CN211734136U - Multiphase multistage biomass sludge treatment system combining hydrothermal and anaerobic ammonia oxidation - Google Patents
Multiphase multistage biomass sludge treatment system combining hydrothermal and anaerobic ammonia oxidation Download PDFInfo
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 70
- 239000010802 sludge Substances 0.000 title claims abstract description 56
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 39
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- 239000007788 liquid Substances 0.000 claims abstract description 24
- 238000009283 thermal hydrolysis Methods 0.000 claims abstract description 21
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 20
- 238000004519 manufacturing process Methods 0.000 claims abstract description 18
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- 238000010992 reflux Methods 0.000 claims description 29
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 23
- 229910052757 nitrogen Inorganic materials 0.000 claims description 12
- 239000012528 membrane Substances 0.000 claims description 11
- 239000007789 gas Substances 0.000 claims description 9
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 9
- 229910052799 carbon Inorganic materials 0.000 abstract description 9
- 238000005728 strengthening Methods 0.000 abstract description 6
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- 230000029087 digestion Effects 0.000 description 13
- 230000035484 reaction time Effects 0.000 description 10
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 9
- 241000894006 Bacteria Species 0.000 description 9
- 230000008569 process Effects 0.000 description 9
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 8
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 7
- 238000007599 discharging Methods 0.000 description 7
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- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 4
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- 230000000696 methanogenic effect Effects 0.000 description 4
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- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 238000009825 accumulation Methods 0.000 description 3
- 230000001079 digestive effect Effects 0.000 description 3
- 239000003337 fertilizer Substances 0.000 description 3
- 235000011389 fruit/vegetable juice Nutrition 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
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- 229910002651 NO3 Inorganic materials 0.000 description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
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- PDNNQADNLPRFPG-UHFFFAOYSA-N N.[O] Chemical compound N.[O] PDNNQADNLPRFPG-UHFFFAOYSA-N 0.000 description 1
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 description 1
- IPQVRLSXWJPESU-UHFFFAOYSA-N [N].ON=O Chemical compound [N].ON=O IPQVRLSXWJPESU-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003115 biocidal effect Effects 0.000 description 1
- 230000009615 deamination Effects 0.000 description 1
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- 239000005431 greenhouse gas Substances 0.000 description 1
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- 150000002500 ions Chemical class 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Separation Using Semi-Permeable Membranes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The utility model discloses a multiphase multistage biomass sludge treatment system combining hydrothermal and anaerobic ammonia oxidation, which comprises a thermal hydrolysis reactor, a heat exchanger, a hydrolysis acid production reactor, an anaerobic methane production-denitrogenation reactor, an aerobic reactor and a granular sludge separation enricher; the thermal hydrolysis reactor is communicated with the heat exchanger, the hydrolysis acidogenic reactor is communicated with the anaerobic methanogenesis-denitrogenation reactor, and the anaerobic methanogenesis-denitrogenation reactor is respectively communicated with the heat exchanger and the granular sludge separation enricher; the liquid inlet end of the aerobic reactor is communicated with the heat exchanger, and the liquid outlet end of the aerobic reactor is communicated with the anaerobic methanogenesis-denitrification reactor; the utility model aims to solve the problems of the prior sludge comprehensive treatment and the tail end discharge, and after the sludge is subjected to hydrothermal strengthening hydrolysis, the sludge is subjected to combined anaerobic and ammonia oxidation treatment, the hydrothermal strengthening hydrolysis technology advantage of the sludge is utilized, the self-supply of a carbon source is realized, and the comprehensive productivity and emission reduction are realized.
Description
Technical Field
The utility model belongs to the technical field of sludge recycling and advanced treatment technology and specifically relates to a heterogeneous multistage living beings sludge treatment system of hydrothermal joint anammox, when realizing mud decrement and resourceful treatment, solve its filtrating and discharge the problem.
Background
In recent years, the pretreatment mode of 'hydrothermal/thermal hydrolysis' can greatly improve the fluidity of sludge and improve the anaerobic digestion performance and the dehydration performance of the sludge, so the pretreatment mode is widely accepted and applied, and the sludge hydrothermal/thermal hydrolysis combined anaerobic digestion becomes the mainstream technology of the sludge treatment industry at present.
But after hydrothermal treatment, most of the organic matters in the sludge are dissolved and hydrolyzed, the hydrothermal sludge filtrate contains high-concentration ammonia nitrogen (3000 mg/L) and total nitrogen (3000 4000mg/L), and particularly after conventional anaerobic digestion, the ammonia nitrogen concentration reaches 3000-3500 mg/L, COD is 8000-10000 mg/L, and the C/N ratio is lower. The ammonia nitrogen returns to the sewage treatment system along with the sludge dewatering filter pressing liquid, the nitrogen load is improved by about 10 to 15 percent, and the sewage treatment investment and the operating cost are increased.
If the digestive juice is treated separately, most of organic matters in the digestive juice are nondegradable substances and are difficult to biodegrade.
In the prior art, the object of denitrification treatment of biomass solid waste is to consider various kinds of sewage such as final digestion filtrate, but not to treat sludge; in the prior art, the treatment process of biomass solid waste comprises the steps of firstly treating sludge, carrying out denitrification treatment on wastewater after the sludge is treated, and carrying out step-by-step treatment on the wastewater, wherein the conventional process flow wastes steps, wastes medicaments and increases treatment time.
And the conventional denitrification process is shown as A2the/O process often has the problems of insufficient carbon source, high cost due to the addition of a large amount of inorganic carbon source and poor denitrification effect when used for treating sludge digestive juice, and the low carbon-nitrogen ratio is not favorable for biological denitrification.
SUMMERY OF THE UTILITY MODEL
The utility model discloses an aim at handles the difficult point of dealing with and terminal emission to present mud is synthesized, carry out the hydrothermal reinforcement hydrolysis back with mud, the total (do not carry out solid-liquid separation) carries out joint anaerobism and ammonia oxidation treatment, utilize the hydrothermal reinforcement hydrolysis technology advantage of self, realize the carbon source self-supply, and anaerobic ammonia oxidation treatment is low to the demand of carbon source itself, oxygen consumption is also low, synthesize and realize saving the material and supply with, reduce the waste material and discharge, realize mud sewage synchronous processing simultaneously, and denitrogenation simultaneously handles, practice thrift whole process steps, and the medicament is saved, and the treatment time is shortened.
The scheme is realized as follows:
a multiphase multistage biomass sludge treatment system combining hydrothermal and anaerobic ammonia oxidation comprises a thermal hydrolysis reactor, a heat exchanger, a hydrolysis acid production reactor, an anaerobic methane production-nitrogen removal reactor, an aerobic reactor and a granular sludge separation enricher; the thermal hydrolysis reactor is communicated with the heat exchanger, the hydrolysis acidogenic reactor is communicated with the anaerobic methanogenesis-denitrogenation reactor, and the anaerobic methanogenesis-denitrogenation reactor is respectively communicated with the heat exchanger and the granular sludge separation enricher; the liquid inlet end of the aerobic reactor is communicated with the heat exchanger, and the liquid outlet end of the aerobic reactor is communicated with the anaerobic methanogenesis-denitrification reactor.
Through the comprehensive treatment of the system, the total nitrogen removal rate of the integrated reactor is 86-92%, and the COD removal rate is more than 85%.
Preferably, the anaerobic methanogenesis-denitrogenation reactor comprises a water inlet, a water outlet, a gas outlet, a reflux port and an aerobic water outlet and inlet; the water inlet is communicated with the water outlet end of the hydrolysis acid-production reactor, and the reflux port is communicated with the heat exchanger; the aerobic water outlet and inlet is communicated with an aerobic reactor; the water inlet and the reflux port are positioned at the same side of the front end of the anaerobic methanogenesis-denitrogenation reactor, and the aerobic water outlet and inlet port is positioned at the middle rear end.
The anaerobic methanogenesis-denitrogenation reactor is of a baffle plate type and comprises a plurality of baffling cavities, a membrane reactor is arranged in the baffling cavity close to the water inlet, and the aerobic water outlet and inlet are arranged on the baffling cavity behind the baffling cavity close to the water inlet.
Mixed liquor after hydrolysis acidogenesis reaction enters into the anaerobic methanogenesis-denitrogenation reactor from the water inlet, and the solution reacts with the membrane reactor in the first baffling cavity, and the reaction is as follows: methanogenic reaction, product CH4+CO2Or HCO3 －(ii) a Part of the solution (anaerobic digestion filtrate) after the reaction flows back to the heat exchanger through the reflux port, the temperature of the filtrate is raised in the heat exchanger, and then the short-cut denitrification reaction (NH 4) is carried out++O2＝＝NO2 －+2H++H2O), enriching nitrite bacteria, accumulating NO2 < - >, and removing COD by 30-35%; removing 57% of ammonia nitrogen; generating nitrogen nitrite.
The liquid after denitrification reaction enters a baffling cavity at the rear end of the anaerobic methanogenesis-denitrogenation reactor through an aerobic water inlet and outlet, and the residual solution in the anaerobic methanogenesis-denitrogenation reactor and the residual solution enter the baffling cavity from the aerobic water inlet and outletThe solution of (2) is subjected to denitrification (ammoxidation: NH)4 ++NO2 －＝＝2N2+2H2O), discharging the discharged water; the upper part is a gas collecting area.
Methane is generated in a baffling cavity at the front end of the anaerobic methane-generating and nitrogen-removing reactor, deamination is performed at the rear end, a backflow port is arranged in the baffling cavity close to the front side, so that solution after methanogenesis reaction can flow back to a heat exchanger as much as possible, an aerobic water inlet is arranged in the baffling cavity at the middle rear end, the influence of two reactions can be reduced to the minimum, most cavities between the baffling cavity at the front end and the baffling cavity at the middle rear end are isolated, all methanogenesis reactions and denitrification reactions are opposite, and no influence can be caused.
In the scheme, the treated sludge can be any biomass solid waste such as kitchen waste, food processing waste, garden waste, antibiotic bacteria residue and the like.
The utility model provides a multiphase multistage sludge treatment method combining hydrothermal and anaerobic ammonia oxidation, which is characterized in that: the method comprises the following steps:
1) carrying out thermal hydrolysis reaction on the sludge;
2) heat exchange is carried out between the pyrohydrolysis material and the filtrate;
3) the water heat reinforced hydrolysis material enters a hydrolysis acidification reactor to carry out anaerobic acid production reaction;
4) the hydrolysis acidification material enters an anaerobic methanogenesis-denitrogenation reactor, the front region of the reactor is a membrane reactor for strengthening methanogens, the middle rear part of the reactor is an anaerobic ammonia oxidation baffling reaction region, part of filtrate of anaerobic digestion filtrate flows back for heat exchange and then enters an aerobic reactor, and the rest filtrate and the effluent of the aerobic reactor perform denitrogenation reaction in a baffling plate reaction region;
5) anaerobic digestion filtrate enters an aerobic reactor to carry out short-range denitrification reaction, the temperature of the filtrate is increased by a heat exchanger, and effluent enters a methanogenesis-ammoxidation reactor to carry out denitrification;
6) and (4) carrying out enrichment and reflux outside the reactor on the anaerobic ammonia oxidation bottom sludge in the convection area.
Preferably, in the step 1), the temperature of the hydrothermal treatment is 150-220 ℃, the pressure is 0.48-2.5 Mpa, the reaction time is 30-60 min, solid-liquid mixed slurry is generated, and the TS solid content: 10 to 15 percent.
Preferably, in the step 2), the discharging temperature after heat exchange is 30-50 ℃.
Preferably, in the step 3), the pH value of the fed material is adjusted to be 7-7.3, and the temperature is 30-45 ℃; the reaction is in a sequencing batch mode, the acidity is accumulated to the pH value of 6.5, and the supernatant enters the next reactor; and the bottom mud is discharged out periodically.
Preferably, in the step 4), the anaerobic ammonia oxidation reaction zone: NO2 －－N：NH4 +Controlling the concentration of N to be 1.5-1, a: c is about 2: 1.
preferably, in the step 5), the heat exchange raises the temperature of the filtrate to 30-40 ℃; DO: 0.5-1.0 mg/L, pH above 8, and free ammonia concentration of 1-10 mg/L. Removing 30-35% of COD in the step; removing 57% of ammonia nitrogen; and generating nitrous acid nitrogen.
Preferably, in the step 5), an aeration device is arranged to disperse the nitrite flocs to enhance the mixing strength; the hydraulic retention time is shortened, the sludge age is between the minimum retention time of nitrite bacteria and nitrate bacteria, and the nitrate bacteria are washed and removed to the maximum extent.
The HRT of the nitrosation system is 2-3 h; the anammox system HRT 4-5 h.
In the application, a pump body and a valve can be arranged at the reflux opening for controlling the total amount of flow distribution and reflux, and the reflux amount can be controlled to only reflux into the heat exchanger for subsequent denitrification reaction; or the reflux liquid from the reflux port can be shunted again, one part of the reflux liquid flows back to the hydrolysis acidogenic reactor, the other part of the reflux liquid flows back to the heat exchanger, and the reflux liquid flows back to the hydrolysis acidogenic reactor to ensure that the concentration of positive and negative ions in the anaerobic methanogenic-denitrogenation reactor is approximate to 1: 1, ensuring full and efficient reaction in the anaerobic methanogenesis-denitrogenation reactor.
To sum up, owing to adopted above-mentioned technical scheme, the beneficial effects of the utility model are that:
1. the utility model discloses in carry out the hydrothermal reinforcement hydrolysis back with mud, carry out joint anaerobism and ammoxidation and handle, utilize the hydrothermal reinforcement hydrolysis technology advantage of self, realize the carbon source and supply by oneself, and synthesize productivity, reduce discharging.
2. The utility model discloses in with the total nitrogen clearance of integral type reactor at 86% ~ 92%, COD clearance more than 85%.
3. The utility model provides a methane-denitrogenation reactor is baffle formula anaerobic ammonium oxidation reactor, realizes through the baffling baffle that the front end baffling chamber produces the methane reaction, and well rear end carries out the denitrogenation reaction, makes solution can cushion through baffling board and baffling chamber and slows down, and the time of dwell is longer, makes the reaction fully go on to enable 2 reactions can be relatively independent and swift reaction.
4. The utility model carries out pretreatment on the sludge, namely, carries out hydrothermal treatment on the sludge, thereby facilitating subsequent treatment operation; can realize the high-efficiency and rapid treatment of the biomass waste pollution sources such as sludge, residues and the like.
5. The utility model discloses well adoption backward flow's mode realizes the carbon source self-feeding, has reduced the input of external carbon source, has reduced manufacturing cost.
6. The utility model discloses the usable nitrite of well anaerobic ammonium oxidation bacterium is nitrogen gas as the ammonia nitrogen oxidation of electron acceptor in with the sewage, and whole denitrogenation process only needs to oxidize 50% ammonia nitrogen for nitrite nitrogen, consequently can save 62.5% aeration rate, reduces 50% basicity and consumes, and the denitrogenation process does not need organic carbon source, and surplus sludge production reduces about 90%, and denitrogenation process greenhouse gas emission reduces more than 90%.
Drawings
FIG. 1 is a schematic view of the overall process flow of the present invention;
FIG. 2 is a schematic diagram of the anaerobic methanogenic-denitrogenation reactor of the present invention;
the labels in the figure are: 1. a thermal hydrolysis reactor; 2. a heat exchanger; 3. a hydrolysis acid production reactor; 4. anaerobic methanogenesis-denitrogenation reactor; 5. an aerobic reactor; 6. a granular sludge separation enricher; 41. a water inlet; 42. a water outlet; 43. an air outlet; 44. a return port; 45. an aerobic water outlet and liquid inlet; 46. a baffling cavity; 47. a membrane reactor.
Detailed Description
All of the features disclosed in this specification, or all of the steps in any method or process so disclosed, may be combined in any combination, except combinations of features and/or steps that are mutually exclusive.
Any feature disclosed in this specification (including any accompanying claims, abstract) may be replaced by alternative features serving equivalent or similar purposes, unless expressly stated otherwise. That is, unless expressly stated otherwise, each feature is only an example of a generic series of equivalent or similar features.
In the description of the present invention, it is to be understood that the terms "upper", "lower", "left", "right", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the designated device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.
Furthermore, the terms "first," "second," and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature.
Example 1
As shown in fig. 1 and 2, a multiphase multistage biomass sludge treatment system combining hydrothermal and anaerobic ammonia oxidation comprises a thermal hydrolysis reactor, a heat exchanger, a hydrolysis acid production reactor, an anaerobic methanogenesis-denitrogenation reactor, an aerobic reactor and a granular sludge separation enricher; the thermal hydrolysis reactor is communicated with the heat exchanger, the hydrolysis acidogenic reactor is communicated with the anaerobic methanogenesis-denitrogenation reactor, and the anaerobic methanogenesis-denitrogenation reactor is respectively communicated with the heat exchanger and the granular sludge separation enricher; the liquid inlet end of the aerobic reactor is communicated with the heat exchanger, and the liquid outlet end of the aerobic reactor is communicated with the anaerobic methanogenesis-denitrification reactor.
The anaerobic methanogenesis-denitrogenation reactor comprises a water inlet, a water outlet, a gas outlet, a reflux port and an aerobic water outlet and inlet; the water inlet is communicated with the water outlet end of the hydrolysis acid-production reactor, and the reflux port is communicated with the heat exchanger; the aerobic water outlet and inlet is communicated with an aerobic reactor; the water inlet and the reflux port are positioned at the same side of the front end of the anaerobic methanogenesis-denitrogenation reactor, and the aerobic water outlet and inlet port is positioned at the middle rear end.
The anaerobic methanogenesis-denitrogenation reactor is of a baffle plate type and comprises a plurality of baffling cavities, a membrane reactor is arranged in the baffling cavity close to the water inlet, and the aerobic water outlet and inlet are arranged on the baffling cavity behind the baffling cavity close to the water inlet.
In the embodiment, municipal sludge is used as a treatment source; the sludge is treated as follows:
1) carrying out thermal hydrolysis reaction on incoming sludge, wherein the temperature of the hydrothermal treatment is 220 ℃, the pressure is 2.5Mpa, and the reaction time is 45 min. The TS solid content of the formed solid-liquid mixed slurry is 13%;
2) carrying out heat exchange between the pyrohydrolysis material and the filtrate, wherein the discharging temperature is 50 ℃ after heat exchange;
3) the water heat reinforced hydrolysis material enters a hydrolysis acidification reactor to carry out anaerobic acid production reaction (hydrogen-producing and acetic acid-producing reaction, product CH)3COOH+CO2+3H2) The feed pH was adjusted to 7 and the temperature was controlled at 35 ℃. The reaction was batch-wise, the acidity accumulated to pH 6.5, deemed complete, and the supernatant entered the next reactor. The bottom mud is discharged periodically and can be used for preparing biological fertilizer;
4) the hydrolyzed and acidified materials enter an anaerobic methanogenesis-denitrogenation reactor, and the front area of the reactor is a fixed membrane component for strengthening methanogens (the reaction is: methanogenic reaction, product CH4+CO2(or HCO)3 －) The middle and rear part is an anaerobic ammonia oxidation baffling reaction area, part of filtrate of anaerobic digestion filtrate flows back to exchange heat and then enters an aerobic reactor, and the rest filtrate b and the effluent of the aerobic reactor carry out denitrification reaction (ammonia oxygen) in the baffling plate reaction areaAnd (3) chemical reaction: NH (NH)4 ++NO2 －＝＝2N2+2H2O), discharging effluent; the upper part is a gas collecting area.
An anaerobic ammonia oxidation reaction zone: NO2 －－N：NH4 +-N concentration is controlled at 1.5; a: c is about 2: 1;
the COD removal of the reactor effluent is 92%, the ammonia nitrogen removal is 85%, the nitrite nitrogen removal is 95%, and the total nitrogen removal is 85%;
5) anaerobic digestion filtrate enters an aerobic reactor to carry out short-cut denitrification reaction (NH 4)++O2＝＝NO2 －+2H++H2O), nitrite enriched bacteria, NO 2-accumulation. Heat exchange to raise the temperature of the filtrate, 35 ℃); DO: 0.5mg/L, pH8, free ammonia concentration 5 mg/L;
removing 33% of COD; removing 57% of ammonia nitrogen; generating nitrogen nitrite;
the effluent enters a methane production-ammonia oxidation reactor for denitrification;
6) carrying out enrichment and reflux outside the reactor on the anaerobic ammonia oxidation bottom mud in the baffling area (not shown in the reactor picture)
In the scheme, the HRT reaction time of the nitrifying system is 3 hours; the anaerobic ammonia oxidation reaction time is 4.5 h;
finally, the total nitrogen removal rate of the reactor effluent is 92 percent and the COD removal rate is 85 percent by the system and the treatment method.
Example 2
As shown in fig. 1 and 2, a multiphase multistage biomass sludge treatment system combining hydrothermal and anaerobic ammonia oxidation comprises a thermal hydrolysis reactor, a heat exchanger, a hydrolysis acid production reactor, an anaerobic methanogenesis-denitrogenation reactor, an aerobic reactor and a granular sludge separation enricher; the thermal hydrolysis reactor is communicated with the heat exchanger, the hydrolysis acidogenic reactor is communicated with the anaerobic methanogenesis-denitrogenation reactor, and the anaerobic methanogenesis-denitrogenation reactor is respectively communicated with the heat exchanger and the granular sludge separation enricher; the liquid inlet end of the aerobic reactor is communicated with the heat exchanger, and the liquid outlet end of the aerobic reactor is communicated with the anaerobic methanogenesis-denitrification reactor.
The anaerobic methanogenesis-denitrogenation reactor comprises a water inlet, a water outlet, a gas outlet, a reflux port and an aerobic water outlet and inlet; the water inlet is communicated with the water outlet end of the hydrolysis acid-production reactor, and the reflux port is communicated with the heat exchanger; the aerobic water outlet and inlet is communicated with an aerobic reactor; the water inlet and the reflux port are positioned at the same side of the front end of the anaerobic methanogenesis-denitrogenation reactor, and the aerobic water outlet and inlet port is positioned at the middle rear end.
The anaerobic methanogenesis-denitrogenation reactor is of a baffle plate type and comprises a plurality of baffling cavities, a membrane reactor is arranged in the baffling cavity close to the water inlet, and the aerobic water outlet and inlet are arranged on the baffling cavity behind the baffling cavity close to the water inlet.
In the embodiment, kitchen waste is used as a treatment source; the kitchen garbage is treated as follows:
1) carrying out thermal hydrolysis reaction on incoming sludge, wherein the temperature of the hydrothermal treatment is 150 ℃, the pressure is 0.5Mpa, and the reaction time is 50 min. The TS solid content of the obtained kitchen waste solid-liquid mixed slurry is 13%.
2) The thermal hydrolysis material and the filtrate are subjected to heat exchange, and the discharging temperature is 40 ℃ after the heat exchange.
3) The water heat reinforced hydrolysis material enters a hydrolysis acidification reactor to carry out anaerobic acid production reaction (hydrogen-producing and acetic acid-producing reaction, product CH)3COOH+CO2+3H2) The feed pH was adjusted to 7.1 and the temperature was controlled at 35 ℃. The reaction was batch-wise, the acidity accumulated to pH 6.5, deemed complete, and the supernatant entered the next reactor. The impurities at the bottom are discharged out periodically, and a biological fertilizer can be prepared;
4) the hydrolyzed and acidified materials enter an anaerobic methanogenesis-denitrogenation reactor, and the front area of the reactor is a fixed membrane component for strengthening methanogens (the reaction is: methanogenic reaction, product CH4+CO2(or HCO)3 －) And the middle rear part is an anaerobic ammonia oxidation baffling reaction area, part of filtrate of anaerobic digestion filtrate flows back to exchange heat and then enters an aerobic reactor, and the rest filtrate and the effluent of the aerobic reactor perform denitrification reaction (ammonia oxidation reaction: NH (NH)4 ++NO2 －＝＝2N2+2H2O), discharging effluent; the upper part is a gas collecting area.
An anaerobic ammonia oxidation reaction zone: NO2 －－N：NH4 +-N concentration is controlled at 1; a: c is about 2: 1
The COD removal of the reactor effluent is 91%, the ammonia nitrogen removal is 86%, the nitrite nitrogen removal is 96% and the total nitrogen removal is 86%;
5) anaerobic digestion filtrate enters an aerobic reactor to carry out short-cut denitrification reaction (NH 4)++O2＝＝NO2 －+2H++H2O), nitrite enriched bacteria, NO 2-accumulation. The temperature of the filtrate is increased by 35 ℃ through heat exchange; DO: 0.5mg/L, pH8, free ammonia concentration of 7 mg/L;
the COD removal was 33%; the ammonia nitrogen removal rate is 57%; generating nitrogen nitrite;
the effluent enters a methane production-ammonia oxidation reactor for denitrification;
6) carrying out enrichment and reflux outside the reactor (not shown in the reactor figure) on kitchen garbage subjected to anaerobic ammonia oxidation in the convection area
In the embodiment, the HRT reaction time of the nitrosation system is 3 h; the anaerobic ammonia oxidation reaction time is 4.5 h;
finally, the total nitrogen removal rate of the reactor is 90 percent and the COD removal rate is 88 percent by the system and the treatment method.
Example 3
As shown in fig. 1 and 2, a multiphase multistage biomass sludge treatment system combining hydrothermal and anaerobic ammonia oxidation comprises a thermal hydrolysis reactor, a heat exchanger, a hydrolysis acid production reactor, an anaerobic methanogenesis-denitrogenation reactor, an aerobic reactor and a granular sludge separation enricher; the thermal hydrolysis reactor is communicated with the heat exchanger, the hydrolysis acidogenic reactor is communicated with the anaerobic methanogenesis-denitrogenation reactor, and the anaerobic methanogenesis-denitrogenation reactor is respectively communicated with the heat exchanger and the granular sludge separation enricher; the liquid inlet end of the aerobic reactor is communicated with the heat exchanger, and the liquid outlet end of the aerobic reactor is communicated with the anaerobic methanogenesis-denitrification reactor.
The anaerobic methanogenesis-denitrogenation reactor comprises a water inlet, a water outlet, a gas outlet, a reflux port and an aerobic water outlet and inlet; the water inlet is communicated with the water outlet end of the hydrolysis acid-production reactor, and the reflux port is communicated with the heat exchanger; the aerobic water outlet and inlet is communicated with an aerobic reactor; the water inlet and the reflux port are positioned at the same side of the front end of the anaerobic methanogenesis-denitrogenation reactor, and the aerobic water outlet and inlet port is positioned at the middle rear end.
The anaerobic methanogenesis-denitrogenation reactor is of a baffle plate type and comprises a plurality of baffling cavities, a membrane reactor is arranged in the baffling cavity close to the water inlet, and the aerobic water outlet and inlet are arranged on the baffling cavity behind the baffling cavity close to the water inlet.
In the embodiment, sludge and kitchen waste slurry are used as treatment sources; the mixture was treated as follows:
1) carrying out thermal hydrolysis reaction on the incoming material, wherein the temperature of the hydrothermal treatment is 180 ℃, the pressure is 1Mpa, and the reaction time is 50 min. The TS solid content of the obtained solid-liquid mixed slurry was 14%.
2) The thermal hydrolysis material and the filtrate are subjected to heat exchange, and the discharge temperature is 35 ℃ after the heat exchange.
3) The water heat reinforced hydrolysis material enters a hydrolysis acidification reactor to carry out anaerobic acid production reaction (hydrogen-producing and acetic acid-producing reaction, product CH)3COOH+CO2+3H2) The feed pH was adjusted to 7 and the temperature was controlled at 35 ℃. The reaction was batch-wise, the acidity accumulated to pH 6.5, deemed complete, and the supernatant entered the next reactor. The impurities at the bottom are discharged out periodically, and a biological fertilizer can be prepared;
4) the hydrolyzed and acidified materials enter an anaerobic methanogenesis-denitrogenation reactor, and the front area of the reactor is a fixed membrane component for strengthening methanogens (the reaction is: methanogenic reaction, product CH4+CO2(or HCO)3 －) And the middle rear part is an anaerobic ammonia oxidation baffling reaction area, part of filtrate of anaerobic digestion filtrate flows back to exchange heat and then enters an aerobic reactor, and the rest filtrate and the effluent of the aerobic reactor perform denitrification reaction (ammonia oxidation reaction: NH (NH)4 ++NO2 －＝＝2N2+2H2O), yielding waterDischarging; the upper part is a gas collecting area.
An anaerobic ammonia oxidation reaction zone: NO2 －－N：NH4 +-N concentration is controlled at 1.5; a: c is about 2: 1
The COD removal of the reactor effluent is 93%, the ammonia nitrogen removal is 88%, the nitrite nitrogen removal is 96% and the total nitrogen removal is 85%;
5) anaerobic digestion filtrate enters an aerobic reactor to carry out short-cut denitrification reaction (NH 4)++O2＝＝NO2 －+2H++H2O), nitrite enriched bacteria, NO 2-accumulation. The temperature of the filtrate is increased by 35 ℃ through heat exchange; DO: 1mg/L, pH8, free ammonia concentration of 5 mg/L;
the COD removal was 35%; the ammonia nitrogen removal rate is 57%; generating nitrogen nitrite;
the effluent enters a methane production-ammonia oxidation reactor for denitrification;
6) carrying out enrichment and reflux outside the reactor (not shown in the reactor figure) on kitchen garbage subjected to anaerobic ammonia oxidation in the convection area
In the embodiment, the HRT reaction time of the nitrosation system is 3 h; the anaerobic ammonia oxidation reaction time is 4.5 h;
finally, the system and the treatment method ensure that the total nitrogen removal rate of the effluent of the reactor is 90 percent and the COD removal rate is 87 percent.
The above description is only exemplary of the present invention and should not be taken as limiting the scope of the present invention, as any modifications, equivalents, improvements and the like made within the spirit and principles of the present invention are intended to be included within the scope of the present invention.
Claims (5)
1. The multiphase multistage biomass sludge treatment system combining hydrothermal and anaerobic ammonia oxidation is characterized in that: comprises a thermal hydrolysis reactor, a heat exchanger, a hydrolysis acid production reactor, an anaerobic methane production-nitrogen removal reactor, an aerobic reactor and a granular sludge separation enricher; the thermal hydrolysis reactor is communicated with the heat exchanger, the hydrolysis acidogenic reactor is communicated with the anaerobic methanogenesis-denitrogenation reactor, and the anaerobic methanogenesis-denitrogenation reactor is respectively communicated with the heat exchanger and the granular sludge separation enricher; the liquid inlet end of the aerobic reactor is communicated with the heat exchanger, and the liquid outlet end of the aerobic reactor is communicated with the anaerobic methanogenesis-denitrification reactor.
2. The multiphase multistage biomass sludge treatment system for hydrothermal combined anaerobic ammonium oxidation according to claim 1, wherein: the anaerobic methanogenesis-denitrogenation reactor comprises a water inlet, a water outlet, a gas outlet, a reflux port and an aerobic water outlet and inlet; the water inlet is communicated with the water outlet end of the hydrolysis acid-production reactor, and the reflux port is communicated with the heat exchanger; the aerobic water outlet and inlet is communicated with the aerobic reactor.
3. The multiphase multistage biomass sludge treatment system for hydrothermal combined anaerobic ammonium oxidation according to claim 2, wherein: the water inlet and the reflux port are positioned at the same side of the front end of the anaerobic methanogenesis-denitrogenation reactor, and the aerobic water outlet and inlet port is positioned at the middle rear end.
4. The multiphase multistage biomass sludge treatment system for hydrothermal combined anaerobic ammonium oxidation according to claim 2, wherein: the anaerobic methanogenesis-denitrogenation reactor is of a baffle plate type and comprises a plurality of baffling cavities, and a membrane reactor is arranged in the baffling cavity close to the water inlet.
5. The multiphase multistage biomass sludge treatment system for hydrothermal combined anaerobic ammonium oxidation according to claim 4, wherein: the aerobic water outlet and inlet is arranged on the baffling cavity behind the baffling cavity close to the water inlet.
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| CN112355034A (en) * | 2020-11-17 | 2021-02-12 | 同济大学 | Organic solid waste harmless pretreatment method based on hydrothermal calcium ion blending |
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| CN110963660A (en) * | 2019-12-26 | 2020-04-07 | 四川深蓝环保科技有限公司 | Multiphase multistage biomass sludge treatment system and method combining hydrothermal treatment with anaerobic ammonium oxidation |
| CN112355034A (en) * | 2020-11-17 | 2021-02-12 | 同济大学 | Organic solid waste harmless pretreatment method based on hydrothermal calcium ion blending |
| US11344934B2 (en) | 2020-11-17 | 2022-05-31 | Tongji University | Method for harmlessly pretreating organic solid waste based on combination of calcium ion and hydrothermal treatment |
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