CN106629710A - System and method for preparing activated carbon - Google Patents
System and method for preparing activated carbon Download PDFInfo
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- CN106629710A CN106629710A CN201611105663.5A CN201611105663A CN106629710A CN 106629710 A CN106629710 A CN 106629710A CN 201611105663 A CN201611105663 A CN 201611105663A CN 106629710 A CN106629710 A CN 106629710A
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 116
- 238000000034 method Methods 0.000 title claims abstract description 33
- 239000010802 sludge Substances 0.000 claims abstract description 187
- 238000000197 pyrolysis Methods 0.000 claims abstract description 122
- 230000004913 activation Effects 0.000 claims abstract description 121
- 239000007788 liquid Substances 0.000 claims abstract description 72
- 238000000926 separation method Methods 0.000 claims abstract description 68
- 238000001035 drying Methods 0.000 claims abstract description 64
- 239000007789 gas Substances 0.000 claims description 122
- 239000003610 charcoal Substances 0.000 claims description 84
- 239000000567 combustion gas Substances 0.000 claims description 49
- 238000009825 accumulation Methods 0.000 claims description 39
- 239000000446 fuel Substances 0.000 claims description 27
- 239000002737 fuel gas Substances 0.000 claims description 26
- 230000007704 transition Effects 0.000 claims description 24
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 19
- 238000007599 discharging Methods 0.000 claims description 19
- 239000003546 flue gas Substances 0.000 claims description 19
- 238000007669 thermal treatment Methods 0.000 claims description 19
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 13
- 239000001301 oxygen Substances 0.000 claims description 13
- 229910052760 oxygen Inorganic materials 0.000 claims description 13
- 239000000463 material Substances 0.000 claims description 11
- 239000002245 particle Substances 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 9
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 8
- 239000001569 carbon dioxide Substances 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 7
- 238000005276 aerator Methods 0.000 claims description 6
- 230000008859 change Effects 0.000 claims description 5
- 238000006555 catalytic reaction Methods 0.000 claims description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 2
- 210000000952 spleen Anatomy 0.000 claims description 2
- 239000002296 pyrolytic carbon Substances 0.000 abstract description 10
- 229910052799 carbon Inorganic materials 0.000 abstract description 2
- 238000001994 activation Methods 0.000 description 100
- 230000003197 catalytic effect Effects 0.000 description 27
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 16
- 238000005265 energy consumption Methods 0.000 description 14
- 239000003054 catalyst Substances 0.000 description 10
- UHZZMRAGKVHANO-UHFFFAOYSA-M chlormequat chloride Chemical compound [Cl-].C[N+](C)(C)CCCl UHZZMRAGKVHANO-UHFFFAOYSA-M 0.000 description 9
- 238000002485 combustion reaction Methods 0.000 description 9
- 230000000694 effects Effects 0.000 description 7
- 239000003345 natural gas Substances 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 229910000831 Steel Inorganic materials 0.000 description 5
- 239000003344 environmental pollutant Substances 0.000 description 5
- 231100000719 pollutant Toxicity 0.000 description 5
- 239000002689 soil Substances 0.000 description 5
- 239000010959 steel Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 239000006229 carbon black Substances 0.000 description 4
- 239000008246 gaseous mixture Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 230000003213 activating effect Effects 0.000 description 2
- 238000007084 catalytic combustion reaction Methods 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000004381 surface treatment Methods 0.000 description 2
- ZCYVEMRRCGMTRW-UHFFFAOYSA-N 7553-56-2 Chemical compound [I] ZCYVEMRRCGMTRW-UHFFFAOYSA-N 0.000 description 1
- 102000002322 Egg Proteins Human genes 0.000 description 1
- 108010000912 Egg Proteins Proteins 0.000 description 1
- 241000700605 Viruses Species 0.000 description 1
- 244000052616 bacterial pathogen Species 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 230000000711 cancerogenic effect Effects 0.000 description 1
- 231100000315 carcinogenic Toxicity 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 231100000584 environmental toxicity Toxicity 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 230000035558 fertility Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 229910052740 iodine Inorganic materials 0.000 description 1
- 239000011630 iodine Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 210000004681 ovum Anatomy 0.000 description 1
- 230000003071 parasitic effect Effects 0.000 description 1
- 244000052769 pathogen Species 0.000 description 1
- 230000001717 pathogenic effect Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000010801 sewage sludge Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
Landscapes
- Treatment Of Sludge (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
The invention provides a system and method for preparing activated carbon. The system comprises a drying unit, a pyrolysis unit, a gas-liquid separation unit, a steam generation unit and an activation unit, wherein the drying unit is suitable for drying sludge; the pyrolysis unit is suitable for pyrolysis of the dried sludge to obtain a pyrolysis gas and sludge pyrolytic carbon; the gas-liquid separation unit is suitable for gas-liquid separation on the pyrolysis gas to obtain a gas and tar; the steam generation unit is suitable for supplying the gas to the steam generation unit to obtain high-temperature steam; and the activation unit is suitable for supplying the sludge pyrolytic carbon and one part of high-temperature steam to the activation unit, so that the sludge pyrolytic carbon is activated to obtain the activated carbon. According to the system, the sludge pyrolytic carbon obtained through pyrolysis of the sludge can be deep processed into high-value activated carbon, energy does not need to be added, and the system and the method are low-carbon and environment-friendly and are suitable for large-scale promotion.
Description
Technical field
The present invention relates to derived energy chemical field, specifically, the present invention relates to prepare the system and method for activated carbon.
Background technology
Containing harmful substances such as substantial amounts of pathogenic bacterium, parasitic ovum, virus, heavy metals in sludge, while having in sludge
Machine matter composition can be utilized by multiple technologies.At present, domestic and international sludge utilization technology species is various, technical sophistication is various,
Wherein main method has：Soil surface treatment and landfill, sludge incineration, agricultural sludge, sludge building material utilization and sludge hot tearing
Solution technology etc..Wherein, soil surface treatment is relatively easy with Landfill, and cost is relatively low, however it is necessary that take substantial amounts of land resource,
Polluted underground water, while constantly fermentation produces substantial amounts of methane, causes serious greenhouse effect；Sludge incineration is in aerobic atmosphere
It is lower fully to react with the Organic substance in sludge, stable inorganic matters are generated, while realizing minimizing and the recycling of sludge.
But sludge incineration high cost, energy consumption are big, there is secondary pollution in burning process, and produce the high carcinogenic gas such as bioxin；
Agricultural sludge is China's most widely used sludge treating method at present, necessary containing substantial amounts of plant growing in its Organic substance
Nutrient substance, can be with improved soil, increase soil fertility, but heavy metal, pathogen and organic pollution in sludge etc.
It is difficult to decompose removal, accumulate in soil when agricultural, cause ecotoxicity problems；It is important development side that sludge building materialization is utilized
One of to, but market bearing capacity deficiency is faced with present, limit its extensive development.
However, at present the system and method for Treatment of Sludge still has much room for improvement.
The content of the invention
It is contemplated that at least solving one of technical problem in correlation technique to a certain extent.For this purpose, the present invention
One purpose is the method and system that proposition prepares activated carbon.The pyrolyzing sludge charcoal depth that the method can obtain pyrolyzing sludge
The activated carbon of high added value is processed as, and without the need for external energy, low-carbon environment-friendly, is adapted to large-scale promotion.
In a first aspect of the present invention, the present invention proposes a kind of system for preparing activated carbon.Enforcement of the invention
Example, the system includes：Drying unit, the drying unit is suitable to be dried in sludge；Pyrolysis unit, the pyrolysis unit
Sludge inlet and pyrolyzing sludge charcoal discharging opening are provided with, the sludge inlet is connected with the drying unit, the pyrolysis
Unit is suitable to be pyrolyzed in the sludge after the drying, to obtain pyrolysis gas and pyrolyzing sludge charcoal；Gas-liquid separation unit, institute
State gas-liquid separation unit to be connected with the pyrolysis unit, be suitable to for the pyrolysis gas to carry out gas-liquid separation, so as to obtain combustion gas and
Tar；Producing steam unit, the producing steam unit is connected with the gas-liquid separation unit, is suitable to the part fuel gas supply extremely
In the producing steam unit, high-temperature steam is obtained；And activation unit, the activation unit goes out respectively with the pyrolyzing sludge charcoal
Material mouth is connected with producing steam unit, is suitable to the pyrolyzing sludge charcoal and part high-temperature steam be supplied to the activation list
Unit so that the pyrolyzing sludge charcoal carries out activation processing, to obtain activated carbon.
Thus, the system for preparing activated carbon according to embodiments of the present invention is single to pyrolysis by the way that the sludge of drying is supplied
Unit carries out pyrolysis processing, obtains pyrolysis gas and pyrolyzing sludge charcoal, and pyrolysis gas obtain combustion gas and tar Jing after gas-liquid separation, wherein
Tar can make the burning of producing steam unit produce high-temperature steam, outside for producing steam unit as the fuel of producing steam unit
Plus the energy, and then high-temperature steam and pyrolyzing sludge charcoal are supplied to activation unit carry out activation processing, obtain activated carbon and high temperature
Flue gas.The system realizes making full use of for sludge, by the deep processing of pyrolyzing sludge charcoal for high added value activated carbon, and energy consumption compared with
It is low, it is environmentally friendly, it is adapted to large-scale promotion.
In addition, the system for preparing activated carbon according to the above embodiment of the present invention can also have following additional technology special
Levy：
Embodiments in accordance with the present invention, the pyrolysis unit is revolving bed, along Flow of Goods and Materials direction, the pyrolysis unit according to
It is secondary including：Feed zone, the feed zone is provided with the sludge inlet, sludge inlet by sewage sludge feed spiral with it is described
Drying unit is connected；Preheating zone, the preheating zone is provided with vapor air vent, and the vapor air vent is single with the drying
Unit is connected, and the vapor air vent is suitable to the vapor obtained by the sludge after drying is preheated and supplies to the drying
In unit；Transition region；Gas-producing area, the gas-producing area is provided with pyrolysis gas air vent, the pyrolysis gas air vent and the gas-liquid
Separative element is connected, and is suitable to the pyrolysis gas of generation be supplied to gas-liquid separation unit；And discharge zone, the discharge zone is arranged
There is the pyrolyzing sludge charcoal discharging opening, wherein, it is provided with heat accumulation type radiant tube in the preheating zone, transition region and gas-producing area.By
This, can further improve the efficiency of the pyrolysis processing.
According to a preferred embodiment of the invention, the quantity that heat accumulation type radiant tube is arranged in the transition region is more than the preheating
The quantity of heat accumulation type radiant tube is set in area and less than the quantity that heat accumulation type radiant tube is arranged in the gas-producing area.Thus, it is possible to
Further improve the efficiency of the pyrolysis processing.
Embodiments in accordance with the present invention, the activation unit is rotary activated furnace, and the rotary activated furnace includes：Plus
Hot-zone, the feed end of the thermal treatment zone is connected with the pyrolyzing sludge charcoal discharging opening by pyrolyzing sludge charcoal discharging spiral, is suitable to
The pyrolyzing sludge charcoal is heated；Region of activation, the region of activation is connected with the thermal treatment zone, is suitable to through the heating
Pyrolyzing sludge charcoal afterwards carries out activation processing, to obtain activated carbon；And cooling area, the cooling area and the region of activation phase
Even, it is suitable to that the activated carbon is lowered the temperature, wherein, the catalytic burner includes：Fuel pre-mix zone, the fuel pre-mix zone
Air intake and fuel gas inlet are provided with, the air that is fed to are suitable to and combustion gas is mixed, obtain gaseous mixture；And be covered with
The carrier of catalyst.According to a preferred embodiment of the invention, the excess air coefficient of the gaseous mixture is 2.Thus, it is possible to enter one
Step improves the efficiency of the activation processing.
Embodiments in accordance with the present invention, the system is further included：Cleaner unit, the cleaner unit and the activation unit
It is connected by flue, is suitable to for the flue gas produced in the activation unit to carry out dedusting.
Embodiments in accordance with the present invention, the system is further included：Heat exchanger, the heat exchanger is arranged at the flue gas
On pipeline.Thus, it is easy to the recycling of heat.
Embodiments in accordance with the present invention, the system is further included：Aerator, the aerator and the thermal treatment zone phase
Even, it is suitable to supply air to the thermal treatment zone.Thus, it is easy to fuel gas buring heat release, it is anti-to promote pyrolyzing sludge charcoal that activation occurs
Should.
Embodiments in accordance with the present invention, the gas-liquid separation unit includes：Pyrolysis gas inlet port, the pyrolysis gas inlet port
It is connected with the pyrolysis gas air vent；First gas pipeline, first gas pipeline is connected with the heat accumulation type radiant tube, fits
In making the detached a part of fuel gas supply of the gas-liquid separation unit to the heat accumulation type radiant tube as fuel；Second Gas Pipe
Road, second gas pipeline is connected by the heat exchanger with the activation unit；And tar outlet, the tar outlet
It is connected with the producing steam unit, is suitable to the detached tar of the gas-liquid separation unit be supplied to the producing steam unit.
Embodiments in accordance with the present invention, the particle diameter of the sludge is not more than 100nm, preferably 45～55nm.Thus, it is possible to aobvious
Write the efficiency for improving the pyrolysis processing.
Embodiments in accordance with the present invention, the producing steam unit includes：Tar enters pipeline, the tar enter pipeline with
The tar outlet is connected, and is suitable to the detached tar of the gas-liquid separation unit be supplied to the producing steam unit；First
Jet chimney, first jet chimney is connected with the drying unit, is suitable to the detached part of the gas-liquid separation unit
High-temperature steam is supplied to the drying unit；And second jet chimney, second jet chimney and the activation unit
It is connected, is suitable to the detached another part high-temperature steam of the gas-liquid separation unit be supplied to the activation unit, according to this
The specific embodiment of invention, it is 1 to supply to the high-temperature steam amount and the pyrolyzing sludge charcoal mass ratio of the activation unit:
1.5。
In another aspect of this invention, the present invention proposes a kind of using the system system for preparing activated carbon described above
The method of standby activated carbon.Embodiments in accordance with the present invention, methods described includes：Sludge is put in the drying unit, is carried out
Drying；Sludge after the drying is sent in the pyrolysis unit by the sludge inlet, pyrolysis processing is carried out, heat is obtained
Vent one's spleen and pyrolyzing sludge charcoal；The pyrolysis gas are supplied to the gas-liquid separation unit, gas-liquid separation is carried out, to obtain combustion gas
And tar；The tar is supplied to the producing steam unit, to obtain high-temperature steam；And by the pyrolyzing sludge charcoal and
The part high-temperature steam is supplied to the activation unit, to carry out activation processing to the pyrolyzing sludge charcoal, obtains activity
Charcoal.
Thus, the method for preparing activated carbon according to embodiments of the present invention is single to pyrolysis by the way that the sludge of drying is supplied
Unit carries out pyrolysis processing, obtains pyrolysis gas and pyrolyzing sludge charcoal, and pyrolysis gas obtain combustion gas and tar Jing after gas-liquid separation, wherein
Tar can make the burning of producing steam unit produce high-temperature steam, outside for producing steam unit as the fuel of producing steam unit
Plus the energy, and then high-temperature steam and pyrolyzing sludge charcoal are supplied to activation unit carry out activation processing, obtain activated carbon and high temperature
Flue gas.The method achieve making full use of for sludge, by the deep processing of pyrolyzing sludge charcoal for high added value activated carbon, and energy consumption compared with
It is low, it is environmentally friendly, it is adapted to large-scale promotion.
Embodiments in accordance with the present invention, methods described is further included：The combustion gas is respectively fed to into the pyrolysis single
The catalytic burner in heat accumulation type radiant tube and/or the activation unit in unit；High-temperature steam described in another part is supplied
To the drying unit, to be dried for the sludge.
Embodiments in accordance with the present invention, the temperature of the activation is 800～950 DEG C.Thus, it is possible to significantly improve the work
Change the efficiency for processing.
Embodiments in accordance with the present invention, the temperature of the pyrolysis is 500～850 DEG C.Thus, it is possible to significantly improve the heat
The efficiency that solution is processed.
Embodiments in accordance with the present invention, the sludge after the drying pass sequentially through the feed zone, preheating zone, transition region,
Gas-producing area and discharge zone, wherein, the temperature of the preheating zone is 150～400 DEG C, and the temperature of the transition region is 400～500
DEG C, the temperature of the gas-producing area is 500～850 DEG C.Thus, it is possible to significantly improve the efficiency of the pyrolysis processing.
Embodiments in accordance with the present invention, oxygen content is that 8～10 mass %, carbon dioxide contain in the flue gas that the burning is produced
Measure and be less than 4mg/m for 4～6 mass %, CO contents3、NOxContent is less than 10mg/m3.Thus, it is possible to significantly improve at the activation
The efficiency of reason, improves activated carbon quality.
The additional aspect and advantage of the present invention will be set forth in part in the description, and partly will become from the following description
Obtain substantially, or recognized by the practice of the present invention.
Description of the drawings
The above-mentioned and/or additional aspect and advantage of the present invention will become from the description with reference to accompanying drawings below to embodiment
It is substantially and easy to understand, wherein：
Fig. 1 shows the structural representation for preparing carbide system according to an embodiment of the invention；And
Fig. 2 shows the schematic flow sheet for preparing carbide method according to an embodiment of the invention.
Specific embodiment
Embodiments of the invention are described below in detail.The embodiments described below is exemplary, is only used for explaining this
It is bright, and be not considered as limiting the invention.
It should be noted that term " first ", " second " are only used for describing purpose, and it is not intended that indicating or implying phase
To importance or the implicit quantity for indicating indicated technical characteristic.Thus, " first " is defined, the feature of " second " can be with
Express or implicitly include one or more this feature.Further, in describing the invention, unless otherwise saying
Bright, " multiple " are meant that two or more.
In describing the invention, it is to be understood that unless otherwise clearly defined and limited, term " connected " should do
Broadly understood, for example, it may be fixedly connected, or be detachably connected, or it is integral；Can be mechanically connected, also may be used
Be electrical connection；Can be joined directly together, it is also possible to be indirectly connected to by intermediary, can be the connection of two element internals
Or the interaction relationship of two elements, unless otherwise clearly restriction.For the ordinary skill in the art, can be with
Above-mentioned term concrete meaning in the present invention is understood as the case may be.
The present invention proposes a kind of system and method for preparing activated carbon, will be described in greater detail respectively below.
The system for preparing activated carbon
In one aspect of the invention, the present invention proposes a kind of system for preparing activated carbon.Enforcement of the invention
Example, referring to Fig. 1, the system includes：Drying unit 1, pyrolysis unit 2, gas-liquid separation unit 3, producing steam unit 4 and activation are single
Unit 5.
Embodiments in accordance with the present invention, drying unit 1 is suitable to be dried in sludge, to carry out follow-up pyrolysis processing.
According to a particular embodiment of the invention, it is adaptable to which the sludge particle diameter of revolving bed is not particularly limited, the present invention's
In some preferred embodiments, in below 100mm, the excessive resource utilization of particle diameter is reduced the sludge particle diameter that the revolving bed is adopted, knot
The characteristics of closing revolving bed, in being embodied as, particle diameter can give full play to revolving bed pyrolysis advantage for 45～55mm, and reach splendid
Resource utilization.
Embodiments in accordance with the present invention, pyrolysis unit 2 is provided with sludge inlet 21 and pyrolyzing sludge charcoal discharging opening 22, should
Sludge inlet is connected with drying unit 1, and pyrolysis unit 2 is suitable to be pyrolyzed in the sludge after drying, to obtain pyrolysis gas
With pyrolyzing sludge charcoal.
Embodiments in accordance with the present invention, the condition of pyrolysis processing is not particularly restricted, and those skilled in the art can be with root
Selected according to being actually needed, according to a particular embodiment of the invention, pyrolysis processing can be carried out under 500～850 degrees Celsius.
Inventor's discovery, if the temperature of pyrolysis processing is too low, cannot make the larger molecular organicses in sludge effectively be decomposed into Jiao
The micromolecular compounds such as oil；And if the temperature of pyrolysis processing is too high, then increase can energy consumption.
According to a particular embodiment of the invention, pyrolysis unit is revolving bed, along Flow of Goods and Materials direction, the pyrolysis unit according to
It is secondary including：Feed zone 201, preheating zone 202, transition region 203, gas-producing area 204 and discharge zone 205.
According to a particular embodiment of the invention, feed zone 201 is provided with sludge inlet 21, and sludge inlet passes through sludge
Feed auger A is connected with drying unit 5.
According to a particular embodiment of the invention, preheating zone 202 is provided with vapor air vent 206, vapor air vent 206
It is connected with drying unit 1, the vapor air vent is suitable to the supply of the vapor obtained by the sludge after drying is preheated
To drying unit.
According to a particular embodiment of the invention, gas-producing area 204 is provided with pyrolysis gas air vent 207, pyrolysis gas air vent 207
It is connected with gas-liquid separation unit 3, is suitable to the pyrolysis gas of generation be supplied to gas-liquid separation unit 3.
According to a particular embodiment of the invention, discharge zone 205 is provided with pyrolyzing sludge charcoal discharging opening 22.
According to a particular embodiment of the invention, it is provided with heat accumulating type spoke in preheating zone 202, transition region 203 and gas-producing area 204
Penetrate pipe 208.According to a preferred embodiment of the invention, the quantity that heat accumulation type radiant tube is arranged in transition region is arranged more than in preheating zone
The quantity of heat accumulation type radiant tube and less than in gas-producing area arrange heat accumulation type radiant tube quantity.
According to a particular embodiment of the invention, the temperature of preheating zone is 150～400 DEG C, the temperature of transition region is 400～
500 DEG C, the temperature of gas-producing area is 500～850 DEG C.
Specifically, with natural gas start heat accumulation type radiant tube, this radial canal it is uneven be distributed in preheating zone, transition region and
Gas-producing area, and its quantitative relation is preheating zone ＜ transition regions ＜ gas-producing area, after normal gas producing, can be separated gas-liquid separation unit
Combustion gas be passed through heat accumulation type radiant tube as fuel；Sludge feeding drying plant is dried, sludge can be from moisture content 80%
Left and right is dried to 50%, Jing sludge inlets and for sludge to send into revolving bed 1 by feed zone, is further dried in preheating zone, by water
Steam is discharged by vapor air vent, and the part high-temperature steam sent with producing steam unit sends into sludge drying unit after mixing,
Preheated sludge separates out volatile matters in gas-producing area high temperature, and between 500～850 DEG C, gained pyrolysis gas pass through gas-producing area temperature
Pyrolysis gas air vent delivers to gas-liquid separation unit, and gained pyrolyzing sludge charcoal sends into activation in discharge zone Jing pyrolyzing sludge charcoals discharging opening
Unit.
Embodiments in accordance with the present invention, gas-liquid separation unit 3 is connected with pyrolysis unit, is suitable to separate pyrolysis gas, so as to
Obtain combustion gas and tar.Specifically, the combustion gas for obtaining has certain calorific value, can be further used as needed for subsequent step
Fuel gas is used, and the tar for obtaining can be stored and for sale, it is also possible to be passed through producing steam unit, uses as fuel
In output high-temperature steam.
Embodiments in accordance with the present invention, gas-liquid separation unit includes：Pyrolysis gas inlet port E, the first gas pipeline 301,
Two Gas Pipes 302 and tar outlet F.Embodiments in accordance with the present invention, combustion gas has certain calorific value, can be used as heat accumulating type
The fuel gas of radial canal and catalytic burner is used, without the need for being passed through extra fuel gas in addition, such that it is able to reduce pyrolysis
Process the energy consumption with activation processing.
According to a particular embodiment of the invention, the pyrolysis gas inlet port E is connected with pyrolysis gas air vent 22.
According to a particular embodiment of the invention, the first gas pipeline 301 is connected with heat accumulation type radiant tube 208, is suitable to make gas
The detached a part of fuel gas supply of liquid separative element 3 is to heat accumulation type radiant tube 208 as fuel.Embodiments in accordance with the present invention,
Combustion gas has certain calorific value, can be used as the fuel gas of heat accumulation type radiant tube, without the need for being passed through extra combustion in addition
Material gas, such that it is able to reduce pyrolysis processing energy consumption.
According to a particular embodiment of the invention, the second gas pipeline 302 is connected by heat exchanger 8 with activation unit 5.According to
Embodiments of the invention, combustion gas has certain calorific value, can be used as the fuel gas of catalytic burner, without the need in addition
Extra fuel gas is passed through, such that it is able to reduce the energy consumption of activation processing.Additionally, the high-temperature flue gas produced by activation unit can be with
Combustion gas carries out heat exchange in heat exchanger, so as to improve the heat of fuel gas with low heat value so that combustion gas is reachable in catalytic burner
To the exothermal effect equal with natural gas.
According to a particular embodiment of the invention, tar outlet F is connected with producing steam unit 4, is suitable to gas-liquid separation unit 3
Detached tar is supplied to producing steam unit 4.
Specifically, the isolated combustion gas of pyrolysis gas Jing gas-liquid separation units and tar.Wherein combustion gas is divided into two-way, the first via
The gas pipelines of combustion gas Jing first are delivered to the heat accumulation type radiant tube of revolving bed, can pass through the burner aperture for adjusting heat accumulation type radiant tube
To control the thermal discharge of radial canal, while adjusting the temperature in each area of revolving bed；Second tunnel combustion gas is being changed by the second gas pipeline
The catalytic burner arranged in the activation unit thermal treatment zone is passed through after exchanging heat in hot device, the purpose exchanged heat in heat exchanger is to improve low
The heat of calorific value fuel gas so that combustion gas can reach the exothermal effect equal with natural gas in catalytic burner.
Embodiments in accordance with the present invention, producing steam unit 4 is connected with gas-liquid separation unit 3, is suitable to supply Some gases
To producing steam unit 4, high-temperature steam is obtained.Embodiments in accordance with the present invention, the high-temperature steam for obtaining can meet follow-up work
Quantity of steam needed for change process, such that it is able to reduce the energy consumption of activation processing.
It should be noted that for the equipment of producing steam unit does not make considered critical, as long as can realize that output high temperature steams
Vapour.According to a particular embodiment of the invention, producing steam unit can be gas fired-boiler.Thus, gas-liquid separation unit output
Tar can be cost-effective to reduce the fuel of extra input as the fuel of gas fired-boiler.
According to a particular embodiment of the invention, producing steam unit includes：Tar enters pipeline 401, the first jet chimney 402
With the second jet chimney 403.
According to a particular embodiment of the invention, tar is connected into pipeline 401 with tar outlet F, is suitable to gas-liquid separation
The detached tar of unit 3 is supplied to producing steam unit.
According to a particular embodiment of the invention, the first jet chimney 402 is connected with drying unit 1, is suitable to gas-liquid separation
The detached part high-temperature steam of unit 3 is supplied to drying unit 1.
According to a particular embodiment of the invention, the second jet chimney 403 is connected with activation unit 5, is suitable to gas-liquid separation
The detached another part high-temperature steam of unit 3 is supplied to activation unit 5.
According to a particular embodiment of the invention, supply to the high-temperature steam amount and pyrolyzing sludge charcoal mass ratio of activation unit
For 1:1.5.Thus, further heating pyrolyzing sludge charcoal so as to reach activation temperature, there is activation to obtain activated carbon.
Specifically, the tar isolated by gas-liquid separation unit is passed directly into producing steam unit combustion heat release, institute's producing steam
It is divided into two-way, first via steam is passed through after the first jet chimney mixes with the vapor for coming from the generation of revolving bed preheating zone
Sludge drying unit, sludge is dried to 50% by moisture content 80%.Second road the second jet chimneys of steam Jing send into swinging
Activation furnace, for activated sludge pyrolytic carbon.
Embodiments in accordance with the present invention, activation unit 5 respectively with pyrolyzing sludge charcoal discharging opening 22 and the phase of producing steam unit 4
Even, it is suitable to pyrolyzing sludge charcoal and part high-temperature steam be supplied to activation unit 5 so that pyrolyzing sludge charcoal carries out activation processing,
To obtain activated carbon.
According to a particular embodiment of the invention, activation unit is rotary activated furnace, and rotary activated furnace includes：The thermal treatment zone
501st, region of activation 502 and cooling area 503.
According to a particular embodiment of the invention, the feed end of the thermal treatment zone 501 passes through sludge with pyrolyzing sludge charcoal discharging opening 22
Pyrolytic carbon discharging spiral B is connected, and is suitable to heat pyrolyzing sludge charcoal.
According to a particular embodiment of the invention, region of activation 502 is connected with the thermal treatment zone 501, is suitable to the dirt after heating
Mud pyrolytic carbon carries out activation processing, to obtain activated carbon.
According to a particular embodiment of the invention, cooling area 503 is connected with region of activation 502, is suitable to that activated carbon is lowered the temperature.
According to a particular embodiment of the invention, catalytic burner 6 is provided with the thermal treatment zone.Specifically, the catalytic burner
Including：Fuel pre-mix zone 601, fuel pre-mix zone is provided with air intake C and fuel gas inlet D, and fuel pre-mix zone is suitable to be passed through
Air and combustion gas mixed, obtain gaseous mixture；And it is covered with the carrier 602 of catalyst.It is of the invention to be embodied as
Example, the carrier for being covered with catalyst is the honeycomb-typed steel for being moistened with catalyst.
Specifically, activation unit is firstly the need of being heated to 800 DEG C, and ensures the oxygen content in stove, and its origin of heat is in urging
Change burner, be poor fuel, oxygen-enriched combusting due to being catalyzed burning, meet the oxygen content in activation furnace；Enforcement of the invention
Example, in the flue gas after catalysis burning, oxygen content 9% or so, carbon dioxide content 5% or so, it is ensured that oxygen content in activation furnace
Meanwhile, carbon dioxide also can react with the white carbon black in pyrolyzing sludge charcoal, improve the quality of activated carbon；Meanwhile, catalytic combustion flue gas
Middle pollutant load is extremely low, and CO is less than 4mg/m3, NOXContent is less than 10mg/m3, pollutant near-zero release.
Embodiments in accordance with the present invention, the condition of activation processing is not particularly restricted, and those skilled in the art can be with root
Selected according to being actually needed, according to a particular embodiment of the invention, activation processing is completed under 800～950 degrees Celsius.
Inventor's discovery, using the temperature activation processing is carried out, and can be significantly improved the efficiency of activation processing and be improved what is prepared
The quality of activated carbon.
Specifically, embodiments in accordance with the present invention, start first the catalytic burner in rotary activated furnace, and make wherein
Excess air coefficient be 2, make combustion gas and air being moistened with the honeycomb-typed steel surface-stable flameless combustion of catalyst,
So as to transmit heat in the way of radiating in rotary activated furnace, further, high-temperature steam is sprayed to pyrolyzing sludge charcoal, made
The temperature of pyrolyzing sludge charcoal is further raised, while constantly activating by the continuous contact with high-temperature steam, generates activated carbon.This
Outward, the carbon dioxide in rotary activated furnace can be to react, so as to improve what is prepared with the white carbon black in pyrolyzing sludge charcoal
The quality of activated carbon, further increases the specific surface area of activated carbon.
Embodiments in accordance with the present invention, the system is further included：Cleaner unit 7, heat exchanger 8 and aerator 9.
According to a particular embodiment of the invention, cleaner unit 7 is connected with activation unit 5 by flue 701, is suitable to work
Changing the flue gas produced in unit 5 carries out dedusting.Embodiments in accordance with the present invention, by rotary activated furnace exclude high-temperature flue gas with
After preparation supply carries out heat exchange to the combustion gas of catalytic burner in heat exchanger, qualified discharge after removing dust device dedusting.Due to
Rotary activated furnace is heated using catalytic burner, pollutant load is extremely low in the tail gas after high-temperature flue gas removing dust,
Wherein CO contents are not higher than 4 milligrams/cubic metre, NOxContent is not higher than 10 milligrams/cubic metre.
According to a particular embodiment of the invention, heat exchanger 8 is arranged on flue 701, additionally, by gas-liquid separation unit
Isolated part high-temperature steam flows through heat exchanger, then is passed through activation unit.Thus, activation processing produce high-temperature flue gas with
The detached Some gases of gas-liquid separation unit can realize heat exchange, such that it is able to effectively improve the calorific value of combustion gas, make combustion gas
The exothermal effect equal with natural gas can be reached when burning in catalytic burner.
According to a particular embodiment of the invention, aerator 9 is connected with air intake C, is suitable to empty to the supply of fuel pre-mix zone
Gas.Thus, the air being passed through combustion gas detached with gas-liquid separation unit is on the honeycomb-typed steel surface for being moistened with catalyst
Stable flameless combustion, so as to transmit heat in the way of radiating in rotary activated furnace.
Thus, the system for preparing activated carbon according to embodiments of the present invention is single to pyrolysis by the way that the sludge of drying is supplied
Unit carries out pyrolysis processing, obtains pyrolyzing sludge charcoal and pyrolysis gas.Pyrolysis gas obtain combustion gas and tar Jing after gas-liquid separation, wherein
Tar can make the burning of producing steam unit produce high-temperature steam as the fuel of producing steam unit, and combustion gas can be respectively as combustion
Material gas supplies the catalytic burner in heat accumulation type radiant tube and/or activation unit to pyrolysis unit, so as to steam to produce
Vapour unit, heat accumulation type radiant tube and catalytic burner external energy.High-temperature steam and pyrolyzing sludge charcoal are supplied to activation unit
Activation processing is carried out, activated carbon and high-temperature flue gas are obtained.It is computed, production 1t activated carbons need 2t steam, 2.5～3t sludge hots
Solution charcoal can produce 1t activated carbons.The system realizes making full use of for sludge, by the work that the deep processing of pyrolyzing sludge charcoal is high added value
Property charcoal, and energy consumption is relatively low, environmentally friendly, is adapted to large-scale promotion.
The method for preparing activated carbon
In another aspect of this invention, the present invention proposes a kind of method for preparing activated carbon.Enforcement of the invention
Example, referring to Fig. 2, the method includes：
S100 is dried
In this step, sludge is put in drying unit, is dried.Thus, to carry out follow-up pyrolysis processing.
According to a particular embodiment of the invention, it is adaptable to which the sludge particle diameter of revolving bed is not particularly limited, the present invention's
In some preferred embodiments, in below 100mm, the excessive resource utilization of particle diameter is reduced the sludge particle diameter that the revolving bed is adopted, knot
The characteristics of closing revolving bed, in being embodied as, particle diameter can give full play to revolving bed pyrolysis advantage for 45～55mm, and reach splendid
Resource utilization.
S200 is pyrolyzed
In this step, the sludge after drying is sent in pyrolysis unit by sludge inlet, carries out pyrolysis processing, obtain
Pyrolysis gas and pyrolyzing sludge charcoal.
Embodiments in accordance with the present invention, the condition of pyrolysis processing is not particularly restricted, and those skilled in the art can be with root
Selected according to being actually needed, according to a particular embodiment of the invention, pyrolysis processing can be carried out under 500～850 degrees Celsius.
Inventor's discovery, if the temperature of pyrolysis processing is too low, cannot make the larger molecular organicses in sludge effectively be decomposed into Jiao
The micromolecular compounds such as oil；And if the temperature of pyrolysis processing is too high, then increase can energy consumption.
According to a particular embodiment of the invention, pyrolysis unit is revolving bed, along Flow of Goods and Materials direction, the pyrolysis unit according to
It is secondary including：Feed zone 201, preheating zone 202, transition region 203, gas-producing area 204 and discharge zone 205.
According to a particular embodiment of the invention, feed zone 201 is provided with sludge inlet 21, and sludge inlet passes through sludge
Feed auger A is connected with drying unit 5.
According to a particular embodiment of the invention, preheating zone 202 is provided with vapor air vent 206, vapor air vent 206
It is connected with drying unit 1, the vapor air vent is suitable to the supply of the vapor obtained by the sludge after drying is preheated
To drying unit.
According to a particular embodiment of the invention, gas-producing area 204 is provided with pyrolysis gas air vent 207, pyrolysis gas air vent 207
It is connected with gas-liquid separation unit 3, is suitable to the pyrolysis gas of generation be supplied to gas-liquid separation unit 3.
According to a particular embodiment of the invention, discharge zone 205 is provided with pyrolyzing sludge charcoal discharging opening 22.
According to a particular embodiment of the invention, it is provided with heat accumulating type spoke in preheating zone 202, transition region 203 and gas-producing area 204
Penetrate pipe 208.According to a preferred embodiment of the invention, the quantity that heat accumulation type radiant tube is arranged in transition region is arranged more than in preheating zone
The quantity of heat accumulation type radiant tube and less than in gas-producing area arrange heat accumulation type radiant tube quantity.
According to a particular embodiment of the invention, the sludge after drying passes sequentially through feed zone, preheating zone, transition region, aerogenesis
Area and discharge zone, wherein, the temperature of preheating zone is 150～400 DEG C, and the temperature of transition region is 400～500 DEG C, the temperature of gas-producing area
Spend for 500～850 DEG C.
Specifically, with natural gas start heat accumulation type radiant tube, this radial canal it is uneven be distributed in preheating zone, transition region and
Gas-producing area, and its quantitative relation is preheating zone ＜ transition regions ＜ gas-producing area, after normal gas producing, can be separated gas-liquid separation unit
Combustion gas be passed through heat accumulation type radiant tube as fuel；Sludge feeding drying plant is dried, sludge can be from moisture content 80%
Left and right is dried to 50%, Jing sludge inlets and for sludge to send into revolving bed 1 by feed zone, is further dried in preheating zone, by water
Steam is discharged by vapor air vent, and the part high-temperature steam sent with producing steam unit sends into sludge drying unit after mixing,
Preheated sludge separates out volatile matters in gas-producing area high temperature, and between 500～850 DEG C, gained pyrolysis gas pass through gas-producing area temperature
Pyrolysis gas air vent delivers to gas-liquid separation unit, and gained pyrolyzing sludge charcoal sends into activation in discharge zone Jing pyrolyzing sludge charcoals discharging opening
Unit.
S300 gas-liquid separations
In this step, pyrolysis gas are supplied to gas-liquid separation unit, carries out gas-liquid separation, to obtain combustion gas and Jiao
Oil.Specifically, the combustion gas for obtaining has certain calorific value, and the fuel gas that can be further used as needed for subsequent step is in addition sharp
With, and the tar for obtaining can be stored and for sale, it is also possible to producing steam unit is passed through, as fuel for the steaming of output high temperature
Vapour.
Embodiments in accordance with the present invention, the method is further included：Accumulation of heat combustion gas being respectively fed in pyrolysis unit
Catalytic burner in formula radial canal and/or activation unit.
Embodiments in accordance with the present invention, gas-liquid separation unit includes：Pyrolysis gas inlet port E, the first gas pipeline 301,
Two Gas Pipes 302 and tar outlet F.Embodiments in accordance with the present invention, combustion gas has certain calorific value, can be used as heat accumulating type
The fuel gas of radial canal and catalytic burner is used, without the need for being passed through extra fuel gas in addition, such that it is able to reduce pyrolysis
Process the energy consumption with activation processing.
According to a particular embodiment of the invention, the pyrolysis gas inlet port E is connected with pyrolysis gas air vent 22.
According to a particular embodiment of the invention, the first gas pipeline 301 is connected with heat accumulation type radiant tube 208, is suitable to make gas
The detached a part of fuel gas supply of liquid separative element 3 is to heat accumulation type radiant tube 208 as fuel.Embodiments in accordance with the present invention,
Combustion gas has certain calorific value, can be used as the fuel gas of heat accumulation type radiant tube, without the need for being passed through extra combustion in addition
Material gas, such that it is able to reduce pyrolysis processing energy consumption.
According to a particular embodiment of the invention, the second gas pipeline 302 is connected by heat exchanger 8 with activation unit 5.According to
Embodiments of the invention, combustion gas has certain calorific value, can be used as the fuel gas of catalytic burner, without the need in addition
Extra fuel gas is passed through, such that it is able to reduce the energy consumption of activation processing.Additionally, the high-temperature flue gas produced by activation unit can be with
Combustion gas carries out heat exchange in heat exchanger, so as to improve the heat of fuel gas with low heat value so that combustion gas is reachable in catalytic burner
To the exothermal effect equal with natural gas.
According to a particular embodiment of the invention, tar outlet F is connected with producing steam unit 4, is suitable to gas-liquid separation unit 3
Detached tar is supplied to producing steam unit 4.
Specifically, the isolated combustion gas of pyrolysis gas Jing gas-liquid separation units and tar.Wherein combustion gas is divided into two-way, the first via
The gas pipelines of combustion gas Jing first are delivered to the heat accumulation type radiant tube of revolving bed, can pass through the burner aperture for adjusting heat accumulation type radiant tube
To control the thermal discharge of radial canal, while adjusting the temperature in each area of revolving bed；Second tunnel combustion gas is being changed by the second gas pipeline
The catalytic burner arranged in the activation unit thermal treatment zone is passed through after exchanging heat in hot device, the purpose exchanged heat in heat exchanger is to improve low
The heat of calorific value fuel gas so that combustion gas can reach the exothermal effect equal with natural gas in catalytic burner.
S400 producing steams
In this step, tar is supplied to producing steam unit, to obtain high-temperature steam.Enforcement of the invention
Example, the high-temperature steam for obtaining can meet the quantity of steam needed for subsequent activation process, such that it is able to reduce the energy of activation processing
Consumption.
It should be noted that for the equipment of producing steam unit does not make considered critical, as long as can realize that output high temperature steams
Vapour.According to a particular embodiment of the invention, producing steam unit can be gas fired-boiler.Thus, gas-liquid separation unit output
Tar can be cost-effective to reduce the fuel of extra input as the fuel of gas fired-boiler.
According to a particular embodiment of the invention, producing steam unit includes：Tar enters pipeline 401, the first jet chimney 402
With the second jet chimney 403.
According to a particular embodiment of the invention, tar is connected into pipeline 401 with tar outlet F, is suitable to gas-liquid separation
The detached tar of unit 3 is supplied to producing steam unit.
Embodiments in accordance with the present invention, the method is further included：Another part high-temperature steam is supplied to drying unit
It is interior, to be dried for sludge.
According to a particular embodiment of the invention, the first jet chimney 402 is connected with drying unit 1, is suitable to gas-liquid separation
The detached part high-temperature steam of unit 3 is supplied to drying unit 1.
According to a particular embodiment of the invention, the second jet chimney 403 is connected with activation unit 5, is suitable to gas-liquid separation
The detached another part high-temperature steam of unit 3 is supplied to activation unit 5.
According to a particular embodiment of the invention, supply to the high-temperature steam amount and pyrolyzing sludge charcoal mass ratio of activation unit
For 1:1.5.Thus, further heating pyrolyzing sludge charcoal so as to reach activation temperature, there is activation to obtain activated carbon.
Specifically, the tar isolated by gas-liquid separation unit is passed directly into producing steam unit combustion heat release, institute's producing steam
It is divided into two-way, first via steam is passed through after the first jet chimney mixes with the vapor for coming from the generation of revolving bed preheating zone
Sludge drying unit, sludge is dried to 50% by moisture content 80%.Second road the second jet chimneys of steam Jing send into swinging
Activation furnace, for activated sludge pyrolytic carbon.
S500 is activated
In this step, by the supply of pyrolyzing sludge charcoal and high-temperature steam to activation unit, to enter to pyrolyzing sludge charcoal
Row activation processing, to obtain activated carbon.
Embodiments in accordance with the present invention, activation unit 5 respectively with pyrolyzing sludge charcoal discharging opening 22 and the phase of producing steam unit 4
Even, it is suitable to pyrolyzing sludge charcoal and part high-temperature steam be supplied to activation unit 5 so that pyrolyzing sludge charcoal carries out activation processing,
To obtain activated carbon.
According to a particular embodiment of the invention, activation unit is rotary activated furnace, and rotary activated furnace includes：The thermal treatment zone
501st, region of activation 502 and cooling area 503.
According to a particular embodiment of the invention, the feed end of the thermal treatment zone 501 passes through sludge with pyrolyzing sludge charcoal discharging opening 22
Pyrolytic carbon discharging spiral B is connected, and is suitable to heat pyrolyzing sludge charcoal.
According to a particular embodiment of the invention, region of activation 502 is connected with the thermal treatment zone 501, is suitable to the dirt after heating
Mud pyrolytic carbon carries out activation processing, to obtain activated carbon.
According to a particular embodiment of the invention, cooling area 503 is connected with region of activation 502, is suitable to that activated carbon is lowered the temperature.
According to a particular embodiment of the invention, catalytic burner 6 is provided with the thermal treatment zone.Specifically, the catalytic burner
Including：Fuel pre-mix zone 601, fuel pre-mix zone is provided with air intake C and fuel gas inlet D, and fuel pre-mix zone is suitable to be passed through
Air and combustion gas mixed, obtain gaseous mixture；And it is covered with the carrier 602 of catalyst.It is of the invention to be embodied as
Example, the carrier for being covered with catalyst is the honeycomb-typed steel for being moistened with catalyst.
Specifically, activation unit is firstly the need of being heated to 800 DEG C, and ensures the oxygen content in stove, and its origin of heat is in urging
Change burner, be poor fuel, oxygen-enriched combusting due to being catalyzed burning, meet the oxygen content in activation furnace；Enforcement of the invention
Example, in the flue gas after catalysis burning, oxygen content 9% or so, carbon dioxide content 5% or so, it is ensured that oxygen content in activation furnace
Meanwhile, carbon dioxide also can react with the white carbon black in pyrolyzing sludge charcoal, improve the quality of activated carbon；Meanwhile, catalytic combustion flue gas
Middle pollutant load is extremely low, and CO is less than 4mg/m3, NOXContent is less than 10mg/m3, pollutant near-zero release.
Embodiments in accordance with the present invention, the condition of activation processing is not particularly restricted, and those skilled in the art can be with root
Selected according to being actually needed, according to a particular embodiment of the invention, activation processing is completed under 800～950 degrees Celsius.
Inventor's discovery, using the temperature activation processing is carried out, and can be significantly improved the efficiency of activation processing and be improved what is prepared
The quality of activated carbon.
Specifically, embodiments in accordance with the present invention, start first the catalytic burner in rotary activated furnace, and make wherein
Excess air coefficient be 2, make combustion gas and air being moistened with the honeycomb-typed steel surface-stable flameless combustion of catalyst,
So as to transmit heat in the way of radiating in rotary activated furnace, further, high-temperature steam is sprayed to pyrolyzing sludge charcoal, made
The temperature of pyrolyzing sludge charcoal is further raised, while constantly activating by the continuous contact with high-temperature steam, generates activated carbon.This
Outward, the carbon dioxide in rotary activated furnace can be to react, so as to improve what is prepared with the white carbon black in pyrolyzing sludge charcoal
The quality of activated carbon, further increases the specific surface area of activated carbon.
Thus, the method for preparing activated carbon according to embodiments of the present invention is single to pyrolysis by the way that the sludge of drying is supplied
Unit carries out pyrolysis processing, obtains pyrolyzing sludge charcoal and pyrolysis gas.Pyrolysis gas obtain combustion gas and tar Jing after gas-liquid separation, wherein
Tar can make the burning of producing steam unit produce high-temperature steam as the fuel of producing steam unit, and combustion gas can be respectively as combustion
Material gas supplies the catalytic burner in heat accumulation type radiant tube and/or activation unit to pyrolysis unit, so as to steam to produce
Vapour unit, heat accumulation type radiant tube and catalytic burner external energy.High-temperature steam and pyrolyzing sludge charcoal are supplied to activation unit
Activation processing is carried out, activated carbon and high-temperature flue gas are obtained.It is computed, production 1t activated carbons need 2t steam, 2.5～3t sludge hots
Solution charcoal can produce 1t activated carbons.Making full use of for sludge is the method achieved, by the work that the deep processing of pyrolyzing sludge charcoal is high added value
Property charcoal, and energy consumption is relatively low, environmentally friendly, is adapted to large-scale promotion.
The solution of the present invention is explained below in conjunction with embodiment.It will be understood to those of skill in the art that following
Embodiment is merely to illustrate the present invention, and should not be taken as limiting the scope of the invention.Unreceipted particular technique or bar in embodiment
Part, carry out according to the technology or condition described by document in the art or according to product description.Agents useful for same or instrument
The unreceipted production firm person of device, be can pass through city available from conventional products.
Embodiment 1
It is 939m by heap density3/ kg, Changping sewage plant sludge of moisture content 80% is passed through drying unit, the dirt after drying
Mud moisture content position 50%, is sent in stove by the feed zone of revolving bed and is pyrolyzed.Revolving bed rotates a circle used time 90min, in burner hearth
Temperature Distribution be：150～400 DEG C of preheating zone；400～500 DEG C of transition region；500～850 DEG C of gas-producing area.Pyrolysis after pyrolysis
Gas is supplied to gas-liquid separation unit and carries out gas-liquid separation, obtains combustion gas and tar.Pyrolysis gas, pyrolyzing sludge charcoal and Jiao after pyrolysis
The yield of oil is shown in Table 1, and the Industrial Analysis of pyrolyzing sludge charcoal and elementary analysiss are shown in Table 2, and the gas componant and calorific value of pyrolysis gas are shown in Table
3.Pyrolyzing sludge charcoal is passed through into rotary activated furnace, the temperature in activation furnace more than 800 DEG C, by catalytic burner so that
Oxygen content is 9% in activation furnace, opens steam so that pyrolyzing sludge charcoal is 1.5 with steam rates:1, pyrolyzing sludge charcoal is in heating
Area rises to 800 DEG C by 600 DEG C, and is rotated into region of activation with body of heater, now after pyrolyzing sludge charcoal and vapor haptoreaction, temperature
Degree is quickly raised to 950 DEG C, and the activation through 30min enters cooling area, generates the activated carbon of high-quality, and its iodine number is more than
1000mg/g。
Products collection efficiency after the pyrolysis of the municipal sludge of table 1.
| Operating mode | Solid productivity/% | Gas yield/% | Oily yield/% | Aquatic product rate/% |
| 1 | 43.50 | 16.75 | 17.25 | 22.50 |
| 2 | 40.15 | 17.50 | 19.85 | 22.50 |
The pyrolyzing sludge charcoal Industrial Analysis of table 2. and elementary analysiss and calorific value
The municipal sludge pyrolysis gas component of table 3. and calorific value
In the description of this specification, reference term " one embodiment ", " some embodiments ", " example ", " specifically show
The description of example " or " some examples " etc. means to combine specific features, structure, material or spy that the embodiment or example are described
Point is contained at least one embodiment of the present invention or example.In this manual, to the schematic representation of above-mentioned term not
Identical embodiment or example must be directed to.And, the specific features of description, structure, material or feature can be with office
Combine in an appropriate manner in one or more embodiments or example.Additionally, in the case of not conflicting, the skill of this area
Art personnel can be tied the feature of the different embodiments or example described in this specification and different embodiments or example
Close and combine.
Although embodiments of the invention have been shown and described above, it is to be understood that above-described embodiment is example
Property, it is impossible to limitation of the present invention is interpreted as, one of ordinary skill in the art within the scope of the invention can be to above-mentioned
Embodiment is changed, changes, replacing and modification.
Claims (10)
1. a kind of system for preparing activated carbon, it is characterised in that include：
Drying unit, the drying unit is suitable to be dried in sludge；
Pyrolysis unit, the pyrolysis unit is provided with sludge inlet and pyrolyzing sludge charcoal discharging opening, the sludge inlet with
The drying unit be connected, the pyrolysis unit is suitable to be pyrolyzed in the sludge after the drying, so as to obtain pyrolysis gas and
Pyrolyzing sludge charcoal；
Gas-liquid separation unit, the gas-liquid separation unit is connected with the pyrolysis unit, is suitable to for the pyrolysis gas to carry out gas-liquid
Separate, to obtain combustion gas and tar；
Producing steam unit, the producing steam unit is connected with the gas-liquid separation unit, is suitable to the part fuel gas supply extremely
In the producing steam unit, high-temperature steam is obtained；And
Activation unit, the activation unit is connected respectively with the pyrolyzing sludge charcoal discharging opening and producing steam unit, is suitable to institute
State the pyrolyzing sludge charcoal and part high-temperature steam to supply to the activation unit so that the pyrolyzing sludge charcoal is carried out at activation
Reason, to obtain activated carbon.
2. system according to claim 1, it is characterised in that the pyrolysis unit is revolving bed, along Flow of Goods and Materials direction,
The pyrolysis unit includes successively：
Feed zone, the feed zone is provided with the sludge inlet, and the sludge inlet is connected with the drying unit；
Preheating zone, the preheating zone is provided with vapor air vent, and the vapor air vent is connected with the drying unit, institute
State the vapor that vapor air vent is suitable to obtained by the sludge after drying is preheated to supply to the drying unit；
Transition region；
Gas-producing area, the gas-producing area is provided with pyrolysis gas air vent, the pyrolysis gas air vent and the gas-liquid separation unit phase
Even, it is suitable to the pyrolysis gas of generation be supplied to the gas-liquid separation unit；And
Discharge zone, the discharge zone is provided with the pyrolyzing sludge charcoal discharging opening,
Wherein, heat accumulation type radiant tube is provided with the preheating zone, transition region and gas-producing area,
Preferably, the quantity of heat accumulation type radiant tube is set in the transition region more than setting heat accumulation type radiant tube in the preheating zone
Quantity and less than in the gas-producing area arrange heat accumulation type radiant tube quantity.
3. system according to claim 1, it is characterised in that the activation unit is rotary activated furnace, the revolution
Formula activation furnace includes：
The thermal treatment zone, the feed end of the thermal treatment zone is connected with the pyrolyzing sludge charcoal discharging opening, is suitable to the pyrolyzing sludge charcoal
Heated；
Region of activation, the region of activation is connected with the thermal treatment zone, is suitable to live the pyrolyzing sludge charcoal after the heating
Change is processed, to obtain activated carbon；And
Cooling area, the cooling area is connected with the region of activation, is suitable to that the activated carbon is lowered the temperature.
4. system according to claim 3, it is characterised in that further include：
Cleaner unit, the cleaner unit is connected with the activation unit by flue, is suitable to produce in the activation unit
Flue gas carry out dedusting；
Heat exchanger, the heat exchanger is arranged on the flue；
Aerator, the aerator is connected with the thermal treatment zone, is suitable to supply air to the thermal treatment zone.
5. system according to claim 4, it is characterised in that the gas-liquid separation unit includes：
Pyrolysis gas inlet port, the pyrolysis gas inlet port is connected with the pyrolysis gas air vent；
First gas pipeline, first gas pipeline is connected with the heat accumulation type radiant tube, is suitable to make the gas-liquid separation list
The detached a part of fuel gas supply of unit is to the heat accumulation type radiant tube as fuel；
Second gas pipeline, second gas pipeline is connected by the heat exchanger with the activation unit；And
Tar outlet, the tar outlet is connected with the producing steam unit, is suitable to detached Jiao of the gas-liquid separation unit
Oil is supplied to the producing steam unit.
6. system according to claim 1, it is characterised in that the particle diameter of the sludge is not more than 100nm, preferably 45～
55nm。
7. system according to claim 5, it is characterised in that the producing steam unit includes：
Tar enters pipeline, and the tar is connected into pipeline with the tar outlet, is suitable to the gas-liquid separation unit point
From tar supply to the producing steam unit；
First jet chimney, first jet chimney is connected with the drying unit, is suitable to the gas-liquid separation unit point
From the part high-temperature steam supply to the drying unit；And
Second jet chimney, second jet chimney is connected with the activation unit, is suitable to the gas-liquid separation unit point
From another part described in high-temperature steam supply to the activation unit,
Optionally, it is 1 to supply to the high-temperature steam amount and the pyrolyzing sludge charcoal mass ratio of the activation unit:1.5.
8. the method that the system of activated carbon prepares activated carbon is prepared described in a kind of any one of utilization claim 1～7, and its feature exists
In, including：
Sludge is put in the drying unit, is dried；
Sludge after the drying is sent in the pyrolysis unit by the sludge inlet, pyrolysis processing is carried out, heat is obtained
Vent one's spleen and pyrolyzing sludge charcoal；
The pyrolysis gas are supplied to the gas-liquid separation unit, gas-liquid separation is carried out, to obtain combustion gas and tar；
The tar is supplied to the producing steam unit, to obtain high-temperature steam；And
The pyrolyzing sludge charcoal and part high-temperature steam is supplied to the activation unit, so as to the pyrolyzing sludge charcoal
Activation processing is carried out, activated carbon is obtained.
9. method according to claim 8, it is characterised in that further include：
Catalysis in the heat accumulation type radiant tube that the combustion gas is respectively fed in the pyrolysis unit and/or the activation unit
Burner；
High-temperature steam described in another part is supplied to the drying unit, to be dried for the sludge.
10. method according to claim 8, it is characterised in that the temperature of the activation processing is 800～950 DEG C,
Optionally, the temperature of the pyrolysis processing is 500～850 DEG C,
Optionally, the sludge after the drying passes sequentially through the feed zone, preheating zone, transition region, gas-producing area and discharge zone, its
In, the temperature of the preheating zone is 150～400 DEG C, and the temperature of the transition region is 400～500 DEG C, the temperature of the gas-producing area
For 500～850 DEG C,
Optionally, it is described burning produce flue gas in oxygen content be 8～10 mass %, carbon dioxide content be 4～6 mass %,
CO contents are less than 4mg/m3、NOxContent is less than 10mg/m3。
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| CN201611105663.5A Pending CN106629710A (en) | 2016-12-05 | 2016-12-05 | System and method for preparing activated carbon |
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