CN204607928U - Mud catalytic pyrolysis gasification prepares the system of biofuel - Google Patents
Mud catalytic pyrolysis gasification prepares the system of biofuel Download PDFInfo
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- CN204607928U CN204607928U CN201520239672.8U CN201520239672U CN204607928U CN 204607928 U CN204607928 U CN 204607928U CN 201520239672 U CN201520239672 U CN 201520239672U CN 204607928 U CN204607928 U CN 204607928U
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Abstract
The utility model proposes the system that mud catalytic pyrolysis gasification prepares biofuel, comprise: desiccation apparatus, without thermal barrier heat accumulating type rotating bed, fluidized-bed gasification device, dedusting and purifying device, combustible gas storage tank, condenser, extraction plant, standing separation tank and rectifying tower, wherein, be connected with desiccation apparatus without thermal barrier heat accumulating type rotating bed, fluidized-bed gasification device is connected with without thermal barrier heat accumulating type rotating bed, dedusting and purifying device is connected with fluidized-bed gasification device, combustible gas storage tank is connected with dedusting and purifying device, condenser is connected with without thermal barrier heat accumulating type rotating bed, extraction plant is connected with condenser, standing separation tank is connected with extraction plant, rectifying tower is connected with standing separation tank.Adopt this system can decrease the generation of foul smell, achieve the efficient combination of mud calcification dehydration and catalyse pyrolysis, not only reduce mummification energy consumption, also improve the quality of pyrolyzing sludge speed and pyrolysis product, running cost is low.
Description
Technical field
The utility model belongs to solid waste resource recovery process field, is specifically related to the system that mud catalytic pyrolysis gasification prepares biofuel.
Background technology
At present, the energy expenditure in the world is mainly based on the fossil oil such as coal, oil and natural gas.Within 2005, to the year two thousand thirty, the primary energy source demand in the whole world will increase by 55% to world energy sources microstructure Prediction, and its average growth rate per annum is 1.8%, and non-renewable fossil oil is still the main source of primary energy source consumption, in demand growth total amount, account for 84%.How adjusting and optimizing energy consumption structure, Looking For Substitutions Of Oil is the important topic that countries in the world face.
Along with China's level of urbanization improves constantly, the quantity discharged of municipal effluent also sharply increases, a large amount of containing parasitic ovum, harmful pathogenic bacteria, heavy metal sewage sludge owing to can produce in sewage treatment process, if do not carry out effectively process and dispose, serious secondary pollution can be caused to environment.According to statistics, the sludge quantity that China's urban wastewater treatment firm in 2013 produces is more than 3,000 ten thousand tons, and wherein have the mud of 80% not dealt carefully with, simple landfill or stacking make many cities be faced with in " malicious mud besieged city ".
Pyrolyzing sludge is under the condition of anaerobic or anoxic, and mud is heated to certain temperature, makes the organism generation thermo-cracking in mud and thermochemical study reaction, generates H
2, CO, CH
4deng the process of inflammable gas, oil-water mixture and solid product.Pyrolyzing sludge is a kind of new sludge hot chemical utilization disposal technology, has the many merits such as environmental pollution is little, cost is low, resource high-efficiency recovery.Pyrolytic process is divided into low temperature pyrogenation (≤500 DEG C) and high temperature pyrolysis.Because high temperature pyrolysis main equipment manufacture difficulty is large, operating requirement is high, and energy consumption is relatively high, and current Research Emphasis both domestic and external is placed on low temperature pyrogenation.Sludge at low temperature pyrolytic technique can overcome the shortcoming of traditional sludge method of disposal effectively.Due to heavy metal accumulation good stability in solid residue, and temperature of reaction is low, avoids Dioxins and generates district, NOx and SOx generates also little, and therefore low temperature pyrogenation technology is the internationally recognized recycling sludge thermochemistry disposal technology having important application prospect.
Existing pyrolyzing sludge technology generally comprises pre-treatment (dehydration, mummification), pyrolysis system, deodoration system, purification system etc., its Problems existing mainly comprises: (1) existing sludge drying technique, because the moisture temperature steamed is lower, generally directly enter Sewage treatment systems, add processing costs, be difficult to realize " minimizing, innoxious, the resource utilization " of mud; (2) existing pyrolyzing sludge system is mainly for the purpose of inflammable gas processed, high heating value fuel oil, and sludge carbon, due to containing heavy metal, needs to carry out landfill disposal, and " charcoal resource " is not utilized effectively; (3) existing Pyrolysis of Sludge from Oil is difficult to the high efficiency separation realizing oil-water mixture, the pyrolytic behavior obtained by condensation contains more moisture, calorific value is lower, owing to containing more acidic component in pyrolytic behavior, also can cause corrosion to the equipment such as boiler, pipeline.
If do not adopt extracting rectifying to prepare pyrolyzing sludge biofuel, prior art Problems existing comprises: in (1) pyrolyzing sludge liquid, oily water separation is incomplete, and the moisture of oil-containing carries out Sewage treatment systems, adds intractability; (2) pyrolysis oil output is lower, light component is less, calorific value is not high, is difficult to effective utilization.
In addition, the pyrolysis oil oxygen level that common sludge method for pyrolysis obtains is high, acid number is comparatively large, viscosity is high, poor stability, is difficult to further utilization, if can obtain the biofuel of high-quality, high heating value, the industrialization will being convenient to pyrolyzing sludge runs and promotes.
Utility model content
The utility model is intended to solve one of technical problem in correlation technique at least to a certain extent.For this reason, an object of the present utility model is to propose the system that a kind of mud catalytic pyrolysis gasification prepares biofuel.
According to an aspect of the present utility model, the utility model proposes the system that a kind of mud catalytic pyrolysis gasification prepares biofuel.The system preparing biofuel according to the mud catalytic pyrolysis gasification of the utility model embodiment comprises:
Desiccation apparatus, described desiccation apparatus has sludge inlet, dewatered sludge outlet, smoke inlet, vapor outlet port, the described sludge inlet described desiccation apparatus that is connected with feeding screw is suitable for mud described in subtend and carries out drying and other treatment, to evaporate portion of water and deodorizing;
Without thermal barrier heat accumulating type rotating bed, described have dewatered sludge entrance, fuel inlet, gas-liquid mixture outlet, sludge carbon outlet and exhanst gas outlet without thermal barrier heat accumulating type rotating bed, and described sludge carbon exit is provided with broken discharging machine; Described dewatered sludge entrance exports with described dewatered sludge and is connected, described exhanst gas outlet is connected with described smoke inlet, describedly be suitable for carrying out catalyse pyrolysis process to the mud after described drying and other treatment without thermal barrier heat accumulating type rotating bed, to obtain gas-liquid mixture and sludge carbon;
Fluidized-bed gasification device, described fluidized-bed gasification device has sludge carbon entrance, gasification agent inlet, gasification mixed gas outlet and dedusting ash entrance, described sludge carbon entrance exports with described sludge carbon and is connected, described fluidized-bed gasification device is suitable for described sludge carbon and vaporized chemical generation steam gasification to react, to obtain combustible gas;
Dedusting and purifying device, described dedusting and purifying device has gasification gas mixture entrance, fuel outlet and dedusting ash outlet, described gasification gas mixture entrance is connected with described gasification mixed gas outlet, described dedusting ash outlet is connected with affiliated dedusting ash entrance, described dedusting and purifying device is suitable for carrying out purifying treatment, to obtain combustible gas to described gasification gas mixture;
Combustible gas storage tank, described combustible gas storage tank has combustible gas entrance, fuel outlet, and described combustible gas entrance is connected with described fuel outlet, and described fuel outlet is connected with described fuel inlet;
Condenser, described condenser has gas-liquid mixture entrance, pyrolysis gas outlet, pyrolytic behavior outlet, recirculated water entrance, circulating water outlet, described gas-liquid mixture entrance exports with described gas-liquid mixture and is connected, described gas-liquid mixture is carried out condensation process by described condenser, to obtain pyrolysis gas and pyrolytic behavior;
Extraction plant, described extraction plant has pyrolytic behavior entrance, methylene dichloride entrance, mixture export.Described pyrolytic behavior entrance exports with described pyrolytic behavior and is connected, and described extraction plant is suitable for utilizing methylene dichloride to carry out extraction treatment to described pyrolytic behavior;
Standing separation tank, described standing separation tank has entry to mixed solution, moisture outlet, extraction phase outlet, described entry to mixed solution is connected with described mixture export, and the mixed solution that described standing separation tank is suitable for described extraction treatment to obtain is separated and obtains organic substance extraction phase and aqueous phase; And
Rectifying tower, described rectifying tower has extraction phase entrance, methylene dichloride outlet, biofuel outlet, phegma entrance, recirculated water entrance, circulating water outlet, described extraction phase entrance exports with described extraction phase and is connected, described methylene dichloride outlet is connected with methylene dichloride entrance, described rectifying tower is suitable for described organic substance extraction to carry out rectification process mutually, obtains biofuel to be separated.
By the system adopting the mud catalytic pyrolysis gasification of the utility model above-described embodiment to prepare biofuel, send in desiccation apparatus after first mud being mixed with a certain amount of additive and carry out drying and other treatment; Secondly dewatered sludge is distributed into and carries out low temperature pyrogenation reaction without thermal barrier heat accumulating type rotating bed, generate gas-liquid mixture and pyrolytic carbon; Wherein, pyrolytic carbon through broken laggard enter the reaction of fluidisation bed gasifying apparatus generation steam gasification, the gasification gas mixture obtained obtains combustible gas and stores in combustible gas storage tank after dedusting and purifying device purification, and may be used for without thermal barrier heat accumulating type rotating bed radiator tube combustion heating; Gas-liquid mixture realizes being separated of pyrolytic behavior and pyrolysis gas by condenser, pyrolytic behavior and appropriate methylene dichloride are uniformly mixed in extraction plant, and be placed in standing separation tank and carry out stratification, organic substance extraction after layering flows into rectifying tower mutually and carries out rectification process, namely separablely obtains high-quality biological diesel oil.Whole system decreases the generation of foul smell, achieve the efficient combination of mud calcification dehydration and catalyse pyrolysis, not only reduce mummification energy consumption, also improve the quality of pyrolyzing sludge speed and pyrolysis product, running cost is low, heat recovery rate is high, resource utilization level is high, product economy is profitable, pyrolysis does not produce dioxin, secondary pollution is little, is beneficial to the industrial applications of pyrolyzing sludge.
In embodiments more of the present utility model, described gasification agent inlet is connected with described moisture outlet with described vapor outlet port, so that the aqueous phase utilizing the moisture obtained of described drying and other treatment and described extraction treatment to obtain is as the vaporized chemical of sludge carbon.
In embodiments more of the present utility model, described rectifying tower recirculated water entrance is connected with condenser circulating water outlet, described rectifying tower circulating water outlet is connected with condenser recirculated water entrance, so that the heat utilizing described condensation process to reclaim is for described rectification process.
Accompanying drawing explanation
Fig. 1 is the structural representation preparing the system of biofuel according to the mud catalytic pyrolysis gasification of the utility model embodiment.
Fig. 2 is the schema preparing the method for biofuel according to the mud catalytic pyrolysis gasification of the utility model embodiment.
Embodiment
According to an aspect of the present utility model, the utility model proposes the system that a kind of mud catalytic pyrolysis gasification prepares biofuel.The mud catalytic pyrolysis gasification describing the utility model specific embodiment in detail below with reference to Fig. 1 prepares the system of biofuel.
According to specific embodiment of the utility model, the system that mud catalytic pyrolysis gasification prepares biofuel comprises:
Desiccation apparatus 10, without thermal barrier heat accumulating type rotating bed 20, fluidized-bed gasification device 30, dedusting and purifying device 40, combustible gas storage tank 50, condenser 60, extraction plant 70, standing separation tank 80 and rectifying tower 90.
Wherein, desiccation apparatus 10 has sludge inlet, dewatered sludge outlet, smoke inlet, vapor outlet port, and the described sludge inlet described desiccation apparatus that is connected with screw feeder is suitable for mud described in subtend and carries out drying and other treatment, to evaporate portion of water and deodorizing.
Have dewatered sludge entrance, fuel inlet, gas-liquid mixture outlet, sludge carbon outlet and exhanst gas outlet without thermal barrier heat accumulating type rotating bed, described sludge carbon exit is provided with broken discharging machine; Described dewatered sludge entrance exports with described dewatered sludge and is connected, described exhanst gas outlet is connected with described smoke inlet, describedly be suitable for carrying out catalyse pyrolysis process to the mud after described drying and other treatment without thermal barrier heat accumulating type rotating bed, to obtain gas-liquid mixture and sludge carbon.
Fluidized-bed gasification device has sludge carbon entrance, gasification agent inlet, gasification mixed gas outlet and dedusting ash entrance, described sludge carbon entrance exports with described sludge carbon and is connected, described fluidized-bed gasification device is suitable for described sludge carbon and vaporized chemical generation steam gasification to react, to obtain combustible gas.
Dedusting and purifying device has gasification gas mixture entrance, fuel outlet and dedusting ash outlet, described gasification gas mixture entrance is connected with described gasification mixed gas outlet, described dedusting ash outlet is connected with affiliated dedusting ash entrance, described dedusting and purifying device is suitable for carrying out purifying treatment, to obtain combustible gas to described gasification gas mixture;
Combustible gas storage tank has combustible gas entrance, fuel outlet, and described combustible gas entrance is connected with described fuel outlet, and described fuel outlet is connected with described fuel inlet;
Condenser has gas-liquid mixture entrance, pyrolysis gas outlet, pyrolytic behavior outlet, recirculated water entrance, circulating water outlet, described gas-liquid mixture entrance exports with described gas-liquid mixture and is connected, described gas-liquid mixture is carried out condensation process by described condenser, to obtain pyrolysis gas and pyrolytic behavior;
Extraction plant has pyrolytic behavior entrance, methylene dichloride entrance, mixture export.Described pyrolytic behavior entrance exports with described pyrolytic behavior and is connected, and described extraction plant is suitable for utilizing methylene dichloride to carry out extraction treatment to described pyrolytic behavior;
Standing separation tank has entry to mixed solution, moisture outlet, extraction phase outlet, and described entry to mixed solution is connected with described mixture export, and the mixed solution that described standing separation tank is suitable for described extraction treatment to obtain is separated and obtains organic substance extraction phase and aqueous phase; And
Rectifying tower has extraction phase entrance, methylene dichloride outlet, biofuel outlet, phegma entrance, recirculated water entrance, circulating water outlet, described extraction phase entrance exports with described extraction phase and is connected, described methylene dichloride outlet is connected with methylene dichloride entrance, described rectifying tower is suitable for described organic substance extraction to carry out rectification process mutually, obtains biofuel to be separated.
By the system adopting the mud catalytic pyrolysis gasification of the utility model above-described embodiment to prepare biofuel, send in desiccation apparatus 10 after first mud being mixed with a certain amount of additive and carry out drying and other treatment; Secondly dewatered sludge is distributed into and carries out low temperature pyrogenation reaction without thermal barrier heat accumulating type rotating bed 20, generate gas-liquid mixture and pyrolytic carbon; Wherein, pyrolytic carbon through broken laggard enter fluidisation bed gasifying apparatus 30 there is steam gasification reaction, the gasification gas mixture obtained obtains combustible gas and stores in combustible gas storage tank 50 after dedusting and purifying device 40 purifies, and may be used for without thermal barrier heat accumulating type rotating bed radiator tube combustion heating; Gas-liquid mixture realizes being separated of pyrolytic behavior and pyrolysis gas by condenser 60, pyrolytic behavior and appropriate methylene dichloride are uniformly mixed in extraction plant 70, and be placed in standing separation tank 80 and carry out stratification, organic substance extraction after layering flows into rectifying tower 90 mutually and carries out rectification process, namely separablely obtains high-quality biological diesel oil.Whole system decreases the generation of foul smell, achieve the efficient combination of mud calcification dehydration and catalyse pyrolysis, not only reduce mummification energy consumption, also improve the quality of pyrolyzing sludge speed and pyrolysis product, running cost is low, heat recovery rate is high, resource utilization level is high, product economy is profitable, pyrolysis does not produce dioxin, secondary pollution is little, is beneficial to the industrial applications of pyrolyzing sludge.
According to specific embodiment of the utility model, the mud first water ratio being greater than 80% and additive respectively by storage bin enter in screw machine material machine mix after send into desiccation apparatus 10, in desiccation apparatus 10, carry out drying and other treatment.The portion of water in mud can be evaporated thus in drying process, meanwhile, also can the absorption of absorption portion by the additive that adds, also can dispel part foul smell simultaneously.According to specific embodiment of the utility model, the temperature of the drying and other treatment in above-mentioned desiccation apparatus 10 can be 100-200 degree Celsius, and then rapidly the water content of mud can be down to nearly less than 55%.
According to specific embodiment of the utility model, the above-mentioned temperature without the catalyse pyrolysis process in thermal barrier heat accumulating type rotating bed is 400-700 degree Celsius.Particularly, contriver finds, comparatively slow near furnace bottom mud mass-and heat-transfer speed, and the temperature therefore by suitably improving lower radiator tube is conducive to that pyrolyzing sludge is even, product characteristics stable.Therefore, according to concrete example of the present utility model, the temperature of upper radiator tube can be set as 400-600 DEG C, and the temperature of lower radiator tube can be set as 500-700 DEG C.The uniformity coefficient of pyrolysis can be improved thus further, improve pyrolysis efficiency.Contriver also finds, at such a temperature, the productive rate of pyrolyzing sludge liquid is the highest, and the biofuel amount that can obtain is maximum, and quality is also optimum.If the temperature of pyrolysis is too high, not only energy consumption can increase, and the acquisition amount of biofuel also can reduce, and its economic benefit is bad.
According to specific embodiment of the utility model, the gasification agent inlet of fluidized-bed gasification device 30 can be connected with the vapor outlet port of desiccation apparatus 10, can also be connected with the moisture outlet of standing separation tank 80.Aqueous phase that the water vapour obtained of drying and other treatment and extraction treatment the obtain vaporized chemical as sludge carbon can be made full use of thus.And then can save separately for the gasification reaction of sludge carbon provides vaporized chemical, save the energy, reduce the cost of lignin-sludge.
According to specific embodiment of the utility model, the recirculated water entrance of rectifying tower 90 is connected with the circulating water outlet of condenser 60, and the circulating water outlet of rectifying tower 90 is connected with the recirculated water entrance of condenser 60.And then circulating hot water needed for rectification process in rectifying tower 90 adopted the gas-liquid mixture that catalyse pyrolysis process is obtained carry out in condensation process process by the hot water heated, meanwhile, this part hot water temperature after the rectification process in rectifying tower 90 is lowered and can also returns condenser 60 and continue on for condensation process.The heat of the condensation process recovery in condensing tower 60 can be made full use of thus for the rectification process in rectifying tower 90.And then saving energy consumption.
The beneficial effect preparing each device in the system of biofuel according to the mud catalytic pyrolysis gasification of the utility model above-described embodiment is all prepared in the method for biofuel at the mud catalytic pyrolysis gasification of above-described embodiment and is embodied to some extent, does not repeat them here.
The method that mud catalytic pyrolysis gasification is prepared biofuel by the system adopting the mud catalytic pyrolysis gasification of the utility model above-described embodiment to prepare biofuel is described below in detail.The method preparing biofuel according to the mud catalytic pyrolysis gasification of the utility model specific embodiment comprises: in described mud, add additive carry out drying and other treatment, to evaporate portion of water and deodorizing; Mud after described drying and other treatment is distributed into together with described additive and carries out catalyse pyrolysis process without in thermal barrier heat accumulating type rotating bed, to obtain gas-liquid mixture and sludge carbon; By described sludge carbon and vaporized chemical, generating gasification in fluidized-bed gasification device is reacted, to obtain combustible gas and to use it for described catalyse pyrolysis process; Described gas-liquid mixture is carried out condensation process, to obtain pyrolysis gas and pyrolytic behavior; Methylene dichloride is utilized to carry out extraction treatment to described pyrolytic behavior, to obtain organic substance extraction phase and aqueous phase; And described organic substance extraction is carried out rectification process mutually, obtain biofuel to be separated.
By the method adopting the mud catalytic pyrolysis gasification of the utility model above-described embodiment to prepare biofuel, after first being mixed with a certain amount of additive by mud, send into desiccation apparatus; Secondly dewatered sludge is distributed into and carries out low temperature pyrogenation reaction without thermal barrier heat accumulating type rotating bed, generate gas-liquid mixture and pyrolytic carbon; Wherein, pyrolytic carbon laggardly enters steam gasification reaction to occur in fluidisation bed gasifying apparatus through broken, and the combustible gas obtained is for without thermal barrier heat accumulating type rotating bed radiator tube combustion heating; Gas-liquid mixture realizes being separated of pyrolytic behavior and pyrolysis gas by condenser, and pyrolytic behavior mixes with appropriate methylene dichloride, stir, after stratification, extraction phase flows into rectifying tower, obtains high-quality biological diesel oil.Whole technical process decreases the generation of foul smell, achieve the efficient combination of mud calcification dehydration and catalyse pyrolysis, not only reduce mummification energy consumption, also improve the quality of pyrolyzing sludge speed and pyrolysis product, running cost is low, heat recovery rate is high, resource utilization level is high, product economy is profitable, pyrolysis does not produce dioxin, secondary pollution is little, is beneficial to the industrial applications of pyrolyzing sludge.
The method that mud catalytic pyrolysis gasification to be prepared biofuel by the system adopting the mud catalytic pyrolysis gasification of the utility model above-described embodiment to prepare biofuel is described in detail below with reference to Fig. 2.
Drying and other treatment
According to specific embodiment of the utility model, first, in mud, add additive and carry out drying and other treatment in desiccation apparatus, to evaporate portion of water and deodorizing.Particularly, the mud that water ratio can be greater than 80% and additive respectively by storage bin enter mix in screw machine material machine after send into desiccation apparatus.
According to specific embodiment of the utility model, the temperature of the drying and other treatment in above-mentioned desiccation apparatus can be 100-200 degree Celsius, and then rapidly the water content of mud can be down to nearly less than 55%.Because calcium oxide water suction heat release can provide heat for drying equipment in additive, therefore can reduce the temperature of sludge drying process, reduce the heat needed for sludge drying process; Meanwhile, also can the sour gas such as hydrogen sulfide of absorption portion by the calcium oxide in additive, thus dispel part foul smell.
According to specific embodiment of the utility model, the above-mentioned quality adding additive in mud can be the 10-50% of mud total mass.Thus under this ratio, not only can promote sludge drying, the activation energy of mud can also be reduced, promote follow-up mud catalyse pyrolysis, thus improve output and the calorific value of pyrolysis gas, reduce the content of oxygen in biofuel simultaneously, improve the quality of biofuel.If the addition of additive is very few, all can weaken the promoter action of mummification and catalysis, the biofuel calorific value of preparation is lower; If the addition of additive is too much, can play inhibition to the pyrolysis of mud, mass-and heat-transfer is obstructed simultaneously, too increases the energy consumption without thermal barrier heat accumulating type rotating bed.
Catalyse pyrolysis process
According to specific embodiment of the utility model, above-mentioned dewatered sludge after drying and other treatment is distributed into and carries out catalyse pyrolysis process without in thermal barrier heat accumulating type rotating bed, to obtain gas-liquid mixture and sludge carbon.
According to specific embodiment of the utility model, moisture percentage in sewage sludge after mummification can be down to less than 55%, calcic mud is evenly distributed into by distribution device and carries out pyrolysis without thermal barrier heat accumulating type rotating bed, rotating bed pyrolysis oven is mainly comprised without thermal barrier heat accumulating type rotating bed, upper and lower heat storage type gas radiation pipe burner, and the auxiliary mechanism such as cloth, discharging.Its furnace bottom is rotating ring-shaped furnace bottom, be positioned in the middle of upper and lower regenerative gas radiator tube, heat storage type gas radiation pipe burner is arranged on annular furnace wall, for mud catalyse pyrolysis provides institute's heat requirement, flue gas in radiator tube and the atmosphere in rotating bed completely cut off, and rotating bed is in anaerobic state.Gas-liquid mixture outlet is set at pyrolysis zone end sidewall of the furnace body, in order to discharge the gas-liquid mixture that pyrolyzing sludge produces.
According to specific embodiment of the utility model, the temperature of above-mentioned catalyse pyrolysis process is 400-700 degree Celsius.Particularly, contriver finds, comparatively slow near furnace bottom mud mass-and heat-transfer speed, and the temperature therefore by suitably improving lower radiator tube is conducive to that pyrolyzing sludge is even, product characteristics stable.Therefore, according to concrete example of the present utility model, the temperature of upper radiator tube can be set as 400-600 DEG C, and the temperature of lower radiator tube can be set as 500-700 DEG C.The uniformity coefficient of pyrolysis can be improved thus further, improve pyrolysis efficiency.Contriver also finds, at such a temperature, the productive rate of pyrolyzing sludge liquid is the highest, and the biofuel amount that can obtain is maximum, and quality is also optimum.If the temperature of pyrolysis is too high, not only once added energy consumption, also reduce the acquisition amount of biofuel, its economic benefit is bad.
Gasification reaction generates combustible gas
According to specific embodiment of the utility model, there is steam gasification and react, to obtain combustible gas in the sludge carbon above-mentioned catalyse pyrolysis process obtained further and vaporized chemical in fluidized-bed gasification device.
According to specific embodiment of the utility model, the sludge carbon that pyrolyzing sludge produces the broken discharging machine of sealing can be adopted to carry out process is laggard enters to carry out gasification process in fluidisation bed gasifying apparatus, there is steam gasification and react.Effectively can ensure the charging stability of fluidized-bed gasification device thus, decrease parking, frequency of maintenance, the sludge carbon after fragmentation is more conducive to the carrying out of gasification reaction.
According to specific embodiment of the utility model, above-mentioned by sludge carbon generating gasification react needed for vaporized chemical can adopt the water vapour evaporating in drying and other treatment process and obtain, and then " waste water " is become " vaporized chemical " namely reduce running cost, turn improve the output of combustible gas, hot conditions has dispelled residual foul smell simultaneously, alleviate the burden of follow-up Odor control, the residue that sludge carbon gasification produces falls by landfill disposal.
According to specific embodiment of the utility model, the temperature of above-mentioned gasification reaction can be 800-900 degree Celsius.Gasification process can be carried out to sludge carbon thus, obtain combustible gas.At such a temperature, sludge carbon can be gasified totally substantially, and can obtain with CO and H
2be main gasification gas, its output is also higher, can be to use without the heating of thermal barrier heat accumulating type rotating bed radiator tube.
According to concrete example of the present utility model, the gasification reaction in fluidized-bed gasification device obtains gasification gas mixture to be needed further across obtaining recycling combustible gas after dust removal process.According to concrete example of the present utility model, combustible gas can return the fuel as above-mentioned regenerative gas radiator tube, for providing heat without the pyrolysis of the mud in thermal barrier heat accumulating type rotating bed, and then pyrolysis can be carried out preparing combustible gas by mud itself to mud, energy consumption can be saved further thus.Further, the flue gas after the combustible gas burning in regenerative gas radiator tube can pass into desiccation apparatus and carry out mummification to mud, and waste gas is discharged after treatment.Realize the sustainable utilization of combustible gas thus, and then save energy consumption further.
Extraction treatment prepares biofuel
According to specific embodiment of the utility model, further the gas-liquid mixture that above-mentioned catalyse pyrolysis process obtains is carried out condensation process, to obtain pyrolysis gas and pyrolytic behavior.Wherein pyrolysis gas can be used as product sale after alkali cleaning, the pyrolytic behavior obtained after condensation can utilize methylene dichloride to carry out extraction treatment to it, to obtain organic substance extraction phase and aqueous phase, and described organic substance extraction is carried out rectification process mutually, obtain biofuel to be separated.
According to specific embodiment of the utility model, the pyrolytic behavior under condensation enters dichloromethane extraction device, and the interpolation part by weight of methylene dichloride is 0.5-1.5:1, has whipping appts at the bottom of tank, and the organic components in pyrolytic behavior is dissolved in methylene dichloride completely.Preferably, the adding proportion of methylene dichloride is 1:1.Can extraction efficiency be improved thus, the organic constituent in pyrolytic behavior can also be made fully to be dissolved in methyl chloride completely simultaneously, and then improve percentage extraction.
According to specific embodiment of the utility model, the mixed solution in extraction plant can be discharged in standing separation tank and carry out standing separation after fully mixing, and can keep the continuity of technique thus.According to specific embodiment of the utility model, the time that extraction leaves standstill can be set to 10-30 minute.Can ensure that organic substance extraction is thought and being fully separated of aqueous phase thus fully, and then improve percentage extraction.According to concrete example of the present utility model, mixing liquid in extraction plant can flow in three standing separation tanks in parallel successively, by controlling, liquid passes in and out flow velocity, parallel pipeline valve makes organic substance extraction want to be separated completely with aqueous phase, time of repose is 10-30min, can reach the effect of continuous feed liquor, separation, fluid.
According to specific embodiment of the utility model, the aqueous phase that extraction standing separation goes out can be entered in fluidized-bed gasification device by pipeline and use as the vaporized chemical of gasification reaction.Can vaporized chemical be saved thus, and then save cost.
According to specific embodiment of the utility model, further, mutually rectification process is carried out to the organic substance extraction that extraction standing separation goes out, obtains biofuel to be separated.According to concrete example of the present utility model, rectification process can be carried out in rectifying tower, and the temperature of rectification process is 40 degrees Celsius, steaming methylene dichloride continuously, obtaining high-quality biological diesel oil by controlling reflux ratio.According to specific embodiment of the utility model, a part for the methylene dichloride steamed can return cycling extraction and utilize, and another part may be used for rectifying backflow.
According to specific embodiment of the utility model, circulating hot water needed for above-mentioned rectification process can adopt the gas-liquid mixture that catalyse pyrolysis process is obtained carry out in condensation process process by the hot water heated, meanwhile, this part hot water temperature after rectification process can also return after being lowered and continue on for condensation process.Significantly can save energy consumption thus.
Embodiment 1
Adopt certain city's sludge from wastewater treatment plant to be raw material, moisture percentage in sewage sludge is 85%, and after drying 16h through 40 DEG C, mud physical-property parameter is as table 1:
Table 1 mud physical properties
Note: mud dry base heat value is 3525kcal/kg, as received basis calorific value is 716kcal/kg.
The calcium oxide of the mud of moisture 85% and 25% (weight percent) is mixed into desiccation apparatus, removes part water by 180 DEG C of flue gas dryings.Water ratio be down to 50% calcification mud send into carry out pyrolysis without thermal barrier heat accumulating type rotating bed, the temperature of upper radiator tube is 520 DEG C, and the temperature of lower radiator tube is 650 DEG C.Pyrolytic carbon that rotating bed pyrolysis obtains through broken laggard enter fluidisation bed gasifying apparatus, the moisture generation steam gasification produced with desiccation apparatus and standing separation tank reacts, temperature of reaction is 890 DEG C, obtained gasification gas enters combustible gas storage tank after dust separation system, is heat without thermal barrier heat accumulating type rotating bed radiator tube by controlling combustible gas flow velocity.The gas-liquid mixture that rotating bed pyrolysis obtains flows in condenser by sidewall of the furnace body delivery line, and uncooled pyrolysis gas can be used for selling as product, and the pyrolytic behavior that condensation is got off enters extraction plant.In extraction plant, the rotating speed of agitator is 600r/min, and the interpolation part by weight of methylene dichloride controls 0.7.Extracting mixed solution completely flows in three standing separation tanks in parallel successively, and standing separation time controling is at 25min, and make the abundant layering of mixed solution, extraction phase enters rectifying tower.The heat supply of rectifying tower carrys out the UTILIZATION OF VESIDUAL HEAT IN of condenser, temperature required lower be 40 DEG C, less energy intensive, the part methylene chloride steamed uses for re-extract, another part be used for backflow.The biodiesel production rate that the rectifying of sludge from wastewater treatment plant air dried basis catalyse pyrolysis obtains is 28%, and calorific value reaches 37MJ/kg.
Embodiment 2
Adopt the oily sludge of certain factory, water ratio is 28%, and in mud, volatile solid component is 56% (weight percent) of dewatered sludge.
The calcium oxide of oily sludge and 15% (weight percent) is mixed into desiccation apparatus, removes part water by 150 DEG C of flue gas dryings.Water ratio be down to 17% calcification mud send into carry out pyrolysis without thermal barrier heat accumulating type rotating bed, the temperature of upper radiator tube is 450 DEG C, and the temperature of lower radiator tube is 550 DEG C.Pyrolytic carbon that rotating bed pyrolysis obtains through broken laggard enter fluidisation bed gasifying apparatus, the moisture generation steam gasification produced with desiccation apparatus and standing separation tank reacts, temperature of reaction is 900 DEG C, obtained gasification gas enters combustible gas storage tank after dust separation system, is heat without thermal barrier heat accumulating type rotating bed radiator tube by controlling combustible gas flow velocity.The gas-liquid mixture that rotating bed pyrolysis obtains flows in condenser by sidewall of the furnace body delivery line, and uncooled pyrolysis gas can be used for selling as product, and the pyrolytic behavior that condensation is got off enters extraction plant.In extraction plant, the rotating speed of agitator is 800r/min, and the interpolation part by weight of methylene dichloride controls 1.0.Extracting mixed solution completely flows in three standing separation tanks in parallel successively, and standing separation time controling is at 30min, and make the abundant layering of mixed solution, extraction phase enters rectifying tower.The heat supply of rectifying tower carrys out the UTILIZATION OF VESIDUAL HEAT IN of condenser, temperature required lower be 40 DEG C, less energy intensive, the part methylene chloride steamed uses for re-extract, another part be used for backflow.The biodiesel production rate that the rectifying of oily sludge air dried basis catalyse pyrolysis obtains is 46%, and calorific value is 41MJ/kg.
In description of the present utility model, it will be appreciated that, term " " center ", " longitudinal direction ", " transverse direction ", " length ", " width ", " thickness ", " on ", D score, " front ", " afterwards ", " left side ", " right side ", " vertically ", " level ", " top ", " end ", " interior ", " outward ", " clockwise ", " counterclockwise ", " axis ", " radial direction ", orientation or the position relationship of the instruction such as " circumference " are based on orientation shown in the drawings or position relationship, only the utility model and simplified characterization for convenience of description, instead of indicate or imply that the device of indication or element must have specific orientation, with specific azimuth configuration and operation, therefore can not be interpreted as restriction of the present utility model.
In addition, term " first ", " second " only for describing object, and can not be interpreted as instruction or hint relative importance or imply the quantity indicating indicated technical characteristic.Thus, be limited with " first ", the feature of " second " can express or impliedly comprise one or more these features.In description of the present utility model, the implication of " multiple " is two or more, unless otherwise expressly limited specifically.
In the utility model, unless otherwise clearly defined and limited, the term such as term " installation ", " being connected ", " connection ", " fixing " should be interpreted broadly, and such as, can be fixedly connected with, also can be removably connect, or integral; Can be mechanical connection, also can be electrical connection; Can be directly be connected, also indirectly can be connected by intermediary, can be the connection of two element internals or the interaction relationship of two elements.For the ordinary skill in the art, the concrete meaning of above-mentioned term in the utility model can be understood as the case may be.
In the utility model, unless otherwise clearly defined and limited, fisrt feature second feature " on " or D score can be that the first and second features directly contact, or the first and second features are by intermediary indirect contact.And, fisrt feature second feature " on ", " top " and " above " but fisrt feature directly over second feature or oblique upper, or only represent that fisrt feature level height is higher than second feature.Fisrt feature second feature " under ", " below " and " below " can be fisrt feature immediately below second feature or tiltedly below, or only represent that fisrt feature level height is less than second feature.
In the description of this specification sheets, specific features, structure, material or feature that the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means to describe in conjunction with this embodiment or example are contained at least one embodiment of the present utility model or example.In this manual, to the schematic representation of above-mentioned term need not for be identical embodiment or example.And the specific features of description, structure, material or feature can combine in one or more embodiment in office or example in an appropriate manner.In addition, when not conflicting, the feature of the different embodiment described in this specification sheets or example and different embodiment or example can carry out combining and combining by those skilled in the art.
Although illustrate and described embodiment of the present utility model above, be understandable that, above-described embodiment is exemplary, can not be interpreted as restriction of the present utility model, those of ordinary skill in the art can change above-described embodiment, revises, replace and modification in scope of the present utility model.
Claims (3)
1. mud catalytic pyrolysis gasification prepares a system for biofuel, it is characterized in that, comprising:
Desiccation apparatus, described desiccation apparatus has sludge inlet, dewatered sludge outlet, smoke inlet, vapor outlet port, and described sludge inlet is connected with feeding screw;
Without thermal barrier heat accumulating type rotating bed, described have dewatered sludge entrance, fuel inlet, gas-liquid mixture outlet, sludge carbon outlet and exhanst gas outlet without thermal barrier heat accumulating type rotating bed, and described sludge carbon exit is provided with broken discharging machine; Described dewatered sludge entrance exports with described dewatered sludge and is connected, and described exhanst gas outlet is connected with described smoke inlet;
Fluidized-bed gasification device, described fluidized-bed gasification device has sludge carbon entrance, gasification agent inlet, gasification mixed gas outlet and dedusting ash entrance, and described sludge carbon entrance exports with described sludge carbon and is connected;
Dedusting and purifying device, described dedusting and purifying device has gasification gas mixture entrance, fuel outlet and dedusting ash outlet, and described gasification gas mixture entrance is connected with described gasification mixed gas outlet, and described dedusting ash outlet is connected with described dedusting ash entrance;
Combustible gas storage tank, described combustible gas storage tank has combustible gas entrance, fuel outlet, and described combustible gas entrance is connected with described fuel outlet, and described fuel outlet is connected with described fuel inlet;
Condenser, described condenser has gas-liquid mixture entrance, pyrolysis gas outlet, pyrolytic behavior outlet, recirculated water entrance, circulating water outlet, and described gas-liquid mixture entrance exports with described gas-liquid mixture and is connected;
Extraction plant, described extraction plant has pyrolytic behavior entrance, methylene dichloride entrance, mixture export, and described pyrolytic behavior entrance exports with described pyrolytic behavior and is connected;
Standing separation tank, described standing separation tank has entry to mixed solution, moisture outlet, extraction phase outlet, and described entry to mixed solution is connected with described mixture export; And
Rectifying tower, described rectifying tower has extraction phase entrance, methylene dichloride outlet, biofuel outlet, phegma entrance, recirculated water entrance, circulating water outlet, described extraction phase entrance exports with described extraction phase and is connected, and described methylene dichloride outlet is connected with methylene dichloride entrance.
2. mud catalytic pyrolysis gasification according to claim 1 prepares the system of biofuel, it is characterized in that, described gasification agent inlet is connected with described moisture outlet with described vapor outlet port respectively.
3. mud catalytic pyrolysis gasification according to claim 1 prepares the system of biofuel, it is characterized in that, described rectifying tower recirculated water entrance is connected with condenser circulating water outlet, and described rectifying tower circulating water outlet is connected with condenser recirculated water entrance.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104789235A (en) * | 2015-04-20 | 2015-07-22 | 北京神雾环境能源科技集团股份有限公司 | Method and system for preparing biodiesel by sludge catalytic pyrolysis and gasification |
| CN112662417A (en) * | 2020-12-08 | 2021-04-16 | 杨清萍 | Continuous production system and method for preparing liquid fuel by directly liquefying biomass |
-
2015
- 2015-04-20 CN CN201520239672.8U patent/CN204607928U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104789235A (en) * | 2015-04-20 | 2015-07-22 | 北京神雾环境能源科技集团股份有限公司 | Method and system for preparing biodiesel by sludge catalytic pyrolysis and gasification |
| CN112662417A (en) * | 2020-12-08 | 2021-04-16 | 杨清萍 | Continuous production system and method for preparing liquid fuel by directly liquefying biomass |
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