CN102583923B - Municipal administration and/or industrial sludge energy-saving and emission-reduction disposal and resource integrated technique and equipment thereof - Google Patents
Municipal administration and/or industrial sludge energy-saving and emission-reduction disposal and resource integrated technique and equipment thereof Download PDFInfo
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- CN102583923B CN102583923B CN201210078846.8A CN201210078846A CN102583923B CN 102583923 B CN102583923 B CN 102583923B CN 201210078846 A CN201210078846 A CN 201210078846A CN 102583923 B CN102583923 B CN 102583923B
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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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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Abstract
The present invention relates to the Environmental Protection Target of killing all pathogen as disposing object, having realized, reducing the mud amount of dumping taking municipal administration and/or industrial sludge, reclaim available resources simultaneously, develop integrated technique and the equipment of comprehensive product. It is characterized in that mud is through containing solid concentration adjustment, pre-thermally homogenising pulp, pyrohydrolysis generates hydrolysis mud, carries out respectively: 1. anaerobic digestion obtains methane product, and biogas is made boiler oil production steam and electricity taking hydrolysate as node. 2. hydrolysate has been continued to chemical hydrolysis reaction, chemical hydrolysis product separates and obtains hydrolysate clear liquid, and hydrolysate clear liquid is the production for building materials insulation stereotype plate and sketch plate, cast-in-situ thermal-insulated material product, fire foam product etc. as the primary raw material of industrial foam agent. The dense slag that separation obtains is incorporated to mutually anaerobic digestor or is used through further processing. 3. final, to dispose object and completed sterilizing, decrement object, its residue is prepared the purposes such as base-material or building block material as Agricultural Fertilizer.
Description
Technical field
The present invention relates to municipal administration and/or industrial sludge energy-saving and emission-reduction disposal and resource integrated techniqueAnd apparatus field, particularly urban wastewater treatment firm is rich in microorganism, metazoa, algaeIn the municipal administration of class, organic matter type and/or industrial sludge, kill all pathogen, reduce mudThe amount of dumping processing, simultaneously the integrated technology neck of Joint Production biogas and hydrolysis bioprotein productTerritory.
Background technology
At present, the urban wastewater treatment firm taking biochemical method as main technique, city's industry of having stable political situationMud is the inevitable outcome dumping. It is carried out in environmental treatment to a kind of perfect sludge treatmentTechnology not yet forms scale. Conventional method, as landfill, dehydration or anhydration and incineration, as engineeringSoil, prepare Agricultural Fertilizer etc. and all exist the technical barrier that a lot of needs solve. Inorganization dumpsHad a strong impact on environmental quality, the way dumping is prohibited because there is secondary pollution.
The annual sludge quantity of China is with 10% speed increase, cost-effective disposal technology, jointCan reduce discharging and become urgent environmental treatment task. In disposal process, its resource is openedSend out utilization more important.
Chinese patent application 01126637.6 discloses separation place of a kind of mud hypoxemia digestion-filmScience and engineering technology, the supernatant that sludge digestion is produced directly discharges by membrane separation device. Due toThe technological core of invention has adopted membrane technology to carry out the separation of supernatant, the transmission rates of film and filmBlocked, reduce the working life of film, be subject to the constraint that industrialization realizes.
Chinese patent application 96196796.X discloses a kind of side that processes residual active sludgeMethod, the white clay obtaining by sulphate pulp production process, adds residual active sludge after thickeningVolume ratio is 1: 5～10, and 75 DEG C～104 DEG C of operating temperatures, are undertaken by solid-liquid separating equipmentDehydration, solid content, by mummification, burns.
Chinese patent ZL200610019063.7 has announced and " has been hydrolyzed residual active sludge with quick limePrepare the production technology of aminosal "; China applies for a patent 200710150330.9 and has announced" a kind of active sludge treatment process "; Chinese patent application 200710150331.3 has announced " onePlant preparation of microprotein ". Above-mentioned three sections of disclosed techniques of patent all only relate to eggThe extraction of white liquid, its technique needs the external world that thermal source is provided, and can not realize energy from supplying with.
Chinese patent application 200920252082.3 has been announced " sludge hydrolytic extraction bioproteinSystem ", above-mentioned process is by again adding mud CaO or Ca (OH)2As changeLearn under inorganic agent condition, carry out chemical hydrolysis, pH is 13, reaction operating pressure P=0.4～0.6MPa, hydrolysis time is greater than 3 hours; After hydrolyzate step-down cooling, obtain by filterTo filtrate and liquid cake, the hydrolysis prods that filtrate be extracted. The recovery rate of this class technique albumen is low.Because hydrolyzing sludge will have high viscosity, solid particles is little, the spy of filter at low temperature (80 DEG C of <)Levy, the production capacity of the low filter of filter operation temperature is very low. The cake moisture of producing is large,For post-processed is brought difficulty.
Summary of the invention
The object of this invention is to provide a kind of sludge energy-saving reduction of discharging place that is suitable for suitability for industrialized productionIntegrated technique and the equipment of reason and resource.
The present invention is achieved in that its method is following steps:
(1) pending mud adds in pulping device (1) after preliminary hydro-extraction, prepares homogeneous mudSlurry;
(2) above-mentioned homogenizing slurry is sent in pyrohydrolysis device (2) to preparation hydrolysis mud; (3)Said hydrolyzed mud is placed in to one-level flash vessel (3), release of pressure flash distillation, release of pressure steam is back toIn pulping device (1), for pulping device (1) provides institute's calorific requirement;
(4) the hydrolysis mud after full flashing device (3) flash distillation is split into two strands, itsIn one access digestion pressure regulator (4) carry out flash distillation cooling;
(5) after the flash distillation of digestion pressure regulator (4), obtain secondary flash distillation hydrolysis mud, secondaryFlash distillation hydrolysis mud is sent in anaeroic digestor (5) and is prepared biogas after heat exchanger cooling;
(6) sludge residue producing after anaeroic digestor (5) digestion reaction is after dehydration separatesPrepare agricultural base manure, clear liquid is delivered to preliminary sedimentation tank (19);
(7) second strand of hydrolysis mud that will distribute from full flashing device (3), sends into chemistryHydrolysis reactor (7), in chemical hydrolysis reaction device (7), will be hydrolyzed mud chemical hydrolysis;
(8) in chemical hydrolysis reaction device (7), by the hydrolysis mud alkali after chemical hydrolysisRegulate after pH value, send in separation equipment, realize and separating, be separated into light, heavy two-phase fluid;
(9) step (8) separation equipment separates the light phase obtaining, i.e. water-solubility protein liquid accessSecondary flash vessel (11) completes once concentration, once concentration in secondary flash vessel (11)Liquid obtains finished product protein concentrate liquid again after follow-up concentrator is concentrated;
(10) steam that digestion pressure regulator (4) and secondary flash vessel (11) produce altogetherThe follow-up concentrator being all in step (9) provides thermal source;
(11) step (8) separation equipment separates the heavy phase fluid obtaining, and is delivered to anaerobism and disappearsChange device (5) and prepare biogas;
(12) biogas being produced by anaeroic digestor (5) is stored in biogas storage tank (6),Biogas, as boiler oil, is produced high-pressure water vapor product; A part for above-mentioned water vapour productDeliver to pyrohydrolysis device (2), as pyrohydrolysis thermal source, all the other are as generating.
Wherein, the follow-up concentration process in step (9) is: once concentration liquid enters long tube and steamsHair device group (12) completes secondary concentration, and secondary concentration liquid enters in scraper evaporator group (13)Complete final concentrating, finished product dope protein content is 15～30%; Digestion pressure regulator (4)The steam producing with secondary flash vessel (11) is long-tube evaporator group (12) and scraper evaporatorGroup (13) provides thermal source; Separation equipment in step (8) is horizontal screw centrifuge (10).
In step (1), the operating condition of pulping device (2) is: controlling mud moisture content is80%～85%, preheat temperature is 95～97 DEG C, and be 2 hours preheating time, stirs preparation allMatter mud; In step (2), the operating condition of pyrohydrolysis device (2) is: pass into steam and carry out waterSeparate, 160 DEG C ± 5 DEG C of temperature, the time of staying is 30 minutes, hydrolysis mud moisture content is 87%～88％。
In step (3), the operating temperature of one-level flash vessel (3) is 140 DEG C ± 5 DEG C; Step (4)The flash temperature of middle digestion pressure regulator (4) is 100 DEG C ± 2 DEG C, and the time of staying is 90 pointsClock; In step (5), the reaction temperature of anaeroic digestor (5) is 30-40 DEG C.
In step (7), pyrohydrolysis reaction condition is: adopt organic acid for adjusting pH value, pHValue is 5～6.9, controls 140 DEG C ± 5 DEG C of temperature, realizes hydrolysis mud chemical hydrolysis, when stopBetween 0.5～3.5 hour; PH value in step (8) after alkali adjusting is 6.5～8.
Described organic acid is acetic acid, citric acid, and at least one in phosphoric acid, alkali is Ca (OH)2。
Realize an equipment for above-mentioned technique, this equipment comprises: pulping device (1), pyrohydrolysis device(2), full flashing device (3), digestion pressure regulator (4), anaeroic digestor (5), natural pondGas storage tank (6), chemical hydrolysis reaction device (7), organic acid feeder (8), alkali feeder (9),Horizontal screw centrifuge (10), secondary flash vessel (11), follow-up concentrator, thermal boiler station (15),Generating set (16), filter and dehydration machine (17), the fertile base-material storage pond of agriculture (18), preliminary sedimentation tank (19).
Described follow-up concentrator is long-tube evaporator group (12) and scraper evaporator group (13).
Described scraper evaporator group can be vacuum scraper evaporator bank.
Described pulping device (1) is continuous mechanical agitator tank, intermittently mechanical agitator tank, static stateAt least one in mixing reactor.
The mode of heating of pyrohydrolysis device (2) is steam direct heating, the heating of steam dividing wall type,Steam-internal tubular type adds at least one of hankering.
Filter and dehydration machine (17) is sedimentation centrifuge, filter centrifugal, and filter, weight is heavyAt least one in device fallen; Horizontal screw centrifuge (10) is realized liquid-solid point to two-phase fluid-mixingFrom.
The beneficial effect that the present invention has is:
(1) the present invention is the integrated technique of the treatment technology to municipal administration and/or industrial sludge, byPyrohydrolysis process, anaerobic digestion process, process of methane is prepared in anaerobic digestion, chemical hydrolysis preparationProtein solution process, slaking residue Dehydration is for base-material process, and each process is organically in conjunction with groupBecome a sludge environment-friendly to process and utilization of resources practical technique. The realization of this technology has very big ringBorder benefit and economic benefit.
(2) 160 DEG C of the pyrohydrolysis process control temperature realizing, inactivation time 30 minutes, peaceEntirely kill all pathogen. The regeneration of no longer surviving of bacterium after residue dehydration.
(3) anaerobic digestion process is produced biogas, is clean generative fuel, and a part is as steamingThe confession saving of fuel of boiler furnace coal and fossil fuel. Heat taking clear energy sources as fuel is movingPower apparatus has been avoided environmental pollution and has been saved construction investment and operating cost. Determine the application of this technologyThe wide plasticity in market.
(4) adopt pyrohydrolysis and anaerobic digestion united mode, strengthened anaerobic digester system,Install compact to designly, easily realize the upgrading of Treatment of Sludge factory.
(5) adopt effectively insulation and steam repeating cyples to utilize, its energy efficiency is high.
(6) chemical heat hydrolysis is prepared and in aqueous soluble protein product, is adopted organic acid and Ca (OH)2'sAcid system production process, secondary metabolite has been avoided Cl-And SO4 2-Ion enters final solid slag product,Reduce the harm to soil.
(7), under 140 DEG C of hot states, adopt sedimentation centrifuge to separate and reclaim light liquid as waterDissolubility albumen, heavy phase is recovered to the technique of anaerobic digestor, has avoided product isolated by filtrationMultiple difficulty.
(8) the mud environmental treatment of the technology of the present invention and the technology of resource, the heat of realization is movingPower is self-supporting saves coal, fossil resource consumption and reduces discharging pollutant SO2、NOX、CO2Deng,Extensively adapted to large, medium and small water treatment plant, the production by recycling obtaining in processing environment mudThe benefit that product bring, has reduced operating cost.
Process costs of the present invention and other process costs contrast, and result is as following table (thisBright every cost is designated as 1):
Table 1: cost contrast table
| Process route | Direct investment | Take up an area (hectare) | Operating cost |
| Compost (biological dewatered) soil utilization | 1.205 | 1.187 | 1.384 |
| Heat drying+burning | 1.245 | 0.896 | 2.135 |
| Extraction+the anaerobic digestion of pyrohydrolysis+organic nitrogen | 1 | 1 | 1 |
Visible, adopt technique of the present invention, can be significantly reduced to this.
Brief description of the drawings
Fig. 1 is process chart of the present invention.
In figure: 1-pulping device, 2-pyrohydrolysis device, 3-full flashing device, 4-digestion pressure regulatesDevice, 5-anaeroic digestor, 6-biogas storage tank, 7-chemical hydrolysis reaction device, 8-organic acid is reinforcedDevice, 9-alkali feeder, 10-horizontal screw centrifuge, No. bis-flash vessels of 11-, 12-long-tube evaporatorGroup, 13-scraper evaporator group, 14-product, 15-thermal boiler station, 16-generating set, 17-Dewaterer, the fertile base-material storage of 18-agriculture pond, 19-preliminary sedimentation tank
Detailed description of the invention
Embodiment mono-
(1) municipal sludge adds in pulping device (1) after preliminary hydro-extraction, controls mud moisture contentBe 80%, preheat temperature is 95 DEG C, and be 2 hours preheating time; Homogenizing slurry is prepared in stirring;
(2) above-mentioned homogenizing slurry is sent in pyrohydrolysis device (2), passed into steam, be prepared into waterSeparate mud; The operating condition of pyrohydrolysis device (2) is: 155 DEG C of temperature, 30 points of the time of stayingClock, hydrolysis mud moisture content is 87%;
(3) said hydrolyzed mud is placed in to one-level flash vessel (3), release of pressure flash distillation, release of pressure steamsVapour is back in pulping device (1), for pulping device (1) provides institute's calorific requirement; One-level flash vessel (3)Operating temperature be 135 DEG C;
(4) the hydrolysis mud after full flashing vapour device (3) flash distillation is split into two strands, oneThigh access digestion pressure regulator (4) carries out flash distillation cooling; Digestion pressure regulator (4)Flash temperature is 98 DEG C, stops 90 minutes;
(5) after the flash distillation of digestion pressure regulator (4), obtain secondary flash distillation hydrolysis mud, secondary dodgesSteaming hydrolysis mud will send in anaeroic digestor (5) and prepare biogas through heat exchange cooling; AnaerobismThe reaction temperature of digester (5) is 30 DEG C;
(6) sludge residue producing after anaeroic digestor (5) digestion reaction separates preparation through dehydrationAgricultural base manure, clear liquid is delivered to preliminary sedimentation tank (19);
(7) second strand of hydrolysis mud that will distribute from full flashing device (3), sends into chemical waterSeparate reactor (7), in chemical hydrolysis reaction device (7), adopting vinegar acid for adjusting pH value is 5,Control 135 DEG C of temperature, realize hydrolysis mud chemical hydrolysis, time of staying 0.5h;
(8) in chemical hydrolysis reaction device (7), by the Ca (OH) for mud of the hydrolysis after chemical hydrolysis2Regulating pH value is 6.5, then sends in horizontal screw centrifuge (10), realizes and separating, and separatesBecome light, heavy two-phase fluid;
(9) separate by horizontal screw centrifuge (10) the light phase obtaining, i.e. water-solubility protein liquid accessSecondary flash vessel (11) completes once concentration, once concentration in secondary flash vessel (11)Liquid enters long-tube evaporator group (12) and completes secondary concentration, and secondary concentration liquid enters at scraper plate and steamsHair device group (13) completes final concentrated; Finished product dope protein content is 15%; This protein liquid canFor making insulation material;
(10) separate by horizontal screw centrifuge (10) the heavy phase fluid obtaining, press and be delivered to through coolingAnaeroic digestor (5) is prepared biogas;
(11) biogas being produced by anaeroic digestor (5) is stored in biogas storage tank (6), natural pondGas, as boiler oil, is produced high-pressure water vapor product; An above-mentioned water vapour product part is delivered toPyrohydrolysis device (2), as pyrohydrolysis thermal source, all the other are as generating;
(12) steam that digestion pressure regulator (4) and secondary flash vessel (11) produce is commonFor long-tube evaporator group (12) and the scraper evaporator group (13) of protein liquid in step (9)Thermal source is provided;
(13) realized sewage sludge harmlessness and reduced discharging disposal target by above-mentioned steps, steam is real simultaneouslyExisting pyrohydrolysis confession.
Embodiment bis-
(1) industrial sludge adds in pulping device (1) after preliminary hydro-extraction, controls slurry moisture contentBe 85%, preheat temperature is 97 DEG C, and be 2 hours preheating time; Homogenizing slurry is prepared in stirring;
(2) above-mentioned homogenizing slurry is sent in pyrohydrolysis device (2), passed into steam, be prepared into waterSeparate mud; The operating condition of pyrohydrolysis device (2) is: 165 DEG C of temperature, 30 points of the time of stayingClock, hydrolysis mud moisture content is 88%;
(3) said hydrolyzed mud is placed in to one-level flash vessel (3), release of pressure flash distillation, release of pressure steamsVapour is back in pulping device (1), for pulping device (1) provides institute's calorific requirement; One-level flash vessel (3)Operating temperature be 145 DEG C;
(4) the hydrolysis mud after full flashing vapour device (3) flash distillation is split into two strands, itsIn-a strand access digestion pressure regulator (4) carries out flash distillation cooling; Digestion pressure regulator (4)Flash temperature be 102 DEG C, stop 90 minutes;
(5) after the flash distillation of digestion pressure regulator (4), obtain secondary flash distillation hydrolysis mud, secondary dodgesSteaming hydrolysis mud will send in anaeroic digestor (5) and prepare biogas, anaerobism through heat exchange coolingThe reaction temperature of digester (5) is 40 DEG C;
(6) sludge residue producing after anaeroic digestor (5) digestion reaction separates preparation through dehydrationAgricultural base manure, clear liquid is delivered to preliminary sedimentation tank (19);
(7) second strand of hydrolysis mud that will distribute from full flashing device (3), sends into chemical waterSeparate reactor (7), in chemical hydrolysis reaction device (7), adopt lemon acid for adjusting pH value6.9, control 145 DEG C of temperature, realize hydrolysis mud chemical hydrolysis, time of staying 3.5h;
(8) in chemical hydrolysis reaction device (7), by the Ca (OH) for mud of the hydrolysis after chemical hydrolysis2Regulating pH value is 8, then sends in horizontal screw centrifuge (10), realizes and separating, and is separated intoGently, heavy two-phase fluid;
(9) separate by horizontal screw centrifuge (10) the light phase obtaining, i.e. water-solubility protein liquid accessSecondary flash vessel (11) completes once concentration, once concentration in secondary flash vessel (11)Liquid enters long-tube evaporator group (12) and completes secondary concentration, and secondary concentration liquid enters at scraper plate and steamsHair device group (13) completes final concentrated; Finished product dope protein content is 30%; This protein liquid canFor making fire foam;
(10) separate by horizontal screw centrifuge (10) the heavy phase fluid obtaining, be delivered to anaerobic digestionDevice (5) is prepared biogas;
(11) biogas being produced by anaeroic digestor (5) is stored in biogas storage tank (6), natural pondGas, as boiler oil, is produced high-pressure water vapor product; An above-mentioned water vapour product part is delivered toPyrohydrolysis device (2), as pyrohydrolysis thermal source, all the other are as generating;
(12) steam that digestion pressure regulator (4) and secondary flash vessel (11) produce is commonFor long-tube evaporator group (12) and the scraper evaporator group (13) of protein liquid in step (9)Thermal source is provided;
(13) realized sewage sludge harmlessness and reduced discharging disposal target by above-mentioned steps, steam is real simultaneouslyExisting pyrohydrolysis confession.
Claims (8)
1. sludge energy-saving reduces discharging and disposes and its resource integrated technique, and it comprises the following steps:
(1) pending mud adds in pulping device (1) after preliminary hydro-extraction, prepares homogenizing slurry;
(2) above-mentioned homogenizing slurry is sent in pyrohydrolysis device (2) to preparation hydrolysis mud;
(3) said hydrolyzed mud is placed in to full flashing device (3), release of pressure flash distillation, release of pressure steam is delivered in pulping device (1), for pulping device (1) provides institute's calorific requirement;
(4) the hydrolysis mud after full flashing device (3) flash distillation is split into two strands, wherein one access digestion pressure regulator (4) carries out flash distillation cooling;
(5) after the flash distillation of digestion pressure regulator (4), obtain secondary flash distillation hydrolysis mud, secondary flash distillation hydrolysis mud is sent in anaeroic digestor (5) and is prepared biogas after heat exchanger cooling;
(6) sludge residue producing after anaeroic digestor (5) digestion reaction is prepared agricultural base manure after dehydration separates, and clear liquid is delivered to preliminary sedimentation tank (19);
(7) second strand of hydrolysis mud that will distribute from full flashing device (3), sends into chemical hydrolysis reaction device (7), in chemical hydrolysis reaction device (7), completes chemical hydrolysis;
(8) in chemical hydrolysis reaction device (7), the hydrolysis mud after chemical hydrolysis is regulated after pH value with alkali, send in separation equipment, realize and separating, be separated into light, heavy two-phase fluid;
(9) step (8) separation equipment separates the light phase obtaining, it is water-solubility protein liquid access secondary flash vessel (11), in secondary flash vessel (11), complete once concentration, once concentration liquid obtains finished product protein concentrate liquid again after follow-up concentrator is concentrated;
(10) steam that digestion pressure regulator (4) and secondary flash vessel (11) produce is jointly for the follow-up concentrator in step (9) provides thermal source;
(11) step (8) separation equipment separates the heavy phase fluid obtaining, and is delivered to anaeroic digestor (5) and prepares biogas;
(12) biogas being produced by anaeroic digestor (5) is stored in biogas storage tank (6), and biogas, as boiler oil, is produced high-pressure water vapor product; A part for above-mentioned water vapour product is delivered to pyrohydrolysis device (2), and as pyrohydrolysis thermal source, all the other are as generating.
2. technique according to claim 1, it is characterized in that the follow-up concentration process in step (9) is: once concentration liquid enters long-tube evaporator group (12) and completes secondary concentration, secondary concentration liquid enters scraper evaporator group (13) and completes final concentrating, and finished product dope protein content is 15～30%; The steam that digestion pressure regulator (4) and secondary flash vessel (11) produce is that long-tube evaporator group (12) and scraper evaporator group (13) provide thermal source; Separation equipment in step (8) is horizontal screw centrifuge (10).
3. technique according to claim 1, it is characterized in that, described in step (1), the operating condition of pulping device (1) is: controlling slurry moisture content is 80%～85%, and preheat temperature is 95～97 DEG C, be 2 hours preheating time, stirs and prepare homogenizing slurry; In step (2), the operating condition of pyrohydrolysis device (2) is: pass into steam and be hydrolyzed, and 160 DEG C ± 5 DEG C of temperature, 30 minutes time of staying, hydrolysis mud moisture content is 87%～88%.
4. technique according to claim 1, is characterized in that, in step (3), the operating temperature of one-level flash vessel (3) is 140 DEG C ± 5 DEG C; In step (4), the flash temperature of digestion pressure regulator (4) is 100 DEG C ± 2 DEG C, and the time of staying is 90 minutes; In step (5), the reaction temperature of anaeroic digestor (5) is 30-40 DEG C.
5. technique according to claim 1, it is characterized in that, in step (7), pyrohydrolysis reaction condition is: adopt organic acid for adjusting pH value, pH value is 5～6.9, control 140 DEG C ± 5 DEG C of temperature, realize hydrolysis mud chemical hydrolysis, organic acid is acetic acid, citric acid, at least one in phosphoric acid, 0.5～3.5 hour time of staying; PH value in step (8) after alkali adjusting is 6.5～8, and alkali is Ca (OH)2。
6. realize the equipment of technique described in claim 1 for one kind, this equipment comprises: pulping device (1), pyrohydrolysis device (2), full flashing device (3), digestion pressure regulator (4), anaeroic digestor (5), biogas storage tank (6), chemical hydrolysis reaction device (7), organic acid feeder (8), alkali feeder (9), horizontal screw centrifuge (10), secondary flash vessel (11), follow-up concentrator, thermal boiler station (15), generating set (16), dewaterer (17), the fertile base-material storage pond of agriculture (18), preliminary sedimentation tank (19), the mode of heating of described pyrohydrolysis device (2) is steam direct heating, the heating of steam dividing wall type, and steam-internal tubular type adds at least one of hankering, described pulping device (1) is continuous mechanical agitator tank, at least one in mechanical agitator tank, static mixing tubular type reactor intermittently.
7. equipment according to claim 6, is characterized in that, described follow-up concentrator is long-tube evaporator group (12) and scraper evaporator group (13).
8. equipment according to claim 6, is characterized in that, dewaterer (17) is sedimentation centrifuge, filter centrifugal, at least one in gravitational settler; Horizontal screw centrifuge (10) is realized liquid-solid separation to two-phase fluid-mixing.
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| CN103204712B (en) * | 2013-03-22 | 2015-04-15 | 天紫环保装备制造（天津）有限公司 | Method for manufacturing fertilizer base materials from garbage containing organic matters |
| CN103274572A (en) * | 2013-05-28 | 2013-09-04 | 国新天汇环境有限公司 | Treatment method of organic solid waste |
| CN104261643A (en) * | 2014-10-27 | 2015-01-07 | 邓立新 | Solar pyrohydrolysis and flash dehydration combined sludge treatment system |
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| CN104944732A (en) * | 2015-06-29 | 2015-09-30 | 同济大学 | Energy-saving recycling treatment disposal system and energy-saving recycling treatment disposal process for organic solid waste |
| CN108423957B (en) * | 2018-02-07 | 2021-02-02 | 同济大学 | Method for realizing sludge quality-based phase-splitting resource recovery |
| CN108409076A (en) * | 2018-03-29 | 2018-08-17 | 天津大学 | A kind of method of biogas cascade utilization in low concentration sludge digestion drying process |
| CN110002712A (en) * | 2019-04-04 | 2019-07-12 | 杨洋 | Sludge energy treatment process |
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| CN111170603A (en) * | 2020-02-28 | 2020-05-19 | 安徽华骐环保科技股份有限公司 | Efficient sludge recycling system and treatment method thereof |
| CN112075320A (en) * | 2020-09-18 | 2020-12-15 | 北京城市排水集团有限责任公司 | System and method for preparing organic nutrient soil from urban domestic sludge, organic nutrient soil and application |
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| JPH0347600A (en) * | 1989-07-13 | 1991-02-28 | Agency Of Ind Science & Technol | Oil recovering from organic sludge |
| CN201605215U (en) * | 2009-12-29 | 2010-10-13 | 天津市裕川置业集团有限公司 | Sludge hydrolysis extracting microbial-protein system |
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| CN102381820A (en) * | 2011-09-20 | 2012-03-21 | 福州开发区三水环保科技有限公司 | Sludge treatment process based on hydrothermal modification technology |
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