a cold outlet that communicate with each other. Among them, the hot outlet of the heat exchanger 17 communicates with the slurry inlet 122, the cold inlet leads to the homogenizing tank 62, the hot inlet of the heat exchanger 17 is connected to the hydrolysis liquid outlet through a pipeline, and the cold outlet leads to the pressure relief tower 15 described below.

[0049] The high-pressure plunger pump 66 described above is used to pressurize the slurry to a suitable pressure value and then input it into the fluidized bed body 11, so that the fluidized bed body 11 is "preset" with pressure.

[0050] The slurry is pressurized to 0.5 - 1.5 Mpa by the high-pressure plunger pump 66, and then enters the heat exchanger 17. Using the high-temperature hydrolysis liquid after fluidized hot hydrolysis as the heat source, the slurry is preheated to 100 - 150 °C; then the above hydrolysis process is carried out; after hydrolysis, the hydrolysis liquid enters the heat exchanger 17 for cooling (the heat is used to preheat the newly incoming slurry), and the temperature drops to 40 - 60 °C and is sent to the subsequent process.

[0051] In the above implementation, referring to the above reaction formula 2: NH4 + +OH - →NH3·H2O, this formula is reversible. In an acidic environment with a pH value of 4.5 - 5.8, when the hydrolysis temperature drops, free ammonia will react again to form ammonium, causing the pH of the hydrolysis liquid to rise, as shown in the following reaction formula 3:

[0052] 3), NH3·H2O→NH4 + +OH -

[0053] According to reaction formulas 1), 2), and 3), it can be seen that the amount of ammonium released in the slurry can be achieved by adjusting the acidity and alkalinity. The precipitation of ammonia gas is closely related to the dissolved oxygen (DO) and hydrolysis temperature of the hydrolysis liquid. Then, by adding a sodium hydroxide solution in proportion before the booster plunger pump to change the acidity and alkalinity of the slurry and controlling the hydrolysis temperature, the effective control of ammonia nitrogen in the hydrolysis liquid can be achieved, and the pH should be adjusted to a weak acidic value of 5.8 - 6.8.

[0054] The pretreatment device also includes a pressure relief tower 15 and an ammonia crystallizer 16.

[0055] The inlet of the pressure relief tower 15 described above communicates with the hydrolysis liquid outlet of the fluidized bed body 11 through a pipeline to receive the hydrolysis liquid discharged from the hydrolysis fluidizing component 1. Since the discharged hydrolysis liquid has a certain pressure, the pressure relief tower 15 can release the pressure in the hydrolysis liquid and at the same time play a role in temporarily storing the hydrolysis liquid, providing buffer time and maintenance time for the subsequent process. Specifically, a spray head 151 is provided at the top of the pressure relief tower 15, and the hydrolysis liquid is introduced into the spray head 151 to be sprayed into the inner cavity of the pressure relief tower 15, and the hydrolysis liquid of the pressure relief tower 15 is discharged from the bottom end.

[0056] The ammonia outlet 121 of the hydrolysis fluidizing component 1 is connected to the ammonia crystallizer 16 through a pipeline, and a valve is also provided on this pipeline for regular discharge. The ammonia crystallizer 16 is in the shape of a container, and sulfuric acid is injected into it. Ammonia reacts with sulfuric acid to form ammonium sulfate, and its chemical reaction formula is as follows:

[0057] 2NH3 + H2SO4 → NH 42 4SO4.

[0058] The ammonia crystallizer 16 is connected to the drying kiln 9. The generated ammonium sulfate can be dried after being discharged to the drying kiln 9, and then used for fertilizer production.

[0059] The pressure relief tower 15 is provided with a gas outlet at the top, and this gas outlet leads to the ammonia crystallizer 16. The gas formed after the hydrolysis liquid volatilizes also contains ammonia, so it is discharged into the ammonia crystallizer 16 together to form a solid state.

[0060] The top of the homogenization tank 62 is provided with an exhaust port 621 leading to the ammonia crystallizer 16 for discharging gases such as ammonia volatilized in the homogenization tank 62. The bottom of the homogenization tank 62 is provided with a sludge discharge port for discharging impurities and residues. The sludge discharge port is connected to the sludge discharge opening through a sludge discharge pipe, and the discharged bottom slag can be transported out or used for drying into fertilizer.

[0061] The pressure relief tower 15 is provided with a liquid outlet at the bottom end, and a drain pipe is connected to the liquid outlet. This drain pipe can lead to the anaerobic device 2, and a reflux component 152, such as a reflux pump, is provided between the anaerobic device 2 and the homogenization component 6. The reflux component 152 returns the hydrolysis liquid discharged from the pressure relief tower 15 to the homogenization component 6 for use in diluting organic waste.

[0062] After the above pretreatment device and process, the BOD of the hydrolysis liquid will not decrease synchronously with the COD index, and indicators such as TN and NH3 in the hydrolysis liquid become adjustable indicators, thus greatly enhancing the biodegradability of organic waste.

[0063] The anaerobic device 2 in the embodiment is a CSTR (Continuous Stirred Tank Reactor), also known as a completely mixed flow reactor. Its working principle is to purify organic pollutants by means of anaerobic activated sludge in the digestion tank. Generally, the hydraulic retention time of the medium-temperature CSTR anaerobic process is 32 days, the hydrolysis time of suspended solids in sewage is about 10d - 15d, the acidification time is about 4h, and the peak period of anaerobic bacteria gas production is about 15d. In the embodiment, since the organic waste has been pretreated through processes such as hydrolysis and acidification, in order to reduce investment and improve the effect of the anaerobic process, the embodiment adopts a high-temperature CSTR anaerobic process with a hydraulic retention time of about 15d.

[0064] The hydrolyzate enters the CSTR tank through a pipeline from the pressure relief tower 15 and comes into full contact with the original anaerobic activated sludge in the tank through stirring. The organic matter in the hydrolyzate is converted into biogas through the metabolism of methanogens, and the hydrolyzate and sludge are mixed into a crude biogas slurry containing a certain amount of solid matter.

[0065] The following is an explanation of the biogas slurry treatment device.

[0066] Reference Figure 4 , and in combination with Figures 1 - 3 , the deep anaerobic reactor 3 is a multi-stage deep anaerobic reactor, also known as an IC anaerobic reactor. It has an inlet, a biogas outlet, an outlet, and a return liquid port. A three-phase separator is also provided at the top of the deep anaerobic reactor 3. The deep anaerobic reactor 3 is a highly efficient multi-stage internal circulation reactor. Compared with the original traditional anaerobic reactor, it has the advantages of less land occupation, higher organic load, stronger shock resistance, more stable performance, and simpler operation and management. When treating high-concentration organic wastewater with a COD of 10,000 - 15,000 mg / L, the general volume load of the traditional anaerobic reactor is 5 - 8 kgCOD / m 3 ; the volume load rate of the IC anaerobic reactor can reach 15 - 30 kgCOD / m 3 .

[0067] An aeration component 41 is provided inside the aerobic nitrification reactor 4. The aeration component 41 is located at the bottom and can be an aeration pipe densely distributed with micropores. The aeration pipe is connected to an external air compressor 43 through a pipeline. The outlet at the top of the deep anaerobic reactor 3 leads to the inlet at the bottom of the aerobic nitrification reactor 4 by means of gravity flow.

[0068] The inlet of the anaerobic ammonium oxidation reactor 5 communicates with the outlet of the aerobic nitrification reactor 4 to receive the biogas slurry after aerobic nitrification. The outlet of the anaerobic ammonium oxidation reactor 5 leads to a transfer container 51.

[0069] The above-mentioned deep anaerobic reactor 3 adopts medium-temperature anaerobic treatment. After the hydrolyzate (biogas slurry) treated by the anaerobic device 2 is treated by the deep anaerobic reactor 3, the biogas generated during the anaerobic process is discharged through a pipeline from the gas collection area of the three-phase separator provided at the top of the reactor and is used for subsequent processes;

[0070] The dilute biogas slurry treated by the deep anaerobic process flows into the aerobic nitrification reactor 4 under the action of gravity. The deep anaerobic reactor 3 and the aerobic nitrification reactor 4 form an A / O process combination for phosphorus removal and continuous removal of organic matter in the sewage, providing an electron acceptor for the subsequent anaerobic ammonium oxidation process;

[0071] The biogas slurry after aerobic treatment flows into the anaerobic ammonium oxidation reactor 5. The advantage of using the anaerobic ammonium oxidation process to treat the biogas slurry is that TN and NH3 can be removed without using the carbon source of the biogas slurry.

[0072] In the above process, the biogas slurry is in full contact with the oxygen in the air ejected from the aeration pipe. The functions of oxygen in the aerobic nitrator are as follows:

[0073] 1) Oxidize NH4 + to generate nitrite NO2 - to provide an electron acceptor for the anaerobic ammonium oxidation process;

[0074] 2) The aerobic nitrification reactor 4 and the deep anaerobic reactor 3 form an A / O phosphorus removal process;

[0075] 3) The functions of oxygen in the aerobic nitrification reactor 4 also include further removing organic matter in the sewage and increasing the dissolved oxygen (DO) in the sewage.

[0076] In addition, the combination of the deep anaerobic reactor 3, the anaerobic ammonium oxidation reactor 5 and the aerobic nitrification reactor 4 can also be regarded as an A / O phosphorus removal process.

[0077] The above-mentioned aerobic nitrification reactor 4 is provided with a sludge discharge port at the bottom end. The sludge discharge port of the aerobic nitrification reactor 4 is connected to the sludge return port of the deep anaerobic reactor 3 through a pipeline and a reflux pump 42 arranged on the pipeline.

[0078] The biogas slurry treatment device further includes a biogas slurry tank 7 and a solid-liquid separator 8. The concentrated liquid outlet of the anaerobic device 2 is led into the biogas slurry tank 7 through a pipeline, and the biogas slurry outlet of the solid-liquid separator 8 is communicated with the liquid inlet of the deep anaerobic reactor 3.

[0079] Specifically, the bottom end of the deep anaerobic reactor 3 is also provided with a sludge discharge port. The sludge discharge port of the deep anaerobic reactor 3 and the sludge discharge port of the aerobic nitrification reactor 4 are connected in parallel through a pipeline and then led into the biogas slurry tank 7 for adding the original biogas slurry. Correspondingly, corresponding valves are arranged on the pipeline to control sludge discharge. At the same time, the valves can also control whether the sludge discharged from the aerobic nitrification reactor 4 is discharged to the deep anaerobic reactor 3 or the biogas slurry tank 7.

[0080] The solid-liquid separator 8 has a marsh residue outlet, a suction inlet leading to the biogas slurry tank 7 and a biogas slurry outlet leading to the filtration tank 71. The solid-liquid separator 8 is a screw dehydrator. The feed inlet of the screw dehydrator serves as the suction inlet and is connected to the biogas slurry tank 7 through a pipeline. A lift pump is arranged between the screw dehydrator and the biogas slurry tank 7, which can input the crude biogas slurry, the sludge discharged from the sludge discharge port of the aerobic nitrification reactor 4, and the sludge discharged from the sludge discharge port of the deep anaerobic reactor 3 into the screw dehydrator for solid-liquid separation; the discharge outlet of the screw dehydrator constitutes the marsh residue outlet, and the marsh residue outlet can be externally connected to a pipeline and led to a drying device not shown in the figure. After solid-liquid separation, the inorganic substances, fixed carbon and large particulate organic matter that are not hydrolyzed in the crude biogas slurry are intercepted and sent to the organic fertilizer production process for treatment.

[0081] The liquid outlet of the screw dehydrator forms a biogas slurry outlet, and the biogas slurry outlet leads to the filtration tank 71 through a pipeline. Then, the feed pump 72 lifts the biogas slurry in the filtration tank 71 to the liquid inlet of the deep anaerobic reactor 3.

[0082] Sometimes, the concentration of the biogas slurry input from the filtration tank 71 to the deep anaerobic reactor 3 may be relatively high, which is not conducive to the anaerobic reaction. Therefore, a liquid with a lower concentration (such as water) can be additionally input at the bottom of the deep anaerobic reactor 3 to dilute the concentration of the biogas slurry.

[0083] The deep anaerobic reactor 3 is provided with a liquid return port, and a reflux device 52 is provided between the transfer container 51 and the liquid return port. During the treatment process, the reflux device 52 recycles the reclaimed water treated by the anaerobic ammonium oxidation reactor 5, thereby saving water. In addition, the reclaimed water in the transfer container 51 can also be used for long-term irrigation and other purposes.

[0084] The biogas outlet of the deep anaerobic reactor 3 is connected to the power generation device through a pipeline, and a fireproof water seal 31 is provided on the pipeline connecting the power generation device and the biogas outlet.

[0085] In order to enhance the ammonia nitrogen removal efficiency of the anaerobic ammonium oxidation reactor 5, a filler is provided in the reactor as the bacterial bed of ANAMMOX (red bacteria). The principle of the anaerobic ammonium oxidation process belongs to the commonly used technology in the art, so it will not be described in detail in the embodiments.

[0086] In the embodiment, the biogas slurry initially entering the biogas slurry tank 7 needs to be adjusted for ammonia nitrogen to make the subsequent deep anaerobic feasible, and this ammonia nitrogen adjustment is realized by the pretreatment device.

[0087] The sludge in the aerobic nitrification reactor 4 contains polyphosphate-accumulating bacteria, which can be pre-cultured in the reactor or the sludge cultured with polyphosphate-accumulating bacteria can be directly injected into the reactor. After the biogas slurry in the aerobic nitrification reactor 4 enters the aerobic state, the PHB stored in the polyphosphate-accumulating bacteria undergoes aerobic decomposition and releases a large amount of energy. Part of this energy is used for the proliferation of polyphosphate-accumulating bacteria, and part is used as the energy for actively absorbing phosphate in the biogas slurry. The phosphate accumulates in the polyphosphate-accumulating bacteria in the form of polyphosphate; a large number of polyphosphate-accumulating bacteria are contained in the aerobic sludge, and the purpose of removing phosphate can be achieved by discharging the sludge.

[0088] The sludge discharged from the aerobic nitrification reactor 4 also contains polyphosphate-accumulating bacteria. Then, in the reflux mode, the sludge refluxed to the deep anaerobic reactor 3 also contains polyphosphate-accumulating bacteria, enabling the deep anaerobic reactor 3 to also achieve the purpose of phosphorus removal.

[0089] The following describes the power generation device.

[0090] Reference Figure 6, the power generation device includes a biogas purification component 91, a voltage stabilizing component 92, and a generator 93 that are connected in sequence.

[0091] The exhaust port of the anaerobic device 2 and the biogas outlet of the biogas slurry treatment device lead to the biogas purification component 91. The biogas generated by the anaerobic device 2 first enters the biogas purification component 91. The biogas purification component 91 is used to purify biogas, remove impurities in the biogas, and reduce the impact on the subsequent generator 93. The voltage stabilizing component 92 is used to temporarily store the purified biogas, adjust and stabilize the pressure of the biogas. The stabilized biogas is transported to the generator 93, so that the flow rate is stable and the power generation of the generator 93 is also stable.

[0092] A booster fan 94 is also provided between the exhaust port of the anaerobic device 2 and the biogas purification component 91. The outlet of the booster fan 94 is connected to the biogas purification component 91 through a pipeline. The outlet of the biogas purification component 91 is connected to the voltage stabilizing component 92 through a pipeline. The outlet of the voltage stabilizing component 92 is connected to the generator 93 serving as a power generation component through a pipeline. The generator 93 is externally connected to a circulating water module. The circulating water module is used to input cooling water into the generator 93 and export the water body after cooling and heating to form a water cycle.

[0093] Considering that the power generation efficiency of the generator 93 is about 30%, most of the rest appears in the form of sensible heat of flue gas and sensible heat of cooling water. Among them, about 40% of the total heat is sensible heat of flue gas, and about 30% is sensible heat of cooling water. In order to improve the thermal efficiency of the device, a flue gas recuperative boiler 95 is provided in the embodiment. The flue gas outlet of the generator 93 is connected to the flue gas recuperative boiler 95 through a pipeline.

[0094] Further preferably, the water inlet of the flue gas recuperative boiler 95 is connected with a water inlet pipe, and the water return port of the circulating water module is connected with a water return pipe. Both the water inlet pipe and the water return pipe are connected to the heat exchange component 96. The heat exchange component 96 is a heat exchanger. The cooling water of the generator 93 enters the heat exchanger after being heated up, so as to heat the soft water entering the flue gas recuperative boiler 95, improve the efficiency of the water body evaporating into steam, and reasonably utilize the waste heat of the circulating water. The circulating cooling water after heat exchange still has a relatively high temperature. Therefore, a radiator is additionally provided on the pipeline for further heat dissipation.

[0095] The steam outlet of the flue gas recuperative boiler 95 is connected to a steam input pipe 111 to recycle the heat of the flue gas recuperative boiler 95 to the hydrolysis fluidization component 1.

[0096] The flue gas outlet of the flue gas recuperative boiler 95 is connected to the drying kiln 9, and the residual heat in the flue gas is fully utilized.

[0097] The described biogas purification component 91 includes a desulfurization module 911 and a dehumidification module 912. Biogas passes through these two modules respectively. Generally, it first passes through the desulfurization module 911 and then through the dehumidification module 912. Since the biogas generated by the anaerobic system in the continuous production line contains a large amount of H2S, the presence of these gases will seriously threaten the operation of the subsequent generator 93. In the embodiment, the dry iron oxide desulfurization process is used to remove H2S in the biogas. The described dehumidification module 912 can use a water separator to remove moisture in the biogas.

[0098] Further preferably, the desulfurization module 911 and the dehumidification module 912 are designed as an integral module. Both the desulfurization module 911 and the dehumidification module 912 are made into tower-shaped containers to form a desulfurization and dehumidification tower, which is convenient for the overall installation and construction of users.

[0099] Further preferably, the voltage stabilizing component 92 is a double-membrane gas storage tank.

[0100] Generally speaking, the anaerobic systems of the above embodiments have the following advantages:

[0101] 1), By adopting fluidized hydrolysis, the suspended solids (SS) in the slurry are greatly reduced, and some insoluble COD under conventional processes is converted into soluble COD that is easy to biodegrade, making the gas production rate of the process higher than that of conventional processes;

[0102] 2), By adjusting the ammonium saturation and pH, the process combination of high temperature and steam stripping makes the ammonia nitrogen index adjustable, enhancing the biodegradability of the hydrolyzate;

[0103] 3), Using the deep anaerobic process and the aeration aerobic process, phosphorus is solidified in the biogas residue and becomes organic fertilizer;

[0104] 4), Using the combination of aerobic and anaerobic ammonium oxidation processes to solve the problem of ammonia nitrogen in biogas slurry at low cost;

[0105] 5), Through the fluidized hydrolysis process, controllable artificial hydrolysis and acidification are realized, minimizing the hydraulic retention time of the slurry. While increasing the gas production, the investment in the anaerobic system is reduced;

[0106] 6), The system adopts a cascade working temperature, and under the condition of ensuring control, the thermal efficiency of the system is higher;

[0107] 7), The system adopts an extreme heat recovery system to achieve low-cost artificial high-efficiency subcritical hydrolysis.

[0108] The above is only the preferred implementation manner of the present invention, and it does not constitute a limitation to the protection scope of the present invention.

Claims

1. A high-temperature chemical environmental protection anaerobic system, characterized in that: It includes a pretreatment device, an anaerobic device (2), a biogas slurry treatment device, a power generation device and a biogas residue recovery device. The pretreatment device includes a hydrolysis fluidization component (1). The hydrolysis liquid outlet of the hydrolysis fluidization component (1) leads to the inlet of the anaerobic device (2). The sludge outlet of the biogas slurry treatment device and the concentrated liquid outlet of the anaerobic device both lead to a solid-liquid separator (8). The biogas slurry outlet of the solid-liquid separator (8) leads to the biogas slurry treatment device, and the biogas residue outlet of the solid-liquid separator (8) leads to the biogas residue recovery device. The exhaust gas outlet of the anaerobic device and the biogas outlet of the biogas slurry treatment device lead to the power generation device. The biogas residue recovery device includes a drying kiln (9) and a granulation and forming component (10). The biogas residue outlet of the solid-liquid separator (8) leads to the drying kiln (9), and the outlet of the drying kiln (9) leads to the granulation and forming component (10). The hydrolysis fluidization component (1) includes a fluidized bed body (11), a housing (12) and a steam distributor (13). An overflow port (14) is opened at the top of the fluidized bed body (11). The pretreatment device is provided with an ammonia crystallizer (16) and a slurry inlet leading to the inside of the fluidized bed body (11). The housing (12) is sleeved outside the fluidized bed body (11), and an overflow cavity is formed between the housing (12) and the fluidized bed body (11). An ammonia gas outlet (121) communicating with the overflow cavity is provided at the top of the housing (12). The ammonia gas outlet (121) leads to the ammonia crystallizer (16), and the ammonia crystallizer (16) is connected to the drying kiln (9). A hydrolysis liquid outlet leading to the overflow cavity is also provided at the bottom of the housing (12). The steam distributor (13) is arranged at the bottom of the fluidized bed body (11) and is externally connected to a steam input pipe (111).

2. The high-temperature chemical environmental protection anaerobic system according to claim 1, wherein: The power generation device includes a biogas purification component (91), a voltage stabilizing component (92) and a generator (93) connected in sequence. The exhaust gas outlet of the anaerobic device (2) and the biogas outlet of the biogas slurry treatment device lead to the biogas purification component (91). The flue gas outlet of the generator (93) is communicated into a flue gas recuperative boiler (95). The flue gas outlet of the flue gas recuperative boiler (95) is connected to the drying kiln (9), and the steam outlet of the flue gas recuperative boiler (95) is connected to the steam input pipe (111).

3. The high-temperature chemical environmental protection anaerobic system according to claim 2, characterized in that: The biogas purification component (91) includes a desulfurization module (911) and a dehumidification module (912) through which biogas respectively passes.

4. The high-temperature chemical environmental protection anaerobic system according to any one of claims 1-3, characterized in that: The pretreatment device further includes a homogenization component (6). The homogenization component (6) includes a homogenization tank (61) and a homogenization tank (62). A cutting pump (63) is provided at the outlet of the homogenization tank (61). A feeding pump (64) is provided at the outlet of the cutting pump (63). The outlet of the feeding pump (64) is connected to the homogenization tank (62) through a pipeline. The outlet of the homogenization tank (62) is connected to the hydrolysis fluidization component (1) through a pipeline.

5. The high-temperature chemical environmental protection anaerobic system according to any one of claims 1-3, characterized in that: The biogas slurry treatment device includes a deep anaerobic reactor (3), an aerobic nitrification reactor (4) and an anaerobic ammonium oxidation reactor (5) connected in sequence. The biogas slurry outlet of the solid-liquid separator (8) leads to the inlet of the deep anaerobic reactor (3).

6. The high-temperature chemical environmental protection anaerobic system according to claim 5, wherein: The deep anaerobic reactor (3) has a liquid inlet, a biogas outlet, a liquid outlet and a liquid return port. An aeration component (41) is arranged inside the aerobic nitrification reactor (4). The liquid outlet of the deep anaerobic reactor (3) leads to the inlet of the aerobic nitrification reactor (4). The liquid inlet of the anaerobic ammonium oxidation reactor (5) communicates with the liquid outlet of the aerobic nitrification reactor (4). The liquid outlet of the anaerobic ammonium oxidation reactor (5) leads to the transfer container (51). The biogas outlet of the deep anaerobic reactor (3) leads to the power generation device.

7. The high-temperature chemical environmental protection anaerobic system according to claim 5, characterized in that: The biogas slurry treatment device further includes a biogas slurry pond (7). The solid-liquid separator (8) has a biogas residue outlet, a biogas slurry outlet and a suction port leading to the biogas slurry pond (7). The concentrated liquid outlet of the anaerobic device (2) is introduced into the biogas slurry pond (7) through a pipeline. The biogas slurry outlet of the solid-liquid separator (8) communicates with the liquid inlet of the deep anaerobic reactor (3).

8. The high-temperature chemical environmental protection anaerobic system according to claim 7, characterized in that: The deep anaerobic reactor (3) is provided with a sludge discharge port. The sludge discharge port of the deep anaerobic reactor (3) and the sludge discharge port of the aerobic nitrification reactor (4) are connected in parallel through a pipeline and then led to the biogas slurry pond (7).

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