CN114031061A - Process for preparing liquid ammonia and struvite from waste ammonia in sludge pyrohydrolysis anaerobic digestion process - Google Patents
Process for preparing liquid ammonia and struvite from waste ammonia in sludge pyrohydrolysis anaerobic digestion process Download PDFInfo
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- CN114031061A CN114031061A CN202111312183.7A CN202111312183A CN114031061A CN 114031061 A CN114031061 A CN 114031061A CN 202111312183 A CN202111312183 A CN 202111312183A CN 114031061 A CN114031061 A CN 114031061A
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 190
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 77
- 230000029087 digestion Effects 0.000 title claims abstract description 52
- 239000010802 sludge Substances 0.000 title claims abstract description 46
- CKMXBZGNNVIXHC-UHFFFAOYSA-L ammonium magnesium phosphate hexahydrate Chemical compound [NH4+].O.O.O.O.O.O.[Mg+2].[O-]P([O-])([O-])=O CKMXBZGNNVIXHC-UHFFFAOYSA-L 0.000 title claims abstract description 27
- 229910052567 struvite Inorganic materials 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims abstract description 24
- 230000008569 process Effects 0.000 title claims abstract description 21
- 239000002699 waste material Substances 0.000 title claims abstract description 19
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 16
- 238000001179 sorption measurement Methods 0.000 claims abstract description 72
- 238000000926 separation method Methods 0.000 claims abstract description 31
- 238000009283 thermal hydrolysis Methods 0.000 claims abstract description 24
- 239000007789 gas Substances 0.000 claims abstract description 22
- 229910000069 nitrogen hydride Inorganic materials 0.000 claims abstract description 17
- 239000003337 fertilizer Substances 0.000 claims abstract description 13
- 239000002912 waste gas Substances 0.000 claims abstract description 10
- 239000000706 filtrate Substances 0.000 claims abstract description 9
- 238000002360 preparation method Methods 0.000 claims abstract description 8
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 7
- 230000023556 desulfurization Effects 0.000 claims abstract description 7
- 238000006243 chemical reaction Methods 0.000 claims abstract description 6
- 238000007599 discharging Methods 0.000 claims abstract description 4
- 238000005192 partition Methods 0.000 claims description 11
- 230000009467 reduction Effects 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 4
- 238000010248 power generation Methods 0.000 claims description 4
- 239000000284 extract Substances 0.000 claims 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 16
- 238000005516 engineering process Methods 0.000 abstract description 7
- 238000003915 air pollution Methods 0.000 abstract description 3
- 238000002485 combustion reaction Methods 0.000 abstract description 3
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 239000012080 ambient air Substances 0.000 abstract description 2
- 239000010865 sewage Substances 0.000 description 7
- 239000003463 adsorbent Substances 0.000 description 5
- 239000003570 air Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 229910000831 Steel Inorganic materials 0.000 description 4
- 239000010959 steel Substances 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 235000015842 Hesperis Nutrition 0.000 description 1
- 235000012633 Iberis amara Nutrition 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 230000000844 anti-bacterial effect Effects 0.000 description 1
- 244000052616 bacterial pathogen Species 0.000 description 1
- 238000009395 breeding Methods 0.000 description 1
- 230000001488 breeding effect Effects 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 210000002421 cell wall Anatomy 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007123 defense Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 239000000618 nitrogen fertilizer Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 244000144977 poultry Species 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 239000003380 propellant Substances 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000010801 sewage sludge Substances 0.000 description 1
- 239000003516 soil conditioner Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 230000001954 sterilising effect Effects 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 210000003462 vein Anatomy 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/26—Phosphates
- C01B25/45—Phosphates containing plural metal, or metal and ammonium
- C01B25/451—Phosphates containing plural metal, or metal and ammonium containing metal and ammonium
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/022—Preparation of aqueous ammonia solutions, i.e. ammonia water
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
- C02F11/04—Anaerobic treatment; Production of methane by such processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
-
- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05B—PHOSPHATIC FERTILISERS
- C05B7/00—Fertilisers based essentially on alkali or ammonium orthophosphates
-
- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05G—MIXTURES OF FERTILISERS COVERED INDIVIDUALLY BY DIFFERENT SUBCLASSES OF CLASS C05; MIXTURES OF ONE OR MORE FERTILISERS WITH MATERIALS NOT HAVING A SPECIFIC FERTILISING ACTIVITY, e.g. PESTICIDES, SOIL-CONDITIONERS, WETTING AGENTS; FERTILISERS CHARACTERISED BY THEIR FORM
- C05G3/00—Mixtures of one or more fertilisers with additives not having a specially fertilising activity
- C05G3/40—Mixtures of one or more fertilisers with additives not having a specially fertilising activity for affecting fertiliser dosage or release rate; for affecting solubility
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/06—Sludge reduction, e.g. by lysis
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Inorganic Chemistry (AREA)
- Pest Control & Pesticides (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
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Abstract
The invention discloses a process for preparing liquid ammonia and struvite from waste ammonia in a sludge pyrohydrolysis anaerobic digestion process, which comprises the following steps: sending the filtrate generated by the anaerobic digestion tank to a struvite preparation device to prepare a struvite slow release fertilizer; gas generated by the anaerobic digestion tank is sent to a first ammonia adsorption separator for ammonia separation and preparation into liquid ammonia, and residual gas is sent to a biogas cabinet after desulfurization treatment; sending the waste gas generated by the thermal hydrolysis device to a second ammonia adsorption separatorSeparating ammonia and preparing into liquid ammonia, and discharging residual gas. The invention realizes the waste NH in the methane by the adsorption separation technology3To avoid NH3The conversion to NOx, either directly or through combustion, into ambient air, causes environmental air pollution.
Description
Technical Field
The invention relates to the technical field of waste gas treatment, in particular to a process for preparing liquid ammonia and struvite from waste ammonia in a sludge pyrohydrolysis anaerobic digestion process.
Background
At present, the annual output of sludge of urban sewage treatment plants in China reaches about 6000 million tons (the water content is about 80%), and the annual output is rapidly increased along with the development of industrialization and the improvement of the living standard of people in China. The sludge contains pathogenic bacteria, heavy metals and other pollutants, and needs to be properly treated before being discharged. The problem of how to economically and continuously realize reduction, harmlessness, stabilization and resource utilization of sewage sludge is not fundamentally solved. The anaerobic digestion is a treatment technology which has low energy consumption and can recycle the sludge, not only can recover the methane and reduce the emission of greenhouse gases, but also can be used as fertilizer, soil conditioner and the like after the sludge is treated by the anaerobic digestion. The marsh gas generated in the anaerobic digestion process contains 60 to 70 percent of methane, and the heat value is about 23000kJ/Nm3The recovered biomass can meet the self capacity requirement of anaerobic digestion, and can also be used for power generation or other energy supply in a plant area.
The high-temperature thermal hydrolysis pretreatment is a common pretreatment technology for anaerobic digestion of sludge, and the technology carries out thermal hydrolysis and flash evaporation treatment on the sludge, so that extracellular polymers and macromolecular organic matters in the sludge are hydrolyzed, cell walls of microorganisms in the sludge are cracked, the organic matter degradation rate and the biogas production rate can be effectively improved, the sanitary performance of the sludge can be improved, and the dehydration rate of the sludge can be reduced. However, a large amount of ammonia (NH) is generated during pyrohydrolysis and anaerobic digestion of sludge3)。NH3Are important precursors for the formation of particulate matter and NOxIf the material is directly discharged, the material will pollute the atmospheric environment. NH in biogas3Most of the NOx is converted to NOx after combustion. NOx contributes to the formation of acid rain and also promotes the formation of atmospheric particulates. Therefore, before the gases produced by thermal hydrolysis are discharged or before the biogas is burnt, the NH is required to be treated3Effective treatment is carried out, otherwise, the environmental air is polluted.
On the other hand, NH3Is a raw material for preparing inorganic nitrogen fertilizer and liquid ammonia. The liquid ammonia is mainly used for producing nitric acid, urea and other chemical fertilizers, is also an important reducing agent for flue gas denitration, and can be used as a raw material of medicines and pesticides. In the defense industry, liquid ammonia is used as a propellant for manufacturing rockets and missiles. Since liquid ammonia is converted to NH after gasification3It is a commonly used "refrigerant" that absorbs a large amount of heat. In addition, the liquid ammonia has a certain bactericidal effect and is used for sterilization, cooling and refrigeration in the poultry breeding industry. If the waste NH generated in the anaerobic digestion process of the sludge can be treated3Effective recovery, not only can avoid NH generated in the process3Resulting in air pollution and also realizes waste NH3And (5) recycling. Except that a large amount of NH is generated in the process of sludge pyrohydrolysis and anaerobic digestion3The filtrate produced during anaerobic digestion also contains a high concentration of NH4 +The method can be used for preparing the struvite slow release fertilizer and is a potential resource.
At present, waste NH generated by the thermal hydrolysis and anaerobic digestion of sludge is lacked3(including thermal hydrolysis waste gas, marsh gas, anaerobic digestion filtrate) recovery technology. The technology is favorable for realizing the harmless and recycling of sludge pyrohydrolysis anaerobic digestion biogas, waste gas generated in the pyrohydrolysis process and anaerobic digestion filtrate, and is an important technical scheme from town sewage plants to the deepening of vein industry. Therefore, it is highly desirable to establish a process for the pyrohydrolysis anaerobic digestion of sludge with waste NH3A device and a process for preparing liquid ammonia and struvite.
Disclosure of Invention
The invention aims to provide a process for preparing liquid ammonia and struvite from waste ammonia in a sludge pyrohydrolysis anaerobic digestion process of a municipal sewage plant, so as to overcome the defects in the prior art.
In order to achieve the above purpose, the invention provides the following technical scheme: a process for preparing liquid ammonia and struvite from waste ammonia in a sludge pyrohydrolysis anaerobic digestion process comprises the following steps: the sludge enters an anaerobic digestion tank after undergoing a thermal hydrolysis reaction by a thermal hydrolysis device, and enters a sludge dewatering workshop after undergoing an anaerobic digestion treatment to be used as a sludge fertilizer after undergoing a dewatering treatment; the process comprises the following steps:
sending the filtrate generated by the anaerobic digestion tank to a struvite preparation device to prepare a struvite slow release fertilizer;
gas generated by the anaerobic digestion tank is sent to a first ammonia adsorption separator for ammonia separation and preparation into liquid ammonia, and residual gas is sent to a biogas cabinet after desulfurization treatment;
and sending the waste gas generated by the thermal hydrolysis device to a second ammonia adsorption separator for ammonia separation and preparing into liquid ammonia, and discharging the residual gas.
Preferably, the biogas tank is connected with a thermal power plant, and the biogas subjected to desulfurization treatment is sent to the thermal power plant for power generation.
Preferably, the electric energy generated by the thermal power plant supplies power to the thermal hydrolysis device, the anaerobic digestion tank, the first ammonia adsorption separator and the second ammonia adsorption separator.
Preferably, a circulation type heat exchange unit is provided between the first ammonia adsorption separator, the second ammonia adsorption separator and the thermal hydrolysis device, and the heat energy of the thermal hydrolysis device is transferred to the first ammonia adsorption separator and the second ammonia adsorption separator through the heat exchange unit.
Preferably, the first ammonia adsorption separator and the second ammonia adsorption separator respectively comprise an adsorption separation layer and a vacuum layer positioned above the adsorption separation layer, and a partition plate capable of being opened or isolated is arranged between the adsorption separation layer and the vacuum layer; the vacuum layer is connected with a pressurizing device and a depressurizing device.
Preferably, after the ammonia concentration in the first ammonia adsorption separator or the second ammonia adsorption separator reaches a set concentration, the gas inlet and the gas outlet of the corresponding ammonia adsorption separator are closed, and the pressure reduction device is used for reducing the pressure in the vacuum layerPumping air, and simultaneously heating the corresponding ammonia adsorption separator through a heat exchange unit; after the vacuum layer is vacuumized, the partition plate is opened to adsorb NH in the separation layer3Releasing to a vacuum layer; to-be-vacuum layer NH3The concentration does not rise any more, and the partition plate is closed; then pressurizing the vacuum layer by a pressurizing device to enable NH3Liquid ammonia is formed and collected.
Compared with the prior art, the invention has the advantages that:
(1) the invention realizes the waste NH in the methane by the adsorption separation technology3To avoid NH3The conversion to NOx, either directly or through combustion, into ambient air, causes environmental air pollution.
(2) The invention leads high concentration NH in the filtrate4 +Used for preparing the struvite slow release fertilizer, not only realizes NH4 +The recycling of the waste water is realized.
(3) The invention fully utilizes the waste heat generated in the sludge pyrohydrolysis process, is used for desorption regeneration of the adsorbent and saves energy.
(4)NH3The energy consumption for preparing liquid ammonia after adsorption and separation and preparing struvite from anaerobic digestion solution is derived from energy for generating electricity by using biogas generated by anaerobic digestion of urban sewage treatment plants, and no additional energy is needed.
Drawings
Fig. 1 is a flow chart of the technical solution of the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further specifically described below by way of embodiments in combination with the accompanying drawings.
Example (b): referring to fig. 1, the sludge is subjected to a thermal hydrolysis reaction in a thermal hydrolysis apparatus and then enters an anaerobic digestion tank connected to the thermal hydrolysis apparatus for anaerobic digestion treatment. The anaerobic digestion tank is connected with a sludge dewatering workshop through a sludge pipeline and is used for conveying sludge to the sludge dewatering workshop for dewatering treatment so as to be used as sludge fertilizer; the anaerobic digestion tank is connected with a struvite preparation device through a filtrate pipeline and is used for producing a struvite slow release fertilizer.
In the structure, the anaerobic digestion tank is connected with a first ammonia adsorption separator through a biogas pipeline and used for adsorbing NH in biogas mixed gas generated by the anaerobic digestion tank3And carrying out adsorption separation, preparing liquid nitrogen, conveying the residual gas to a desulfurizing tower connected with the first ammonia adsorption separator for desulfurization treatment, conveying the residual gas to a biogas cabinet, then entering a thermal power plant in a sewage treatment plant for power generation, and generating electric energy which can be used for generating power for electric energy equipment such as a thermal hydrolysis device, an anaerobic digestion tank, pressure reduction and pressurization of ammonia adsorption separation and the like.
The pyrohydrolysis device is connected with a second ammonia adsorption separator through a waste gas pipeline to adsorb NH in waste gas generated by the pyrohydrolysis device3And (4) performing adsorption separation, preparing liquid nitrogen, and reasonably discharging residual waste gas.
The first ammonia adsorption separator and the second ammonia adsorption separator have the same structure and respectively comprise an adsorption separation layer and a vacuum layer positioned above the adsorption separation layer, a partition plate is arranged between the adsorption separation layer and the vacuum layer, and the adsorption separation layer and the vacuum layer can be communicated or isolated by opening or closing the partition plate; the vacuum layer is connected with a pressurizing device and a depressurizing device which are respectively used for pressurizing or vacuumizing the vacuum layer.
In this example, the adsorption separation layer of the first and second ammonia adsorption separators contains NH3An adsorbent capable of adsorbing NH contained in the gas when the gas passes through3Adsorbing to separate it from other parts of the gas, and maintaining the NH at a certain temperature and reducing the pressure3Releasing the liquid ammonia, pressurizing the liquid ammonia to form liquid ammonia, and collecting the liquid ammonia. During the collection, the baffle can rotate 15 jiaos automatically to set up the honeycomb duct on the baffle, the liquid ammonia steel bottle is connected to the honeycomb duct, makes liquid ammonia flow in the liquid ammonia steel bottle through the honeycomb duct under pressure and the action of gravity through the slope of baffle.
In this embodiment, a circulating heat exchange unit is disposed between the first ammonia adsorption separator, the second ammonia adsorption separator and the thermal hydrolysis device, and the heat energy of the thermal hydrolysis device is transferred to the first ammonia adsorption separation unit through the heat exchange unitA second ammonia adsorption separator, thereby providing the ammonia adsorption separator with NH3The desired temperature at release. The medium of the heat exchange unit may be recycled water of a sewage treatment plant.
The specific structures and principles of the devices used in this embodiment are the prior art, and therefore, details of the parts that are not relevant to the protection content of the present invention are not described herein.
A process for preparing liquid ammonia and struvite from waste ammonia in a sludge pyrohydrolysis anaerobic digestion process comprises the following steps:
(1) the sludge enters an anaerobic digestion tank after being subjected to a thermal hydrolysis reaction by a thermal hydrolysis device, and enters a sludge dewatering workshop after being subjected to anaerobic digestion treatment, and the sludge is used as a sludge fertilizer after being subjected to dewatering treatment.
(2) And (3) enabling filtrate generated by anaerobic digestion to enter a struvite preparation device to produce and prepare the struvite slow release fertilizer.
(3) The marsh gas generated in the anaerobic digestion process enters a first ammonia adsorption separator, the adsorption separation layer and the vacuum layer of the first ammonia adsorption separator are separated by a partition plate, and the marsh gas is put with NH3And the adsorbent enters a desulfurizing tower for desulfurization after being adsorbed by the adsorbent.
(4) The desulfurized biogas enters a biogas cabinet to generate electricity in a thermal power plant in a sewage treatment plant, and the generated electric energy is generated by electric energy equipment which is needed to be used, such as a thermal hydrolysis device, an anaerobic digestion tank, pressure reduction and pressurization of ammonia adsorption separation, and the like.
(5) The waste gas generated by pyrohydrolysis enters a second ammonia adsorption separator to react with NH3And carrying out selective recovery.
(6) To-be-ammonia adsorption separator outlet NH3When the concentration reaches the set concentration, the air inlet and the air outlet of the ammonia adsorption separator are closed, the vacuum layer of the ammonia adsorption separator is pumped by the pressure reduction equipment, and meanwhile, the heat energy of the pyrohydrolysis device is transferred to the ammonia adsorption separator through the heat exchange unit to heat the ammonia adsorption separator (to 80 ℃);
(7) after the vacuum layer is vacuumized, opening the ammonia selective adsorption separation layer and the vacuum layer partition plate, decompressing the adsorption separation layer, and at the moment, reducing NH in the adsorbent3Release to true from an adsorptive separation layerEmpty layer, layer to be evacuated NH3The concentration does not rise any more, and the vacuum layer and the partition plate of the adsorption separation layer are closed. The baffle automatically tilts by 15 degrees.
(8) Supercharging equipment pressurizes to 8 atmospheric pressures to the vacuum layer, forms liquid ammonia, opens the honeycomb duct of baffle, and liquid ammonia gets into the liquid ammonia steel bottle under pressure and gravity action, treats all back that get into, closes steel bottle and honeycomb duct, and the baffle resets, opens ammonia adsorption separator's air inlet and gas outlet and continues the operation.
The above embodiments are merely illustrative of the technical ideas and features of the present invention, and the purpose thereof is to enable those skilled in the art to understand the contents of the present invention and implement the present invention, and not to limit the protection scope of the present invention. All equivalent changes and modifications made according to the spirit of the present invention should be covered within the protection scope of the present invention.
Claims (6)
1. A process for preparing liquid ammonia and struvite from waste ammonia in a sludge pyrohydrolysis anaerobic digestion process comprises the following steps: the sludge enters an anaerobic digestion tank after undergoing a thermal hydrolysis reaction by a thermal hydrolysis device, and enters a sludge dewatering workshop after undergoing an anaerobic digestion treatment to be used as a sludge fertilizer after undergoing a dewatering treatment; the method is characterized by comprising the following steps:
sending the filtrate generated by the anaerobic digestion tank to a struvite preparation device to prepare a struvite slow release fertilizer;
gas generated by the anaerobic digestion tank is sent to a first ammonia adsorption separator for ammonia separation and preparation into liquid ammonia, and residual gas is sent to a biogas cabinet after desulfurization treatment;
and sending the waste gas generated by the thermal hydrolysis device to a second ammonia adsorption separator for ammonia separation and preparing into liquid ammonia, and discharging the residual gas.
2. The process for preparing liquid ammonia and struvite from waste ammonia in the sludge pyrohydrolysis anaerobic digestion process according to claim 1, wherein the biogas tank is connected with a thermal power plant, and biogas subjected to desulfurization treatment is sent to the thermal power plant for power generation.
3. The process for preparing liquid ammonia and struvite from waste ammonia generated in the sludge pyrohydrolysis anaerobic digestion process according to claim 2, wherein electric energy generated by the thermal power plant supplies power to the pyrohydrolysis device, the anaerobic digestion tank, the first ammonia adsorption separator and the second ammonia adsorption separator.
4. The process for preparing liquid ammonia and struvite from waste ammonia in the sludge pyrohydrolysis anaerobic digestion process as claimed in claim 1, wherein a circulating heat exchange unit is arranged between the first ammonia adsorption separator, the second ammonia adsorption separator and the pyrohydrolysis device, and heat energy of the pyrohydrolysis device is transferred to the first ammonia adsorption separator and the second ammonia adsorption separator through the heat exchange unit.
5. The process for preparing liquid ammonia and struvite from waste ammonia in the sludge pyrohydrolysis anaerobic digestion process according to claim 4, wherein the first ammonia adsorption separator and the second ammonia adsorption separator respectively comprise an adsorption separation layer and a vacuum layer positioned above the adsorption separation layer, and a partition plate capable of being opened or isolated is arranged between the adsorption separation layer and the vacuum layer; the vacuum layer is connected with a pressurizing device and a depressurizing device.
6. The process for preparing liquid ammonia and struvite from waste ammonia in the sludge pyrohydrolysis anaerobic digestion process according to claim 5, wherein after the ammonia concentration in the first ammonia adsorption separator or the second ammonia adsorption separator reaches a set concentration, the gas inlet and the gas outlet of the corresponding ammonia adsorption separator are closed, the pressure reduction device extracts gas from the vacuum layer, and simultaneously the temperature of the corresponding ammonia adsorption separator is raised through the heat exchange unit; after the vacuum layer is vacuumized, the partition plate is opened to adsorb NH in the separation layer3Releasing to a vacuum layer; to-be-vacuum layer NH3The concentration does not rise any more, and the partition plate is closed; then pressurizing the vacuum layer by a pressurizing device to enable NH3Liquid ammonia is formed and collected.
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| CN106746467A (en) * | 2017-01-25 | 2017-05-31 | 同济大学 | A kind of sludge resource recovery method based on digested sludge hydro-thermal process |
| CN112811789A (en) * | 2021-01-05 | 2021-05-18 | 北京城市排水集团有限责任公司 | Sludge carbonization treatment method based on pyrohydrolysis process |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106746467A (en) * | 2017-01-25 | 2017-05-31 | 同济大学 | A kind of sludge resource recovery method based on digested sludge hydro-thermal process |
| CN112811789A (en) * | 2021-01-05 | 2021-05-18 | 北京城市排水集团有限责任公司 | Sludge carbonization treatment method based on pyrohydrolysis process |
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Application publication date: 20220211 |