CN109534654B - Sludge treatment system and method - Google Patents
Sludge treatment system and method Download PDFInfo
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- CN109534654B CN109534654B CN201910022266.9A CN201910022266A CN109534654B CN 109534654 B CN109534654 B CN 109534654B CN 201910022266 A CN201910022266 A CN 201910022266A CN 109534654 B CN109534654 B CN 109534654B
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- roller dryer
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- heat exchanger
- dryer
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- 239000010802 sludge Substances 0.000 title claims abstract description 152
- 238000000034 method Methods 0.000 title claims abstract description 16
- 239000010881 fly ash Substances 0.000 claims abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 43
- 239000007789 gas Substances 0.000 claims description 40
- 239000000428 dust Substances 0.000 claims description 30
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 20
- 239000003546 flue gas Substances 0.000 claims description 20
- 239000000463 material Substances 0.000 claims description 11
- 238000009835 boiling Methods 0.000 claims description 9
- 239000007921 spray Substances 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 7
- 230000001877 deodorizing effect Effects 0.000 claims description 5
- 238000002485 combustion reaction Methods 0.000 claims description 2
- 238000010438 heat treatment Methods 0.000 abstract description 10
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 239000002699 waste material Substances 0.000 abstract description 4
- 239000004566 building material Substances 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000001035 drying Methods 0.000 description 41
- 239000010865 sewage Substances 0.000 description 24
- 238000001704 evaporation Methods 0.000 description 11
- 230000008020 evaporation Effects 0.000 description 11
- 239000000446 fuel Substances 0.000 description 9
- 239000002994 raw material Substances 0.000 description 8
- 230000001105 regulatory effect Effects 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- 239000003517 fume Substances 0.000 description 3
- 230000000630 rising effect Effects 0.000 description 3
- 239000002893 slag Substances 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000004043 dyeing Methods 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 150000003071 polychlorinated biphenyls Chemical group 0.000 description 2
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 1
- ISPYQTSUDJAMAB-UHFFFAOYSA-N 2-chlorophenol Chemical compound OC1=CC=CC=C1Cl ISPYQTSUDJAMAB-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 239000011651 chromium Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 150000004826 dibenzofurans Chemical class 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 238000005469 granulation Methods 0.000 description 1
- 230000003179 granulation Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 239000010954 inorganic particle Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 244000000010 microbial pathogen Species 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- NFBOHOGPQUYFRF-UHFFFAOYSA-N oxanthrene Chemical class C1=CC=C2OC3=CC=CC=C3OC2=C1 NFBOHOGPQUYFRF-UHFFFAOYSA-N 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 230000003071 parasitic effect Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
Classifications
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/001—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals for sludges or waste products from water treatment installations
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Treatment Of Sludge (AREA)
- Drying Of Solid Materials (AREA)
Abstract
The invention relates to a sludge treatment system and a method, wherein the system comprises a first roller dryer, a second roller dryer, a third roller dryer, a fluidized bed furnace, a first heat exchanger and a second heat exchanger, wherein the third roller dryer is a jacketed roller dryer; the discharge port of the first roller dryer is communicated with the feed port of the second roller dryer, the discharge port of the second roller dryer is communicated with the feed port of the third roller dryer, and the discharge port of the third roller dryer is communicated with the fluidized bed furnace. The sludge treatment system and the method of the invention basically take self-heating sludge as a heat source, have low energy consumption, treat waste with waste, generate small fly ash volume, can be used as building materials, and can furthest utilize the sludge as resources; in addition, the invention is not limited by the production scale and has great popularization value.
Description
Technical Field
The invention relates to a sludge treatment system and a sludge treatment method, in particular to a self-heating type sludge treatment system and a self-heating type sludge treatment method.
Background
Sludge is a product after sewage treatment, and is an extremely complex non-uniform mass composed of organic residues, bacterial cells, inorganic particles, colloid and the like. The main characteristics of the sludge are high water content (up to 99% or more), high organic matter content, easy decomposition and stinking, fine particles, small specific gravity and colloidal liquid state. The sludge contains a large amount of organic matters such as benzene, chlorophenol, polychlorinated biphenyl (PCB), polychlorinated dibenzofuran (PCDFs), polychlorinated dibenzodioxin (PCDDs) and the like; pathogenic microorganisms such as parasitic ova; heavy metals such as cadmium, chromium, copper, nickel, mercury, lead, zinc and the like, such as improper treatment, easily cause secondary pollution to the environment.
The sewage in China is divided into two parts of industry and town life, and the statistical annual-differentiation data of the Chinese environment show that the industrial sewage discharge in China is basically maintained at about 200 hundred million tons/year in 2009-2014, and the urban domestic sewage discharge is increased from 354 hundred million tons to 510 hundred million tons. The conservation estimation is that according to 200 hundred million tons of industrial sewage discharge per year and 4 percent of annual increase rate of urban domestic sewage discharge, the total sewage discharge amount in China in 2020 reaches 855 hundred million tons. In 2014, the effective treatment rate of industrial sewage in China is 96%, the effective treatment rate of urban domestic sewage is 97%, the industrial sewage treatment capacity in 2014 is 200 hundred million tons, and the urban domestic sewage treatment capacity is 495 hundred million tons. Assuming that the effective sewage treatment rate is kept unchanged, the industrial sewage treatment capacity in 2020 is 200 hundred million tons and the urban domestic sewage treatment capacity is 626 hundred million tons.
In general, 1 ten thousand tons of domestic sewage can be treated by a sewage treatment plant to produce 5-8 tons of sludge with the water content of 80%, and 10-30 tons of sludge can be treated by 1 ten thousand tons of industrial sewage. The output is calculated according to 7 tons and 20 tons respectively, so that the urban domestic sludge production amount in China is 4382 ten thousand tons in 2020, and the industrial sludge production amount is 4000 ten thousand tons and is 8382 ten thousand tons in total. The production amount of the town domestic sludge is more than 50% of the total sludge, but the town domestic sludge and part of the industrial sludge have higher heat value, and according to research data report, the heat value of the dry town domestic sludge and papermaking and printing and dyeing sludge reaches 2300-3000 kcal/kg, and the relative heat value of other industrial sludge is lower, for example, the dry sludge with high heat value is used as a heat source to burn, heat and dry the other sludge with low heat value, and then the dried sludge with low heat value is used as a building material raw material, so that all the sludge can be recycled. The sludge is used as fuel, especially papermaking sludge and municipal sludge, which contains a large amount of organic matters, and can be directly used as fuel after drying, but the existing sludge drying equipment generally needs high-temperature flue gas as a heat source when the sludge is dried, the high-temperature flue gas mostly comes from a hot blast stove, the traditional hot blast stove cannot burn low-heat value sludge, especially for municipal domestic sewage treatment plants, as the heat source is not provided, municipal sludge is difficult to dry, if the high-temperature flue gas generated by burning coal is used as the heat source, the drying cost is too high, and the sludge is not economical, but the sludge is used as fuel, so the following problems exist: (1) Although municipal domestic sludge contains higher organic matters, the effective heat value of the dried sludge can reach more than 2000kcal/kg, but the sludge with the heat value is difficult to use in a common chain furnace boiler; (2) When the effective heat value of the sludge reaches 2000kcal/kg, a fluidized bed furnace can be theoretically used, but most of the dried sludge produced by the existing drying equipment is powdery or blocky, the powdery or blocky sludge is difficult to use, and the fluidized bed furnace can be used only by granulation; (3) The flue gas of the fluidized bed furnace is directly used as a heat source, so that the heat efficiency is high, but the flue gas and dust of the fluidized bed furnace are more. In addition, if the high-temperature flue gas is adopted to directly dry the sludge, when the temperature of the sludge is higher than 300 ℃, organic matters in the sludge can be degraded into combustible gas, and proper treatment is needed.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide a sludge treatment system and a sludge treatment method, which can improve the dehydration efficiency and the dehydration depth of sludge and solve the problems of sludge drying, incineration and resource utilization under the condition of not increasing energy cost.
In order to solve the technical problems, the technical scheme of the invention is as follows:
the sludge treatment system comprises a first roller dryer, a second roller dryer, a third roller dryer, a fluidized bed furnace, a first heat exchanger and a second heat exchanger, wherein the third roller dryer is a jacketed roller dryer;
the discharge port of the first roller dryer is communicated with the feed port of the second roller dryer, the discharge port of the second roller dryer is communicated with the feed port of the third roller dryer, and the discharge port of the third roller dryer is communicated with the fluidized bed furnace;
the air outlet of the boiling furnace is communicated with a first medium inlet of a first heat exchanger, a first medium outlet of the first heat exchanger is communicated with an air inlet of a first roller dryer, an air outlet of the first roller dryer is communicated with a first induced draft fan, an output port of the first induced draft fan is communicated with a first medium inlet of a second heat exchanger, a second medium inlet of the second heat exchanger is communicated with the atmosphere, a second medium outlet of the second heat exchanger is communicated with a second induced draft fan, an output port of the second induced draft fan is communicated with a second medium inlet of the first heat exchanger, a second medium outlet of the first heat exchanger is communicated with an air inlet of a jacket of a third roller dryer, an air outlet of the jacket of the third roller dryer is communicated with an air inlet of the second roller dryer, and a volatile gas outlet of the third roller dryer is communicated with the boiling furnace;
the air outlet of the second roller dryer is communicated with a third induced draft fan, and the output port of the third induced draft fan is communicated with the fluidized bed furnace;
and a sludge crushing mechanism is arranged in the first roller dryer and/or the second roller dryer.
Optionally, the device further comprises a third heat exchanger and a first dust remover communicated with the air outlet of the second roller dryer, the air outlet of the first dust remover is communicated with the first medium inlet of the third heat exchanger, the first medium outlet of the third heat exchanger is communicated with the input port of the third induced draft fan, and preferably, the discharge port of the first dust remover is communicated with the feed inlet of the third roller dryer.
Alternatively, the first, second and third drum dryers, fluidized bed furnace, first and second heat exchangers are all commercially available
Optionally, the device further comprises a first spiral feeding mechanism, wherein the first spiral feeding mechanism is used for feeding materials falling from the discharge hole of the second roller dryer and/or the discharge hole of the first dust remover into the third roller dryer. Optionally, a hopper for receiving materials is arranged below the discharge port of the second roller dryer and the discharge port of the first dust remover, and the hopper is matched with the first spiral feeding mechanism to control the feeding rate to the third roller dryer.
Optionally, the cooling tower and the pump are sequentially communicated, the second medium outlet of the third heat exchanger is communicated with the cooling tower, and the output port of the pump is communicated with the second medium inlet of the third heat exchanger.
The dust in the gas can be removed by the first dust remover, the gas load is reduced, the gas enters the third heat exchanger, and the vapor in the gas is condensed, so that the gas quantity can be greatly reduced, the combustibility of the gas is improved, and the gas can be completely recycled and burned; the sludge in the third heat exchanger is dried by hot air, and the water vapor is removed and then recycled, so that the gas can be ensured to have enough oxygen to meet the burning requirement of the fluidized bed furnace; the sewage discharge amount can be reduced by recycling the cooling water.
Optionally, the device further comprises a second spiral feeding mechanism, wherein the second spiral feeding mechanism receives the material falling from the discharge hole of the first roller dryer and feeds the material into the second roller dryer.
Optionally, a second dust remover is communicated between the air outlet of the first roller dryer and the first induced draft fan. Optionally, the discharge port of the second dust remover is communicated with the feed port of the second roller dryer.
Optionally, the system further comprises an exhaust gas treatment system, wherein the exhaust gas treatment system comprises a spray tower, a deodorizing tower and a chimney which are sequentially communicated, and an air inlet of the spray tower is communicated with a first medium outlet of the second heat exchanger.
Optionally, the first heat exchanger and the second heat exchanger are vertical heat exchangers, and further are vertical gas heat exchangers; the third heat exchanger is a condensing tower.
Optionally, the dust remover is a cyclone dust remover or a cloth bag dust remover. Preferably, the first dust remover is a cloth bag dust remover, and the second dust remover is a cyclone dust remover.
A method of sludge treatment using a system as described above, comprising the steps of:
starting a first induced draft fan, a second induced draft fan, a third induced draft fan, a first roller dryer, a second roller dryer and a third roller dryer, igniting a fluidized bed furnace, simultaneously inputting sludge to be treated with the water content of 55-65wt% into the first roller dryer, and obtaining first semi-dried sludge with the water content of 42-48wt% at a discharge hole of the first roller dryer;
conveying the first semi-dry sludge into a second roller dryer, and obtaining second semi-dry sludge with the water content of 23-27wt% at a discharge hole of the second roller dryer;
conveying the second semi-dry sludge into a third roller dryer, and obtaining dry granular sludge with the water content of 4-6wt% at a discharge hole of the third roller dryer;
and (3) inputting the dried sludge into a fluidized bed furnace for combustion to obtain flue gas and fly ash, and entering a post-treatment procedure after the flue gas sequentially enters a first heat exchanger, a first roller dryer and a second heat exchanger.
In the system of the invention, the sludge drying is divided into three stages of drying, and the three stages of drying have the following characteristics: the sludge crushing mechanism is arranged in the first section drying equipment and the second section drying equipment, so that the sludge is more favorable for drying, but the sludge crushing mechanism is not arranged in the last section drying equipment, so that the dried sludge can keep the particle size of 3-12 mm when the high-temperature drying section is used for drying, the boiling burning requirement of the fluidized bed furnace can be met, the sludge burnout rate reaches 99% when the fluidized bed furnace burns, the fly ash generated in the burning process is less, the burned slag falls to the lower part of the furnace, and optionally, the slag is conveyed out of the furnace through a slag discharging screw; the incineration temperature is kept at 800-900 ℃, harmful substances such as dioxin and the like can be effectively decomposed, coking is not generated during sludge incineration, the effective use of a furnace body is protected, high-temperature flue gas at 800-900 ℃ generated by a fluidized bed furnace is cooled to 450-480 ℃ on one hand, meanwhile, air is heated to 370-410 ℃, a concurrent drying mode is adopted, the temperature of sludge is not higher than 300 ℃ as far as possible, and the degradation of sludge organic matters is reduced while the aim of drying is achieved; the three-section fuel sludge drying method is adopted, so that the water content of the final sludge is ensured to be about 5wt%, and the incineration is facilitated; the temperature in the third roller dryer exceeds 300 ℃, and the indirect heating drying mode is adopted, so that the sludge is degraded at a higher temperature, and the generated combustible gas is independently led to the fluidized bed furnace for burning, so that the pollution load of condensed water is reduced, the environment is protected, and the total heat utilization rate of the system can be improved.
The high-temperature flue gas at 800-900 ℃ generated by the fluidized bed furnace is cooled to 450-480 ℃ after passing through the first heat exchanger to serve as a drying heat source of the first roller dryer, but the temperature is higher, alternatively, 50% of tail gas of the first roller dryer after dust removal is led to an inlet of the first roller dryer to serve as a drying heat source after being mixed with cooled flue gas in order to reduce the decomposition of organic matters in sludge and reduce the pollution load of condensed water, so that the system is more environment-friendly, and the total heat utilization rate of the system can be improved; the gas with the temperature of 115-125 ℃ from the first roller dryer enters a second heat exchanger after being dedusted by a second deduster, the temperature of the gas is reduced to 90-95 ℃ by normal-temperature air in the second heat exchanger, and then the non-condensable gas is led to a spray tower for treatment, so that the gas quantity can be reduced to the greatest extent, the equipment investment of a subsequent tail gas treatment device is reduced, and after the tail gas treatment, the indexes of various pollutants of the discharged gas reach or are lower than the secondary standards of national standards GB14554-93 and GB 16297-1996; the low-temperature hot air with the heated temperature of 80-90 ℃ is led to the first heat exchanger for continuous heating, the temperature of the hot air after heat exchange can be increased to 370-410 ℃ and used as a heat source for indirect heating and drying of the third roller dryer, the sludge drying efficiency is improved, the energy consumption is saved, the temperature of the hot air after leaving the jacket of the third roller dryer is 260-280 ℃, then the hot air enters the second roller dryer and is directly contacted with the sludge for drying, the temperature of the gas leaves the second roller dryer and is reduced to 120 ℃, the temperature after removing the water vapor through dust removal and heat exchange is further reduced to 80-90 ℃, and finally the gas is led to the fluidized bed furnace for burning.
In general, the sludge treatment system and the method of the invention reasonably distribute and recycle the flue gas and the hot air, have high heat utilization rate, dry the sludge in sections, and enable the sludge to be dried under the environment-friendly condition, the obtained sludge has low water content and is in a particle state, thereby being beneficial to sludge incineration and fly ash reduction, and the dried sludge is directly sent into an incinerator to be incinerated at a higher temperature. The system takes the sludge incineration heat as a heat source, has low energy consumption, uses waste to treat waste, generates small fly ash body, can be used as building materials, and can maximally utilize the sludge as a resource; in addition, the invention is not limited by the production scale and has great popularization value.
Drawings
Fig. 1 is a schematic diagram of a sludge treatment system according to a first embodiment of the present invention.
Detailed Description
The present invention will be described in detail with reference to examples. It should be noted that, without conflict, the embodiments of the present invention and features of the embodiments may be combined with each other. For convenience of description, the words "upper", "lower", "left" and "right" are used hereinafter to denote only the directions corresponding to the upper, lower, left, and right directions of the drawings, and do not limit the structure.
As shown in fig. 1, the sludge treatment system comprises a first roller dryer 10, a second roller dryer 7, a third roller dryer 8, a fluidized bed furnace 11, a first heat exchanger 12 and a second heat exchanger 15, wherein the third roller dryer is a jacketed roller dryer;
the discharge port of the first roller dryer 10 is communicated with the feed port of the second roller dryer 7, the discharge port of the second roller dryer is communicated with the feed port of the third roller dryer, and the discharge port of the third roller dryer is communicated with the fluidized bed furnace;
the air outlet of the boiling furnace is communicated with a first medium inlet of a first heat exchanger 12, a first medium outlet of the first heat exchanger is communicated with an air inlet of a first roller dryer, an air outlet of the first roller dryer is communicated with a first induced draft fan 19, an output port of the first induced draft fan is communicated with a first medium inlet of a second heat exchanger, a second medium inlet of the second heat exchanger is communicated with the atmosphere, a second induced draft fan 13 is communicated with a second medium outlet of the second heat exchanger, an output port of the second induced draft fan is communicated with a second medium inlet of the first heat exchanger, a second medium outlet of the first heat exchanger is communicated with an air inlet of a jacket of a third roller dryer, an air outlet of the jacket of the third roller dryer is communicated with an air inlet of the second roller dryer, and a volatile gas outlet of the third roller dryer is communicated with the boiling furnace;
the air outlet of the second roller dryer is communicated with a third induced draft fan 5, and the output port of the third induced draft fan 5 is communicated with the fluidized bed furnace;
and a sludge crushing mechanism is arranged in the first roller dryer and/or the second roller dryer.
The device also comprises a third heat exchanger 3 and a first dust remover 4 communicated with the air outlet of the second roller dryer, wherein the air outlet of the first dust remover is communicated with a first medium inlet of the third heat exchanger, a first medium outlet of the third heat exchanger is communicated with an input port of a third induced draft fan, and preferably, a discharge port of the first dust remover is communicated with a feed inlet of the third roller dryer.
The device also comprises a first spiral feeding mechanism 6, wherein the first spiral feeding mechanism is used for feeding materials falling from the discharge port of the second roller dryer and/or the discharge port of the first dust remover into the third roller dryer. And a hopper 9 for receiving materials is arranged below the discharge port of the second roller dryer and the discharge port of the first dust remover.
The cooling tower heat exchanger further comprises a cooling tower 1 and a pump 2 which are sequentially communicated, wherein a second medium outlet of the third heat exchanger is communicated with the cooling tower, and an output port of the pump is communicated with a second medium inlet of the third heat exchanger.
And a second screw feeding mechanism 20, which receives the material falling from the discharge port of the first roller dryer and feeds the material into the second roller dryer.
The second dust remover 14 is communicated between the air outlet of the first roller dryer and the first induced draft fan 19. The discharge port of the second dust remover is communicated with the feed port of the second roller dryer. Optionally, a part of the flue gas at the outlet of the first induced draft fan is introduced into the first drum dryer by means of a fifth induced draft fan 21.
The system also comprises a tail gas treatment system, wherein the tail gas treatment system comprises a spray tower 16, a deodorizing tower 17 and a chimney 18 which are sequentially communicated, and an air inlet of the spray tower is communicated with a first medium outlet of the second heat exchanger.
The first heat exchanger 12 and the second heat exchanger 15 are vertical heat exchangers; the third heat exchanger is a condensing tower.
The invention is further illustrated by taking the treatment of sludge from a municipal domestic sewage treatment plant and industrial sludge from a plant as an example, wherein the water content of the sludge from the municipal domestic sewage treatment plant is 65wt%, the water content of the papermaking sludge is 55wt%, and the water content of the sludge after mixing is 60%. When the method is implemented, 5000kcal/kg coal is used as fuel, the temperature of flue gas of the fluidized bed furnace is controlled to 600-650 ℃ after the coal is combusted, then the temperature of hot air is regulated to 300-360 ℃ and the temperature of flue gas after heat exchange is regulated to 300-350 ℃, the sludge is fed into the first roller dryer, the rotating speed of each roller dryer is regulated to ensure that the moisture content of the dried sludge meets the process requirement, when the sludge is fed into the second roller dryer, the temperature of flue gas of the fluidized bed furnace is increased to 800-1000 ℃, the temperature of air is heated to 380-410 ℃ through the first heat exchanger, the temperature of flue gas is reduced to 450-480 ℃ after the first heat exchanger, the sludge feeding amount of the first roller dryer is regulated to be normal, the temperature of high-temperature air in a jacket of the third roller dryer is normal, and the sludge in a cylinder body of the third roller dryer 8 begins to gasify in a large amount, drying the heated cylinder of the third roller dryer 8 to obtain dried granular sludge with the water content of 4-6wt%, feeding the dried granular sludge into a fluidized bed furnace along with air output by a third induced draft fan through a second pipeline to serve as fuel for burning and heating, directly introducing gas generated in the sludge drying process in the cylinder of the third roller dryer into the fluidized bed furnace to serve as fuel for burning and heating, reducing the temperature to 330-350 ℃, feeding the low-temperature air into the cylinder of the third roller dryer to serve as a heat source, directly contacting with sludge, drying the fuel sludge with the water content of about 45%, drying the sludge with the water content of about 25wt% through the second roller dryer, feeding the sludge into a first spiral feeding mechanism, feeding the sludge into the third roller dryer through the first spiral feeding mechanism, and continuously drying the sludge, the gas with the temperature of 115-125 ℃ coming out of the second roller dryer enters a third heat exchanger after being dedusted by a first deduster, the first deduster recovers sludge and enters a first spiral feeding mechanism, the sludge is also fed to the third roller dryer by the first spiral feeding mechanism to be dried continuously, the temperature of the gas is reduced to 90-95 ℃ by cold water in the third heat exchanger, then the non-condensable gas is led into a boiling furnace to be burnt, meanwhile, the condensed sewage hot water is led into a sewage treatment system to be treated again, and the heated clean hot water is cooled by a cold water tower and then recycled. The high temperature fume of 800-1000 deg.c produced in the boiling furnace is cooled to 450-480 deg.c in the first heat exchanger, and the fume is first heated in the cylinder of the first roller drier to dry sludge directly, and the fume is then dedusted in the second deduster to the second heat exchanger, cooled to 90-95 deg.c in the second heat exchanger with normal temperature air, treated in the spray tower, treated in the sewage treating system, and heated to 80-90 deg.c in the vertical heat exchanger for further use. The non-condensable gas entering the spray tower is sprayed, absorbed and purified by 10% sodium hydroxide alkali liquor, the non-condensable gas after spraying and absorbing is introduced into the deodorizing tower for deodorizing by using active carbon, and the non-condensable gas after reaching the standard is treated and finally discharged into the atmosphere.
The invention will be further described by way of example with a (dried) sludge throughput of 50 tons/day, the relevant parameters being shown in table 1:
TABLE 1
2. Calculation of sludge drying process
2.1 calculation conditions
Dry sludge treatment capacity X0:2083.33kg/h
Initial average water content S0 of sludge: 60 percent of
Drying evaporation quantity Ld:1206.14kg/h
Dried fuel sludge amount X3:877.19kg/h (moisture content 5%)
Ambient temperature T0:20 DEG C
2.2 calculation
2.2.1 requiring heat QT
A) Drying a section of required heat Q1T calculation:
raw material outlet temperature T1:70 DEG C
a) The heat required for evaporation of water in the raw material Q1a:
Q1a＝X0*S0*(T1-T0)＝62499.9kcal/h
b) Heat required for evaporation of water Q1b:
latent heat of evaporation Cj1 at 70 ℃): 557.30kcal/kg
Heat required for water evaporation at 70 ℃ in one stage:
Q1b＝Cj1*L1＝316641.14kcal/h
c) The heat Q1c is required for the water vapor temperature to rise:
specific heat Cjw =0.45 kcal/kg of water vapor
Temperature T of the outlet gas of the drum 1: 120 DEG C
Q1c＝L1*Cj*(T-T1)＝13188.83kcal/h
d) Heat Q1d is required for rising the temperature of sludge
Sludge specific heat Cjn =0.40 kcal/kg
Sludge temperature T1:70 DEG C
Q1d＝X0*(1-S1)*Cjn*(T1-T0)＝57291.58kcal/h
e) Total heat quantity Q1
Q1＝Q1a+Q1b+Q1c+Q1d＝449621.45kcal/h
f) The actual necessary heat quantity Q1T
Drying heat efficiency (k): 80 percent of
Q1T＝Q1/k＝562026.81kcal/h
B) Calculation of the heat quantity Q2T required for the second drying stage:
raw material outlet temperature T2:90 DEG C
a) The water heating heat quantity Q2a in the two-stage raw material:
Q2a＝X1*S1*(T2-T1)＝13636.44kcal/h
b) Heat required for evaporation of water in the two-stage feedstock, Q2b:
latent heat of evaporation Cj2 at 90 ℃): 546.12kcal/kg
The heat required by the two-stage 90 ℃ water evaporation:
Q2b＝Cj2*L2＝220659.79kcal/h
c) The heat Q2c is required for the water vapor temperature to rise:
specific heat Cjw =0.45 kcal/kg of water vapor
Drum 2 outlet gas temperature T:120 DEG C
Q2c＝L2*Cj w*(T-T2)＝5454.68kcal/h
d) Heat Q2d is needed for rising of sludge temperature
Sludge specific heat Cjn =0.40 kcal/kg
Sludge temperature T2:90 DEG C
Q2d＝X1*(1-S2)*Cjn*(T2-T1)＝9090.96kcal/h
e) Total heat quantity Q2
Q2＝Q2a+Q2b+Q2c+Q2d＝248841.87kcal/h
f) The actual necessary heat quantity Q2T
Drying heat efficiency (k): 80 percent of
Q2T＝Q2/k＝311052.34kcal/h
B) The heat required for three drying stages, Q3T, was calculated:
raw material outlet temperature T3:300 DEG C
a) The water in the three-stage raw materials is heated to 100 ℃ to require heat quantity Q3a:
Q3a＝X2*S2*(100-T2)＝1111.11*0.25*(100-90)
＝2777.78kcal/h
b) Heat required for water evaporation in the three-stage raw material Q3b:
latent heat of evaporation Cj3 at 100 ℃): 539kcal/kg
Three sections of heat required by water evaporation at 100℃:
Q3b＝Cj3*L3＝539*233.92
＝126082.92kcal/h
c) The heat Q3c is required for the water vapor temperature to rise:
specific heat Cjw =0.45 kcal/kg of water vapor
Temperature Tv2 of gas entering the fluidized bed furnace: 330 DEG C
Q3c＝L3*Cj*(Tv2-100)＝233.92*0.45*230
＝24210.72kcal/h
d) Heat Q3d is needed for rising of sludge temperature
Sludge specific heat Cjn =0.40 kcal/kg
Sludge temperature T3:300 DEG C
Q3d＝X2*(1-S3)*Cjn*(T3-T2)＝1111.11*(1-0.05)*0.40*(300-90)
＝88666.58kcal/h
e) Total heat quantity Q3
Q3＝Q3a+Q3b+Q3c+Q3d＝241737.99kcal/h
f) Actual necessary heat quantity Q3T
Drying heat efficiency (k): 80 percent of
Q3T＝Q3/k＝302172.49kcal/h
B) Total heat QT actually required for sludge drying
QT＝Q1T+Q2T+Q3T
＝562026.81+311052.34+302172.49＝1175251.64kcal/h
2.2.2 providing heat Qc
A) Heat Q1c generated by incineration of organic gas
Organic heating value Cy:4000kcal/kg
The volatile organic matter content is (M) of the absolute dry sludge: 20 percent of
Sludge absolute amount Yd:833.33kg/h
Q1c＝Yd*M*Cy＝833.33*0.20*4000
＝666664kcal/h
B) Heat Q2c provided by sludge incineration
Dry sludge amount X3:877.19kg/h
Dry sludge calorific value Cx:2000kcal/kg
Q2c＝X3*Cx＝1754380kcal/h
B) The utilization rate of the total heat of the burning of the fluidized bed furnace is 50 percent (experience value)
Qc＝(Q1c+Q2c)*0.5＝1210522kcal/h
2.2.3 actual thermal equilibrium Qc-QT
＝1210522-1175251.64＝35270.36kcal/h
It can be seen that for the sludge to be treated with the average water content not higher than 60%, the heat value of the sludge after drying is not lower than 2000kcal/kg, the total utilization rate of the heat of the sludge incineration reaches 50%, the heat provided by the sludge incineration can meet the requirement of sludge drying, and the heat is still rich. Practice proves that for a plurality of sludge such as municipal sludge, papermaking sludge, printing and dyeing sludge and the like, the heat value of the sludge after drying is not lower than 2000kcal/kg, and the total utilization rate of the sludge incineration heat is not lower than 50%.
In conclusion, the treatment system and the method have strong continuity and high dehydration degree, do not need external heat sources, greatly reduce energy cost and can carry out drying treatment on various sludge organic combinations with certain heat values.
The foregoing examples are set forth in order to provide a more thorough description of the present invention, and are not intended to limit the scope of the invention, since modifications of the invention in various equivalent forms will occur to those skilled in the art upon reading the present invention, and are within the scope of the invention as defined in the appended claims.
Claims (7)
1. The sludge treatment system is characterized by comprising a first roller dryer, a second roller dryer, a third roller dryer, a fluidized bed furnace, a first heat exchanger and a second heat exchanger, wherein the third roller dryer is a jacketed roller dryer;
the discharge port of the first roller dryer is communicated with the feed port of the second roller dryer, the discharge port of the second roller dryer is communicated with the feed port of the third roller dryer, and the discharge port of the third roller dryer is communicated with the fluidized bed furnace;
the air outlet of the boiling furnace is communicated with a first medium inlet of a first heat exchanger, a first medium outlet of the first heat exchanger is communicated with an air inlet of a first roller dryer, an air outlet of the first roller dryer is communicated with a first induced draft fan, an output port of the first induced draft fan is communicated with a first medium inlet of a second heat exchanger, a second medium inlet of the second heat exchanger is communicated with the atmosphere, a second medium outlet of the second heat exchanger is communicated with a second induced draft fan, an output port of the second induced draft fan is communicated with a second medium inlet of the first heat exchanger, a second medium outlet of the first heat exchanger is communicated with an air inlet of a jacket of a third roller dryer, an air outlet of the jacket of the third roller dryer is communicated with an air inlet of the second roller dryer, and a volatile gas outlet of the third roller dryer is communicated with the boiling furnace;
the air outlet of the second roller dryer is communicated with a third induced draft fan, and the output port of the third induced draft fan is communicated with the fluidized bed furnace;
the first roller dryer and the second roller dryer are internally provided with a sludge crushing mechanism, and the third roller dryer is not internally provided with a sludge crushing mechanism; the device also comprises a third heat exchanger and a first dust remover communicated with the air outlet of the second roller dryer, wherein the air outlet of the first dust remover is communicated with a first medium inlet of the third heat exchanger, and a first medium outlet of the third heat exchanger is communicated with an input port of a third induced draft fan; the discharge port of the first dust remover is communicated with the feed port of the third roller dryer; a second dust remover is communicated between the air outlet of the first roller dryer and the first induced draft fan, and part of flue gas at the outlet of the first induced draft fan is introduced into the first roller dryer through a fifth induced draft fan.
2. The system of claim 1, further comprising a first screw feed mechanism that feeds material falling from the second drum dryer outlet and/or the first dust collector outlet into the third drum dryer.
3. The system of claim 1, further comprising a cooling tower and a pump in communication, wherein the second medium outlet of the third heat exchanger is in communication with the cooling tower, and wherein the output of the pump is in communication with the second medium inlet of the third heat exchanger.
4. The system of claim 1, further comprising a second screw feed mechanism that receives material falling from the first drum dryer outlet and feeds the material into the second drum dryer.
5. The system of any of claims 1-4, further comprising an exhaust gas treatment system comprising a spray tower, a deodorizing tower, and a chimney in sequential communication, an air inlet of the spray tower in communication with the first medium outlet of the second heat exchanger.
6. The system of any one of claims 1-4, wherein the first heat exchanger and the second heat exchanger are both vertical heat exchangers; the third heat exchanger is a condensing tower.
7. A method of sludge treatment, characterized in that it is carried out with a system according to any one of claims 1-6, comprising the steps of:
starting a first induced draft fan, a second induced draft fan, a third induced draft fan, a first roller dryer, a second roller dryer and a third roller dryer, igniting a fluidized bed furnace, simultaneously inputting sludge to be treated with the water content of 55-65wt% into the first roller dryer, and obtaining first semi-dried sludge with the water content of 42-48wt% at a discharge hole of the first roller dryer;
conveying the first semi-dry sludge into a second roller dryer, and obtaining second semi-dry sludge with the water content of 23-27wt% at a discharge hole of the second roller dryer;
conveying the second semi-dry sludge into a third roller dryer, and obtaining dry granular sludge with the water content of 4-6wt% at a discharge hole of the third roller dryer;
and (3) inputting the dry granular sludge into a fluidized bed furnace for combustion to obtain flue gas and fly ash, and entering a post-treatment procedure after the flue gas sequentially enters a first heat exchanger, a first roller dryer and a second heat exchanger.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201397018Y (en) * | 2009-04-02 | 2010-02-03 | 成都宝迪加航科技发展有限公司 | Internally heated contact-type cylinder dryer |
| CN202032591U (en) * | 2011-05-06 | 2011-11-09 | 安徽博瑞特热能设备股份有限公司 | Sludge incineration and tail gas pollution control system for energy-self-sufficient fluidized bed |
| CN206872653U (en) * | 2017-05-04 | 2018-01-12 | 湖南佰霖生物技术股份有限公司 | A kind of sludge confesses heat dehydration drying system |
| CN209721907U (en) * | 2019-01-10 | 2019-12-03 | 湖南碧汇泉环保科技有限公司 | A kind of sludge treating system |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201397018Y (en) * | 2009-04-02 | 2010-02-03 | 成都宝迪加航科技发展有限公司 | Internally heated contact-type cylinder dryer |
| CN202032591U (en) * | 2011-05-06 | 2011-11-09 | 安徽博瑞特热能设备股份有限公司 | Sludge incineration and tail gas pollution control system for energy-self-sufficient fluidized bed |
| CN206872653U (en) * | 2017-05-04 | 2018-01-12 | 湖南佰霖生物技术股份有限公司 | A kind of sludge confesses heat dehydration drying system |
| CN209721907U (en) * | 2019-01-10 | 2019-12-03 | 湖南碧汇泉环保科技有限公司 | A kind of sludge treating system |
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