CN115215527A - Sludge low-temperature drying and gasification melting coupling treatment process and system - Google Patents
Sludge low-temperature drying and gasification melting coupling treatment process and system Download PDFInfo
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Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/485—Entrained flow gasifiers
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
- C10J2300/0923—Sludge, e.g. from water treatment plant
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1861—Heat exchange between at least two process streams
Abstract
The invention provides a low-temperature drying and gasification melting coupling treatment process and system for sludge, wherein the treatment process comprises the following steps: s1, sludge drying treatment: the water content in the water-containing sludge is reduced to below 30 percent through a dehydration drying process; s2, gasification and melting treatment of the dried sludge: the dried sludge is gasified and melted in a gasification furnace with the temperature of more than 800 ℃; s3, flue gas waste heat utilization: high-temperature flue gas discharged by the gasification furnace exchanges heat with air to obtain high-temperature air, and the high-temperature air is reused in the step S2 and the step S1; s4, comprehensively utilizing the incinerator slag: the low-temperature sludge drying and gasification melting coupling treatment process and system not only realize the comprehensive utilization of heat generated by burning organic matters in the sludge, but also perform harmless treatment and resource utilization on the generated inorganic slag, do not generate toxic and harmful substances such as dioxin, and have the advantages of cleanness, environmental protection and high efficiency.
Description
Technical Field
The invention relates to the technical field of sludge treatment, in particular to a low-temperature drying and gasification melting coupling treatment process and system for sludge.
Background
The municipal sludge mainly refers to a precipitate generated in the wastewater treatment process, and comprises a comprehensive solid substance composed of solid particles such as silt, fibers, animal and plant residues and the like mixed in domestic sewage and industrial wastewater, coagulated floccules thereof, various colloids, organic matters, adsorbed metal elements, microorganisms, germs, insect eggs and the like. Wherein, the organic sludge is urban sludge rich in organic matters, and the organic sludge is mainly characterized in that: high organic matter content, high water content, easy decay and odor, and contains plant nutrients, parasitic ova, pathogenic microbes, etc. Common organic sludge is mainly: municipal sludge, livestock and poultry manure, kitchen waste, printing and dyeing sludge, drug sludge, coal slime and the like.
In order to avoid secondary pollution of the municipal sludge to the environment, sludge treatment is very important. At present, domestic and foreign sludge treatment methods mainly comprise: landfill method, compost method, drying method, incineration method, etc. The landfill method is used for carrying out landfill after the sludge is dehydrated until the water content reaches a specific range, so that not only is a large amount of land occupied, but also the pollution leakage risk is caused; in addition, the composting process can also cause soil or water pollution; therefore, the conventional sludge treatment method is a drying and burning combined method, the method firstly dehydrates and dries sludge, then sends the sludge into a burning furnace for burning, the burned furnace slag can be reused or buried, the whole sludge treatment process is simple and efficient, however, the conventional sludge burning process is very easy to generate toxic substance dioxin due to low burning temperature, and the dioxin cannot be effectively removed by the conventional flue gas treatment facility; in addition, the fly ash that the sludge incineration produced belongs to the danger and gives up, and the waste residue has heavy metal to separate out the risk. Therefore, the problem of municipal sludge treatment has become a bottleneck restricting the sewage treatment industry.
Among the urban sludge with different components and various types, organic matters can ferment to generate harmful gas to pollute air if the urban sludge is placed regardless of the characteristics of the organic sludge, and heavy metals in inorganic matters can pollute soil; if the sludge is simply buried, even the water content of the dewatered and dried sludge is more than 20 percent, which not only occupies the space of a landfill, but also threatens the underground water, so the safe disposal of the organic sludge is particularly urgent and important.
Generally, organic sludge treatment can be divided into two parts, namely organic matter treatment and inorganic matter treatment, wherein the emphasis of the organic matter treatment is to remove organic matters in sludge, and the emphasis of the inorganic matter treatment is to remove heavy metals in sludge. Meanwhile, organic matters in the sludge have a certain calorific value, and heat generated by the organic matters can be recovered through incineration; furthermore, it is also conceivable to recover inorganic substances in the sludge which are beneficial to the soil; therefore, the sludge can be treated, and the comprehensive utilization of resources can be realized.
Therefore, a sludge treatment technology is urgently needed to effectively utilize the heat generated by the incineration of organic matters in sludge and perform harmless treatment and resource utilization on the generated inorganic slag.
Disclosure of Invention
The invention designs a sludge low-temperature drying and gasification melting coupling treatment process and system, which aim to overcome the technical problems that toxic and harmful substances such as dioxin are easily generated in the existing sludge drying and incineration process, heat generated by organic matter combustion in the sludge treatment process cannot be recovered, and elements beneficial to soil in inorganic matters cannot be comprehensively utilized.
In order to solve the problems, the invention discloses a low-temperature drying and gasification melting coupling treatment process for sludge, which comprises the following steps:
s1, sludge drying treatment: reducing the water content in the water-containing sludge to below 30% by a dehydration drying process to obtain dried sludge;
s2, carrying out gasification and melting treatment on the dried sludge: conveying the dried sludge obtained by the treatment in the step S1 to a gasification furnace, and introducing air serving as combustion-supporting air into the gasification furnace to gasify and melt the dried sludge at the temperature of over 800 ℃;
s3, flue gas waste heat utilization: exchanging heat between the high-temperature flue gas discharged by the gasification furnace and air to obtain high-temperature air, and introducing a part of the high-temperature air serving as combustion-supporting air into the gasification furnace in the step S2; using another part of high-temperature air in the step S1 to dry the sludge;
s4, comprehensive utilization of the incinerator slag: and detecting the phosphorus content in the slag discharged by the gasification furnace, and determining a resource utilization mode of the slag according to the phosphorus content in the slag.
Further, the step S1 includes:
s12, sludge low-temperature drying: and (3) drying the sludge by adopting a low-temperature drying device, and reducing the water content in the sludge to be below 30% to obtain the dried sludge.
Further, the step S1 includes:
s11, mechanical dehydration of sludge: reducing the water content of the water-containing sludge to below 70% by using mechanical dewatering equipment;
s12, low-temperature sludge drying: and (4) drying the sludge treated in the step (S11) by using a low-temperature drying device, introducing part of the high-temperature air generated in the step (S3) into the low-temperature drying device, and reducing the water content in the sludge to be below 30% to obtain the dried sludge.
Further, in the step S2, the gasification furnace is an entrained flow gasification furnace; the dried sludge is fed by powder, and the granularity of the dried sludge is less than 3mm.
Further, the step S2 includes:
s21, firstly storing the dried sludge powder with the water content reduced to below 30% in a storage bin, controlling the blanking amount by a rotary feeder, and conveying the dried sludge powder into a combustion chamber at the lower part of the gasification furnace by pneumatic conveying of conveyed air; simultaneously, introducing combustion-supporting air into the gasification furnace;
s22, controlling the temperature of the first combustion chamber to be more than 900 ℃, and pyrolyzing organic matters in the sludge and melting inorganic matters in a high-temperature and oxygen-deficient environment in the first combustion chamber;
and S23, enabling the smoke in the first combustion chamber to ascend into a second combustion chamber positioned at the upper part of the gasification furnace, and carrying out peroxy combustion in the second combustion chamber, wherein in the peroxy combustion process, the temperature of the second combustion chamber is controlled to be more than 800 ℃, the retention time of the smoke in the second combustion chamber is more than 2S, the slag formed by peroxy combustion falls into a slag pool at the bottom of the gasification furnace, and the smoke carries fine ash to continue upwards and is discharged from an outlet at the upper part of the gasification furnace.
Further, in the step S21, the combustion-supporting air introduced into the gasification furnace includes primary combustion-supporting air introduced into the primary combustion chamber and secondary combustion-supporting air introduced into the secondary combustion chamber, wherein the primary combustion-supporting air is air at 300 to 400 ℃, and the flow rate of the primary combustion-supporting air is 500 to 800Nm 3 H; the secondary combustion-supporting air is normal temperature air, and the flow of the secondary combustion-supporting air is 10000-15000 Nm 3 /h。
Further, the step S3 includes:
s31, firstly carrying out primary heat exchange on high-temperature flue gas discharged by the gasification furnace and air to obtain primary high-temperature air, and introducing the primary high-temperature air serving as primary combustion-supporting air into the gasification furnace in the step S2;
s32, continuously carrying out secondary heat exchange on the flue gas subjected to the primary heat exchange and air to obtain secondary high-temperature air, and introducing the secondary high-temperature air into the low-temperature drying equipment in the step S1 to dry sludge; and the flue gas after secondary heat exchange is subjected to dust removal, desulfurization and denitrification treatment and then is discharged to the atmosphere.
Further, in the step S4, determining a resource utilization mode of the slag according to the phosphorus content in the slag includes:
s41, when the phosphorus content in the slag is more than or equal to 8%, carrying out ore dressing on the slag to obtain concentrate with higher phosphorus content and tailings with lower phosphorus content, wherein the concentrate is used as phosphate ore, and the tailings are used as a phosphorus-containing curing agent or a building raw material;
s42, when the phosphorus content in the slag is less than 8%, directly using the slag as a phosphorus-containing curing agent or a building raw material.
Further, before the step S2, the content of heavy metals in the sludge is detected, when the content of heavy metals in the sludge exceeds the standard, fuel is filled into the gasification furnace used in the step S2, the temperature in the gasification furnace is increased to over 1200 ℃, the slag in the gasification furnace is melted into a vitreous state, and then the slag is crushed into the sludge molten phosphate fertilizer.
A system of a low-temperature sludge drying and gasification fusion coupling treatment process is used for the low-temperature sludge drying and gasification fusion coupling treatment process.
The low-temperature sludge drying and gasification melting coupling treatment process and system have the following advantages:
the sludge low-temperature drying and gasification melting coupling treatment process and system adopt an integrated process of sludge drying and gasification melting coupling, organic sludge after dehydration and drying is gasified at high temperature through an entrained-flow bed gasifier, the entrained-flow bed gasifier is enabled to achieve gasification self-sustaining operation by utilizing the self heat value of the sludge, and high-temperature smoke generated at the same time generates high-temperature air through a heat exchanger, and the high-temperature air can be supplied to low-temperature drying equipment at the front end and used as combustion-supporting air of the gasifier, so that the energy consumption of low-temperature drying can be reduced, the full utilization of smoke waste heat is realized, and the purposes of saving energy and reducing cost are achieved;
secondly, in the sludge treatment process, the slag after gasification and melting treatment can be comprehensively recycled according to different phosphorus contents;
thirdly, in the sludge treatment process, products obtained after the sludge is gasified and melted do not need to be buried, so that the environmental risk is reduced, and the land is saved;
fourthly, the high-temperature flue gas discharged by the gasification furnace does not contain toxic and harmful substances such as dioxin and the like.
In a word, the sludge low-temperature drying and gasification melting coupling treatment process and system realize comprehensive utilization of heat generated by burning organic matters in sludge, perform harmless treatment and resource utilization on generated inorganic slag, do not generate toxic and harmful substances such as dioxin, and have the advantages of cleanness, environmental protection and high efficiency.
Drawings
FIG. 1 is a flow chart of a low-temperature sludge drying and gasification melting coupling treatment process according to the invention;
FIG. 2 is a schematic structural diagram of a low-temperature sludge drying and gasification fusion coupling disposal system according to the present invention;
FIG. 3 is a schematic view of the structure of the gasification furnace;
FIG. 4 is a schematic view of the mixing chamber of the present invention.
Description of reference numerals:
1. a sludge drying apparatus; 101. a mechanical dewatering device; 102. a low temperature drying apparatus; 2. a gasification furnace; 201. a combustion chamber; 202. a second combustion chamber; 203. a nozzle; 2031. a first nozzle; 2032. a second nozzle; 2033. a third nozzle; 204. a smoke discharge port; 205. a slag discharge port; 206. a spray cooling port; 3. a high temperature heat exchanger; 4. a low temperature heat exchanger; 5. a tail gas treatment device; 501. a bag-type dust collector 501; 502. a wet scrubbing tower; 503. a first chimney; 6. a mixing chamber; 601. a first air inlet; 602. A second air inlet; 603. an air outlet; 604. a mixing chamber; 7. a hot blast stove; 8. a hot air treatment device; 801. a condenser; 802. a spray tower; 803. a second chimney; 9. a slag treatment device; 901. a slag cooler; 902. provided is mineral processing equipment.
Detailed Description
In order to make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in detail below.
As shown in fig. 1 to 4, a low-temperature sludge drying and gasification fusion coupling treatment process comprises the following steps:
s1, sludge drying treatment: reducing the water content in the water-containing sludge to be below 30 percent by a dehydration drying process to obtain dried sludge;
s2, gasification and melting treatment of the dried sludge: conveying the dried sludge obtained by the treatment in the step S1 to a gasification furnace, and introducing air serving as combustion-supporting air into the gasification furnace to gasify and melt the dried sludge at the temperature of over 800 ℃;
s3, flue gas waste heat utilization: after the heat exchange between the high-temperature flue gas discharged by the gasification furnace and air is carried out, high-temperature air is obtained, and a part of the high-temperature air is taken as combustion-supporting air and is introduced into the gasification furnace in the step S2; and using the other part of high-temperature air in the step S1 to dry the sludge.
S4, comprehensive utilization of the incinerator slag: and detecting the phosphorus content in the slag discharged by the gasification furnace, and determining a resource utilization mode of the slag according to the phosphorus content in the slag.
Wherein, the steps S3 and S4 are parallel steps without the sequence.
As some examples of the application, the sludge can be organic sludge, and can also be other sludge with higher heat value, such as sludge with the heat value higher than 1200 Kcal/kg.
Preferably, the sludge is organic sludge.
Further, the step S1 includes:
s11, mechanical dehydration of sludge: reducing the water content of the water-containing sludge to below 70% by using mechanical dewatering equipment;
s12, low-temperature sludge drying: and (4) drying the sludge treated in the step (S11) by using low-temperature drying equipment, and reducing the water content in the sludge to be below 30% to obtain the dried sludge.
As some examples of the present application, in the step S11, one or more of a plate-and-frame filter press, a stacked-screw sludge dewatering machine, a belt filter press, and the like may be used to reduce the water content in the water-containing sludge to below 70%.
Preferably, in step S11, the water content in the water-containing sludge may be reduced to 70% or less by using a plate-and-frame filter press.
Through the treatment of the step S11, partial moisture in the sludge can be removed, the energy consumption of the subsequent step S12 during low-temperature sludge drying is reduced, and the low-temperature sludge drying efficiency is improved.
More preferably, in step S11, the water content in the water-containing sludge is reduced to between 70% and 60%, such as about 65%, by the mechanical dewatering equipment, so that on one hand, the treatment efficiency of the mechanical dewatering equipment can be improved; on the other hand, it was found through trial and error that: when the sludge with the water content reduced to 70-60% is subjected to low-temperature sludge drying in the subsequent step S12, the sludge can be dried to the water content reduced to below 30% by using the residual heat of the high-temperature flue gas generated by the rear-end gasification furnace, and other auxiliary heat sources are not required to be added.
As some examples of the present application, in the step S11, the purpose of reducing the water content in the water-containing sludge to below 70% by the mechanical dewatering device is to ensure that the water content of the sludge can be controlled to below 70% before the sludge is subjected to low-temperature drying in the step S12, so when the water content in the water-containing sludge to be treated is below 70%, the step S11 may not be performed, and the step S12 may be performed directly.
As some embodiments of the present application, in step S12, after the heat exchange between the high-temperature flue gas generated by the rear-end gasification furnace and the air is performed, part of the obtained high-temperature air is introduced into the low-temperature drying apparatus in step S12, the heat of the high-temperature air is used to dry the sludge until the water content is reduced to below 30%, and the low-temperature drying apparatus adopts the heat of the high-temperature air to replace a common heat source, such as a heat pump type heat source, so that the utilization of the waste heat of the high-temperature flue gas can be realized, and the energy consumption of the low-temperature drying apparatus can be reduced.
As some embodiments of the present application, in the step S12, while the sludge is dried by using the residual heat of the high-temperature flue gas, a backup heat source, such as a hot air generating device, may be added to the low-temperature drying apparatus, and the backup heat source may supplement heat to the low-temperature drying apparatus when the heat value of the sludge is relatively low, such as the heat value of the dried sludge is lower than 1200 Kcal/kg.
As some embodiments of the application, the standby heat source can also supplement heat to the low-temperature drying equipment when the water content of the sludge entering the low-temperature drying equipment is higher than 70%, so that the dried sludge with the water content of below 30% can be obtained after the treatment of the step S1.
Specifically, as some embodiments of this application, reserve heat source is the natural gas hot-blast furnace, the natural gas hot-blast furnace produces hot-blastly through burning the natural gas, later mix with room temperature air, the high temperature air that produces through the high temperature flue gas heat transfer in the hot-blast mixing chamber of pressure regulating formula, reaches behind the pressure and the temperature demand of low temperature mummification equipment, let in the low temperature mummification equipment, take away the moisture in the mud through the heat exchange, the gas of low temperature mummification equipment combustion gas is through condenser, spray column processing back, finally discharges through the chimney.
Preferably, the low-temperature drying equipment has the requirement of pressure generally being slight negative pressure and the requirement of temperature generally being 70-90 ℃.
In the step S1, the purpose of dehydration and drying treatment of the water-containing sludge is mainly to improve the heat value of the sludge and provide a basis for subsequent passing through the step S2 for sludge gasification and melting treatment.
Preferably, in the step S2, the gasification furnace is an entrained flow gasification furnace, and tests show that: the mode of entrained flow bed gasification melting is adopted, the temperature in the gasifier can reach 800-1500 ℃, and the temperature in the gasifier can meet the requirement of sludge gasification melting.
Preferably, the gasification furnace is a multi-nozzle entrained-flow pyrolysis gasification furnace.
Furthermore, in the step S2, the dried sludge is fed by powder, and the particle size of the dried sludge is less than 3mm; preferably, the particle size of the dried sludge is less than 1mm.
In the step S2, when the sludge is fed by powder, the heating specific surface area of the sludge is large, the thermal efficiency is high, the multi-nozzle entrained-flow bed pyrolysis gasification furnace is used, the mixing effect of the sludge and air is excellent, the retention time of the sludge in the furnace is short, the reaction rate is high, the conversion rate is high, and compared with other gasification incineration modes, the sludge is easier to gasify and melt. Moreover, when the sludge is fed by powder, granulation is not needed, and equipment investment can be reduced.
In addition, in the entrained-flow bed gasification furnace, the entrained-flow bed gasification furnace can achieve self-sustaining stable operation by utilizing the self heat value of the dried sludge, thereby greatly reducing the fuel consumption and achieving the aim of carbon neutralization. Simultaneously, compared with other gasification incineration equipment, the entrained flow gasifier that this application adopted is small, simple structure, and equipment cost is low.
Further, in the step S2, the process of gasification and melting of the dried sludge includes:
s21, firstly storing the dried sludge powder with the water content reduced to below 30% in a storage bin, controlling the blanking amount by a rotary feeder, and conveying the dried sludge powder into a combustion chamber at the lower part of the gasification furnace by pneumatic conveying of conveyed air; simultaneously, introducing combustion-supporting air into the gasification furnace;
s22, controlling the temperature of the first combustion chamber to be more than 900 ℃, and under the high-temperature and oxygen-deficient environment in the first combustion chamber, pyrolyzing organic matters in the sludge and melting inorganic matters under the action of high temperature;
s23, the flue gas in the first combustion chamber rises to enter a second combustion chamber positioned at the upper part of the gasification furnace, the peroxy combustion is carried out in the second combustion chamber, in the peroxy combustion process, the temperature of the second combustion chamber is controlled to be more than 800 ℃, the residence time of the flue gas in the second combustion chamber is more than 2S, inorganic matter slag formed by the peroxy combustion falls into a slag pool at the bottom of the gasification furnace, and the flue gas carries fine ash to continue upwards and is discharged from an outlet at the upper part of the gasification furnace.
Preferably, in step S23, the temperature of the second combustion chamber is controlled to be 850 ℃.
More preferably, in the step S22, the temperature of the first combustion chamber is controlled to reach 900 to 1000 ℃; in the step S23, the temperature of the second combustion chamber is controlled to reach 850 to 950 ℃.
Further, in the step S21, the dried sludge powder is blown into the gasification furnace through conveying air, the temperature of the conveying air is 100-180 ℃, and the flow rate of the conveying air is 200-500 Nm 3 /h。
Further, in the step S2, the blowing speed of the dried sludge powder into the gasification furnace through the conveying air is 30 to 80t/d.
Further, in the step S21, the combustion-supporting air introduced into the gasifier includes primary combustion-supporting air introduced into the first combustion chamber and secondary combustion-supporting air introduced into the second combustion chamber, wherein the primary combustion-supporting air is air at 300 to 400 ℃, and the flow rate of the primary combustion-supporting air is 500 to 800Nm 3 H; the secondary combustion-supporting air is normal temperature air, and the flow of the secondary combustion-supporting air is 10000-15000 Nm 3 H is the ratio of the total weight of the catalyst to the total weight of the catalyst. The primary combustion-supporting air adopts part of high-temperature air obtained after heat exchange between high-temperature flue gas discharged by the gasification furnace and air, and the secondary combustion-supporting air adopts normal-temperature air.
Further, in the step S2, the internal pressure of the gasification furnace is a slight positive pressure state, preferably 8 to 13kpa, and more preferably 10kpa.
Further, in the step S2, the carbon conversion rate of the gasification furnace may reach 99% or more.
Specifically, in the gasification furnace, the dried sludge and air mainly react as follows:
and (3) pyrolysis process: cracking reaction organic matter → CO + H 2 +CH 4 +C 2 +…
Oxidation reaction C +1/2O 2 ＝CO；C+O 2 ＝CO 2
Reduction reaction of C + CO 2 ＝2CO；C+H 2 O＝CO+H 2 ；CO+H 2 O＝CO 2 +H 2 The peroxide combustion process: 2CO + O 2 ＝2CO 2 ；2H 2 +O 2 ＝2H 2 O
Further, the following results are obtained through detection and analysis: the main components of the flue gas discharged from the outlet at the top of the gasification furnace are as follows: n is a radical of 2 、O 2 、CO 2 、H 2 O、SO 2 And the like, wherein the contents of the components are shown in the following table 1:
TABLE 1 main components and contents of flue gas discharged from gasification furnace
| Components | N 2 | O 2 | CO 2 | H 2 O | SO 2 |
| Content (Vt%) | 53～68 | 8～14 | 6～10 | 16～25 | 0.1～0.3 |
Therefore, in the gasification and melting process, the organic matters are completely pyrolyzed and gasified in the gasifier to generate clean gas, the temperature of the flue gas reaches about 700-900 ℃, harmful substances such as dioxin are not generated, the subsequent flue gas treatment is simple, and the flue gas treatment cost can be saved.
Further, after heat exchange is carried out between the flue gas discharged from the outlet at the upper part of the gasification furnace and air, the flue gas enters a bag-type dust remover for dust removal treatment, and then is subjected to desulfurization and denitrification treatment by a wet washing tower and then is discharged through a chimney.
Further, the step S3 includes the steps of:
s31, firstly carrying out primary heat exchange on high-temperature flue gas discharged by the gasification furnace and air to obtain primary high-temperature air, and introducing the primary high-temperature air into the gasification furnace in the step S2 as primary combustion-supporting air;
s32, continuously carrying out secondary heat exchange on the flue gas subjected to the primary heat exchange and air to obtain secondary high-temperature air, and introducing the secondary high-temperature air into the low-temperature drying device in the step S1 to dry sludge; and introducing the flue gas subjected to secondary heat exchange into a bag-type dust remover for dust removal treatment, performing desulfurization and denitrification treatment in a wet washing tower, and discharging through a chimney.
Specifically, the temperature of the flue gas discharged from the outlet at the top of the gasification furnace is about 700 to 900 ℃, the temperature of the flue gas is reduced to 400 to 500 ℃ after the primary heat exchange in the step S31, and the temperature of the obtained primary high-temperature air is about 300 to 400 ℃, and the primary high-temperature air can be directly used as primary combustion air at the temperature of 300 to 400 ℃.
In addition, after the flue gas after primary heat exchange is continuously subjected to secondary heat exchange with air, the temperature of the flue gas is reduced to 150-200 ℃, the temperature of the obtained secondary high-temperature air is about 200-300 ℃, and the secondary high-temperature air can be introduced into the low-temperature drying equipment in the step S1 to dry sludge.
Further, in the step S4, determining a resource utilization mode of the slag according to the phosphorus content in the slag includes:
s41, when the phosphorus content in the slag is more than or equal to 8%, carrying out ore dressing on the slag to obtain concentrate with higher phosphorus content and tailings with lower phosphorus content, wherein the concentrate is used as phosphate ore, and the tailings are used as a phosphorus-containing curing agent or a building raw material;
and S42, when the phosphorus content in the slag is less than 8%, directly using the slag as a phosphorus-containing curing agent or a building raw material.
The phosphorus content in the slag in the step S4 is P in the slag 2 O 5 Weight ofDividing the content.
Specifically, the following were found through investigation: due to different sludge components of each municipal sludge plant, the obtained slag component of the gasification furnace has fluctuation, wherein P in the gasification furnace slag 2 O 5 The content is usually in the range of 8% to 12%. When the phosphorus content in the slag is more than or equal to 8 percent, the phosphorus content in the slag can be improved by a phosphate ore dressing technology, preferably a photoelectric ore dressing technology, so that the phosphorus content in the concentrate obtained by ore dressing can reach the phosphorus content of low-grade phosphate ore, preferably, the phosphorus content in the concentrate obtained by ore dressing is more than or equal to 18 percent, and more preferably more than or equal to 25 percent.
In addition, the tailings after mineral separation mainly contain SiO 2 、Al 2 O 3 、CaO、Fe 2 O 3 And the like, and also contains a small amount of phosphorus, so that the tailings after mineral separation can be prepared into a phosphorus-containing curing agent for curing river sludge or be used as a raw material for building materials such as bricks, cement and the like.
When the phosphorus content in the slag is less than 8 percent, the slag can be directly used as a phosphorus-containing curing agent or raw materials of building materials such as bricks, cement and the like because the phosphorus content of the slag is not high and the phosphorus recovery value is low.
Further, before the step S2 is performed, the content of heavy metals in the sludge should be detected, and when the content of heavy metals in the sludge exceeds the standard, the content of heavy metals in the slag is too high, and at this time, no matter how much the content of phosphorus in the slag is, the slag cannot be used as a phosphorus-containing curing agent or a raw material of building materials such as bricks and cement, and the step S2 should be adjusted, specifically:
and (3) filling fuels such as natural gas into the gasification furnace used in the step (S2), and raising the temperature in the gasification furnace to over 1200 ℃, preferably 1300-1500 ℃, so that the slag in the gasification furnace can be melted into a vitreous state to achieve harmlessness, the vitreous slag can be used for paving roads and can also be used as raw materials for manufacturing landscape bricks, cement and the like, and the vitreous slag can be crushed to prepare a sludge-melted phosphate fertilizer. Preferably, the temperature of the first combustion chamber of the gasification furnace is increased to over 1200 ℃, so that the slag in the gasification furnace can be melted into a vitreous state, and after the vitreous state slag is crushed, a sludge molten phosphate fertilizer can be directly obtained, and the sludge molten phosphate fertilizer is rich in elements such as phosphorus, calcium, magnesium and the like and can be used for replacing the existing calcium magnesium phosphate fertilizer.
Wherein, for the content of the heavy metal in the sludge, each city or country has different standards, and whether the content of the heavy metal in the sludge exceeds the standard can be judged by referring to the corresponding standards.
In addition, in the application, if the heavy metal in the sludge has a recovery value, the hot slag can be directly introduced into a smelting furnace, preferably a submerged arc furnace, for smelting without water quenching slag, and the valuable metal can be recovered.
In addition, this application still provides a mud low temperature mummification and gasification melting coupling processing system, the system is used for realizing foretell mud low temperature mummification and gasification melting coupling processing technology, the system is including the mud mummification equipment 1, gasifier 2, heat exchanger and the tail gas processing apparatus 5 that connect gradually, wherein:
the sludge discharge port of the sludge drying equipment 1 is connected with the feeding nozzle 203 in the gasification furnace 2;
the flue gas discharge port 204 of the gasification furnace 2 is connected with the inlet of the high-temperature medium channel in the heat exchanger, the inlet of the low-temperature medium channel in the heat exchanger is connected with the external atmosphere, the high-temperature flue gas discharged from the flue gas discharge port 204 of the gasification furnace 2 and the external atmosphere exchange heat through the heat exchanger to generate high-temperature air, wherein one part of the high-temperature air is introduced into the gasification furnace 2 as combustion-supporting air, and the other part of the high-temperature air is introduced into the sludge drying equipment 1 to dry sludge;
and introducing the flue gas discharged from the outlet of the high-temperature medium channel in the heat exchanger into the tail gas treatment device 5 for tail gas treatment.
Further, the heat exchanger includes that set gradually: a high temperature heat exchanger 3 and a low temperature heat exchanger 4, wherein:
the flue gas discharge port 204 of the gasification furnace 2 is connected with the inlet of the high-temperature medium channel in the high-temperature heat exchanger 3, the inlet of the low-temperature medium channel in the high-temperature heat exchanger 3 is connected with the external atmosphere, the high-temperature flue gas discharged from the flue gas discharge port 204 of the gasification furnace 2 and the external atmosphere perform primary heat exchange through the high-temperature heat exchanger 3, primary high-temperature air is discharged from the outlet of the low-temperature medium channel in the high-temperature heat exchanger 3 after the primary heat exchange, the outlet of the low-temperature medium channel in the high-temperature heat exchanger 3 is connected with the air inlet nozzle 203 in the gasification furnace 2, and the primary high-temperature air generated by the primary heat exchange is introduced into the gasification furnace 2;
the inlet of the high-temperature medium channel in the low-temperature heat exchanger 4 is connected with the outlet of the high-temperature medium channel in the high-temperature heat exchanger 3, the inlet of the low-temperature medium channel in the low-temperature heat exchanger 4 is connected with the external atmosphere, high-temperature flue gas after primary heat exchange and the external atmosphere continue to pass through the low-temperature heat exchanger 4 for secondary heat exchange, secondary high-temperature air is discharged from the outlet of the low-temperature medium channel in the low-temperature heat exchanger 4 after the secondary heat exchange, the outlet of the low-temperature medium channel in the low-temperature heat exchanger 4 is connected with the air inlet of the sludge drying equipment 1, the secondary high-temperature air generated by the secondary heat exchange is introduced into the sludge drying equipment 1, and flue gas discharged from the outlet of the high-temperature medium channel in the low-temperature heat exchanger 4 is introduced into the tail gas treatment device 5 for tail gas treatment.
In the working process, firstly, water-containing sludge is conveyed into the sludge drying equipment 1, and is dehydrated and dried by the sludge drying equipment 1 until the water content is reduced to below 30 percent to obtain dried sludge; and then the dried sludge is sent into the gasification furnace 2 through a feeding nozzle 203, meanwhile, primary high-temperature air discharged by the high-temperature heat exchanger 3 and normal-temperature air are sent into the gasification furnace 2 as combustion-supporting air, the dried sludge is subjected to self-sustaining combustion in the gasification furnace 2 under the action of high temperature in the furnace, high-temperature flue gas generated by combustion is discharged through a flue gas discharge port 204 and then sequentially introduced into high-temperature medium channels in the high-temperature heat exchanger 3 and the low-temperature heat exchanger 4, and after primary and secondary heat exchange, the flue gas is introduced into the tail gas treatment device 5 for tail gas treatment and then is discharged to the atmosphere.
Further, the sludge drying device 1 comprises a mechanical dewatering device 101 and a low-temperature drying device 102 which are connected in sequence, and after the water-containing sludge passes through the mechanical dewatering device 101 and the low-temperature drying device 102, the water content is reduced to below 30% to form the dried sludge.
As some examples of the present application, the mechanical dewatering apparatus 101 may be one or a combination of plate and frame filter presses, stacked-screw sludge dewaterers, belt filter presses, and the like.
Preferably, the mechanical dewatering device 101 is a plate and frame filter press.
Further, a low-temperature medium outlet in the low-temperature heat exchanger 4 is communicated with an air inlet of the low-temperature drying device 102 through a mixing chamber 6.
Further, the gasification furnace 2 includes a first combustion chamber 201 located at a lower portion thereof and a second combustion chamber 202 located at an upper portion thereof, and an upper end of the first combustion chamber 201 is communicated with a lower end of the second combustion chamber 202.
Further, a plurality of nozzles 203 are arranged on the side wall of the gasification furnace 2, and the nozzles 203 are used for injecting combustion air and dried sludge into the furnace.
Furthermore, the nozzles 203 at least include a first nozzle 2031, a second nozzle 2032 and a third nozzle 2033, the first nozzle 2031 is a feeding nozzle, and the air and the dried sludge powder are conveyed into the gasification furnace 2 through the first nozzle 2031; the second nozzle 2032 and the third nozzle 2033 are both air intake nozzles, and the second nozzle 2032 is used for feeding primary combustion air into the gasification furnace 2; the third nozzle 2033 is used for feeding secondary combustion air into the gasifier 2; the primary combustion-supporting air is primary high-temperature air discharged by the high-temperature heat exchanger 3, and the secondary combustion-supporting air is normal-temperature air.
Preferably, the nozzle 203 is disposed on a side wall of a middle lower portion of the gasification furnace 2, that is, when a total height of the gasification furnace 2 is denoted as H, a height of the nozzle 203 is between 0.2H and 0.5H.
Preferably, the first nozzle 2031 and the second nozzle 2032 are disposed on a side wall of the first combustion chamber 201, and the first nozzle 2031 is located on an upper side of the second nozzle 2032; the third nozzle 2033 is disposed on a side wall of the second combustion chamber 202.
As some embodiments of the present application, six nozzles 203 are disposed on the sidewall of the gasification furnace 2, the six nozzles 203 include two first nozzles 2031, two second nozzles 2032, and two third nozzles 2033, and the two first nozzles 2031, the second nozzles 2032, and the third nozzles 2033 are respectively disposed opposite to each other by 180 °.
Preferably, the outlets of the first nozzle 2031 and the second nozzle 2032 are arranged to be inclined downward, and the third nozzle 2033 is arranged to be horizontal.
Further, the gasification furnace 2 further comprises a flue gas discharge port 204 and a spray cooling port 206 at the upper part thereof, and the spray cooling port 206 can spray water mist downwards from the top of the gasification furnace 2 to control the temperature of the high-temperature flue gas.
Further, the tail gas processing apparatus 5 includes a bag-type dust collector 501, a wet scrubbing tower 502 and a first chimney 503, a feed inlet of the bag-type dust collector 501 is connected with an outlet of a high-temperature medium channel in the low-temperature heat exchanger 4, a feed inlet of the wet scrubbing tower 502 is connected with a clean gas discharge port of the bag-type dust collector 501, a clean gas outlet of the wet scrubbing tower 502 is connected with the first chimney 503, and flue gas discharged from the gasification furnace 2 is subjected to primary heat exchange and secondary heat exchange, purified by the tail gas processing apparatus 5 and then discharged to the atmosphere through the first chimney 503.
Further, mixing chamber 6 has first air inlet 601, second air inlet 602 and gas outlet 603, first air inlet 601 and outside atmosphere are connected, second air inlet 602 with the exit linkage of the low temperature medium passageway in low temperature heat exchanger 4, gas outlet 603 and the air inlet of low temperature mummification machine 102 are connected, in addition, mixing chamber 6 still has mixing chamber 604, first air inlet 601, second air inlet 602 and gas outlet 603 all with mixing chamber 604 is connected, the air warp of first air inlet 601, the input of second air inlet 602 after mixing chamber 604 is even, pass through gas outlet 603 is arranged to in the low temperature mummification machine 102.
As some embodiments of this application, as shown in fig. 4, mixing chamber 6 is established inner tube and outer tube together by the cover and is formed, the both ends of outer tube are sealed, the both ends of inner tube are uncovered, form respectively first air inlet 601 and gas outlet 603 set up on the lateral wall of outer tube second air inlet 602 is located set up the through-hole on the inside inner tube lateral wall of outer tube, the through-hole will outer tube and inner tube intercommunication make via the secondary high temperature air that first air inlet 601 got into and via the air that second air inlet 602 got into can mix in the inner tube, later pass through gas outlet 603 discharges, so, the inner space of inner tube and outer tube and the through-hole have constituted mixing chamber 604 jointly, make mixing chamber 6 can be fast with the gas mixture homogeneous that two kinds of temperatures are different.
As some embodiments of the present application, the temperature of the gas discharged into the mixing chamber 604 through the first gas inlet 601 is room temperature, the temperature of the gas discharged into the mixing chamber 604 through the second gas inlet 602 is 250 ℃, and the temperature of the gas discharged through the gas outlet 603 after being uniformly mixed in the mixing chamber 604 is 70 to 90 ℃.
Furthermore, the system for low-temperature sludge drying and gasification fusion coupling treatment further comprises: and a hot air outlet of the hot air furnace 7 is communicated with the mixing chamber 604, so that when the heat value of the sludge is lower, heat is supplemented to the low-temperature drying equipment 102 through the mixing chamber 6.
Further, the system for low-temperature sludge drying and gasification fusion coupling treatment further comprises: and the hot air treatment device 8 is communicated with an air outlet of the low-temperature drying machine 102, and is used for purifying hot air discharged by the low-temperature drying machine 102.
Further, the hot air processing apparatus 8 includes: the condenser 801, the spray tower 802 and the second chimney 803, the air inlet of the condenser 801 is communicated with the exhaust port of the low-temperature dryer 102, the feed inlet of the spray tower 802 is communicated with the exhaust port of the condenser 801, and the second chimney 803 is communicated with the exhaust port of the spray tower 802.
Further, the system for low-temperature sludge drying and gasification fusion coupling treatment further comprises: a slag processing apparatus 9, the slag processing apparatus 9 including a slag cooler 901 and a beneficiation plant 902, the slag cooler 901 communicating with the slag discharge port 205 of the gasifier 2 to cool the slag to room temperature; the feed inlet of the beneficiation equipment 902 is communicated with the slag cooler 901, and the slag cooled to room temperature by the slag cooler 901 can be sent to the beneficiation equipment 902 for beneficiation treatment.
Preferably, the beneficiation equipment 902 is photoelectric beneficiation equipment.
The contents of the substances described in the present application, such as the water content of sludge and the phosphorus content in slag, are not particularly limited, and are all in weight percent.
The sludge low-temperature drying and gasification fusion coupling treatment process and system described in the present application are exemplified by the following specific examples:
example 1
The water-containing organic sludge with the heavy metal content not exceeding the standard has the water content of 200t/d, the total solid content, namely the total content of organic matters and inorganic matters is 20 percent, in the organic sludge, the proportion of the organic matters accounting for the total solid content is generally 40 to 60 percent, and is assumed to be 50 percent, so that the proportion of the organic matters to the inorganic matters is respectively 10 percent.
The amount of sludge after mechanical dewatering was 114.3t/d, wherein the water content of the sludge was 65%, the organic matter ratio was 17.5%, and the inorganic matter ratio was 17.5%. And then the amount of the dried sludge obtained after low-temperature drying is 57.1t/d, namely 2.38t/h, and at the moment, the water content in the sludge is 30%, the organic matter ratio is 35%, and the inorganic matter ratio is 35%.
The dried sludge passes through the temperature of 150 ℃ and the speed of 350Nm 3 The/h of conveying air is sent into a combustion chamber at the lower part of the gasification furnace. At the same time, the heat produced by primary heat exchange is introduced into a combustion chamber at 400 deg.C and 650Nm 3 The first high temperature air of/h is used as the first combustion-supporting air, the temperature in the first combustion chamber is controlled to be about 900-950 ℃, the sludge is pyrolyzed and gasified in the first combustion chamber, and the gasified fuel gas (the main components are CO, CO2, N2 and water vapor) carries a part of fly ash (the fly ash rate is about 1)0%) into the second combustion chamber. Introducing 25 ℃ C, 14134Nm into a second combustion chamber 3 And/h secondary combustion-supporting air is used for carrying out peroxy combustion on the gasified fuel gas. The temperature of the secondary combustion chamber is controlled to be 850-900 ℃, and the residence time of the flue gas is 2-5S. Meanwhile, a cooling water spray nozzle is arranged at the top of the gasification furnace, so that the over-high smoke temperature is prevented, and the consumption of cooling water is 1.35t/h. And controlling the oxygen content of the flue gas at the outlet of the second combustion chamber to be about 10 percent. 16453Nm of outlet flue gas amount of the second combustion chamber 3/ h, temperature about 700 ℃.
The high-temperature flue gas discharged by the gasification furnace is subjected to two-stage heat exchange, the temperature is reduced to 180 ℃, and then the high-temperature flue gas enters a bag-type dust remover for dust removal and is discharged after wet desulfurization and denitration; and simultaneously generating primary high-temperature air at 400 ℃ and secondary high-temperature air at 300 ℃, introducing the primary high-temperature air into a primary combustion chamber as primary combustion-supporting air, introducing the secondary high-temperature air into a mixing chamber, uniformly mixing with room-temperature air, and introducing into low-temperature drying equipment.
The gasification furnace slag of the combustion chamber is discharged through a furnace slag discharge port at the bottom of the combustion chamber, and the slag discharge amount is 0.75t/h. After the phosphorus content of the gasification furnace slag is measured, the resource utilization direction of the gasification furnace slag is judged.
After the components of the slag discharged from the gasification furnace were measured, the following table 2 was obtained:
table 2 main components and contents of slag discharged from gasification furnace in example 1
| Components | SiO 2 | Al 2 O 3 | CaO | Fe 2 O 3 | MgO | K 2 O |
| Content (wt%) | 27.8 | 11.1 | 17.3 | 28.0 | 2.56 | 0.91 |
| Components | TiO 2 | Na 2 O | P 2 O 5 | SO 3 | Others are | / |
| Content (wt%) | 0.73 | 0.93 | 9.7 | 0.4 | 0.6 | / |
According to the inspection, when the phosphorus content in the obtained slag is 9.7 percent, namely more than or equal to 8 percent, the slag is subjected to mineral separation to obtain concentrate with the phosphorus content of 22 percent and tailings with the phosphorus content of 3 percent, the concentrate is used as phosphate ore, and the tailings are used as phosphorus-containing curing agents or building raw materials.
Example 2
Organic sludge containing heavy metals of 200t/d, in which the water content is 80% and the total solid content, i.e., the total content of organic matter + inorganic matter, is 20%, in organic sludge, the proportion of organic matter in the total solid content is generally 40% to 60%, here, 50% is assumed, and thus the ratio of organic matter to inorganic matter is 10%, respectively.
The amount of sludge after mechanical dehydration became 114.3t/d, wherein the water content of the sludge was 65%, the organic matter ratio was 17.5%, and the inorganic matter ratio was 17.5%. Then the sludge which is dried at low temperature and enters the gasification furnace is 57.1t/d, namely 2.38t/h, and at the moment, the water content of the sludge is 30%, the organic matter ratio is 35%, and the inorganic matter ratio is 35%.
The dried sludge passes through the temperature of 150 ℃ and the speed of 350Nm 3 The delivery air is sent into a combustion chamber at the lower part of the gasification furnace. At the same time, 300Nm is introduced into a combustion chamber 3 H auxiliary fuel natural gas and 400 ℃ and 4000Nm 3 The primary combustion-supporting air is generated by primary heat exchange at 400 ℃ and 650Nm 3 The primary high-temperature air of the per hour is taken as primary combustion-supporting air, and the temperature of a primary combustion chamber is controlled to reach 1300-1500 ℃. The sludge is pyrolyzed and gasified in a combustion chamber to gasify fuel gas (the main components are CO and CO) 2 、N 2 Water vapor) with a portion of fly ash (fly ash rate about 10%) enters the second combustion chamber. Introducing 25 ℃ and 15000Nm into a secondary combustion chamber 3 And/h secondary combustion-supporting air is used for carrying out peroxy combustion on the gasified fuel gas. The temperature of the secondary combustion chamber is controlled to be 850-900 ℃, and the residence time of the flue gas is 2-4S. Meanwhile, a cooling water spray nozzle is arranged at the top of the gasification furnace, so that the over-high temperature of the flue gas is prevented, and the cooling water amount is about 2t/h. And controlling the oxygen content of the flue gas at the outlet of the secondary combustion chamber to be about 10 percent. The outlet flue gas amount of the second combustion chamber is about 20500Nm 3 H, a temperature of about 700 ℃.
The temperature of the flue gas is reduced to 180 ℃ after passing through the two-stage heat exchanger, and then the flue gas enters a bag-type dust remover for dust removal and is discharged after wet desulfurization and denitration; and simultaneously generating primary high-temperature air at 400 ℃ and secondary high-temperature air at 300 ℃, introducing the primary high-temperature air into a primary combustion chamber as primary combustion-supporting air, introducing the secondary high-temperature air into a mixing chamber, uniformly mixing with room-temperature air, and introducing into low-temperature drying equipment.
The gasification furnace slag reaches a molten state at high temperature in a combustion chamber, liquid slag flows to a furnace slag discharge port at the bottom along the furnace wall to be discharged, then the liquid slag falls into a slag pool below to obtain water-quenched slag, and the water-quenched slag is discharged through a slag extractor, wherein the slag discharge amount is 0.75t/h.
The molten slag obtained in the embodiment belongs to a vitreous body, heavy metals can be sealed in the vitreous body state to achieve harmlessness, and then the molten slag is crushed to prepare a sludge molten phosphate fertilizer which can replace a calcium magnesium phosphate fertilizer.
The low-temperature sludge drying and gasification melting coupling treatment process and system have the following advantages:
the sludge low-temperature drying and gasification fusion coupling treatment process and system adopt an integrated process of sludge drying and gasification fusion coupling, organic sludge after dehydration and drying is gasified at high temperature through an entrained-flow bed, the entrained-flow bed gasification furnace achieves gasification self-sustaining operation by utilizing the self heat value of the sludge, and meanwhile, high-temperature smoke generated generates high-temperature air through a heat exchanger, and the high-temperature air can be supplied to low-temperature drying equipment at the front end and used as combustion-supporting air of the gasification furnace, so that the energy consumption of low-temperature drying can be reduced, the full utilization of smoke waste heat is realized, and the purposes of saving energy and reducing cost are achieved;
secondly, in the sludge treatment process, the slag after gasification and melting treatment can be comprehensively recycled according to different phosphorus contents;
thirdly, in the sludge treatment process, products obtained after the sludge is gasified and melted do not need to be buried, so that the environmental risk is reduced, and the land is saved;
fourthly, the high-temperature flue gas discharged by the gasification furnace does not contain toxic and harmful substances such as dioxin and the like.
In a word, the sludge low-temperature drying and gasification melting coupling treatment process and system not only realize comprehensive utilization of heat generated by burning organic matters in sludge, but also perform harmless treatment and resource utilization on the generated inorganic slag, do not generate toxic and harmful substances such as dioxin, and have the advantages of cleanness, environmental protection and high efficiency.
Although the present invention is disclosed above, the present invention is not limited thereto. In the description herein, references to the description of the term "one embodiment," "some embodiments," "an illustrative embodiment," "an example," "a specific example," or "some examples" or the like mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Various changes and modifications may be effected by one skilled in the art without departing from the spirit and scope of the invention, as defined in the appended claims.
Claims (10)
1. A low-temperature sludge drying and gasification fusion coupling treatment process is characterized by comprising the following steps:
s1, sludge drying treatment: reducing the water content in the water-containing sludge to below 30% by a dehydration drying process to obtain dried sludge;
s2, carrying out gasification and melting treatment on the dried sludge: conveying the dried sludge obtained by the treatment in the step S1 to a gasification furnace, and introducing air serving as combustion-supporting air into the gasification furnace to gasify and melt the dried sludge at the temperature of over 800 ℃;
s3, flue gas waste heat utilization: after the heat exchange between the high-temperature flue gas discharged by the gasification furnace and air is carried out, high-temperature air is obtained, and a part of the high-temperature air is taken as combustion-supporting air and is introduced into the gasification furnace in the step S2; using another part of high-temperature air in the step S1 to dry the sludge;
s4, comprehensive utilization of the incinerator slag: and detecting the phosphorus content in the slag discharged by the gasification furnace, and determining a resource utilization mode of the slag according to the phosphorus content in the slag.
2. The low-temperature sludge drying and gasification melting coupling treatment process according to claim 1, wherein the step S1 comprises:
s12, low-temperature sludge drying: and (3) drying the sludge by adopting a low-temperature drying device, and reducing the water content in the sludge to be below 30% to obtain the dried sludge.
3. The low-temperature sludge drying and gasification fusion-coupled treatment process according to claim 1 or 2, wherein the step S1 comprises:
s11, mechanical dehydration of sludge: reducing the water content of the water-containing sludge to below 70% by mechanical dewatering equipment;
s12, low-temperature sludge drying: and (4) drying the sludge treated in the step (S11) by adopting a low-temperature drying device, introducing part of high-temperature air generated in the step (S3) into the low-temperature drying device, and reducing the water content in the sludge to be below 30% to obtain the dried sludge.
4. The low-temperature sludge drying and gasification melting coupling treatment process as claimed in claim 1, wherein in the step S2, the gasification furnace is an entrained flow gasification furnace; the dried sludge is fed by powder, and the particle size of the dried sludge is less than 3mm.
5. The low-temperature sludge drying and gasification fusion-coupled treatment process according to claim 1 or 4, wherein the step S2 comprises:
s21, firstly storing the dried sludge powder with the water content reduced to below 30% in a storage bin, controlling the blanking amount by a rotary feeder, and conveying the dried sludge powder into a combustion chamber at the lower part of the gasification furnace by pneumatic conveying of conveyed air; simultaneously, introducing combustion-supporting air into the gasification furnace;
s22, controlling the temperature of the first combustion chamber to be more than 900 ℃, and pyrolyzing organic matters in the sludge and melting inorganic matters in a high-temperature and oxygen-deficient environment in the first combustion chamber;
and S23, enabling the smoke in the first combustion chamber to rise into a second combustion chamber positioned at the upper part of the gasification furnace, carrying out peroxy combustion in the second combustion chamber, controlling the temperature of the second combustion chamber to be more than 800 ℃ in the peroxy combustion process, enabling the retention time of the smoke in the second combustion chamber to be more than 2S, enabling the slag formed by the peroxy combustion to fall into a slag pool at the bottom of the gasification furnace, and enabling the smoke to carry fine ash to continue upwards and be discharged from an outlet at the upper part of the gasification furnace.
6. The low-temperature sludge drying and gasification melting coupling treatment process according to claim 5, wherein in the step S21, the combustion-supporting air introduced into the gasifier comprises primary combustion-supporting air introduced into the primary combustion chamber and secondary combustion-supporting air introduced into the secondary combustion chamber, wherein the primary combustion-supporting air is air at 300-400 ℃, and the flow rate of the primary combustion-supporting air is 500-800 Nm 3 H; the secondary combustion-supporting air is normal temperature air, and the flow of the secondary combustion-supporting air is 10000-15000 Nm 3 /h。
7. The low-temperature sludge drying and gasification melting-coupling treatment process according to claim 6, wherein the step S3 comprises:
s31, firstly carrying out primary heat exchange on high-temperature flue gas discharged by the gasification furnace and air to obtain primary high-temperature air, and introducing the primary high-temperature air into the gasification furnace in the step S2 as primary combustion-supporting air;
s32, continuously carrying out secondary heat exchange on the flue gas subjected to the primary heat exchange and air to obtain secondary high-temperature air, and introducing the secondary high-temperature air into the low-temperature drying equipment in the step S1 to dry the sludge; and the flue gas after secondary heat exchange is subjected to dust removal, desulfurization and denitrification treatment and then is discharged to the atmosphere.
8. The low-temperature sludge drying and gasification fusion-coupling treatment process as claimed in claim 1, wherein in the step S4, determining a resource utilization mode of the slag according to the phosphorus content in the slag comprises:
s41, when the phosphorus content in the slag is more than or equal to 8%, carrying out ore dressing on the slag to obtain concentrate with higher phosphorus content and tailings with lower phosphorus content, wherein the concentrate is used as phosphate ore, and the tailings are used as a phosphorus-containing curing agent or a building raw material;
and S42, when the phosphorus content in the slag is less than 8%, directly using the slag as a phosphorus-containing curing agent or a building raw material.
9. The low-temperature sludge drying and gasification melting coupling treatment process as claimed in claim 1, wherein before the step S2, the content of heavy metals in the sludge is detected, when the content of heavy metals in the sludge exceeds a standard, fuel is filled into the gasification furnace used in the step S2, the temperature in the gasification furnace is increased to over 1200 ℃, the slag in the gasification furnace is melted into a vitreous state, and then the slag is crushed into the sludge molten phosphate fertilizer.
10. A system for sludge low-temperature drying and gasification fusion coupling treatment process, which is characterized in that the system is used for the sludge low-temperature drying and gasification fusion coupling treatment process of any one of the claims 1 to 9.
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