CN109231331B - CO removal of sludge digestion biogas slurry2Special deamination device and process - Google Patents
CO removal of sludge digestion biogas slurry2Special deamination device and process Download PDFInfo
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- CN109231331B CN109231331B CN201811097211.6A CN201811097211A CN109231331B CN 109231331 B CN109231331 B CN 109231331B CN 201811097211 A CN201811097211 A CN 201811097211A CN 109231331 B CN109231331 B CN 109231331B
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- 238000006481 deamination reaction Methods 0.000 title claims abstract description 59
- 230000009615 deamination Effects 0.000 title claims abstract description 57
- 239000010802 sludge Substances 0.000 title claims abstract description 48
- 230000029087 digestion Effects 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 26
- 239000002002 slurry Substances 0.000 claims abstract description 125
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 238000005262 decarbonization Methods 0.000 claims abstract description 16
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 claims abstract description 14
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 claims abstract description 14
- 235000012538 ammonium bicarbonate Nutrition 0.000 claims abstract description 14
- 239000001099 ammonium carbonate Substances 0.000 claims abstract description 14
- 238000005086 pumping Methods 0.000 claims abstract description 7
- 238000000926 separation method Methods 0.000 claims abstract description 4
- 238000010521 absorption reaction Methods 0.000 claims description 4
- 239000007789 gas Substances 0.000 abstract description 53
- 229910000069 nitrogen hydride Inorganic materials 0.000 abstract description 27
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 abstract description 16
- 238000004064 recycling Methods 0.000 abstract description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 31
- 229910002092 carbon dioxide Inorganic materials 0.000 description 27
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 22
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 11
- 229910021529 ammonia Inorganic materials 0.000 description 11
- 229910052757 nitrogen Inorganic materials 0.000 description 11
- 238000009283 thermal hydrolysis Methods 0.000 description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 8
- 230000009286 beneficial effect Effects 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 6
- 239000000243 solution Substances 0.000 description 6
- 239000003153 chemical reaction reagent Substances 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 239000003513 alkali Substances 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 238000002425 crystallisation Methods 0.000 description 4
- 230000018044 dehydration Effects 0.000 description 4
- 238000006297 dehydration reaction Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- MHJAJDCZWVHCPF-UHFFFAOYSA-L dimagnesium phosphate Chemical compound [Mg+2].OP([O-])([O-])=O MHJAJDCZWVHCPF-UHFFFAOYSA-L 0.000 description 3
- 229910000395 dimagnesium phosphate Inorganic materials 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000005273 aeration Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 238000004332 deodorization Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 1
- -1 carbonic acid hinge Chemical class 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000003306 harvesting Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000012163 sequencing technique Methods 0.000 description 1
- 239000010801 sewage sludge Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
- Treatment Of Sludge (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses sludge digestionCO removal of biogas slurry2The special equipment and process for deaminizing includes removing CO2Device, deamination device and decarbonization tower, and removing CO2The device is connected with the deamination device through a decarbonization tower; performing solid-liquid separation on the anaerobic digestion biogas slurry to obtain sludge digestion biogas slurry and biogas residues, performing pyrohydrolysis on the biogas residues to generate pyrohydrolysis pressure-release gas, and removing CO from the sludge digestion biogas slurry2Removal of CO in the plant2Entering a deamination device to remove NH3(ii) a CO after removal2And NH3Respectively pumping out the ammonium bicarbonate by a vacuum pump, and then reacting the ammonium bicarbonate in a decarbonizing tower to generate ammonium bicarbonate; the special device and the process are used for treating CO in biogas slurry2Carrying out green harmless removal with ammonia nitrogen and simultaneously realizing CO2And recycling of ammonia nitrogen.
Description
Technical Field
The invention belongs to the technical field of sewage sludge treatment, and particularly relates to CO removal of sludge digestion biogas slurry2A special deamination device and a process.
Background
With the development of urbanization and sewage treatment in China, the sludge yield reaches 4300 ten thousand tons per year (calculated by water content of 80%), 40% of nitrogen elements in sewage are transferred to sludge, and therefore the sludge contains abundant nitrogen elements and has great resource utilization value. The anaerobic digestion treatment of the sludge converts carbon into methane for recycling, while nitrogen exists in the biogas slurry in the form of ammonia nitrogen, and if a large amount of ammonia nitrogen in the biogas slurry is not effectively removed or recycled, the emission reduction target of sewage treatment is greatly reduced. In addition, biogas slurry mainly comes from the sludge digestion dehydration process, and a large amount of dehydration agents are required to be added in the traditional anaerobic sludge digestion dehydration process. The thermal hydrolysis technology is developed for realizing sludge high-dry dehydration at the earliest time, and thermal hydrolysis is also used for dehydrating digested sludge recently to realize non-chemical high-dry dehydrationDewatering and improving the anaerobic digestion performance. Most of CO in the biogas residue can be generated in the thermal hydrolysis process2And ammonia nitrogen is released in the pressure-release steam, and finally the high-COD low-ammonia nitrogen pyrohydrolysis liquid flows back again for anaerobic digestion. Most of nitrogen elements in the sludge enter dehydrated biogas slurry and thermal hydrolysis pressure-release steam, and if the nitrogen elements are randomly discharged, secondary pollution is caused, and a large amount of nitrogen resources are wasted. The nitrogen element in the biogas slurry is reasonably and efficiently recycled, considerable economic benefit and obvious environmental benefit are generated, and the method has important significance on the sustainable development of China. The traditional biological treatment of the high ammonia nitrogen biogas slurry needs to consume a large amount of carbon sources and energy, and the traditional air stripping treatment has large alkali addition amount and is easy to cause air pollution. Therefore, how to realize the high-efficiency recovery of nitrogen resources in the dehydrated biogas slurry and the thermal hydrolysis pressure-release steam is a problem which needs to be solved urgently. Considering the whole chain of anaerobic sludge digestion, if thermal hydrolysis and biogas slurry deamination can be combined, the energy consumption and material consumption of the system can be effectively reduced.
At present, the existing ammonia removal process comprises air stripping, ammonia distillation, membrane deamination and the like, and the basic principle is that alkali or lime is added to adjust the pH value of liquid to be more than 11 so that ammonia nitrogen is changed into NH3The form exists. The patent (publication number is CN106315726A) application discloses a combined deamination system of natural pond liquid decarbonization, preheats raw material natural pond liquid and gets into the decarbonization device, and raw material natural pond liquid after the decarbonization gets into the deamination device, and ammonia is taken out by the vapor in the deamination device after, gets into ammonia water storage tank through the condenser cooling and retrieves ammonia, nevertheless does not realize CO2Is not beneficial to CO recycling2Emission reduction; and an additional heat source is required, so that the heat energy consumption cost is high.
The patent application (publication number is CN103613107A) discloses a biogas slurry deamination and ammonia recovery method, wherein a vacuum pump is used for pumping a deamination device to a vacuum state, and a solid filler is filled in the deamination device; the ammonia gas in the deamination device is blown into the sulfuric acid solution by introducing air to obtain the ammonium sulfate solution, the pH value of the biogas slurry is adjusted to be more than 9 by adding the calcium hydroxide solution, and NH is absorbed by a large amount of sulfuric acid reagent3The production cost is too high, and the sulfuric acid solution can cause harm to the environment. Patent application(publication No. CN203683105U) discloses a biogas slurry deamination and ammonia recovery device, which comprises a plurality of ammonia deamination and absorption devices connected in series and is connected with a vacuum pump to realize ammonia recovery, but does not consider that a large amount of CO exists in the biogas slurry2With HCO3 -The pH value of the biogas slurry is low, and the NH is not beneficial4 +The removal is efficient. And ammonia gas is absorbed by virtue of multistage alkali liquor in series connection, the process is complex, a large amount of chemical reagents are consumed, and the cost is high. The patent (publication number CN204251370U) discloses a deamination process and equipment for alcohol biogas slurry, wherein preheated alcohol biogas slurry is heated, raw steam and steam provided by a reboiler are used for heating the heated alcohol biogas slurry for deamination, and ammonia is absorbed by ammonia-carrying gas phase through dilute sulfuric acid; washing with sodium hydroxide gas washing device to absorb carbon dioxide; but does not take into account CO2Solubility in water less than NH3When deamination is carried out in a vacuum environment, a large amount of CO is generated2The discharge of the intake air, the sodium hydroxide scrubber does not function and requires the consumption of large amounts of chemical reagents, which results in the production of large amounts of wastewater. From the aspects of environmental protection and resource recovery, the process has no requirement of green production and does not realize CO2Emission reduction and higher production cost.
The patent application (publication No. CN105236668A) discloses a biogas slurry pretreatment method for biological deamination assisted by magnesium hydrogen phosphate, wherein corresponding equivalent magnesium hydrogen phosphate powder is added, the pH value is adjusted to 9.5 by sodium hydroxide, the reaction is carried out for 12-36h, and a proper amount of magnesium hydrogen phosphate absorbs free ammonia in biogas slurry to reduce the content of the free ammonia in the biogas slurry. The method needs to consume a large amount of chemical reagents, has high production cost and excessively long reaction time, and is not beneficial to industrial continuous production. Similarly, the patent application (publication No. CN102030431A) also has the same problem. The patent (CN206934810U) discloses a natural pond liquid waste water and marsh gas tail gas integrated processing device, has reduced the boiling point of waste water under the negative pressure condition, makes the ammonia nitrogen volatilize more easily, through V type injection apparatus board analytical equipment, strengthens the decomposition rate of weak acid weak base salt such as carbonic acid hinge, bicarbonate hinge, need not plus alkali lye, provides the advantage for the deamination of deamination device, and the ammonia nitrogen clearance can reach more than 80%, and recycle tail gas carbon source obtains the ammonium bicarbonate crystallization. However, the patent has complex process, various devices and huge one-time investment cost of the devices, and is not beneficial to large-scale popularization and utilization. Similarly, the patent application of CN107021600A has the same problem.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provide CO removal of sludge digestion biogas slurry2Deamination device and process for CO in biogas slurry2Carrying out green harmless removal with ammonia nitrogen and simultaneously realizing CO2And recycling of ammonia nitrogen.
In order to achieve the purpose, the invention adopts the technical scheme that:
in a first aspect, CO removal of sludge digestion biogas slurry2Special arrangements for deamination, including CO removal2Device, deamination device and decarbonation tower, and the decarbonation2The device is connected with the deamination device through the decarbonization tower; wherein,
the CO removal2The device is of a horizontal cylinder structure, a plurality of circular turnplates are uniformly distributed in the device, a first biogas slurry inflow port and CO connected with a first vacuum pump are arranged at the top of the device2The bottom of the gas outlet is provided with a first gas inlet pipeline, a gas channel with a plurality of gas holes uniformly distributed and a first biogas slurry outlet;
the deamination device comprises a second biogas slurry inflow port positioned above the side part and NH positioned at the top and connected with a second vacuum pump3The second air inlet pipeline and the second biogas slurry outlet are positioned at the bottom of the discharge port;
and the CO removal2The first biogas slurry outlet of the device is communicated with the second biogas slurry inlet of the deamination device.
Preferably, the CO removal is carried out2Plant CO2Gas outlet and the deamination device NH3The discharge ports are connected through the decarbonization tower.
Preferably, the CO removal is carried out2The apparatus also includes a mechanical motor.
Preferably, the gas passage is connected to the first gas inlet pipe through a control valve.
Preferably, a tail gas absorption device is arranged at the top of the decarbonization tower.
Second aspect, by the above CO removal2Special deamination device for removing CO from sludge digestion biogas slurry2The deammoniation process includes solid-liquid separation of anaerobic digested marsh liquid to obtain sludge digested marsh liquid and marsh dregs, thermal hydrolysis of marsh dregs to produce pressure releasing gas, and CO elimination of sludge digested marsh liquid2The deamination comprises the following steps:
firstly pumping sludge digestion biogas slurry into the CO removal system2In the device, CO is removed in a high-temperature vacuum environment2To obtain CO removal2Biogas slurry, said CO removal2Biogas slurry enters a deamination device to remove NH3(ii) a Wherein the CO removal is performed2The vacuum degree in the device is-0.08 MPa, and the temperature of the sludge digestion biogas slurry is 50 ℃; the vacuum degree in the deamination device is 0.07-0.08 MPa, and CO is removed2The biogas slurry temperature is 70-80 ℃;
(ii) CO after said removal2And NH3And respectively pumping the ammonium bicarbonate out by a first vacuum pump and a second vacuum pump, and then feeding the ammonium bicarbonate into the decarbonizing tower to react to generate the ammonium bicarbonate.
In some preferred embodiments, the CO removal is performed2The device is of a horizontal cylinder structure, and the liquid level of the sludge digestion biogas slurry does not exceed the CO removal2The height of the device is 1/3-1/2, which can increase CO2The volatile area of the sludge digestion biogas slurry is increased, and the sludge digestion biogas slurry treatment capacity in unit time is increased. CO in sludge digestion biogas slurry2And NH3Respectively with HCO3 -、NH4 +In the form of CO2Solubility in water less than NH3With CO removal before deamination2Improve the pH value of the biogas slurry and is beneficial to NH3And (4) removing and recycling.
In some preferred embodiments, the first gas inlet pipeline and the second gas inlet pipeline convey gas which are pressure-release gas generated in the process of pyrohydrolysis of the biogas residues and contain a large amount of NH3In the CO removal2The sludge digestion biogas slurry in the device is dissolved and absorbed, so that the deodorization of the pyrohydrolysis pressure-release gas and the utilization of nitrogen elements are realized;in some preferred embodiments, the pressure-release gas is used as a heat source, and the heat carried by the pressure-release gas enters the sludge digestion biogas slurry to maintain the temperature of the biogas slurry, so that energy is effectively saved.
In some preferred embodiments, the CO removal is performed2The device is internally provided with a plurality of circular turntables which rotate at a speed of 50-60 r/min, and biogas slurry is stirred through the circular turntables to indirectly increase CO2Increase of CO content in biogas slurry2And (4) volatilization efficiency.
In some preferred embodiments, the CO removal is performed2The vacuum degree in the device is-0.08 MPa, the biogas slurry temperature is 50 ℃, and CO is added2Solubility in water is much less than NH3CO, especially in a vacuum environment and at elevated temperatures2The solubility in water is further reduced, which is favorable for CO2And (4) removing.
In some preferred embodiments, the vacuum CO removal2The bottom of the device is provided with a gas pipeline, a plurality of air holes are distributed on the pipeline, and the thermal hydrolysis pressure-release gas flows in the pipeline, so that the contact area of the pressure-release gas and the biogas slurry is increased, and NH in the pressure-release gas is promoted3Dissolving in biogas slurry. Meanwhile, the pressure-release gas jetted from the air holes has an aeration effect on the biogas slurry, so that the flow of the biogas slurry and CO are promoted2And (6) volatilizing.
In some preferred embodiments, the CO removal is performed2CO removal from plant exhaust2The pH value of the biogas slurry is more than 9, so that ammonia nitrogen is in the form of NH3Form exists and is removed, and CO is removed by controlling biogas slurry2The temperature and the residence time in the device are adjusted to remove CO2The amount of the biogas slurry reaches the aim of controlling the pH value of the biogas slurry.
In some preferred embodiments, the CO is achieved in step (ii) by low temperature crystallization2And NH3The joint collection and utilization of. In some preferred embodiments, step (ii) is carried out by introducing air and using CO in the air2So as to balance the reaction and fully react to obtain the ammonium bicarbonate.
Compared with the prior art, the invention has the beneficial effects that:
(1) CO removal in the present invention2The heat source of the special deamination device is provided by pressure-release gas generated by pyrohydrolysis of the biogas residues, ammonia gas and heat in the pressure-release gas are subjected to pollution-free treatment and efficient recycling, the energy consumption cost of the whole system is reduced, and the special deamination device is environment-friendly.
(2) CO removal in the present invention2The special deamination device respectively introduces negative pressure environment to promote CO2And NH3The mass transfer from the liquid phase to the gas phase realizes the fixation of the carbon element and the nitrogen element under the condition of no need of adding chemical reagents, and meets the requirement of green clean production.
Drawings
FIG. 1 shows CO removal of sludge digestion biogas slurry2The structure diagram of the special deamination device and the process flow schematic diagram;
FIG. 2 shows CO removal2The structure of the device is shown schematically;
FIG. 3 shows NH removal3The structure of the device is shown schematically;
in the figure, 1 is a mechanical motor, and 2 is CO removal2The device comprises a first biogas slurry inlet and a second biogas slurry inlet which are respectively arranged at 3 and 17, a circular turntable 4, a first vacuum pump and a second vacuum pump which are respectively arranged at 5 and 14, and CO 62The discharge ports 7 and 16 are respectively a first air inlet pipeline and a second air inlet pipeline, 8 is a control valve, 9 is a gas channel, 10 is an air hole, 11 and 13 are respectively a first biogas slurry discharge port and a second biogas slurry discharge port, 12 is NH removal3Device, 15 is NH3And (7) discharging the air.
Detailed Description
To better illustrate the objects, aspects and advantages of the present invention, the present invention will be further described with reference to the following detailed description and accompanying drawings.
Referring to the attached figures 1-3, CO removal of sludge digestion biogas slurry2Special arrangements for deamination, including CO removal2Device 2, deamination device 12 and decarbonization tower, and removing CO2Device 2 and deamination device 12 are connected via a decarbonization tower. Wherein CO is removed2The device 2 is of a horizontal cylinder structure, a plurality of circular turntables 4 are uniformly distributed in the device, a first biogas slurry inflow port 3 and CO connected with a first vacuum pump 5 are arranged at the top of the device2An air outlet 6, a first air inlet pipeline 7 arranged at the bottom and uniformly distributedA gas channel 9 with a plurality of air holes 10 and a first biogas slurry outlet 11. The deamination device 12 comprises a second biogas slurry inflow port 13 positioned above the side part and NH positioned at the top part and connected with a second vacuum pump 143 A discharge port 15, a second air inlet pipeline 16 and a second biogas slurry discharge port 17 which are positioned at the bottom and are used for removing CO2The first biogas slurry outlet 11 of the device 2 is communicated with the second biogas slurry inlet 13 of the deamination device 12. CO removal2Plant 2CO2Gas outlet 6 and deamination device 12NH3The discharge port 15 is connected through a decarbonization tower for removing CO2The device 2 also comprises a mechanical motor 1, a gas channel 9 is connected with the first gas inlet pipeline 7 through a control valve 8, and the top of the decarburization tower is provided with a tail gas absorption device.
With reference to FIG. 1, CO removal is carried out by2Special deamination device for removing CO from sludge digestion biogas slurry2Performing a deamination process, performing solid-liquid separation on anaerobic digestion biogas slurry to obtain sludge digestion biogas slurry and biogas residues, and performing pyrohydrolysis on the biogas residues to generate pyrohydrolysis pressure-release gas; sludge digestion biogas slurry is pumped into the first step for removing CO2In the device 2, CO is removed in a high-temperature vacuum environment2To obtain CO removal2Biogas slurry CO removal2The biogas slurry enters a deamination device 12 to remove NH3And CO is removed2The vacuum degree in the device 2 is-0.08 MPa, the temperature of the sludge digestion biogas slurry is 50 ℃, the vacuum degree in the deamination device 12 is 0.07-0.08 MPa, and CO is removed2The biogas slurry temperature is 70-80 ℃, and the removed CO2And NH3Pumped out by a first vacuum pump 5 and a second vacuum pump 14 respectively and then enters a decarbonization tower to react to generate ammonium bicarbonate.
In a preferred embodiment, CO is removed2The device 2 is of a horizontal cylinder structure, and the liquid level of the sludge digestion biogas slurry does not exceed the CO removal2The height of the device 2 is 1/3-1/2, which can increase CO2The volatile area of the sludge digestion biogas slurry is increased, and the sludge digestion biogas slurry treatment capacity in unit time is increased. CO in sludge digestion biogas slurry2And NH3Respectively with HCO3 -、NH4 +In the form of CO2Solubility in water less than NH3Before deamination, CO removal is carried out2Improve the pH value of the biogas slurry and is beneficial to NH3Is removed back toAnd (6) harvesting.
In another preferred example, the gas conveyed by the first gas inlet pipeline 7 and the second gas inlet pipeline 16 is the pressure-release gas generated in the process of pyrohydrolysis of the biogas residues, and contains a large amount of NH3In the removal of CO2The device 2 is dissolved and absorbed in the sludge digestion biogas slurry to realize deodorization of thermal hydrolysis pressure release gas and utilization of nitrogen elements, the pressure release gas is used as a heat source, and heat carried by the pressure release gas enters the sludge digestion biogas slurry to maintain the temperature of the biogas slurry, so that energy is effectively saved.
In another preferred embodiment, CO is removed2Device 2 is inside to be set up evenly distributed and has a plurality of circular carousel 4, and the rotational speed of circular carousel 4 is 50 ~ 60r/min, stirs natural pond liquid through a plurality of circular carousels 4, increases CO indirectly2Increase of CO content in biogas slurry2And (4) volatilization efficiency. CO removal2The vacuum degree in the device 2 is-0.08 MPa, the biogas slurry temperature is 50 ℃, and CO is added2Solubility in water is much less than NH3CO, especially in a vacuum environment and at elevated temperatures2The solubility in water is further reduced, which is favorable for CO2And (4) removing.
In another preferred embodiment, vacuum CO removal2The bottom of the device 2 is provided with a gas pipeline 9, a plurality of air holes 10 are distributed on the pipeline, the thermal hydrolysis pressure-release gas flows in the pipeline, the contact area of the pressure-release gas and the biogas slurry is increased, and NH in the pressure-release gas is promoted3Dissolved in the biogas slurry, and the pressure-release gas ejected from the air holes 10 has an aeration effect on the biogas slurry, so that the flow of the biogas slurry and CO are promoted2And (6) volatilizing. CO removal2CO removal from plant 22The pH value of the biogas slurry is more than 9, so that ammonia nitrogen is in the form of NH3Form exists and is removed, and CO is removed by controlling biogas slurry2The temperature and the residence time in the device 2 are adjusted to remove CO2The amount of the biogas slurry reaches the aim of controlling the pH value of the biogas slurry. CO realization by low temperature crystallization2And NH3Can also be introduced into the air to utilize CO in the air2So as to balance the reaction and fully react to obtain the ammonium bicarbonate. CO removal in the production process2CO of plant 22The removal efficiency is more than 80 percent, and NH is removed3NH of plant 123The removal efficiency is more than 80%.
Examples
Feeding the high ammonia nitrogen backflow biogas slurry into CO removal2In the device 2, the liquid level of the biogas slurry is subjected to CO removal2At 1/3 of the height of the device 2, the reserved space can improve CO2The volatilization area of (c). Starting the vacuum pump 5 to remove CO2The vacuum degree in the device 2 is pumped to-0.08 MPa, then the control valve 8 is opened to introduce pressure-release gas generated in the sludge pyrohydrolysis process, a large amount of ammonia gas contained in the pyrohydrolyzed pressure-release gas can be dissolved, absorbed and recycled by the biogas slurry, and heat carried by the pressure-release gas enters the biogas slurry as a heat source to heat the biogas slurry. Starting the circular turntable 4 to stir the biogas slurry, and after the retention time is 10-20 minutes, CO2And after the removal operation is finished, the pH value of the biogas slurry is about 9.5.
CO removal2Biogas slurry discharge port 11 and NH removal of device 23The biogas slurry inlet 13 of the device 12 is connected to remove CO2The biogas slurry enters into NH removal3Device 12 proceeds to start NH removal3The vacuum pump 14 of the device 12 pumps the ammonia gas to-0.07 MPa for ammonia gas removal. CO removal2And NH3The gas is pumped out by vacuum pumps 5 and 14, CO is removed2Device 2 and NH removal3The exhaust pipes 6, 15 of the device 12 are respectively connected with a decarbonization tower, CO2And NH3And pumping the gas into a decarbonizing tower to prepare ammonium bicarbonate. Air can be introduced in the crystallization process, and CO in the air can be utilized2To meet the requirement of preparing ammonium bicarbonate.
In order to meet the actual production requirement, the special device can be set to be in sequencing batch treatment and parallel treatment, the treatment object is not limited to sludge anaerobic digestion biogas slurry, and the special device is suitable for ammonia nitrogen removal treatment of the backflow biogas slurry based on the problem of overhigh ammonia nitrogen concentration of the backflow biogas slurry in the anaerobic digestion process.
Finally, it should be noted that the above embodiments are only for illustrating the technical solutions of the present invention and not for limiting, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that modifications or equivalent substitutions may be made on the technical solutions of the present invention without departing from the spirit and scope of the technical solutions of the present invention, which should be covered by the claims of the present invention.
Claims (2)
1. CO removal of sludge digestion biogas slurry2The special deamination device is characterized by comprising CO removal2Device, deamination device and decarbonation tower, the decarbonation2The device is connected with the deamination device through the decarbonization tower, a tail gas absorption device is arranged at the top of the decarbonization tower, anaerobic digestion biogas slurry is subjected to solid-liquid separation to obtain sludge digestion biogas slurry and biogas residues, and the biogas residues are subjected to pyrohydrolysis to generate pyrohydrolysis pressure-release gas;
the CO removal2The device is of a horizontal cylinder structure, a plurality of circular turnplates are uniformly distributed in the device, a first biogas slurry inflow port and CO connected with a first vacuum pump are arranged at the top of the device2The bottom of the gas outlet is provided with a first gas inlet pipeline, a gas channel with a plurality of uniformly distributed gas holes and a first biogas slurry outlet, and the gas outlet also comprises a mechanical motor, wherein the gas channel is connected with the first gas inlet pipeline through a control valve;
the deamination device comprises a second biogas slurry inflow port positioned above the side part and NH positioned at the top and connected with a second vacuum pump3The second air inlet pipeline and the second biogas slurry outlet are positioned at the bottom of the discharge port;
the CO removal2The first biogas slurry outlet of the device is communicated with the second biogas slurry inlet of the deamination device, and CO is removed2Plant CO2Gas outlet and the deamination device NH3The discharge ports are connected through the decarbonization tower;
and the gas conveyed by the first gas inlet pipeline and the second gas inlet pipeline is the biogas residue pyrohydrolysis pressure-release gas.
2. CO removal of sludge digestion biogas slurry2A process for removing CO from a sludge-digested biogas slurry according to claim 12The special deamination device is used for removing CO from sludge digestion biogas slurry by the following steps2And (3) deamination treatment:
firstly pumping sludge digestion biogas slurry with the temperature of 50 DEG CThe vacuum degree of the entering is minus 0.08MPa2In the device, the liquid level does not exceed the CO removal2The device has the height of 1/3-1/2, and CO is removed in a high-temperature vacuum environment2The obtained CO is removed at 70-80 deg.C and pH above 92Biogas slurry, said CO removal2The biogas slurry enters a deamination device with the vacuum degree of 0.07-0.08 MPa to remove NH3(ii) a The CO removal2The rotating speed of the circular turntable in the device is 50-60 r/min;
(ii) CO after said removal2And NH3And respectively pumping the ammonium bicarbonate out by a first vacuum pump and a second vacuum pump, introducing air into the decarbonizing tower, and reacting to generate the ammonium bicarbonate.
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| CN113336404A (en) * | 2021-04-29 | 2021-09-03 | 北京城市排水集团有限责任公司 | Resource method for developing thermal hydrolysis sludge carbon source |
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