CN107446629A - The system and method for handling low-order coal - Google Patents
The system and method for handling low-order coal Download PDFInfo
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- CN107446629A CN107446629A CN201710771707.6A CN201710771707A CN107446629A CN 107446629 A CN107446629 A CN 107446629A CN 201710771707 A CN201710771707 A CN 201710771707A CN 107446629 A CN107446629 A CN 107446629A
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- 239000003245 coal Substances 0.000 title claims abstract description 132
- 238000000034 method Methods 0.000 title claims abstract description 47
- 238000002309 gasification Methods 0.000 claims abstract description 275
- 238000000197 pyrolysis Methods 0.000 claims abstract description 188
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims abstract description 134
- 239000007789 gas Substances 0.000 claims abstract description 90
- 239000002245 particle Substances 0.000 claims abstract description 68
- 238000001035 drying Methods 0.000 claims abstract description 59
- 239000002351 wastewater Substances 0.000 claims abstract description 55
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 52
- 238000004140 cleaning Methods 0.000 claims abstract description 35
- 239000004744 fabric Substances 0.000 claims abstract description 32
- 238000012545 processing Methods 0.000 claims abstract description 29
- 239000000571 coke Substances 0.000 claims abstract description 26
- 230000008569 process Effects 0.000 claims abstract description 21
- 238000001556 precipitation Methods 0.000 claims abstract description 12
- 239000000567 combustion gas Substances 0.000 claims description 45
- 238000000746 purification Methods 0.000 claims description 32
- 239000002737 fuel gas Substances 0.000 claims description 25
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 12
- 239000003546 flue gas Substances 0.000 claims description 12
- 238000003860 storage Methods 0.000 claims description 4
- 238000009825 accumulation Methods 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 238000002485 combustion reaction Methods 0.000 claims description 2
- 239000002918 waste heat Substances 0.000 abstract description 18
- 239000000463 material Substances 0.000 abstract description 13
- 150000001299 aldehydes Chemical class 0.000 abstract description 6
- 238000006243 chemical reaction Methods 0.000 description 17
- 238000011084 recovery Methods 0.000 description 8
- 238000001914 filtration Methods 0.000 description 6
- 150000003384 small molecules Chemical class 0.000 description 6
- 230000008859 change Effects 0.000 description 5
- 238000002156 mixing Methods 0.000 description 5
- KSSNXJHPEFVKHY-UHFFFAOYSA-N phenol;hydrate Chemical compound O.OC1=CC=CC=C1 KSSNXJHPEFVKHY-UHFFFAOYSA-N 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 239000003077 lignite Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000003780 insertion Methods 0.000 description 2
- 230000037431 insertion Effects 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 239000004449 solid propellant Substances 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 206010013786 Dry skin Diseases 0.000 description 1
- 238000004380 ashing Methods 0.000 description 1
- 238000011953 bioanalysis Methods 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/12—Heating the gasifier
- C10J2300/1207—Heating the gasifier using pyrolysis gas as fuel
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/169—Integration of gasification processes with another plant or parts within the plant with water treatments
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Gasification And Melting Of Waste (AREA)
Abstract
The invention discloses the system and method for processing low-order coal, system includes：Breaker, drying device, pyrolytic gasification reactor, first-class heat exchanger, secondary heat exchanger, pyrolysis gas cleaning device, three-level heat exchanger, gasification burning purifier and precipitation filter, pyrolytic gasification reactor include：Low-order coal particle entrance, steam distributing device, pyrolysis gas outlet, exhanst gas outlet, the control device that discharges of the coke, gasifying agent nozzle, gasification burning outlet, residue after gasifying outlet after conical separator, radiant tube, drying.The system can realize that low-order coal is pyrolyzed to obtain the direct gasification of high-temperature semi-coke, without increasing the transporting equipment of high-temperature material, scattering and disappearing for heat in transportation is avoided simultaneously, used additionally by the phenol wastewater obtained in system is converted into steam containing phenol in the presence of system waste heat as cloth gas and gasifying agent, the not only phenol wastewater during effective handling process, the aldehydes matter in phenol wastewater can also be converted into the energy.
Description
Technical field
The invention belongs to technical field of coal chemical industry, and specifically, the present invention relates to a kind of system for handling low-order coal and side
Method.
Background technology
The development of pyrolytic process, gasification process in chemical engineering industry is restricted by phenolic wastewater treatment technique.Containing phenol
Waste water has the characteristics of source is wide, harm is big, and difficulty of governance is very big, is effectively treated and realizes that recycling is extremely important.
At present, the processing method of the phenol wastewater during coal pyrolysis gas is mainly extraction, absorption method, burning method, life
Thing method etc..Wherein, extraction easily causes extractant there is the problem of continuous phase viscosity is big, back-mixing is serious in extraction process
Loss and secondary pollution；Regenerating active carbon difficulty, the macroreticular resin cost used in absorption method is higher；Caused in burning method big
Measure energy resource consumption；Bioanalysis is relatively specific for handling low concentration phenol wastewater.
Therefore, the technology of existing processing coal is further improved.
The content of the invention
It is contemplated that at least solves one of technical problem in correlation technique to a certain extent.Therefore, the present invention
One purpose is to propose a kind of system and method for handling low-order coal, and the pyrolysis that can realize low-order coal using the system obtains
The direct gasification of high-temperature semi-coke, so as to which the transporting equipment of high-temperature material need not be increased, while avoid hot in transportation
Amount is scattered and disappeared, additionally by the phenol wastewater obtained in system is converted into steam containing phenol in the presence of system waste heat and as
Cloth gas and gasifying agent use, phenol wastewater that not only can be effectively during handling process, can also be by phenol wastewater
Aldehydes matter is efficiently converted into the energy.
In one aspect of the invention, the present invention proposes a kind of system for handling low-order coal.According to the implementation of the present invention
Example, the system include：
Breaker, the breaker have low-order coal entrance and low-order coal particle outlet；
Drying device, low-order coal particle outlet after the drying device has low-order coal particle entrance and dried are described low
Rank coal particle entrance is connected with the low-order coal particle outlet；
Pyrolytic gasification reactor, the pyrolytic gasification reactor include：
Conical separator, the conical separator are located in the pyrolytic gasification reactor, and the pyrolytic gasification is anti-
Device is answered to be divided into top-down pyrolysis section and gasification section, and the lower end of the conical separator has opening；
Radiant tube, the radiant tube are arranged in the pyrolysis section；
Low-order coal particle entrance after drying, after the drying low-order coal particle entrance be located at the pyrolysis section top and with institute
Low-order coal particle outlet after drying is stated to be connected；
Steam distributing device, the steam distributing device are located at the pyrolysis section, and positioned at low order coal particle after the drying
Below entrance；
Gas outlet is pyrolyzed, the pyrolysis gas outlet is located at the pyrolysis section；
Exhanst gas outlet, the exhanst gas outlet are located at the pyrolysis section and are connected with the drying device；
Discharge of the coke control device, and the control device that discharges of the coke is located at the gasification section, and respectively with the opening and the gas
Change section connection；
Gasifying agent nozzle, the gasifying agent nozzle are located at the gasification section；
Gasification burning exports, and the gasification burning outlet is located in the gasification section；
Residue after gasifying exports, and the residue after gasifying outlet is located at the gasification section；
First-class heat exchanger, solid discharge after the first-class heat exchanger has residue after gasifying entrance and exchanged heat, the gasification are residual
Slag entrance is connected with residue after gasifying outlet；
Secondary heat exchanger, the secondary heat exchanger are pyrolyzed gas outlet, the heat after having pyrolysis fuel gas inlet and heat exchange
Solution fuel gas inlet is connected with the pyrolysis gas outlet；
Gas cleaning device is pyrolyzed, the pyrolysis gas cleaning device is pyrolyzed fuel gas inlet, purification pyrolysis after having heat exchange
Gas outlet and the outlet of the first profit, fuel gas inlet is pyrolyzed after the heat exchange and is connected with being pyrolyzed gas outlet after the heat exchange；
Three-level heat exchanger, gasification burning exports after the three-level heat exchanger has gasification burning entrance and heat exchange, the gas
Change fuel gas inlet with gasification burning outlet to be connected；
Gasification burning purifier, the gasification burning purifier have gasification burning entrance, purification gasification after heat exchange
Gas outlet and the outlet of the second profit, gasification burning entrance is connected with gasification burning outlet after the heat exchange after the heat exchange；
Filter is precipitated, there is the precipitation filter profit entrance, pyrolysis oil export and oil removing phenol wastewater to go out
Mouthful, the profit entrance is connected with first profit outlet and second profit outlet respectively, and the first-class heat exchanger is entered
One step has one-level phenol wastewater entrance and one-level steam (vapor) outlet containing phenol, and the oil removing phenol wastewater outlet contains phenol with the one-level
Waterwater entrance is connected, and two level steam containing phenol goes out after the secondary heat exchanger further has two level steam inlet containing phenol and heat exchange
Mouthful, the two level steam inlet containing phenol is connected with the one-level steam (vapor) outlet containing phenol, and the three-level heat exchanger further has three
Three-level steam (vapor) outlet containing phenol behind level steam inlet containing phenol and heat exchange, the three-level steam inlet containing phenol contains with two level after the heat exchange
Phenol steam (vapor) outlet is connected, after the heat exchange three-level steam (vapor) outlet containing phenol respectively with the steam distributing device and the gasifying agent nozzle
It is connected.
The system of processing low-order coal according to embodiments of the present invention in pyrolytic gasification reactor by setting conical separator
Top-down pyrolysis section and gasification section will be divided into pyrolytic gasification reactor so that the first radiant tube in pyrolysis section of low-order coal
In the presence of pyrolytic reaction occurs, obtain being pyrolyzed combustion gas and pyrolysis char, obtained pyrolysis char is through conical separator lower end
Opening is directly entered gasification section and generation gasification reaction is contacted with gasifying agent, obtain gasification burning and residue after gasifying, and will obtain
Residue after gasifying supplies pyrolysis combustion gas to secondary heat exchanger and pyrolysis gas cleaning device through first-class heat exchanger recovery waste heat successively
In recovery waste heat and purification successively, gasification burning is supplied successively to three-level heat exchanger and gasification gas cleaning device in return successively
Waste heat and purification are received, and is supplied after the oil mixing with water that pyrolysis gas cleaning device and the gas cleaning device that gasifies are obtained to filtering
And precipitation process, phenol wastewater is obtained, and obtained phenol wastewater is converted into by one-level, two level and three-level heat exchanger successively
Steam containing phenol, then using the steam containing phenol as the cloth steam of pyrolysis section in pyrolytic gasification reactor and the gasifying agent of gasification section
Use, phenol therein can be cracked into small molecule and be converted into energy use, and reduce cloth steam and gasifying agent into
This.Thus, the pyrolysis that can realize low-order coal using the system obtains the direct gasification of high-temperature semi-coke, so as to without increase
The transporting equipment of high-temperature material, while scattering and disappearing for heat in transportation is avoided, contain phenol additionally by by what is obtained in system
Waste water is converted into steam containing phenol in the presence of system waste heat and is used as cloth gas and gasifying agent to use, and not only can effectively handle
Phenol wastewater in technical process, the aldehydes matter in phenol wastewater can also be efficiently converted into the energy.
In addition, the system of processing low-order coal according to the above embodiment of the present invention can also have technology additional as follows special
Sign：
In some embodiments of the invention, the side wall of the conical separator and the radial direction of the pyrolytic gasification reactor
Plane is in 45~75 degree of angles.As a result, high-temperature semi-coke caused by pyrolysis section is directly heat-fed to gasification section, it is high without increase
The transporting equipment of warm material.
In some embodiments of the invention, the steam distributing device includes steam jet and blast cap, the steam jet
Inserted from the side wall of the pyrolysis section in the pyrolysis section, and one end on the steam jet in the pyrolysis section with
The blast cap is connected, and the other end of the steam jet is connected with three-level steam (vapor) outlet containing phenol after the heat exchange, the blast cap side
Multiple stomatas being interspersed are disposed with wall, the blast cap is located at the underface of low-order coal particle entrance after the drying.By
This, can significantly improve the pyrolysis efficiency of low-order coal.
In some embodiments of the invention, the distance of the blast cap and low-order coal particle entrance after the drying is 300
~1000 millimeters.
In some embodiments of the invention, a diameter of 6~16 millimeters of the stomata.Thus, it is possible to further improve
The pyrolysis efficiency of low-order coal.
In some embodiments of the invention, the axial direction of the duct of the stomata and the pyrolytic gasification reactor in 0~
45 degree of angles.Thus, it is possible to further improve the pyrolysis efficiency of low-order coal.
In some embodiments of the invention, including multiple heat accumulation type radiant tubes, the multiple heat accumulation type radiant tube
It is interspersed in the pyrolysis section.Thus, it is possible to further improve the pyrolysis efficiency of low-order coal.
In some embodiments of the invention, the control device that discharges of the coke includes：Motor, drive screw and star-like feed
Valve, the drive screw are inserted in the gasification section and through the another side of the gasification section from the side wall of the gasification section
Wall, one end of the drive screw outside the gasification section are connected with motor, the drive screw in the gasification section
Part is connected with the star-like feed valve, and the arrival end of the star-like feed valve is connected with the opening, the star-like feed valve
The port of export connected with the gasification section.Thus, it is possible to realize pyrolysis gas and the mutual cut-off of gasification, the steady of each system is added
It is qualitative, while avoid gasification burning from sealing in pyrolysis section and reduce pyrolysis fuel gases calorific value.
In some embodiments of the invention, including multiple gasifying agent nozzles, the multiple gasifying agent nozzle are located at
The bottom of the gasification section side wall.Thus, it is possible to significantly improve the gasification efficiency of high-temperature semi-coke.
In some embodiments of the invention, the pyrolysis section and the height ratio of the gasification section are (2~5)：1.
In some embodiments of the invention, the pyrolysis gas outlet is located at the bottom of the pyrolysis section side wall, described
Gasification burning outlet is positioned at the top of the gasification section side wall.
In another aspect of the invention, the present invention proposes a kind of method that low-order coal is handled using said system.Root
According to embodiments of the invention, methods described includes：
(1) low-order coal is supplied and break process is carried out into the breaker, to obtain low order coal particle；
(2) the low order coal particle is supplied into the drying device and processing is dried, so as to low after being dried
Rank coal particle；
(3) in the presence of cloth steam, low order coal particle after the drying is supplied to the pyrolytic gasification reactor
Pyrolysis section carry out pyrolysis processing, to obtain being pyrolyzed combustion gas, flue gas and high-temperature semi-coke, the high-temperature semi-coke is separated through taper
Device, which supplies to contact with gasifying agent to the gasification section, carries out gasification process, to obtain gasification burning and residue after gasifying, by described in
Flue gas supplies to be used into the drying device as dried medium；
(4) residue after gasifying is supplied into the first-class heat exchanger and exchanged heat, so as to residue after being exchanged heat；
(5) the pyrolysis fuel gas supply is exchanged heat into the secondary heat exchanger, so that pyrolysis is fired after exchange heat
Gas；
(6) fuel gas supply will be pyrolyzed after the heat exchange and carries out purified treatment into the pyrolysis gas cleaning device, so as to
It is purified pyrolysis combustion gas and the first profit；
(7) gasification burning is supplied into the three-level heat exchanger and exchanged heat, so as to combustion of gasifying after being exchanged heat
Gas；
(8) gasification burning after the heat exchange is supplied and carries out purified treatment into the gasification burning purifier, so as to
It is purified gasification burning and the second profit；
(9) second profit that first profit and step (8) obtained step (6) obtains is supplied to described heavy
Handled in the filter of shallow lake, to obtain pyrolysis oil and oil removing phenol wastewater, and by the oil removing phenol wastewater supply to
Exchanged heat in the first-class heat exchanger, obtain one-level steam containing phenol, and the one-level steam containing phenol is supplied to the two level
Exchanged heat in heat exchanger, so as to two level steam containing phenol after being exchanged heat, then by two level steam containing phenol after the heat exchange supply to
Exchanged heat in the three-level heat exchanger, so that three-level steam containing phenol supplies the cloth is used as into step (3) after being exchanged heat
Expect that steam and the gasifying agent use.
The method of processing low-order coal according to embodiments of the present invention in pyrolytic gasification reactor by setting conical separator
Top-down pyrolysis section and gasification section will be divided into pyrolytic gasification reactor so that the first radiant tube in pyrolysis section of low-order coal
In the presence of pyrolytic reaction occurs, obtain being pyrolyzed combustion gas and pyrolysis char, obtained pyrolysis char is through conical separator lower end
Opening is directly entered gasification section and generation gasification reaction is contacted with gasifying agent, obtain gasification burning and residue after gasifying, and will obtain
Residue after gasifying supplies pyrolysis combustion gas to secondary heat exchanger and pyrolysis gas cleaning device through first-class heat exchanger recovery waste heat successively
In recovery waste heat and purification successively, gasification burning is supplied successively to three-level heat exchanger and gasification gas cleaning device in return successively
Waste heat and purification are received, and is supplied after the oil mixing with water that pyrolysis gas cleaning device and the gas cleaning device that gasifies are obtained to filtering
And precipitation process, phenol wastewater is obtained, and obtained phenol wastewater is converted into by one-level, two level and three-level heat exchanger successively
Steam containing phenol, then using the steam containing phenol as the cloth steam of pyrolysis section in pyrolytic gasification reactor and the gasifying agent of gasification section
Use, phenol therein can be cracked into small molecule and be converted into energy use, and reduce cloth steam and gasifying agent into
This.Thus, the pyrolysis that can realize low-order coal using this method obtains the direct gasification of high-temperature semi-coke, so as to without increase
The transporting equipment of high-temperature material, while scattering and disappearing for heat in transportation is avoided, contain phenol additionally by by what is obtained in system
Waste water is converted into steam containing phenol in the presence of system waste heat and is used as cloth gas and gasifying agent to use, and not only can effectively handle
Phenol wastewater in technical process, the aldehydes matter in phenol wastewater can also be efficiently converted into the energy.
The additional aspect and advantage of the present invention will be set forth in part in the description, and will partly become from the following description
Obtain substantially, or recognized by the practice of the present invention.
Brief description of the drawings
The above-mentioned and/or additional aspect and advantage of the present invention will become in the description from combination accompanying drawings below to embodiment
Substantially and it is readily appreciated that, wherein：
Fig. 1 is the system structure diagram of processing low-order coal according to an embodiment of the invention；
Fig. 2 is steam cloth in pyrolytic gasification reactor in the system according to the processing low-order coal of further embodiment of the present invention
The structural representation of glassware；
Fig. 3 is control of being discharged of the coke in the system according to the processing low-order coal of another embodiment of the invention in pyrolytic gasification reactor
The structural representation of device processed；
Fig. 4 is the method flow schematic diagram of processing low-order coal according to an embodiment of the invention；
Fig. 5 is the method flow schematic diagram according to the processing low-order coal of further embodiment of the present invention.
Embodiment
Embodiments of the invention are described below in detail, the example of the embodiment is shown in the drawings, wherein from beginning to end
Same or similar label represents same or similar element or the element with same or like function.Below with reference to attached
The embodiment of figure description is exemplary, it is intended to for explaining the present invention, and is not considered as limiting the invention.
In the description of the invention, it is to be understood that term " " center ", " longitudinal direction ", " transverse direction ", " length ", " width ",
" thickness ", " on ", " under ", "front", "rear", "left", "right", " vertical ", " level ", " top ", " bottom ", " interior ", " outer ", " up time
The orientation or position relationship of the instruction such as pin ", " counterclockwise ", " axial direction ", " radial direction ", " circumference " be based on orientation shown in the drawings or
Position relationship, it is for only for ease of and describes the present invention and simplify description, rather than indicates or imply that signified device or element must
There must be specific orientation, with specific azimuth configuration and operation, therefore be not considered as limiting the invention.
In addition, term " first ", " second " are only used for describing purpose, and it is not intended that instruction or hint relative importance
Or the implicit quantity for indicating indicated technical characteristic.Thus, define " first ", the feature of " second " can be expressed or
Implicitly include at least one this feature.In the description of the invention, " multiple " are meant that at least two, such as two, three
It is individual etc., unless otherwise specifically defined.
In the present invention, unless otherwise clearly defined and limited, term " installation ", " connected ", " connection ", " fixation " etc.
Term should be interpreted broadly, for example, it may be fixedly connected or be detachably connected, or integrally；Can be that machinery connects
Connect or electrically connect；Can be joined directly together, can also be indirectly connected by intermediary, can be in two elements
The connection in portion or the interaction relationship of two elements, limited unless otherwise clear and definite.For one of ordinary skill in the art
For, the concrete meaning of above-mentioned term in the present invention can be understood as the case may be.
In the present invention, unless otherwise clearly defined and limited, fisrt feature can be with "above" or "below" second feature
It is that the first and second features directly contact, or the first and second features pass through intermediary mediate contact.Moreover, fisrt feature exists
Second feature " on ", " top " and " above " but fisrt feature are directly over second feature or oblique upper, or be merely representative of
Fisrt feature level height is higher than second feature.Fisrt feature second feature " under ", " lower section " and " below " can be
One feature is immediately below second feature or obliquely downward, or is merely representative of fisrt feature level height and is less than second feature.
In one aspect of the invention, the present invention proposes a kind of system for handling low-order coal.According to the implementation of the present invention
Example, with reference to figure 1, the system includes：Breaker 100, drying device 200, pyrolytic gasification reactor 300, first-class heat exchanger
400th, secondary heat exchanger 500, pyrolysis gas cleaning device 600, three-level heat exchanger 700, gasification burning purifier 800 and precipitation
Filter 900.
According to an embodiment of the invention, breaker 100 has low-order coal entrance 101 and low-order coal particle outlet 102, and
Suitable for block low-order coal is carried out into break process, to obtain low order coal particle.It should be noted that those skilled in the art can
It is actually needed with basis and the particle diameter of low order coal particle is selected, and breaker can be disintegrating machine.
According to an embodiment of the invention, low order coal particle after drying device 200 has low-order coal particle entrance 201 and dried
Outlet 202, low-order coal particle entrance 201 is connected with low-order coal particle outlet 102, and suitable for obtained low order coal particle is carried out
Drying process, so as to low order coal particle after being dried.Specifically, the drying process can use heat smoke as dried medium
Contact drying is carried out to low order coal particle.
According to an embodiment of the invention, include with reference to figure 1, pyrolytic gasification reactor 300：Conical separator 31, radiant tube
32nd, low-order coal particle entrance 301, pyrolysis gas outlet 302, flue gas go out after steam distributing device 33, the control device 34 that discharges of the coke, drying
Mouth 303, gasifying agent nozzle 304, the gentle ashing slags outlet 306 in gasification burning outlet 305.
According to an embodiment of the invention, it is located at reference to figure 1, conical separator 31 in pyrolytic gasification reactor 300, and by heat
Top-down pyrolysis section 35 and gasification section 36, and the lower end tool of conical separator 31 are divided into solution gasification reactor 300
There is opening 307.Thus, by arranging that conical separator will be divided into certainly in pyrolytic gasification reactor in pyrolytic gasification reactor
Pyrolysis section and gasification section under above, and cause pyrolysis section and gasification section to pass through open communication so that it is being pyrolyzed in low-order coal
High-temperature semi-coke caused by Duan Fasheng pyrolytic reactions is directly entered gasification section and gasification reaction occurs, without increase high-temperature material
Transporting equipment, while scattering and disappearing for heat in transportation is avoided, it is high using the reactor gas production and energy utilization rate in addition.
According to one embodiment of present invention, the side wall of conical separator 31 and the radial direction of pyrolytic gasification reactor 300 are put down
Face is in 45~75 degree of angles.Dropped into as a result, being glided in high temperature pyrolysis semicoke caused by pyrolysis section in self gravitation effect into gas
Change section, without increasing the transporting equipment of high-temperature material.
According to still a further embodiment, radiant tube 32 is arranged in pyrolysis section 35, according to one of present invention tool
Body embodiment, multiple radiant tubes 32 can be arranged in pyrolysis section 35, and multiple radiant tubes 32 are interspersed in pyrolysis section 35.
Thus, it is possible to so that uniform distribution of temperature field in pyrolysis section, and low-order coal can again pass by radiant tube in dropping process
Alternating expression cloth, so as to improve the pyrolysis efficiency of low-order coal.
According to still another embodiment of the invention, steam distributing device 33 is located at pyrolysis section 35, and the low order after drying
The lower section of coal particle entrance 301.Thus, low-order coal particle entrance will can be supplied after drying in the presence of steam distributing device
Drying after low order coal particle break up so that low-order coal is dispersed in pyrolysis section, so as to improve the pyrolysis efficiency of low-order coal.
According to the specific embodiment of the present invention, with reference to figure 1-2, steam distributor 33 includes steam jet 331 and wind
Cap 332, steam spray 331 are located in pyrolysis section 35 out of pyrolysis section 35 side wall insertion pyrolysis section 35 on steam jet 331
One end be connected with blast cap 332, multiple stomatas 333 being interspersed are disposed with the side wall of blast cap 332, blast cap 332 is located at drying
The underface of low-order coal particle entrance 301 afterwards.Specifically, supplying steam by steam jet, steam enters blast cap through thereon
Stomata sprays, so as to which the low-order coal of the supply of low-order coal particle entrance after drying be broken up so that low-order coal is equal in pyrolysis section
It is even scattered, so as to improve the pyrolysis efficiency of low-order coal.
According to another specific embodiment of the present invention, the distance of blast cap 332 and low-order coal particle entrance 301 after drying can
Think 300~1000 millimeters.
According to another specific embodiment of the present invention, the diameter of the stomata 333 on blast cap 332 can be 6~16 millimeters.
Inventor has found that the blast cap in the aperture can ensure that the low-order coal of the application is dispersed, so as to improve pyrolysis efficiency.
According to another specific embodiment of the present invention, the duct and the axial direction of pyrolytic gasification reactor 300 of stomata 333 are in
0~45 degree of angle.Inventor has found that the axial angle purpose of duct and pyrolytic gasification reactor is the uniformity for ensureing cloth,
As 45 ° of the axial angle ＞ of duct and gasification reactor, the scope of breaing up of cloth is far below pyrolysis oven inside dimension, causes cloth
Expect skewness, cause partial thermal decomposition insufficient；As 0 ° of the axial angle ＜ of duct and gasification reactor, cloth gas is downward
Blow, can still result in and cause cloth skewness, pyrolysis it is insufficient.Thus, the stomata arranged using the application structure can be protected
It is uniform to demonstrate,prove low order pyrolysis of coal.
According to still another embodiment of the invention, the control device 34 that discharges of the coke is located at gasification section 36, and separates respectively with taper
The lower ending opening 303 of device 31 connects with gasification section 36.
According to the specific embodiment of the present invention, with reference to figure 1 and 3, the control device 34 that discharges of the coke includes：Motor 341, transmission
Screw rod 342 and star-like feed valve 343, drive screw 342 is interior from the side wall insertion gasification section 36 of gasification section 36 and runs through gasification section
36 other end side wall, and one end of the drive screw 342 outside gasification section is connected with motor 342, positioned at gasification section 36
The interior part of drive screw 342 is connected with star-like feed valve 343, and the arrival end 344 of star-like feed valve 343 is connected with opening 306,
The port of export 345 of star-like feed valve 343 connects with gasification section 36.Thus, high warm can not only be controlled by star-shape feeding valve
Solve the quantitative gasification of semicoke, and by star-shape feeding valve and conical separator be implemented in combination with pyrolysis gas and gasification it is mutual every
It is disconnected, the stability of each system is added, while avoid gasification burning from sealing in pyrolysis section and reduce pyrolysis fuel gases calorific value.
According to still another embodiment of the invention, dry after low-order coal particle entrance 301 be located at pyrolysis section 35 and with drying
Low-order coal particle outlet 202 is connected afterwards, and low order coal particle is supplied to pyrolysis section after the drying suitable for will be obtained in drying device
Middle carry out pyrolysis processing.According to the specific embodiment of the present invention, low-order coal particle entrance 301 can be arranged in heat after drying
Solve the top of section 35.Specifically, during being somebody's turn to do, low order coal particle is initially stored in feed bin after drying, then by feeding spiral shell
Rotation is supplied to low-order coal particle entrance after drying.
According to still another embodiment of the invention, pyrolysis gas outlet 302 is located at pyrolysis section 35, and suitable for pyrolysis section is produced
Raw pyrolysis combustion gas discharge pyrolytic gasification reactor.According to the specific embodiment of the present invention, pyrolysis gas outlet 302 can be with
It is arranged in the side wall of pyrolysis section 35, such as pyrolysis gas outlet can be arranged in the bottom of pyrolysis section side wall.
According to still another embodiment of the invention, exhanst gas outlet 303 is located at 35 pyrolysis sections and is connected with drying device 200,
And used suitable for flue gas caused by pyrolysis section is supplied into drying device as dried medium.Thus, system heat sources are being improved
Drying cost is reduced while making full use of.
According to still another embodiment of the invention, gasifying agent nozzle 304 is located at gasification section 16, and suitable for being supplied to gasification section
Gasifying agent, gasification reaction occurs so that being contacted with high temperature pyrolysis semicoke.According to the specific embodiment of the present invention, gasification
Section 16 can arrange multiple gasifying agent nozzles, and multiple gasifying agent nozzles 36 can be located at the bottom of the side wall of gasification section 36.By
This so that the gasifying agent of penetrating fully contacts with entering the high temperature pyrolysis semicoke of gasification section, so as to improve high temperature pyrolysis semicoke
Gasification efficiency.Specifically, gasifying agent can be the one or more in steam, air, oxygen-enriched air, oxygen.
According to still another embodiment of the invention, gasification burning outlet 305 is arranged in gasification section 36.According to the one of the present invention
Individual specific embodiment, gasification burning outlet 305 can be arranged in the side wall of gasification section 36, such as gasification burning outlet can position
In the top of gasification section side wall.
According to still another embodiment of the invention, the lime-ash that gasifies exports 306 and is located at gasification section 36, and suitable for gasification section is produced
Raw gasification lime-ash discharge pyrolytic gasification reactor.According to the specific embodiment of the present invention, gasification lime-ash outlet 306 can be with
The bottom of gasification section is arranged, and can be in gasification lime-ash exit arrangement spiral discharging device.
According to still another embodiment of the invention, the height of pyrolysis section and gasification section ratio can be (2~5)：1.Inventor
It was found that this kind of arrangement can ensure that gasification reaction is fully carried out while ensureing that low-order coal is fully pyrolyzed, and reduce
Body of heater cost.
Thus, by setting conical separator to be divided into pyrolytic gasification reactor from upper in pyrolytic gasification reactor
Pyrolysis section and gasification section under and so that pyrolysis first occurs in pyrolysis section for low order coal particle anti-after drying in the presence of radiant tube
Should, obtain being pyrolyzed combustion gas and pyrolysis char, opening of the obtained pyrolysis char through conical separator lower end are directly entered gasification section
Contacted with gasifying agent and gasification reaction occurs, obtain gasification burning.Thus, low-order coal can be realized using the pyrolytic gasification reactor
Pyrolysis obtain the direct gasification of high-temperature semi-coke, so as to which the transporting equipment of high-temperature material need not be increased, while avoid fortune
Heat is lost during defeated, high using the reactor gas production and energy utilization rate in addition.
According to an embodiment of the invention, first-class heat exchanger 400 has solid discharge after residue after gasifying entrance 401 and heat exchange
402, residue after gasifying entrance 401 and residue after gasifying outlet 306 is connected, and is suitable to obtain in pyrolytic gasification reactor gasification section
Residue after gasifying carries out heat exchange processing, residue after gasifying after being exchanged heat.
According to an embodiment of the invention, pyrolysis combustion gas goes out after secondary heat exchanger 500 has pyrolysis fuel gas inlet 501 and heat exchange
Mouth 502, pyrolysis fuel gas inlet 501 is connected with pyrolysis gas outlet 302, and is suitable to obtain pyrolytic gasification reactor pyrolysis section
Pyrolysis combustion gas carries out heat exchange processing, to be pyrolyzed combustion gas after being exchanged heat.
According to an embodiment of the invention, being pyrolyzed gas cleaning device 600 has pyrolysis fuel gas inlet 601, purification after heat exchange
The profit of gas outlet 602 and first outlet 603 is pyrolyzed, fuel gas inlet 601 is pyrolyzed after heat exchange with being pyrolyzed gas outlet 502 after heat exchange
It is connected, and combustion gas is pyrolyzed after the heat exchange suitable for will be obtained in secondary heat exchanger and carries out purified treatment, to be purified pyrolysis combustion
Gas and the first profit, and obtained purification pyrolysis combustion gas is stored in gas holder.It should be noted that the pyrolysis gas-purification fills
It can be any purifier of the prior art to put, if can realize pyrolysis gas-purification it is isolated purification pyrolysis combustion gas and
Profit.
According to an embodiment of the invention, gasification burning goes out after three-level heat exchanger 700 has gasification burning entrance 701 and heat exchange
Mouth 702, gasification burning entrance 701 is connected with gasification burning outlet 305, and is suitable to obtain pyrolytic gasification reactor gasification section
Gasification burning carries out purified treatment, so as to gasification burning after being exchanged heat.
According to an embodiment of the invention, gasification burning purifier 800 has gasification burning entrance 801, purification after heat exchange
Gasification burning outlet 802 and the second profit outlet 803, gasification burning entrance 801 and gasification burning outlet 702 after heat exchange after heat exchange
It is connected, and gasification burning carries out purified treatment after the heat exchange suitable for will be obtained in three-level heat exchanger, to be purified gasification combustion
Gas and the second profit, and obtained purification gasification combustion gas is stored in gas holder, then by purification gasification fuel gas supply to pyrolysis
Used in radiant tube in gasification reactor as fuel.It should be noted that the gasification burning purifier can be existing
Any purifier in technology, as long as can realize that gasification burning purification separation is purified gasification burning and profit.
According to an embodiment of the invention, precipitating filter 900 has profit entrance 901, pyrolysis oil export 902 and oil removing
Phenol wastewater outlet 903, profit entrance 901 are connected with the outlet 603 of the first profit and the second profit outlet 803 respectively, while suitable
Sunk in by the second profit for being pyrolyzed the first profit obtained in gas cleaning device and being obtained in gasification gas cleaning device
Form sediment and filter, so as to isolated pyrolysis oil and phenol wastewater.Specifically, due to the density variation of tar and phenol water, can be achieved quiet
Put natural layering, phenol water is on upper strata, and tar is in lower floor.
According to an embodiment of the invention, first-class heat exchanger 400 further there is one-level phenol wastewater entrance 403 and one-level to contain
Phenol steam (vapor) outlet 404, oil removing phenol wastewater outlet 903 are connected with one-level phenol wastewater entrance 403, and secondary heat exchanger 500 enters one
Step has two level steam (vapor) outlet containing phenol 504 after two level steam inlet containing phenol 503 and heat exchange, two level steam inlet containing phenol 503 and one
Level steam (vapor) outlet containing phenol 404 is connected, and three-level heat exchanger 700 further has three-level after three-level steam inlet containing phenol 703 and heat exchange
Steam (vapor) outlet containing phenol 704, three-level steam inlet containing phenol 703 are connected with two level steam (vapor) outlet containing phenol 504 after heat exchange, three-level after heat exchange
Steam (vapor) outlet containing phenol 704 is connected with steam distributing device 33 and the gasifying agent nozzle 304 respectively.Specifically, and oil removing is contained into phenol
Waste water supplies to be exchanged heat into first-class heat exchanger, obtains one-level steam containing phenol, and one-level steam containing phenol is supplied to two level and changed
Exchanged heat in hot device, so as to two level steam containing phenol after being exchanged heat, then two level steam containing phenol after heat exchange is supplied to three-level and changed
Exchanged heat in hot device, so that three-level steam containing phenol supplies into pyrolytic gasification reactor and is used as cloth steam after being exchanged heat
Used with gasifying agent, phenol therein can be cracked into small molecule and be converted into energy use, and it is gentle to reduce cloth steam
The cost of agent, so that being produced in the system without phenol wastewater.It should be noted that first-class heat exchanger, secondary heat exchanger
It is indirect heat exchanger with three-level heat exchanger, i.e., passage includes tube side and shell side.
The system of processing low-order coal according to embodiments of the present invention in pyrolytic gasification reactor by setting conical separator
Top-down pyrolysis section and gasification section will be divided into pyrolytic gasification reactor so that the first radiant tube in pyrolysis section of low-order coal
In the presence of pyrolytic reaction occurs, obtain being pyrolyzed combustion gas and pyrolysis char, obtained pyrolysis char is through conical separator lower end
Opening is directly entered gasification section and generation gasification reaction is contacted with gasifying agent, obtain gasification burning and residue after gasifying, and will obtain
Residue after gasifying supplies pyrolysis combustion gas to secondary heat exchanger and pyrolysis gas cleaning device through first-class heat exchanger recovery waste heat successively
In recovery waste heat and purification successively, gasification burning is supplied successively to three-level heat exchanger and gasification gas cleaning device in return successively
Waste heat and purification are received, and is supplied after the oil mixing with water that pyrolysis gas cleaning device and the gas cleaning device that gasifies are obtained to filtering
And precipitation process, phenol wastewater is obtained, and obtained phenol wastewater is converted into by one-level, two level and three-level heat exchanger successively
Steam containing phenol, then using the steam containing phenol as the cloth steam of pyrolysis section in pyrolytic gasification reactor and the gasifying agent of gasification section
Use, phenol therein can be cracked into small molecule and be converted into energy use, and reduce cloth steam and gasifying agent into
This.Thus, the pyrolysis that can realize low-order coal using the system obtains the direct gasification of high-temperature semi-coke, so as to without increase
The transporting equipment of high-temperature material, while scattering and disappearing for heat in transportation is avoided, contain phenol additionally by by what is obtained in system
Waste water is converted into steam containing phenol in the presence of system waste heat and is used as cloth gas and gasifying agent to use, and not only can effectively handle
Phenol wastewater in technical process, the aldehydes matter in phenol wastewater can also be efficiently converted into the energy.
As described above, the system of processing low-order coal according to embodiments of the present invention, which can have, is selected from the advantages of following at least
One of：
The system of processing low-order coal according to embodiments of the present invention will be pyrolyzed, phenol wastewater caused by gasification is directly used in
Internal system consumes, without adding phenolic wastewater treatment system, while by the organic matter in phenol wastewater by being pyrolyzed, gasifying
Method is converted into the energy, and energy utilization rate is high；
Phenol wastewater is converted into the energy resource consumption of the steam containing phenol by the system of processing low-order coal according to embodiments of the present invention
Come from internal system, without adding extra power consumption, save energy；
The system of processing low-order coal according to embodiments of the present invention is directed to organic solid fuel, using pyrolysis reactor, gas
Change the method that reactor is combined, realize the pyrolytic gasification of organic solid fuel, gas production is high, energy utilization rate is high；
The simple system of processing low-order coal according to embodiments of the present invention, system can produce two kinds of combustion gas, wherein low heat value
Fuel gases calorific value is available for inside reactor to use, and middle high heating value combustion gas can be outside for using；
The system of processing low-order coal according to embodiments of the present invention mutually separates pyrolysis section with gasification section, adds each system
The stability of system.
In another aspect of the invention, the present invention proposes a kind of method that low-order coal is handled using said system.Root
According to embodiments of the invention, with reference to figure 4, this method includes：
S100：Low-order coal is supplied into breaker and carries out break process
In the step, break process is carried out specifically, low-order coal is supplied into breaker, to obtain low-order coal
Grain.It should be noted that those skilled in the art can be selected the particle diameter of low order coal particle according to being actually needed, and
Breaker can be disintegrating machine.
S200：Low order coal particle is supplied processing is dried into drying device
In the step, processing is dried into drying device specifically, low order coal particle obtained above is supplied, with
Just low order coal particle after being dried.Specifically, the drying process can use heat smoke as dried medium to low-order coal
Grain carries out contact drying.
S300：Low order coal particle after drying is supplied to pyrolytic gasification reactor and is pyrolyzed and gasification process, and will
To flue gas supply to drying device
In the step, specifically, by the dry of the supply of low-order coal particle entrance after drying in the presence of steam distributing device
Low order coal particle is broken up after dry so that low-order coal is dispersed in pyrolysis section, and low order coal particle is first in pyrolysis section after drying
Pyrolytic reaction occurs in the presence of radiant tube, obtains being pyrolyzed combustion gas, flue gas and pyrolysis char, obtained pyrolysis char is through taper point
Opening every device lower end, which is directly entered gasification section and contacted with gasifying agent, occurs gasification reaction, obtains gasification burning and residue after gasifying,
And flue gas is supplied and used into the drying device in step S200 as dried medium.Thus, reacted using the pyrolytic gasification
Device can realize that the pyrolysis of low-order coal obtains the direct gasification of high-temperature semi-coke, be set so as to increase the transport of high-temperature material
It is standby, while scattering and disappearing for heat in transportation is avoided, it is high using the reactor gas production and energy utilization rate in addition.
S400：Residue after gasifying is supplied and exchanged heat into first-class heat exchanger
In the step, exchanged heat specifically, the residue after gasifying obtained in pyrolytic gasification reactor gasification section is supplied to one-level
Heat exchange processing is carried out in device, residue after gasifying after being exchanged heat.
S500：Pyrolysis fuel gas supply is exchanged heat into secondary heat exchanger
In the step, specifically, the pyrolysis combustion gas that pyrolytic gasification reactor pyrolysis section is obtained carries out heat exchange processing, so as to
Combustion gas is pyrolyzed after being exchanged heat.
S600：Fuel gas supply will be pyrolyzed after heat exchange and carries out purified treatment into pyrolysis gas cleaning device
In the step, specifically, fuel gas supply is pyrolyzed to being pyrolyzed combustion gas after the heat exchange that will be obtained in above-mentioned secondary heat exchanger
Purified treatment is carried out in purifier, to be purified pyrolysis combustion gas and the first profit, and obtained purification is pyrolyzed combustion gas
It is stored in gas holder.It should be noted that the pyrolysis gas cleaning device can be any purifier of the prior art, only
The isolated purification pyrolysis combustion gas of pyrolysis gas-purification and profit can be realized.
S700：Gasification burning is supplied into three-level heat exchanger and exchanged heat
In the step, specifically, the gasification burning that pyrolytic gasification reactor gasification section is obtained is supplied to three-level heat exchanger
Middle carry out purified treatment, so as to gasification burning after being exchanged heat.
S800：Gasification burning after heat exchange is supplied purified treatment is carried out into gasification burning purifier
In the step, specifically, gasification burning is supplied to gas-purification after the heat exchange that will be obtained in above-mentioned three-level heat exchanger
Purified treatment is carried out in device, to be purified gasification burning and the second profit, and obtained purification gasification combustion gas is stored
In gas holder, then used in the radiant tube in purification gasification fuel gas supply to pyrolytic gasification reactor as fuel.Need
Illustrate, the gasification burning purifier can be any purifier of the prior art, as long as gasification burning can be realized
Purification separation is purified gasification burning and profit.
S900：The second obtained profit of the first obtained profits of step S600 and step S800 is supplied to precipitation filtering dress
Handled in putting, and obtained oil removing phenol wastewater is supplied into one-level, two level and three-level heat exchanger successively, exchanged heat
Three-level steam containing phenol is supplied into step S300 afterwards uses as cloth steam and gasifying agent
In the step, specifically, the first profit obtained in gas cleaning device and gasification gas cleaning device will be pyrolyzed
In obtained the second profit supply and carry out precipitation filtering into precipitation filter, given up so as to isolated pyrolysis oil and containing phenol
Water.Specifically, due to the density variation of tar and phenol water, can be achieved to stand natural layering, phenol water on upper strata, tar in lower floor,
Then oil removing phenol wastewater is supplied and exchanged heat into first-class heat exchanger, obtain one-level steam containing phenol, and one-level is steamed containing phenol
Vapour supplies to be exchanged heat into secondary heat exchanger, so as to two level steam containing phenol after being exchanged heat, then will after heat exchange two level containing phenol steaming
Vapour is supplied into three-level heat exchanger and exchanged heat, so that three-level steam containing phenol is supplied to pyrolytic gasification reactor after being exchanged heat
Middle to be used as cloth steam and gasifying agent, phenol therein can be cracked into small molecule and be converted into energy use, and reduce
The cost of cloth steam and gasifying agent, so that being produced in this technique without phenol wastewater.It should be noted that one-level exchanges heat
Device, secondary heat exchanger and three-level heat exchanger are indirect heat exchanger, i.e., passage includes tube side and shell side.
The method of processing low-order coal according to embodiments of the present invention in pyrolytic gasification reactor by setting conical separator
Top-down pyrolysis section and gasification section will be divided into pyrolytic gasification reactor so that the first radiant tube in pyrolysis section of low-order coal
In the presence of pyrolytic reaction occurs, obtain being pyrolyzed combustion gas and pyrolysis char, obtained pyrolysis char is through conical separator lower end
Opening is directly entered gasification section and generation gasification reaction is contacted with gasifying agent, obtain gasification burning and residue after gasifying, and will obtain
Residue after gasifying supplies pyrolysis combustion gas to secondary heat exchanger and pyrolysis gas cleaning device through first-class heat exchanger recovery waste heat successively
In recovery waste heat and purification successively, gasification burning is supplied successively to three-level heat exchanger and gasification gas cleaning device in return successively
Waste heat and purification are received, and is supplied after the oil mixing with water that pyrolysis gas cleaning device and the gas cleaning device that gasifies are obtained to filtering
And precipitation process, phenol wastewater is obtained, and obtained phenol wastewater is converted into by one-level, two level and three-level heat exchanger successively
Steam containing phenol, then using the steam containing phenol as the cloth steam of pyrolysis section in pyrolytic gasification reactor and the gasifying agent of gasification section
Use, phenol therein can be cracked into small molecule and be converted into energy use, and reduce cloth steam and gasifying agent into
This.Thus, the pyrolysis that can realize low-order coal using this method obtains the direct gasification of high-temperature semi-coke, so as to without increase
The transporting equipment of high-temperature material, while scattering and disappearing for heat in transportation is avoided, contain phenol additionally by by what is obtained in system
Waste water is converted into steam containing phenol in the presence of system waste heat and is used as cloth gas and gasifying agent to use, and not only can effectively handle
Phenol wastewater in technical process, the aldehydes matter in phenol wastewater can also be efficiently converted into the energy.
Below with reference to specific embodiment, present invention is described, it is necessary to which explanation, these embodiments are only to describe
Property, without limiting the invention in any way.
Embodiment
With reference to figure 5, aqueous 33% Indonesia's lignite is passed through into crusher in crushing, the Indonesia's lignite particle warp that then will be obtained
After 120 DEG C of flue gas dryings, aqueous 15% is obtained, particle diameter ＜ 6mm drying Indonesia lignite particle, is then sent to feed bin
In, it is transported in pyrolytic gasification reactor by feeding screw, after steam cloth, is fallen by self gravitation,
Pyrolytic reaction occurs by being contacted with radiant tube, obtains high temperature pyrolysis combustion gas, high temperature pyrolysis semicoke and flue gas, obtained high warm
Solution combustion gas is purified pyrolysis combustion gas and the second profit by secondary heat exchanger, pyrolysis gas cleaning device, obtained purification heat
Pyrolysis combustion gas gas holder storage is delivered in solution combustion gas, and obtained flue gas is supplied into drying device to be used as dried medium, is obtained
High temperature pyrolysis semicoke is delivered to gasification section by star-like feed valve, at the same by gasifying agent nozzle spray into gasifying agent (superheated steam,
Temperature is 400 DEG C) gasification reaction occurs, obtained high-temperature ash is delivered to ash silo storage after first-class heat exchanger exchanges heat, obtained
Gasification burning is purified gasification burning and the second profit after three-level heat exchanger and gasification gas cleaning device, and what is obtained is net
Change gasification burning and deliver to the storage of gasification burning gas holder, then by the radiation in purification gasification fuel gas supply to pyrolytic gasification reactor
Used in pipe as fuel, the second oil that the first profit and gasification gas cleaning device that pyrolysis gas cleaning device obtains obtain
Water is supplied into precipitation filter and handled, and obtains pyrolysis oil and phenol wastewater, and phenol wastewater is then passed through into one successively
Level, two level and three-level heat exchange heat exchanger heat exchange, three-level steam containing phenol (260 DEG C) after being exchanged heat, and obtained three-level is contained into phenol
Steam is supplied into pyrolytic gasification reactor to be used as cloth steam and gasifying agent.
Each yield distribution of Indonesia's lignite pyrolytic gasification (mass fraction) of table 1
| It is pyrolyzed combustion gas/% | Gasification burning/% | Gasify lime-ash/% |
| 42.22 | 43.46 | 14.32 |
Gasification burning yield=(gasification burning amount-effective gasifying agent consumption)/furnace coal weight
Table 2 is pyrolyzed combustion gas, gasification burning Lower heat 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 specific features, structure, material or the spy for combining the embodiment or example description
Point is contained at least one embodiment or example of the present invention.In this manual, to the schematic representation of above-mentioned term not
Identical embodiment or example must be directed to.Moreover, specific features, structure, material or the feature of description can be with office
Combined in an appropriate manner in one or more embodiments or example.In addition, in the case of not conflicting, the skill of this area
Art personnel can be tied the different embodiments or example and the feature of different embodiments or example described in this specification
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, changed, replacing and modification.
Claims (10)
- A kind of 1. system for handling low-order coal, it is characterised in that including：Breaker, the breaker have low-order coal entrance and low-order coal particle outlet；Drying device, low-order coal particle outlet after the drying device has low-order coal particle entrance and dried, the low-order coal Particle entrance is connected with the low-order coal particle outlet；Pyrolytic gasification reactor, the pyrolytic gasification reactor include：Conical separator, the conical separator are located in the pyrolytic gasification reactor, and by the pyrolytic gasification reactor It is divided into top-down pyrolysis section and gasification section, and the lower end of the conical separator has opening；Radiant tube, the radiant tube are arranged in the pyrolysis section；Low-order coal particle entrance after drying, low-order coal particle entrance is located at the pyrolysis section top and done with described after the drying Low-order coal particle outlet is connected after dry；Steam distributing device, the steam distributing device are located at the pyrolysis section, and positioned at low-order coal particle entrance after the drying Lower section；Gas outlet is pyrolyzed, the pyrolysis gas outlet is located at the pyrolysis section；Exhanst gas outlet, the exhanst gas outlet are located at the pyrolysis section and are connected with the drying device；Discharge of the coke control device, and the control device that discharges of the coke is located at the gasification section, and respectively with the opening and the gasification section Connection；Gasifying agent nozzle, the gasifying agent nozzle are located at the gasification section；Gasification burning exports, and the gasification burning outlet is located in the gasification section；Residue after gasifying exports, and the residue after gasifying outlet is located at the gasification section；First-class heat exchanger, the first-class heat exchanger have solid discharge after residue after gasifying entrance and heat exchange, and the residue after gasifying enters Mouth is connected with residue after gasifying outlet；Secondary heat exchanger, the secondary heat exchanger are pyrolyzed gas outlet, the pyrolysis combustion after having pyrolysis fuel gas inlet and heat exchange Gas entrance is connected with the pyrolysis gas outlet；Gas cleaning device is pyrolyzed, the pyrolysis gas cleaning device is pyrolyzed fuel gas inlet, purification pyrolysis combustion gas after having heat exchange Outlet and the outlet of the first profit, fuel gas inlet is pyrolyzed after the heat exchange and is connected with being pyrolyzed gas outlet after the heat exchange；Three-level heat exchanger, gasification burning exports after the three-level heat exchanger has gasification burning entrance and heat exchange, the gasification combustion Gas entrance is connected with gasification burning outlet；Gasification burning purifier, the gasification burning purifier have gasification burning entrance, purification gasification combustion gas after heat exchange Outlet and the outlet of the second profit, gasification burning entrance is connected with gasification burning outlet after the heat exchange after the heat exchange；Filter is precipitated, the precipitation filter has profit entrance, pyrolysis oil export and the outlet of oil removing phenol wastewater, institute State profit entrance respectively with first profit outlet and second profit outlet to be connected, the first-class heat exchanger further has There are one-level phenol wastewater entrance and one-level steam (vapor) outlet containing phenol, the oil removing phenol wastewater outlet enters with the one-level phenol wastewater Mouth is connected, and the secondary heat exchanger further has two level steam (vapor) outlet containing phenol after two level steam inlet containing phenol and heat exchange, described Two level steam inlet containing phenol is connected with the one-level steam (vapor) outlet containing phenol, and the three-level heat exchanger further there is three-level to be steamed containing phenol Three-level steam (vapor) outlet containing phenol after vapour entrance and heat exchange, the three-level steam inlet containing phenol goes out with two level steam containing phenol after the heat exchange Mouth is connected, and three-level steam (vapor) outlet containing phenol is connected with the steam distributing device and the gasifying agent nozzle respectively after the heat exchange.
- 2. system according to claim 1, it is characterised in that the side wall of the conical separator and the pyrolytic gasification are anti- The sagittal plane for answering device is in 45~75 degree of angles.
- 3. system according to claim 1, it is characterised in that the steam distributing device includes steam jet and blast cap, institute State steam jet to insert in the pyrolysis section from the side wall of the pyrolysis section, and be located at the pyrolysis section on the steam jet Interior one end is connected with the blast cap, and the other end of the steam jet is connected with three-level steam (vapor) outlet containing phenol after the heat exchange, It is disposed with multiple stomatas being interspersed in the blast cap side wall, the blast cap is located at low-order coal particle entrance after the drying Underface；Optional, the distance of the blast cap and low-order coal particle entrance after the drying is 300~1000 millimeters.
- 4. system according to claim 3, it is characterised in that a diameter of 6~16 millimeters of the stomata.
- 5. the system according to claim 3 or 4, it is characterised in that reacted with the pyrolytic gasification in the duct of the stomata The axial direction of device is in 0~45 degree of angle.
- 6. system according to claim 1, it is characterised in that including multiple heat accumulation type radiant tubes, the multiple storage Hot type radiant tube is interspersed in the pyrolysis section.
- 7. system according to claim 1, it is characterised in that the control device that discharges of the coke includes：Motor, drive screw and Star-like feed valve, the drive screw are inserted in the gasification section and through the another of the gasification section from the side wall of the gasification section One end side wall, one end of the drive screw outside the gasification section are connected with motor, the biography in the gasification section Dynamic screw portion is connected with the star-like feed valve, and the arrival end of the star-like feed valve is connected with the opening, described star-like The port of export of feed valve connects with the gasification section.
- 8. system according to claim 1, it is characterised in that including multiple gasifying agent nozzles, the multiple gasification Agent nozzle is located at the bottom of the gasification section side wall.
- 9. system according to claim 1, it is characterised in that the height ratio of the pyrolysis section and the gasification section for (2~ 5)：1；Optional, the pyrolysis gas outlet is located at the bottom of the pyrolysis section side wall, and the gasification burning outlet is positioned at described The top of gasification section side wall.
- 10. a kind of method that system using any one of claim 1-9 handles low-order coal, it is characterised in that including：(1) low-order coal is supplied and break process is carried out into the breaker, to obtain low order coal particle；(2) the low order coal particle is supplied into the drying device and processing is dried, so as to low-order coal after being dried Particle；(3) in the presence of cloth steam, low order coal particle after the drying is supplied to the heat of the pyrolytic gasification reactor Solve section and carry out pyrolysis processing, to obtain being pyrolyzed combustion gas, flue gas and high-temperature semi-coke, the high-temperature semi-coke is supplied through conical separator Gasification process is carried out to being contacted to the gasification section with gasifying agent, to obtain gasification burning and residue after gasifying, by the flue gas Supply uses into the drying device as dried medium；(4) residue after gasifying is supplied into the first-class heat exchanger and exchanged heat, so as to residue after being exchanged heat；(5) the pyrolysis fuel gas supply is exchanged heat into the secondary heat exchanger, to be pyrolyzed combustion gas after being exchanged heat；(6) fuel gas supply will be pyrolyzed after the heat exchange and carries out purified treatment into the pyrolysis gas cleaning device, to obtain Purification pyrolysis combustion gas and the first profit；(7) gasification burning is supplied into the three-level heat exchanger and exchanged heat, so as to gasification burning after being exchanged heat；(8) gasification burning after the heat exchange is supplied and carries out purified treatment into the gasification burning purifier, to obtain Purification gasification combustion gas and the second profit；(9) second profit that first profit and step (8) obtained step (6) obtains, which is supplied to described, to be precipitated Handled in filter device, to obtain pyrolysis oil and oil removing phenol wastewater, and the oil removing phenol wastewater is supplied to described Exchanged heat in first-class heat exchanger, obtain one-level steam containing phenol, and the one-level steam containing phenol is supplied to the secondary heat exchange Exchanged heat in device, so as to two level steam containing phenol after being exchanged heat, then two level steam containing phenol after the heat exchange supplied to described Exchanged heat in three-level heat exchanger, so that three-level steam containing phenol is supplied and steamed into step (3) as the cloth after being exchanged heat Vapour and the gasifying agent use.
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Application publication date: 20171208 |