CN104531222B - Pyrolysis of coal system and method using spouted bed reactor - Google Patents
Pyrolysis of coal system and method using spouted bed reactor Download PDFInfo
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- CN104531222B CN104531222B CN201410834185.6A CN201410834185A CN104531222B CN 104531222 B CN104531222 B CN 104531222B CN 201410834185 A CN201410834185 A CN 201410834185A CN 104531222 B CN104531222 B CN 104531222B
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- 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
- C10J3/64—Processes with decomposition of the distillation products
- C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
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- 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
- C10J3/62—Processes with separate withdrawal of the distillation products
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- 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
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/86—Other features combined with waste-heat boilers
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- 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
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- 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
- C10J2300/0943—Coke
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- 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
- C10J2300/0953—Gasifying agents
- C10J2300/0956—Air or oxygen enriched air
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- 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
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
The invention discloses a kind of pyrolysis of coal system and method for utilization spouted bed reactor, belong to pyrolysis of coal field.This system includes：Spouted bed reactor through pipeline connection, deflection plate down-flow fluidized bed using ECT, the first gas-solid separator, the second gas-solid separator, preboiler, water scrubber, air preheater, returning charge valve；The present invention also provides a kind of pyrolysis of coal method using this system, enables to couple deflection plate down-flow fluidized bed using ECT by spouted bed reactor, forms pyrolysis and gasification PROCESS COUPLING is pyrolyzed to coal.This system heat transfer efficiency high, gross energy utilization rate high it is achieved that during pyrolysis of coal calorific value of gas, high-quality semicoke and tar three coproduction；And invest that low, equipment operation energy consumption is low, there is not semicoke and heat carrier separating-purifying problem；Using the pyrolysis of spouted bed reactor, fully, bed temperature is stable, is substantially not present thermograde for gas-particle two-phase contact.
Description
Technical field
The present invention relates to pyrolysis of coal field, more particularly to a kind of pyrolysis of coal system of utilization spouted bed reactor and side
Method.
Background technology
" rich coal, oil-poor, few gas " is the current Energy Situation of China.High speed development with Chinese national economy and the people
The continuous improvement of living standard, the imbalance between supply and demand of primary energy petrochina becomes increasingly conspicuous, Chinese crude oil net importation amount in 2008
1.79 hundred million tons, 49.0% is reached to the interdependency of oil overseas, and by being limited in national power and foreign exchange, China is difficult to support so
Large-scale petroleum import is it would be highly desirable to solve oil and gas gap problem.Compared with oil, coal in China yield and consumption figure
The proportion accounting in primary energy is always held at more than 70%, how Development of Novel Coal Chemical Industry, builds large-scale new coalification
Work Poly-generation project, producing oil replacement product is becoming the vital task of China's energy construction.
Coal fast pyrolysis process can obtain high-quality tar, clean semicoke and coal gas under compared with temperate condition, and high-quality is burnt
Oil can hydrofinishing be the chemical products such as light-end products.Mostly pyrolysis of coal process is the endothermic reaction, and traditional handicraft solves pyrolysis of coal
It is solid thermal carriers heat supply (as shown in Figure 1) (DG pyrolytic process, the U.S.'s oil as Dalian University of Technology that journey needs the mode of heat
Shale company's T OSCOAL technique, Lurgi-ruhr-gas technique of German Rule LURGI etc.) or gas heat carrier heat supply
(as shown in Figure 2,3) (as vertical furnace technology, multistage revolution furnace technology etc.).Solid thermal carriers heat supply commonly used combustion parts heat
The reaction heat heating solid thermal carriers of solution semicoke release, are pyrolytic process heat supply by gas-solid separating device separation heat carrier；Gas
Body heat carrier heat supply then commonly used combustion parts semicoke or pyrolysis coal gas produce heat smoke be pyrolytic process heat supply.Solid
Heat carrier heat supply commonly used double bed pyrolytic process, investment is high, and heat carrier is heated using recirculating fluidized bed, and apparatus body is relatively
High (tens meters or even rice up to a hundred), equipment operation energy consumption is high；Meanwhile, technique pyrolysis char and heat carrier phase when being pyrolyzed is mixed
Close, semicoke separating-purifying has difficulty；The commonly used at present vertical furnace technology of gas heat carrier heat supply and multistage revolution furnace technology,
Equipment investment is few.But vertical furnace technology belongs to moving bed, exist in stove axially and radial temperature profile uneven it is easy to coking；
Simultaneously as producing excessively simple, auxiliary facility is few, and environmental pollution is serious, and each place government has begun to rectify；Multistage turns round
Furnace technology produces high warm flue gas using the space combustion partial thermal decomposition coal gas between distillation container outer wall and Inner Wall of Combustion Chamber,
With heat exchange pattern to pyrolytic process indirect heating, heat transfer efficiency is low, technique gross energy utilization rate is low.
Content of the invention
Based on the problems of above-mentioned prior art, the present invention provides a kind of pyrolysis of coal system of utilization spouted bed reactor
System and method, can solve solid thermal carriers technique exist semicoke with heat carrier separating-purifying difficulty is big, cost of investment is high, equipment fortune
Row high energy consumption, and existing gas heat carrier pyrolytic process exists in stove axially and radial temperature profile is uneven, heat transfer efficiency is low,
The low problem of technique gross energy utilization rate.
For solving above-mentioned technical problem, the present invention provides a kind of pyrolysis of coal system of employing spouted bed reactor, including：
Spouted bed reactor, which is provided with coal entrance, pyrolysis char outlet, pyrolysis gas air inlet and mixed gas and gives vent to anger
Mouthful；
Deflection plate down-flow fluidized bed using ECT, which is provided with pyrolysis char entrance, gasification char outlet, preheated air entrance and water vapour and enters
Mouth, gasification gas outlet, are provided with deflection plate in this deflection plate down-flow fluidized bed using ECT, and described deflection plate is between pyrolysis char entrance and gasification half
Between burnt outlet, and between described preheated air entrance and steam entry and gasification gas outlet；
Described deflection plate is alternately arranged both sides in deflection plate down-flow fluidized bed using ECT, and neighbouring baffle(s) spacing is regarding treatment scale
Fixed, typically in 100～1200mm, deflection plate can arrange air-distribution device (as aperture and blast cap etc.), setting cloth wind dress on deflection plate
Put and can improve gas-particle two-phase contact area, stably gasification bed temperature and promotion gasification char flowing, it is to avoid deflection plate down-flow fluidized bed using ECT
Interior feed blocking problem, also can be not provided with air-distribution device (as aperture and blast cap etc.), can simplify structure, be easy to safeguard；
The outlet of described spouted bed reactor is connected with the pyrolysis char entrance of described deflection plate down-flow fluidized bed using ECT through returning charge valve；
First gas-solid separator, is connected with the gasification gas outlet of described deflection plate down-flow fluidized bed using ECT, this first gas-solid separator
Gasification char outlet connect in described deflection plate down-flow fluidized bed using ECT, the pyrolysis gas of gasification gas outlet and described spouted bed reactor
Air inlet is connected；
Second gas-solid separator, is connected with the mixed gas gas outlet of described spouted bed reactor, this second gas solid separation
The pyrolysis char outlet of device connects to described spouted bed reactor, and mixed gas outlet is connected with waste heat boiler, described waste heat
The steam outlet of boiler is connected with the steam entry of described deflection plate down-flow fluidized bed using ECT；
Air preheater, is connected with the steam outlet of described waste heat boiler, the preheated air outlet of this air preheater
It is connected with the preheated air entrance of described deflection plate down-flow fluidized bed using ECT；
Water scrubber, is connected with the gas exit of described waste heat boiler, and this water scrubber is provided with mixed gas outlet and tar
Outlet.
The present invention provides a kind of pyrolysis of coal method of utilization spouted bed reactor, using pyrolysis of coal system of the present invention
System, comprises the following steps：
Coal particle enters in spouted bed reactor, carries out in the presence of deflection plate down-flow fluidized bed using ECT produced high-temperature gasification coal gas
Pyrolysis, pyrolysis temperature is 600～800 DEG C, and coal particle mean residence time in spouted bed reactor is 1～3s, heat after pyrolysis
Solution coal gas and the gasification gas entering form mixed gas, enter second from the mixed gas gas outlet of described spouted bed reactor
Gas-solid separator；
The produced high-temperature gasification coal gas of described deflection plate down-flow fluidized bed using ECT is：The pyrolysis char that described spouted bed reactor is discharged enters
Enter described deflection plate down-flow fluidized bed using ECT to carry out after gasification forms gasification gas, separating output to described spouted bed through the first gas-solid separator
The high-temperature gasification coal gas of reactor；
Mixed gas in the second gas-solid separator, in pyrolysis char returning charge to described spouted bed reactor, after separating
Enter waste heat boiler and produce, with water heat exchange, the saturated vapor that temperature is 140 DEG C～160 DEG C, a part of saturated vapor enters described folding
Stream plate down-flow fluidized bed using ECT as occur gasification reaction gasifying agent, remaining saturated vapor air inlet preheater preheated air, preheating
Air and the water vapour as gasifying agent are mixed into described deflection plate down-flow fluidized bed using ECT；
Mixed gas through residual heat boiler for exchanging heat enters water scrubber and is directly cooled to 60 DEG C～80 DEG C, isolates mixed gas
Discharge respectively with after tar.
Beneficial effects of the present invention are：Deflection plate down-flow fluidized bed using ECT is coupled by spouted bed reactor, forms pyrolysis and gasified
Journey couples, and heat transfer efficiency is high, gross energy utilization rate high it is achieved that calorific value of gas, high-quality semicoke and tar during pyrolysis of coal
Three coproduction；And invest that low, equipment operation energy consumption is low, there is not semicoke and heat carrier separating-purifying problem；Using spouted bed
Reactor is pyrolyzed, and fully, bed temperature is stable, is substantially not present thermograde for gas-particle two-phase contact.
Brief description
In order to be illustrated more clearly that the technical scheme of the embodiment of the present invention, below will be to required use in embodiment description
Accompanying drawing be briefly described it should be apparent that, drawings in the following description are only some embodiments of the present invention, for this
For the those of ordinary skill in field, on the premise of not paying creative work, other can also be obtained according to these accompanying drawings
Accompanying drawing.
Fig. 1 is the solid thermal carriers heat supply process schematic diagram of prior art；
Fig. 2 is the gas heat carrier heat supply process schematic diagram of prior art；
Fig. 3 is the gas heat carrier heat supply process schematic diagram of prior art；
Fig. 4 is pyrolysis of coal system schematic provided in an embodiment of the present invention；
In Fig. 4：1- spouted bed reactor；11- coal entrance；12- pyrolysis char exports；13- mixed gas gas outlet；2- returns
Material valve；3- deflection plate down-flow fluidized bed using ECT；31- pyrolysis char entrance；32- gasification char exports；33- gasification gas exports；34- water vapour
Entrance；35- preheated air entrance；36- deflection plate；4- first gas-solid separator；41- gasification gas gas outlet；42- gasification char
Returning charge mouth；5- second gas-solid separator；51- mixed gas exports；52- pyrolysis char returning charge mouth；6- waste heat boiler；61- water steams
Vapor outlet；62- filler；63- mixed gas delivery outlet；7- air preheater；71- steam entry；72- air intake；73-
Preheated air exports；74- discharge outlet；8- water scrubber；81- mixed gas outlet；82- tar outlet；A- gasification gas；B-
Water vapour；C- preheated air；D- air.
Specific embodiment
Below the embodiment it is clear that described is clearly and completely described to the technical scheme in the embodiment of the present invention
It is only a part of embodiment of the present invention, rather than whole embodiments.Based on embodiments of the invention, ordinary skill
The every other embodiment that personnel are obtained under the premise of not making creative work, broadly falls into protection scope of the present invention.
As shown in figure 1, the embodiment of the present invention provides a kind of pyrolysis of coal system of utilization spouted bed reactor, realize low cost
Efficiently pyrolysis of coal, this system includes：
Spouted bed reactor, which is provided with coal entrance, pyrolysis char outlet, pyrolysis gas air inlet and mixed gas and gives vent to anger
Mouthful；
Deflection plate down-flow fluidized bed using ECT, which is provided with pyrolysis char entrance, gasification char outlet, gasification gas outlet, preheated air
Entrance and steam entry, preheated air entrance and steam entry are each provided at deflection plate down-flow fluidized bed using ECT bottom, and this deflection plate is descending
Be provided with deflection plate in bed, between deflection plate exports between pyrolysis char entrance and gasification char, and between gasification gas outlet with
Between steam entry；
The pyrolysis char outlet of spouted bed reactor is connected with the pyrolysis char entrance of deflection plate down-flow fluidized bed using ECT through returning charge valve；
First gas-solid separator, is connected with the gasification gas outlet of deflection plate down-flow fluidized bed using ECT, the gas of this first gas-solid separator
Change semicoke returning charge mouth to connect to deflection plate down-flow fluidized bed using ECT, gasification gas gas outlet and the spouted bed of this first gas-solid separator are reacted
The pyrolysis gas air inlet of device is connected；
Second gas-solid separator, is connected with the mixed gas gas outlet of spouted bed reactor, this second gas-solid separator
Pyrolysis char returning charge mouth connects to spouted bed reactor, and mixed gas gas outlet is connected with waste heat boiler, the water of waste heat boiler
Steam (vapor) outlet is connected with the steam entry of deflection plate down-flow fluidized bed using ECT；
Air preheater, is connected with the steam outlet of waste heat boiler, preheated air outlet and the folding of this air preheater
The preheated air entrance of stream plate down-flow fluidized bed using ECT is connected；
Water scrubber, is connected with the mixed gas delivery outlet of waste heat boiler, this water scrubber is provided with mixed gas outlet and Jiao
Oily outlet.
In above-mentioned pyrolysis of coal system, in spouted bed reactor, it is provided with guide pipe, guide pipe is between coal entrance and pyrolysis char
Between outlet, and between pyrolysis gas air inlet and mixed gas gas outlet.
In above-mentioned pyrolysis of coal system, the deflection plate in deflection plate down-flow fluidized bed using ECT is 45 °～55 ° downward deflection plates of angle.?
In deflection plate down-flow fluidized bed using ECT, setting angle is 45 °～55 ° downward deflection plates, can improve the pyrolysis char gasification reaction time.Folding
Stream plate is alternately arranged both sides in deflection plate down-flow fluidized bed using ECT, neighbouring baffle(s) spacing depending on treatment scale, typically 100～
1200mm, deflection plate can arrange air-distribution device (as aperture and blast cap etc.), and on deflection plate, setting air-distribution device can improve gas-solid two
Contact area, stably gasification bed temperature and promotion gasification char flowing, it is to avoid feed blocking problem in deflection plate down-flow fluidized bed using ECT,
Also air-distribution device (as aperture and blast cap etc.) can be not provided with, structure can be simplified, be easy to safeguard.
In above-mentioned pyrolysis of coal system, coal entrance is located at the concentrated phase section of spouted bed reactor lower part；Pyrolysis char outlet is located at
The middle part of spouted bed reactor；Pyrolysis gas air inlet is located at the bottom of spouted bed reactor；Mixed gas gas outlet is located at spouted
The top of bed reactor.The pyrolysis char of spouted bed reactor exported at the middle part of spouted bed reactor, it is to avoid coal particle
Short stream occurs in spouted bed pyrolytic process, increased the pyrolysis of coal time of staying simultaneously, effectively increase tar and gas yield.
In above-mentioned pyrolysis of coal system, pyrolysis char entrance and gasification gas exit are each provided at deflection plate down-flow fluidized bed using ECT top；Gas
Change semicoke outlet and be located at deflection plate down-flow fluidized bed using ECT bottom.
Returning charge valve in said system is provided with air intake, controls spouted bed reactor to deflection plate by input air amount
The amount of input pyrolysis char in down-flow fluidized bed using ECT.
The embodiment of the present invention also provides a kind of pyrolysis of coal method of utilization spouted bed reactor, using shown in above-mentioned Fig. 1
Pyrolysis of coal system, comprises the following steps：
Coal particle enters in spouted bed reactor, carries out in the presence of deflection plate down-flow fluidized bed using ECT produced high-temperature gasification coal gas
Pyrolysis, pyrolysis temperature is 600～800 DEG C, and coal particle mean residence time in spouted bed reactor is 1～3s, heat after pyrolysis
Solution coal gas and the gasification gas entering form mixed gas, enter the second gas-solid from the mixed gas gas outlet of spouted bed reactor
Separator；Because deflection plate down-flow fluidized bed using ECT produced high-temperature gasification coal gas is as pyrolysis gas, compared with the conventional method, shorten tar
The thermal cracking time.
Deflection plate down-flow fluidized bed using ECT produced high-temperature gasification coal gas is：The pyrolysis char that spouted bed reactor is discharged enters deflection plate
After down-flow fluidized bed using ECT carries out gasification formation gasification gas, separate output to the high-temperature gasification of spouted bed reactor through the first gas-solid separator
Coal gas；
In the second gas-solid separator, in pyrolysis char returning charge to spouted bed reactor, the mixed gas after separating enters
Waste heat boiler and water heat exchange produce the saturated vapor that temperature is 140 DEG C～160 DEG C, and it is descending that a part of saturated vapor enters deflection plate
Bed is as the gasifying agent that gasification reaction occurs, remaining saturated vapor air inlet preheater preheated air, the air of preheating and work
Water vapour for gasifying agent is mixed into deflection plate down-flow fluidized bed using ECT；
Mixed gas through residual heat boiler for exchanging heat enters water scrubber and is directly cooled to 60 DEG C～80 DEG C, isolates mixed gas
Discharge respectively with after tar.
In above-mentioned pyrolysis of coal method, in spouted bed reactor internal circulation flow, flow velocity is 1～6 meter per second to coal particle.Coal
Granule circulates in spouted bed reactor in the presence of the mozzle of setting.
In above-mentioned pyrolysis of coal method, the pyrolysis char that spouted bed reactor is discharged enters deflection plate down-flow fluidized bed using ECT and is gasified
For：During 45 °～55 ° downward deflection plate up-downgoings that pyrolysis char is arranged in deflection plate down-flow fluidized bed using ECT, under deflection plate
Row bed bottom enters to contact along the up preheated air of deflection plate with the mixed gas gas-particle two-phase of water vapour is gasified, gasification
Temperature is 850～950 DEG C.
In above-mentioned pyrolysis of coal method, coal particle is realized by the density contrast of gas flow rate and coal particle and gasification gas and exists
Circulation in spouted bed, realizes gasification gas and coal directly contact in spouted bed reactor and raw fountain type fluidisation, in reactor
Fully, mass-and heat-transfer effect is good, and bed temperature is uniform for gas-solid contact.
In above-mentioned pyrolysis of coal method, gasification gas produced by deflection plate down-flow fluidized bed using ECT is consisted of by percent by volume：CO
(19.6～22%), CO2 (9.9～13.4%), H2 (11.9～17.5%), CH4 (0.7～3.4%), N2 (48.9～
55.3%)；
The mixed gas that spouted bed reactor is discharged is consisted of by percent by volume：CO (10.1～12.2%), CO2(2.5
～4.7%), H2(44.0～51.4%), CH4(1.6～2.8%), N2(30.5～39.5%), remaining be C2～C4Hydro carbons.
Further, in above-mentioned pyrolysis of coal method, raw material, in addition to can be using coal, also can adopt biomass, rubbish, mould
Material, mud etc..Gasifying medium can be using air, oxygen-enriched air, pure oxygen and water vapour or their mixture.
With reference to specific embodiment, the system and method for the present invention is described further.
Embodiment 1
(11) pyrolysis of coal：
Fine coal enters spouted bed reactor lower part concentrated phase section by feeding screw, in the produced gasification of deflection plate down-flow fluidized bed using ECT
It is pyrolyzed under coal gas effect.In spouted bed reactor, coal particle mean residence time is 2.5s, and pyrolysis temperature is 600 DEG C, pressure
Power is normal pressure.Gasification gas is mixed with pyrolysis coal gas after pyrolysis, and mixed gas consists of：CO：10.5%th, CO2：4.2%th, H2：
47%th, CH4：2.1%th, N2：32.1%th, remaining is C2～C4 hydro carbons.
(12) mixed gas and pyrolysis char are separated：
Reacted mixed gas enters the second gas-solid separator from spouted bed reactor head, and wherein pyrolysis char passes through
To spouted bed reactor, mixed gas then enters waste heat boiler and produces high temperature saturation with water heat exchange for second gas-solid separator returning charge
Steam, temperature is at 147 DEG C.
(13) separating tar and mixed gas：
The mixed gas going out waste heat boiler is directly cooled to 68 DEG C through water scrubber, carries out the separation of tar and mixed gas.
(14) pyrolysis char gasification：
Pyrolysis char is entered to become a mandarin plate plate down-flow fluidized bed using ECT by returning charge valve, in the presence of air+water vapour (gasifying agent), is produced
Raw high-temperature gasification coal gas adverse current directly carries out gas-particle two-phase with the semicoke by each flap on deflection plate down-flow fluidized bed using ECT and contacts, and enters circulation of qi promoting
Change conversion.Gasification temperature controls at 850 DEG C, produced coal gas composition：CO：18.1%th, CO2：10.7%th, H2：13.7%th, CH4：
1.3%th, N2：56.2%.
Gasification gas enters the first gas-solid separator from deflection plate down-flow fluidized bed using ECT top, and its partial vaporization semicoke is through first
To deflection plate down-flow fluidized bed using ECT, remaining semicoke produced passes through deflection plate down-flow fluidized bed using ECT gasification char and exports for gas-solid separator returning charge
The the second returning charge valve connecting is discharged.
(15) there is steam in waste heat boiler：
Using the heat of mixed gas, there is steam in waste heat boiler, a portion is as the gasification of deflection plate down-flow fluidized bed using ECT
Agent, another part air inlet preheater preheated air, the air after preheating and the blended entrance of water vapour as gasifying agent
Deflection plate down-flow fluidized bed using ECT bed bottom.
After above-mentioned reaction, the product quality percentage ratio obtaining consists of：Coal gas：21.3%th, tar：8.8%, half
Burnt：69.9%.
Embodiment 2
(21) pyrolysis of coal：
Fine coal enters spouted bed reactor lower part concentrated phase section by feeding screw, in the produced gasification of deflection plate down-flow fluidized bed using ECT
It is pyrolyzed under coal gas effect.In spouted bed reactor, coal particle mean residence time is 1.2s, and pyrolysis temperature is controlled to 750
DEG C, pressure is normal pressure.Gasification gas is mixed with pyrolysis coal gas after pyrolysis, and mixed gas is consisted of by percent by volume：CO：
11.9%th, CO2：3.4%th, H2：49.7%th, CH4：1.7%th, N2：32.3%th, remaining is C2～C4Hydro carbons.
(22) mixed gas and pyrolysis char are separated：
Reacted mixed gas enters gas-solid separator from spouted bed reactor head, and wherein pyrolysis char is through gas-solid
To spouted bed, mixed gas then enters waste heat boiler and water heat exchange and produces high temperature saturated vapor for separator returning charge, and temperature is 156
℃.
(23) separating tar and mixed gas：
The mixed gas going out waste heat boiler is directly cooled to 76 DEG C through water scrubber, carries out the separation of tar and mixed gas.
(24) pyrolysis char gasification：
Pyrolysis char is entered to become a mandarin plate plate down-flow fluidized bed using ECT by returning charge valve, in the presence of air+steam gasification agent, is produced
High-temperature gasification coal gas adverse current directly carries out gas-particle two-phase with the semicoke by each flap on deflection plate down-flow fluidized bed using ECT and contacts, and is gasified
Conversion, gasification temperature controls at 900 DEG C, and produced coal gas is pressed percent by volume and formed：CO：21.9%th, CO2：10.1%th, H2：
16.8%th, CH4：0.9%th, N2：50.3%.
Gasification gas enters the first gas-solid separator from deflection plate down-flow fluidized bed using ECT top, and its partial vaporization semicoke is through first
To deflection plate down-flow fluidized bed using ECT, remaining semicoke produced passes through deflection plate down-flow fluidized bed using ECT gasification char and exports for gas-solid separator returning charge
The the second returning charge valve connecting is discharged.
(25) there is steam in waste heat boiler：
Using the heat of mixed gas, there is steam in waste heat boiler, a portion is as the gasification of deflection plate down-flow fluidized bed using ECT
Agent, another part air inlet preheater preheated air, the air after preheating and the blended entrance of water vapour as gasifying agent
Deflection plate down-flow fluidized bed using ECT bed bottom.
After above-mentioned reaction, the product quality percentage ratio obtaining consists of：Coal gas：24.7%th, tar：8.5%, half
Burnt：66.8%.
Beneficial effects of the present invention are：This system passes through the knot coupling using spouted bed reactor with deflection plate down-flow fluidized bed using ECT
It is achieved that pyrolysis and gasification PROCESS COUPLING, heat transfer efficiency is high for structure, gross energy utilization rate high it is achieved that calorific value during pyrolysis of coal
Three coproduction of coal gas, high-quality semicoke and tar；And invest that low, equipment operation energy consumption is low, there is not semicoke and heat carrier divides
From purification problem, solve that the semicoke that existing solid thermal carriers technique exists is big with heat carrier separating-purifying difficulty, cost of investment
The technological deficiencies such as height, equipment operation energy consumption height；Using the pyrolysis of spouted bed reactor, fully, bed temperature is steady for gas-particle two-phase contact
Fixed, it is substantially not present thermograde, shortens the pyrolytic process tar thermal cracking time, tar yield can improve to 7～9
(wt) %, solves existing gas heat carrier pyrolytic process and exists in stove and axially lack with the uneven technology of radial temperature profile
Fall into.
The above, the only present invention preferably specific embodiment, but protection scope of the present invention is not limited thereto,
Any those familiar with the art in the technical scope of present disclosure, the change or replacement that can readily occur in,
All should be included within the scope of the present invention.Therefore, protection scope of the present invention should be with the protection model of claims
Enclose and be defined.
Claims (8)
1. a kind of pyrolysis of coal system of utilization spouted bed reactor is it is characterised in that include：
Spouted bed reactor, which is provided with coal entrance, pyrolysis char outlet, pyrolysis gas air inlet and mixed gas gas outlet；
Deflection plate down-flow fluidized bed using ECT, which is provided with pyrolysis char entrance, gasification char outlet, gasification gas outlet, preheated air entrance
And steam entry, described preheated air entrance and steam entry are each provided at described deflection plate down-flow fluidized bed using ECT bottom, this deflection plate
It is provided with deflection plate, between described deflection plate exports between pyrolysis char entrance and gasification char, and between described gas in down-flow fluidized bed using ECT
Change between gas exit and steam entry；Deflection plate in described deflection plate down-flow fluidized bed using ECT is 45 °～55 ° downward bafflings of angle
Plate；Described deflection plate is alternately arranged both sides in deflection plate down-flow fluidized bed using ECT, and neighbouring baffle(s) spacing is 100～1200mm, folding
Stream plate setting air-distribution device；
The pyrolysis char entrance phase through returning charge valve and described deflection plate down-flow fluidized bed using ECT for the pyrolysis char outlet of described spouted bed reactor
Even；
First gas-solid separator, is connected with the gasification gas outlet of described deflection plate down-flow fluidized bed using ECT, the gas of this first gas-solid separator
Change semicoke returning charge mouth to connect to described deflection plate down-flow fluidized bed using ECT, the gasification gas gas outlet of this first gas-solid separator and described spray
The pyrolysis gas air inlet of dynamic bed reactor is connected；
Second gas-solid separator, is connected with the mixed gas gas outlet of described spouted bed reactor, this second gas-solid separator
Pyrolysis char returning charge mouth connects to described spouted bed reactor, and mixed gas gas outlet is connected with waste heat boiler, described waste heat
The steam outlet of boiler is connected with the steam entry of described deflection plate down-flow fluidized bed using ECT；
Air preheater, is connected with the steam outlet of described waste heat boiler, and the preheated air of this air preheater exports and institute
The preheated air entrance stating deflection plate down-flow fluidized bed using ECT is connected；
Water scrubber, is connected with the mixed gas delivery outlet of described waste heat boiler, this water scrubber is provided with mixed gas outlet and Jiao
Oily outlet.
2. the pyrolysis of coal system of utilization spouted bed reactor according to claim 1 is it is characterised in that described spouted bed is anti-
Answer in device and be provided with guide pipe, between described guide pipe exports between described coal entrance and pyrolysis char, and between described pyrolysis gas
Between air inlet and mixed gas gas outlet.
3. the pyrolysis of coal system of the utilization spouted bed reactor according to any one of claim 1 to 2 is it is characterised in that institute
State the concentrated phase section that coal entrance is located at described spouted bed reactor lower part；
Described pyrolysis char outlet is located at the middle part of described spouted bed reactor；
Described pyrolysis gas air inlet is located at the bottom of described spouted bed reactor；
Described mixed gas gas outlet is located at the top of described spouted bed reactor.
4. the pyrolysis of coal system of the utilization spouted bed reactor according to any one of claim 1 to 2 is it is characterised in that institute
State pyrolysis char entrance and gasification gas exit is each provided at described deflection plate down-flow fluidized bed using ECT top；
Described gasification char outlet is located at described deflection plate down-flow fluidized bed using ECT bottom.
5. a kind of pyrolysis of coal method of utilization spouted bed reactor is it is characterised in that adopt described in any one of Claims 1-4
Pyrolysis of coal system, comprise the following steps：
Coal particle enters in spouted bed reactor, carries out heat in the presence of deflection plate down-flow fluidized bed using ECT produced high-temperature gasification coal gas
Solution, pyrolysis temperature is 600～800 DEG C, and coal particle mean residence time in spouted bed reactor is 1～3s, is pyrolyzed after pyrolysis
Coal gas forms mixed gas with the gasification gas entering, and enters the second gas from the mixed gas gas outlet of described spouted bed reactor
Solid separator；
The produced high-temperature gasification coal gas of described deflection plate down-flow fluidized bed using ECT is：The pyrolysis char that described spouted bed reactor is discharged enters institute
State deflection plate down-flow fluidized bed using ECT to carry out after gasification forms gasification gas, separating output to the reaction of described spouted bed through the first gas-solid separator
The high-temperature gasification coal gas of device；The pyrolysis char that described spouted bed reactor is discharged enters described deflection plate down-flow fluidized bed using ECT and is gasified
For：During 45 °～55 ° downward deflection plate up-downgoings that pyrolysis char is arranged in described deflection plate down-flow fluidized bed using ECT, and described
Deflection plate down-flow fluidized bed using ECT bottom enters and contacts with the mixed gas gas-particle two-phase of water vapour along the up preheated air of described deflection plate
Gasified, gasification temperature is 850～950 DEG C；
In the second gas-solid separator, in pyrolysis char returning charge to described spouted bed reactor, the mixed gas after separating enters
Waste heat boiler and water heat exchange produce the saturated vapor that temperature is 140 DEG C～160 DEG C, and a part of saturated vapor enters described deflection plate
Down-flow fluidized bed using ECT is as the gasifying agent that gasification reaction occurs, remaining saturated vapor air inlet preheater preheated air, the air of preheating
It is mixed into described deflection plate down-flow fluidized bed using ECT with the water vapour as gasifying agent；
Mixed gas through residual heat boiler for exchanging heat enters water scrubber and is directly cooled to 60 DEG C～80 DEG C, isolates mixed gas and Jiao
Oil is discharged.
6. the pyrolysis of coal method of utilization spouted bed reactor according to claim 5 is it is characterised in that described coal particle exists
Described spouted bed reactor internal circulation flow, flow velocity is 1～6 meter per second.
7. the pyrolysis of coal method of utilization spouted bed reactor according to claim 6 is it is characterised in that described coal particle exists
Circulate in the presence of the mozzle of setting in described spouted bed reactor.
8. the pyrolysis of coal method of the utilization spouted bed reactor according to any one of claim 5 to 7 is it is characterised in that institute
State gasification gas produced by deflection plate down-flow fluidized bed using ECT to consist of by percent by volume：CO (19.6～22%), CO2(9.9～
13.4%), H2(11.9～17.5%), CH4(0.7～3.4%), N2(48.9～55.3%)；
The mixed gas that described spouted bed reactor is discharged is consisted of by percent by volume：CO (10.1～12.2%), CO2(2.5
～4.7%), H2(44.0～51.4%), CH4(1.6～2.8%), N2(30.5～39.5%), remaining be C2～C4Hydro carbons.
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| CN106753489B (en) * | 2016-11-25 | 2022-05-10 | 华能国际电力股份有限公司 | Coal pyrolysis steam, tar and coal gas co-production system and process based on pulverized coal furnace |
| CN109652104B (en) * | 2017-10-12 | 2021-02-09 | 中国石油化工股份有限公司 | Down bed-entrained flow bed pyrolysis-gasification integrated method and device |
| CN109652103B (en) * | 2017-10-12 | 2021-08-03 | 中国石油化工股份有限公司 | Down bed-fixed bed pyrolysis-gasification integrated method and device |
| CN110117500B (en) * | 2019-05-05 | 2021-03-23 | 东南大学 | Spouted fluidized bed with tar catalytic cracking function |
| CN110684561B (en) * | 2019-11-23 | 2021-05-18 | 湖南碧霄环境科技有限公司 | Humidity-controlled and wind-controlled rolling bottom gasification furnace |
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