CN103695013B - System and method for pyrolysis of carbon-containing solid fuel - Google Patents
System and method for pyrolysis of carbon-containing solid fuel Download PDFInfo
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- CN103695013B CN103695013B CN201210366310.6A CN201210366310A CN103695013B CN 103695013 B CN103695013 B CN 103695013B CN 201210366310 A CN201210366310 A CN 201210366310A CN 103695013 B CN103695013 B CN 103695013B
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 179
- 239000004449 solid propellant Substances 0.000 title claims abstract description 66
- 238000000034 method Methods 0.000 title claims abstract description 55
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title abstract description 15
- 229910052799 carbon Inorganic materials 0.000 title abstract description 13
- 239000007787 solid Substances 0.000 claims abstract description 192
- 239000012265 solid product Substances 0.000 claims abstract description 52
- 238000011027 product recovery Methods 0.000 claims abstract description 26
- 239000012263 liquid product Substances 0.000 claims abstract description 17
- 239000007789 gas Substances 0.000 claims description 211
- 239000000969 carrier Substances 0.000 claims description 125
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- 239000002737 fuel gas Substances 0.000 claims description 33
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- 238000002161 passivation Methods 0.000 claims description 4
- 239000011261 inert gas Substances 0.000 claims description 3
- 210000000952 spleen Anatomy 0.000 claims description 3
- 238000009833 condensation Methods 0.000 claims description 2
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- 239000002912 waste gas Substances 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 25
- 230000009286 beneficial effect Effects 0.000 abstract description 3
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- 239000003245 coal Substances 0.000 description 33
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 13
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- 239000008187 granular material Substances 0.000 description 7
- 239000003034 coal gas Substances 0.000 description 6
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- 229910052756 noble gas Inorganic materials 0.000 description 5
- 230000033228 biological regulation Effects 0.000 description 4
- 239000000567 combustion gas Substances 0.000 description 3
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- 238000001035 drying Methods 0.000 description 3
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 2
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- Solid Fuels And Fuel-Associated Substances (AREA)
Abstract
The invention provides a system and a method for pyrolyzing a solid fuel containing carbon. The system comprises: the pyrolysis device is used for pyrolyzing the carbon-containing solid fuel by utilizing the heat of the solid heat carrier and the gas heat carrier to generate crude pyrolysis gas and solid products, and the solid heat carrier and the gas heat carrier are introduced in amounts such that the heat of the solid heat carrier and the heat of the gas heat carrier are insufficient to supply all heat required by the pyrolysis of the carbon-containing solid fuel; the solid product recovery unit, the liquid product recovery unit and the heat carrier supply unit are communicated with the pyrolysis device and output the gas heat carrier and the solid heat carrier to the pyrolysis device. The system and the method for pyrolyzing the carbon-containing solid fuel adopt the solid heat carrier and the gas heat carrier to supply heat for the pyrolysis reaction, thereby being beneficial to improving the yield of liquid products on one hand and reducing the operation difficulty of the system on the other hand.
Description
Technical field
The present invention relates to carbonic solid fuels pyrolysis art, in particular to a kind of internal heat type pyrolysis system and side thereof
Method.
Background technology
Along with the scarcity day by day of petroleum resources, for ensureing the modern industry demand to the energy, sight is gradually turned to by people
The alternative energy source coal of oil.At present, pyrolysis of coal method is the study hotspot of coal chemical technology, and pyrolysis of coal refers to that coal is in isolation
In air or inert atmosphere, decomposes produces gaseous state coal gas, tar liquid and the process of solid-state semicoke.The main component of coal gas
Including H2、CO、CO2And CH4, semicoke is less as moisture and the higher fuel of calorific value uses, and tar can process extraction height
The fine chemistry thing of added value.
Internal heat type method for pyrolysis generally uses gas heat carrier or solid thermal carriers to pyrolysis of coal process heat supply, United States Patent (USP)
US5401364 discloses a kind of semicoke and the method for tar of pyrolysis of coal high heating value, and the method utilizes gas heat carrier to carry out
Being dried and pyrolysis of coal.Chinese patent CN102010728 discloses a kind of pyrolysis of coal and produces semicoke, the method for burnt oil and gas,
The method uses solid thermal carriers mode of heating, in semicoke pyrolysis produced by size separation method and heat carrier mixture
Bulky grain semicoke separate as product, by-product tar and middle calorific value of gas simultaneously.
But, owing to the circulation ratio of gas is required higher by gas heat carrier mode of heating, it is therefore desirable to bigger wind
Power supplies, and simultaneously containing substantial amounts of noble gas in gas heat carrier, these noble gases also can enter exsiccator and pyrolysis dress
In putting, cause the calorific value of gas heat carrier relatively low and be difficult to ensure that its stability burnt, and then causing the heat of discharged producer gas
It is worth relatively low；After pyrolysis completes, gas heat carrier can enter tar recovery unit along with tar, but due to gas heat carrier
In the existence of a large amount of noble gases, cause tar dividing potential drop low and then cause the tar response rate low.
Solid thermal carriers mode of heating overcomes the drawback existing for gas heat carrier, but there is again new problem, by
Big in solid thermal carriers circulating load, simple dependence solid thermal carriers heat supply makes pyrolysis installation operating condition be difficult to regulate；And,
Owing to lacking carrier gas purging effect, gaseous products time of staying in pyrolysis installation is long, and tar easily occurs secondary response, leads
Cause tar yield reduces.
Summary of the invention
It is desirable to provide a kind of carbonic solid fuels that is pyrolyzed is pyrolyzed solid processed, the system of liquids and gases fuel and side
Method, improves the productivity of tar, has obtained middle calorific value of gas and made pyrolysis of coal process convenient to operate and control.
To achieve these goals, according to an aspect of the invention, it is provided one is for pyrolytic carbon material carbon containing
The system of solid fuel, this system includes: pyrolysis installation, in wherein carbonaceous material carbonic solid fuels utilize solid thermal carriers and
The heat of gas heat carrier carries out pyrolysis and produces thick pyrolysis gas and the introduction volume of solid product, solid thermal carriers and gas heat carrier
The thermal capacitance heat making solid thermal carriers and gas heat carrier is all not enough to be supplied separately to the pyrolysis of carbonaceous material carbonic solid fuels
Required net quantity of heat；Solid product recovery unit, connects with pyrolysis installation, for by solid product cooling and/or passivation；Liquid
State product recovery units, gas phase connection pyrolysis installation, receive the thick pyrolysis gas that pyrolysis installation produces, and thick pyrolysis gas is carried out cold
Solidifying, to obtain liquid product and fuel gas；With heat carrier feeding unit, connect with pyrolysis installation, and export gas heat carrier
With in solid thermal carriers to pyrolysis installation.
Preferably, solid product recovery unit connects with liquid product recovery unit, from liquid product recovery unit
Part fuel gas mixture with solid product and/or solid product with solid thermal carriers in solid product recovery unit changes
Heat.
Preferably, solid product recovery unit includes: the first solid separator, connects with pyrolysis installation, is used for separating admittedly
State product and solid thermal carriers, fuel gas from the bottom of the first solid separator introduce, by purging with solid product and consolidate
The mixture heat exchange of body heat carrier, and idetified separation solid product and solid thermal carriers；And chiller, cool down and/or be passivated
Isolated solid product.
Preferably, heat carrier feeding unit includes burner, and the fuel gas after a part of heat exchange of wherein burning produces
Combustion tail gas, at least part of combustion tail gas introduces in pyrolysis installation as gas heat carrier；Also include with heat carrier feeding unit
Solid thermal carriers heating unit, connects with solid product recovery unit, is used for making solid thermal carriers be heated to be high-temp solid heat and carries
High-temp solid heat carrier is also delivered in pyrolysis installation by body.
Preferably, the fuel gas after a part of heat exchange is admitted in burner burning and produces combustion tail gas, another part
Fuel gas after heat exchange enters pyrolysis installation as gas heat carrier after mixing with a part of combustion tail gas.
It is further preferred that said system also includes exsiccator, in solid thermal carriers heating unit, solid thermal carriers
And/or external fuel combustion produces high-temp solid heat carrier and heat smoke, heat smoke, another part of combustion tail gas and be dried
Tail gas is together as being dried in the exsiccator that medium introducing connects with pyrolysis oven.
It is further preferred that system also includes the blender being located between exsiccator and pyrolysis installation, in wherein mixing to come
The carbonaceous material carbonic solid fuels of self-desiccation device and the high-temp solid heat carrier from heat carrier feeding unit.
Preferably, the introduction volume of solid thermal carriers makes its heat provided for pyrolysis be more than or equal to gas heat carrier institute
The heat provided, it is possible to for the heat of carbonaceous material carbonic solid fuels pyrolysis offer 50 ~ 95%, the heat of preferably 55 ~ 90%, enter
The heat of one step preferably 70 ~ 85%, the introduction volume of gas heat carrier can be for the heat of carbonaceous material pyrolysis offer 10 ~ 50%, gas
Body heat carrier can for carbonic solid fuels be pyrolyzed offer 5 ~ 50%, preferably 10 ~ 45%, the heat of preferably 10 ~ 30%.
Preferably, it is 500 ~ 800 DEG C that solid thermal carriers and gas heat carrier enter the temperature of pyrolysis installation, preferably 600 ~
700℃。
According to another aspect of the present invention, it is provided that a kind of method of pyrolytic carbon material carbonic solid fuels, including:
Under the heat effect of solid thermal carriers and gas heat carrier, carbonaceous material carbonic solid fuels is made to be pyrolyzed, solid thermal carriers
The thermal capacitance heat of solid thermal carriers and gas heat carrier is made all to be not enough to be supplied separately to carbonaceous with the introduction volume of gas heat carrier
Net quantity of heat needed for the pyrolysis of material carbonic solid fuels；The thick pyrolysis gas that condensation pyrolysis produces, to obtain fluid oil and flammable
Gas；With solid product is carried out cooling process and solid product is cooled down and/or is passivated.
Further, method also includes making fuel gas and solid product and/or pyrolysis product and solid thermal carriers
Mixture heat exchange.
Further, method also includes: separate pyrolysis product and solid thermal carriers, and be passed through in separation process can
Combustion gas body is to carry out heat exchange and idetified separation solid product and solid thermal carriers.
Further, method also includes: the fuel gas after a part of heat exchange of burning produces combustion tail gas, at least partly fires
It is used as gas heat carrier after burning the fuel gas mixing after tail gas and another part heat exchange.
Further, method also includes, can directly use clean pyrolysis gas to heat as gas heat carrier.
Further, above-mentioned gas heat carrier is vented one's spleen selected from high temperature inert gas, high-temperature hot, is not involved in carbonic solid fuels
Solve the high-temperature tail gas of thermal response, high-temp waste gas and one or more in the group of high-temperature tail gas composition.
Further, said method also includes: burning solid heat carrier and/or external fuel carry to produce high-temp solid heat
Body and heat smoke, and high-temp solid heat carrier is delivered in pyrolysis installation.
Further, said method also includes: heat of mixing flue gas, another part of combustion tail gas and dry tail gas are formed
Dry medium for dried carbonaceous material carbonic solid fuels.Preferably, the heat that solid thermal carriers provide for pyrolysis is more than
Or equal to the heat that gas heat carrier is pyrolysis offer, it is possible to it is pyrolyzed the heat of offer 50 ~ 95% for carbonic solid fuels, preferably
The heat of 55 ~ 90%, the heat of preferably 70 ~ 85%, gas heat carrier can be for the warm of carbonic solid fuels pyrolysis offer 5 ~ 50%
Amount, the heat of preferably 10 ~ 45%, the heat of preferably 15 ~ 30%.
Preferably, it is 500 ~ 800 DEG C that solid thermal carriers and gas heat carrier enter the temperature of pyrolysis installation, preferably 600 ~
700℃。
Preferably, pyrolysis temperature controls to obtain semicoke, coalite tar and medium calorific value gas product at 400 ~ 700 DEG C.
System and method employing solid thermal carriers and the gas heat carrier of the carbonic solid fuels pyrolysis of the present invention are jointly
Pyrolytic reaction heat supply, is on the one hand beneficial to improve the yield of liquid product, on the other hand, reduces the operation easier of system.
In this manual, carbonic solid fuels is a wide in range concept, and it may include but be not limited to: coal, coal are direct
Liquefied residue, heavy oil residue, Jiao, petroleum coke, oil-sand, shale oil, carbonaceous industrial waste or tailing, biomass, synthetic plastic, conjunction
Become polymer, damaged tire, Municipal solid rubbish, Colophonium and/or their mixture.Carbonic solid fuels is preferably pyrolyzed low order
Coal.
Accompanying drawing explanation
The Figure of description of the part constituting the application is used for providing a further understanding of the present invention, and the present invention shows
Meaning property embodiment and explanation thereof are used for explaining the present invention, are not intended that inappropriate limitation of the present invention.In the accompanying drawings:
Fig. 1 shows the system schematic of the carbonic solid fuels pyrolysis according to the present invention.
Detailed description of the invention
It should be noted that in the case of not conflicting, the embodiment in the application and the feature in embodiment can phases
Combination mutually.Describe the present invention below with reference to the accompanying drawings and in conjunction with the embodiments in detail.
As it is shown in figure 1, in an embodiment of the invention, it is provided that a kind of carbonic solid fuels is pyrolyzed solid, liquid processed
With the system of gaseous fuel, this system includes that pyrolysis installation 4, solid product recovery unit, heat carrier feeding unit and liquid are produced
Thing recovery unit 10.In pyrolysis installation 4, the water content carbonic solid fuels less than 15% utilizes solid thermal carriers and air heat
The heat of carrier carries out pyrolysis and produces thick pyrolysis gas and solid product.The introduction volume of described solid thermal carriers and gas heat carrier makes
The heat of described solid thermal carriers and described gas heat carrier is all not enough to be supplied separately to described carbonic solid fuels pyrolysis institute
The net quantity of heat needed.Solid product recovery unit, connects with described pyrolysis installation 4, for by described solid product cooling and/or
Passivation.Liquid product recovery unit 10, gas phase connects described pyrolysis installation 4, receives the thick pyrolysis that described pyrolysis installation 4 produces
Gas, and described thick pyrolysis gas is condensed, to obtain liquid product and fuel gas.Heat carrier feeding unit, with described warm
Solve device 4 to connect, and export in described gas heat carrier and solid thermal carriers extremely described pyrolysis installation 4.
The system of the carbonic solid fuels pyrolysis gentle fuel of solid, liquid processed of the present invention, utilizes solid thermal carriers solid for carbon containing
Fluid fuel pyrolysis provides a part of heat, and another part heat is provided by gas heat carrier.Outside providing heat for pyrolysis, draw
The gas heat carrier entered has purging effect to the gaseous products in pyrolysis installation 4, reduces pyrolysis gaseous products in pyrolysis installation 4
The time of staying, thus decrease tar secondary reaction, be conducive to improving tar yield, and on the other hand, solid thermal carriers
Introduce and mean that the introduction volume of gas heat carrier reduces so that in gaseous products, the content of noble gas reduces, and then improves gas
The calorific value of state product.Simultaneously as the controllability of gas heat carrier heat-supplying mode is preferable, can be according to reality in pyrolytic process
The pyrolysis temperature on border and the heating load of pressure regulating gas heat carrier, overcome the drawback that solid thermal carriers heat supply is difficult to regulate and control.
As it is shown in figure 1, in an embodiment of the invention, optionally, particle diameter be about 3 ~ 60mm, be preferably 10 ~
30mm carbonic solid fuels granule is admitted in exsiccator 1 be dried.Exsiccator 1 is preferably Rotary drying stove, and wherein, carbon containing is solid
Fluid fuel particle temperature is risen to about 120 DEG C by room temperature, and water content reduces to not higher than 15%, preferably smaller than 10%.The temperature of exsiccator 1
Degree is 100 DEG C～200 DEG C, to ensure that carbonic solid fuels granule will not produce pyrolysis and chemical change when removing moisture removal.Can
Any of mode is taked to provide heat for exsiccator 1, to keep the temperature of exsiccator 1, it is preferable that to use and derive from heat load
The combustion tail gas of body feeding unit is as the thermal source of dried carbonaceous solids fuel particle.Exsiccator 1 discharge temperature is about 100 DEG C and does
Dry tail gas, is entered in the first gas-particle separation device 2 by acidproof, anticorrosion, high-temperature resistant pipeline.First gas-particle separation device 2 is preferably
Cyclone cluster or cyclone cluster cascade, its effect is to remove the fine solid particle and/or dust, such as fine breeze being dried in medium.Portion
The dry tail gas isolating fine solid particle and/or dust can empty as dedusting tail gas after desulfurization etc. processes.Preferably,
Another part of dedusting tail gas returns in exsiccator 1 with the combustion tail gas mixing Posterior circle from heat carrier feeding unit.Preferably,
By the introduction volume of regulation dedusting tail gas, the operation temperature of exsiccator 1 is controlled between 100 DEG C～200 DEG C.First gas-solid point
The fine solid particle collected from device 2 and/or dust are preferably sent in heat carrier feeding unit burning, for dried carbonaceous solids
Fuel particle and heating solid dielectric provide thermal source.For extensive pyrolysis system, it is also possible to select portion collection
Fine solid particle and/or dust are compressing, form the solid of such as moulded coal.
Pyrolysis installation 4, is optionally connected with exsiccator 1, carbonic solid fuels or dried carbonic solid fuels profit
It is pyrolyzed wherein with the heat of gas heat carrier and solid thermal carriers.The dry carbonic solid fuels granule of drying device 1,
Solid thermal carriers and gas heat carrier enter pyrolysis installation 4 from different entrances.Preferably, carbonic solid fuels granule and solid
Heat carrier from the top of pyrolysis installation 4 introduce, gas heat carrier by gas distributor (not shown) from the bottom of pyrolysis installation 4
Enter in pyrolysis installation 4.Pyrolysis installation 4 can be common reactor such as moving bed, fluid bed, air flow bed, spouted bed, cylinder,
Rotating disk, rotary kiln etc..Requiring difference according to product specification, carbonic solid fuels time of staying in pyrolysis installation 4 controls
10 minutes to 1.5 hours.Preferably, the system of the present invention also includes for hybrid solid heat carrier and dried carbonaceous solids fuel
Blender 3, blender 3 can be provided separately between exsiccator 1 and pyrolysis installation 4, it is also possible to is directly incorporated in pyrolysis installation 4
Internal.In pyrolysis installation 4, carbonic solid fuels heats at solid thermal carriers and gas heat carrier simultaneously and issues heat solution, shape
Become solid product and gaseous products, the gaseous products of formation is the most i.e. taken away by gas heat carrier, it is to avoid gas
The secondary response of the tar in state product, improves the productivity of tar.
Solid product and solid thermal carriers are discharged from the bottom of pyrolysis installation 4, and are admitted in solid product recovery unit.
Solid product recovery unit can include the first solid separator 7 and chiller 11.In a preferred embodiment, solid product
It is introduced in the first solid separator 7 with the mixture of solid thermal carriers, and relies on granularity difference or density contrast to be sized out.Preferably
Ground, will introduce the bottom of the first solid separator 7 from the fuel gas of liquid product recovery unit 10 and/or gas heat carrier
To purge the mixture on top, loosen mixture whereby, reach the effect of idetified separation solid product and solid thermal carriers.With this
Meanwhile, fuel gas and mixture heat exchange obtain the middle temperature fuel gas of temperature about 350 DEG C.Through the first solid separator 7 points
The solid product separated out subsequently enters chiller 11.In chiller 11, solid product is in the spray of cooling medium, such as water
Drench lower cooling inactivation and/or passivation, form the solid product being easy to follow-up storage and transport, such as burnt or semicoke.Chiller
11 can use cooler pan, direct chiller, indirect cooling device or other cooling device.Preferably, divide through the first solid
It is introduced in the second solid separator 8 from the isolated solid thermal carriers of device 7, with further in isolated solid thermal carriers
Isolate powdery solid granules, such as coke powder.
The gas heat carrier that rises and the gaseous products of pyrolysis generation as together with thick pyrolysis gas from pyrolysis installation 4 top from
Open pyrolysis installation 4, and be admitted to dedusting in the second gas-particle separation device 9.In an exemplary embodiment, second gas-solid point
Be preferably cyclone cluster or cyclone cluster cascade from device 9, for dedusting and collect fine solid particle that above-mentioned thick pyrolysis gas wraps and/or
Dust, above-mentioned fine solid particle and/or dust comprise solid product fine grained and/or the dust of significant proportion, this fine grained and/
Or dust is subsequently passed in heat carrier feeding unit burn and/or be pressed into block moulded coal.
Liquid product recovery unit 10, gas phase connect described pyrolysis installation 4, receive in described pyrolysis installation 4 produce thick
Pyrolysis gas, and pyrolysis gas thick after described dedusting is condensed, to obtain liquid form product, such as tar, and fuel gas.Flammable
Gas is mainly by CO2、CH4、CO、H2Form with lighter hydrocarbons etc., a certain proportion of fuel gas with for gas heat carrier, if to this end, uncommon
Even hope the combustion gas obtaining middle calorific value high heating value, such as coal gas, then need the gas heat carrier controlling to be incorporated in pyrolysis installation 4
Amount, it is preferable that control gas heat carrier amount can for be pyrolyzed offer 10% ~ 50% heat, more preferably, it is provided that
The heat of 10% ~ 30%.When needing, can directly use clean pyrolysis gas to heat as gas heat carrier, the most finally pyrolysis gained is flammable
Gas is high heating value combustion gas.Liquid product recovery unit 10 can use conventional chilling reclaimer such as cooling tower, shell cooling dress
Put, absorb cooling tower and electric fishing storage etc..In one embodiment of the present invention, fuel gas is divided into two strands, and one is made
Sent outside for gas products, another strand be admitted in the first solid separator 7 of heat carrier feeding unit with solid product and/or
Solid thermal carriers heat exchange.
In an embodiment of the invention, heat carrier feeding unit carries for receiving, provide and/or be produced as pyrolysis
The solid thermal carriers of heating load and gas heat carrier.For playing the effect of heat carrier, i.e. keep the temperature in pyrolysis installation 4 and be
Pyrolysis provide temperature that whole institutes calorific requirements, solid thermal carriers and described gas heat carrier enter described pyrolysis installation 4 or with contain
Temperature during carbon solid fuel contact is about 500 ~ 800 DEG C.
Preferably, heat carrier feeding unit includes burner 6 and solid thermal carriers heating unit 5.Above-mentioned solid thermal carriers
Heating unit 5 can include heater and lifting device, and, heater and lifting device can be wholely set formation and have lifting
The heater of function, such as riser burner, rotary kiln are internal is equipped with gas lift device, fluidized bed combustor outfit gas
Lifting device, or, heater is provided separately with lifting device and is interconnected, and the solid thermal carriers that heater produces are boosted
Device enters pyrolysis installation 4 or blender 3 after promoting.
In one embodiment, heat carrier feeding unit receive from solid product recovery unit solid thermal carriers and
The middle temperature fuel gas that fuel gas heat exchange obtains.In burner 6, the described middle temperature fuel gas that burns produces combustion tail gas,
At least part of described combustion tail gas is introduced in described pyrolysis installation 4 as described gas heat carrier.In described solid thermal carriers
In heating unit 5, described solid thermal carriers and/or fuel combustion produce high-temp solid heat carrier and heat smoke, optionally by institute
State heat smoke, another part of described combustion tail gas and dedusting tail gas together as being dried medium introducing and described pyrolysis installation
In the exsiccator 1 of 4 connections.Preferably, a part of described middle temperature fuel gas is admitted in described burner 6 burning, another portion
Described middle temperature fuel gas is divided to enter described pyrolysis installation 4 as described gas heat carrier after mixing with described combustion tail gas.Excellent
Selection of land, the source of gas heat carrier be not limited to combustion tail gas, middle temperature fuel gas and/or their mixture, air heat carries
Body can be that high temperature inert gas, high-temperature hot are vented one's spleen, are not involved in the high-temperature tail gas of carbonic solid fuels pyrolytic reaction, high temperature gives up
Gas and/or their mixture, high temperature referred herein refers to that temperature is at about 500 ~ 800 DEG C.Optionally, the carbon containing of the present invention
The heat needed in solid fuel dry run is mainly provided by the heat smoke produced during reheating solid thermal carriers, not foot
The combustion tail gas produced by burner 6 is divided to supplement, so that the heat of whole pyrolysis system obtains abundant, reasonably sharp further
With, improve the utilization ratio of heat.
In another embodiment of the present invention, additionally provide a kind of carbonic solid fuels method for pyrolysis.The heat of the present invention
Solution method uses solid thermal carriers and gas heat carrier jointly to provide pyrolysis institute calorific requirement, and described solid thermal carriers and air heat
The introduction volume of carrier makes the heat of described solid thermal carriers and described gas heat carrier all be not enough to be supplied separately to described carbon containing
Net quantity of heat needed for solid fuel pyrolysis.The consumption that the addition of solid thermal carriers decreases gas heat carrier is the most therein
The content of noble gas, thus, on the one hand can improve the yield of tar when reclaiming tar, on the other hand, add and come out of the stove
The calorific value of coal gas, has obtained middle calorific value of gas；Meanwhile, the addition of gas heat carrier enhances the controllability of system, in pyrolysis
During can overcome simple solid thermal carriers heat supply difficult according to the heating load of actual pyrolysis temperature regulation gas heat carrier
Drawback with regulation and control.
The present invention is not intended to the consumption of solid thermal carriers and gas heat carrier is done any restriction, uses gas as long as meeting simultaneously
Body heat carrier and the requirement that solid thermal carriers are pyrolytic reaction heat supply.Preferably, solid thermal carriers provide the heat of 50 ~ 90%
Amount, gas heat carrier provides the heat of 10 ~ 50%, it is highly preferred that solid thermal carriers provide the heat of 70% ~ 90%.When solid for carbon containing
When fluid fuel pyrolysis provides the ratio of the solid thermal carriers of heat and the heat of gas heat carrier to be about 9:1 ~ 1:1, can not only
Enough making full use of the heat of solid thermal carriers provide 50 ~ 90%, and pyrolytic process can be played preferably by gas heat carrier
Regulation effect.Owing to the specific heat of different solid thermal carriers is different, the specific heat of different gas heat carriers is the most different, this area skill
Art personnel can select appropriate material amounts to complete the heat of the present invention according to heat balance according to the specific heat size of material used
Amount distribution, reaches the heat balance of whole system/technique.
In one preferred embodiment of the present invention, above-mentioned solid thermal carriers and gas heat carrier connect with carbonic solid fuels
Temperature when touching is 500 ~ 800 DEG C.Solid thermal carriers and air heat bed temperature are 500 ~ 800 DEG C, if heat carrier temperature
Too high, then high to equipment requirements, and be easily caused liquid product twice decomposition thus reduce yield；If heat carrier temperature mistake
Low, then heat carrier circulating load is big, and equipment volume is big.
Use solid thermal carriers when carbonic solid fuels pyrolytic reaction heat supply, solid thermal carriers and carbonic solid fuels it
Between contact area its heat-transfer effect bigger the best, therefore, the preferred solid thermal carriers of the present invention are the aluminium oxide that particle diameter is less than 2mm
Granule, ceramic particle.And, the distribution of process and product in order to improve pyrolytic reaction, preferably solid thermal carriers are load
There are the alumina particle of catalyst, ceramic particle, sandstone granule.Can select the corresponding catalyst can according to the demand of product
Increase the productivity of required product.
As a example by pyrolysis low-order coal, the method that above-mentioned carbonic solid fuels is pyrolyzed is described below.Raw coal drying device 1 is dried
After the moisture-free coal that obtains to enter blender 3 and the solid thermal carriers that temperature is 500 ~ 800 DEG C being mixed to form in blender 3 mixed
Compound, this mixture contacts with the gas heat carrier that temperature is 500 ~ 800 DEG C further in pyrolysis installation 4 and starts pyrolysis,
Pyrolysis temperature controls to obtain semicoke, coalite tar and medium calorific value gas product at 400 ~ 700 DEG C.In said process, mixture is excellent
Selecting and entered in pyrolysis installation 4 by the top of pyrolysis installation 4, gas heat carrier enters pyrolysis installation 4 from the bottom of pyrolysis installation 4.
In pyrolytic process, due to the gas heat carrier purging effect to mixture, accelerate conduction of heat, decrease pyrolysis gas and stop
Stay the time, it is to avoid the secondary response of the tar in pyrolysis gas.
Oarse-grained semicoke in thermal decomposition product enters the first solid with solid thermal carriers from the bottom of pyrolysis installation 4 and separates
After device 7 is separated, oarse-grained semicoke enters in chiller 11 and is cooled to less than 200 DEG C and reclaims and i.e. obtain semicoke product, solid
Heat carrier enters the second solid separator 8 and carries out further separating treatment, and the coke powder of wherein most is from the second solid separator 8
In separate, remaining solid matter enters and enters into circulation profit in blender 3 after solid thermal carriers heating unit 5 reheating
With；The after in thermal decomposition product, the short grained semicoke of part, gas heat carrier and gaseous products are removed by the top of pyrolysis installation 4
The semicoke of two gas-particle separation device 9 small particles separates with gaseous material, and short grained semicoke enters solid thermal carriers heating unit
5 as fuel heat solid thermal carriers, gaseous material through liquid product recovery unit 10 compression be cooled to 60 ~ 120 DEG C after, tar
Becoming liquid to be recovered, the middle calorific value of gas part that can not coagulate reclaims, and a part and gas heat carrier enter from bottom
First solid separator 7, and in the first solid separator 7, it is heated to 250 ~ 350 DEG C, then make temperature at 250 ~ 350 DEG C
Middle calorific value of gas enters burner 6 and burns, and the combustion tail gas of generation is pyrolytic reaction heat supply as gas heat carrier.Pass through high temperature
Solid product hankers calorific value of gas in advance, reasonably make use of heat energy；And, middle calorific value of gas can be to the semicoke of solid-state and solid
Heat carrier plays the effect of loosening, and is conducive to strengthening both separation.
Below in conjunction with embodiment and comparative example, further illustrate beneficial effects of the present invention.
Following example use flow process as shown in Figure 1 raw coal carries out pyrolysis processing, the particle diameter of handled raw coal
Between 3 ~ 50mm, become and be grouped into as shown in table 1.Raw coal enters exsiccator with the flow velocity of 145833kg/h in terms of wet basis, and
Being heated to moisture at 210 DEG C and obtain moisture-free coal below 5%, the calorific value of moisture-free coal is 5975Kcal/kg, and in terms of butt
Enter blender with the flow velocity of 97125kg/h to mix with solid thermal carriers.
Table 1
| Content (wt%) | |
| Moisture | 33.40 |
| Fixed carbon | 31.14 |
| Volatile material | 25.47 |
| Ash | 9.99 |
Embodiment 1
The solid thermal carriers used are the alumina particle that particle diameter is less than 2mm, and temperature when entering blender is 700 DEG C,
Specific heat is 1.91kJ/kg. DEG C, and flow is 220000kg/h, and the gas heat carrier of employing is 800 DEG C from burner and temperature,
Specific heat is 1.71kJ/kg. DEG C, and solid thermal carriers provide the heat of 85% for pyrolytic reaction, and gas heat carrier provides for pyrolytic reaction
The heat of 15%.Moisture-free coal is pyrolyzed formation semicoke, tar and middle calorific value of gas at 530 DEG C, and the flow of various products is shown in Table 2, receives
Rate is shown in Table 3.
Embodiment 2
The solid thermal carriers used are the alumina particle that particle diameter is less than 2mm, and temperature when entering blender is 700 DEG C,
Specific heat is 1.91kJ/kg. DEG C, and flow is 240000kg/h, and the temperature of gas heat carrier is 700 DEG C, and specific heat is 1.76kJ/kg.
DEG C, solid thermal carriers provide the heat of 90% for pyrolytic reaction, and gas heat carrier provides the heat of 10% for pyrolytic reaction.Moisture-free coal
At 530 DEG C, pyrolysis forms semicoke, tar and middle calorific value of gas, and flow is shown in Table 2, and yield is shown in Table 3.
Embodiment 3
The solid thermal carriers used are that particle diameter is less than 2mm alumina particle, and temperature when entering blender is 700 DEG C, than
Heat is 1.91kJ/kg. DEG C, and flow is 180000kg/h, and the gas heat carrier of employing is 800 DEG C from burner and temperature, than
Heat is 1.62kJ/kg. DEG C, and solid thermal carriers provide the heat of 70% for pyrolytic reaction, and gas heat carrier provides for pyrolytic reaction
The heat of 30%.Moisture-free coal is pyrolyzed formation semicoke, tar and middle calorific value of gas at 530 DEG C, and flow is shown in Table 2, and yield is shown in Table 3.
Embodiment 4
The solid thermal carriers used are the alumina particle that particle diameter is less than 2mm, and temperature when entering blender is 600 DEG C,
Specific heat is 1.74kJ/kg. DEG C, and flow is 550000kg/h, and the gas heat carrier of employing is 600 DEG C from burner and temperature,
Specific heat is 1.59kJ/kg. DEG C, and solid thermal carriers provide the heat of 85% for pyrolytic reaction, and gas heat carrier provides for pyrolytic reaction
The heat of 15%.Moisture-free coal is pyrolyzed formation semicoke, tar and middle calorific value of gas at 530 DEG C, and flow is shown in Table 2, and yield is shown in Table 3.
Embodiment 5
The solid thermal carriers used are the alumina particle that particle diameter is less than 2mm, and temperature when entering blender is 600 DEG C,
Specific heat is 1.74kJ/kg. DEG C, and flow is 330000kg/h, and the gas heat carrier of employing is 800 DEG C from burner and temperature,
Specific heat is 1.71kJ/kg. DEG C, and solid thermal carriers provide the heat of 50% for pyrolytic reaction, and gas heat carrier provides for pyrolytic reaction
The heat of 50%.Moisture-free coal is pyrolyzed formation semicoke, tar and middle calorific value of gas at 530 DEG C, and flow is shown in Table 2, and yield is shown in Table 3.
Embodiment 6
The solid thermal carriers used are the alumina particle that particle diameter is less than 2mm, and temperature when entering solid mixer is 600
DEG C, specific heat is 1.74kJ/kg. DEG C, and flow is 380000kg/h, and the gas heat carrier of employing is 600 DEG C from burner and temperature,
Specific heat is 1.59kJ/kg. DEG C, and solid thermal carriers provide the heat of 55% for pyrolytic reaction, and gas heat carrier provides for pyrolytic reaction
The heat of 45%.Moisture-free coal is pyrolyzed formation semicoke, tar and middle calorific value of gas at 530 DEG C, and flow is shown in Table 2, and yield is shown in Table 3.
Embodiment 7
The solid thermal carriers used are the alumina particle that particle diameter is less than 2mm, and temperature when entering solid mixer is 700
DEG C, specific heat is 1.91kJ/kg. DEG C, and flow is 40000kg/h, and the gas heat carrier of employing is 700 DEG C from burner and temperature,
Specific heat is 1.76kJ/kg. DEG C, and solid thermal carriers provide the heat of 10% for pyrolytic reaction, and gas heat carrier provides for pyrolytic reaction
The heat of 90%.Moisture-free coal is pyrolyzed formation semicoke, tar and middle calorific value of gas at 530 DEG C, and flow is shown in Table 2, and yield is shown in Table 3.
Embodiment 8
The solid thermal carriers used are the alumina particle that particle diameter is less than 2mm, and temperature when entering solid mixer is 600
DEG C, specific heat is 1.74kJ/kg. DEG C, and flow is 630000kg/h, and the gas heat carrier of employing is 700 DEG C from burner and temperature,
Specific heat is 1.76kJ/kg. DEG C, and solid thermal carriers provide the heat of 95% for pyrolytic reaction, and gas heat carrier provides for pyrolytic reaction
The heat of 5%.Moisture-free coal is pyrolyzed formation semicoke, tar and middle calorific value of gas at 530 DEG C, and flow is shown in Table 2, and yield is shown in Table 3.
Comparative example 1
The gas heat carrier used is 600 DEG C from burner and temperature, and thermal capacitance is 1.62kJ/kg. DEG C, gas heat carrier
The heat of 100% is provided for pyrolytic reaction.Moisture-free coal is pyrolyzed formation semicoke, tar at 530 DEG C, and flow is shown in Table 2, and yield is shown in Table 3.
Comparative example 2
The solid thermal carriers used are the alumina particle that particle diameter is less than 2mm, and temperature when entering blender is 700 DEG C,
Thermal capacitance is 1.91kJ/kg. DEG C, and flow velocity is 350000kg/h, and solid thermal carriers provide the heat of 100%, moisture-free coal for pyrolytic reaction
At 530 DEG C, pyrolysis forms semicoke, tar and middle calorific value of gas, and the flow of various products is shown in Table 2, and yield is shown in Table 3.
Table 2
Table 3
From the data in table 2 to table 3, the productivity that embodiment 1 to 8 adopts the tar being obtained by the present invention is more right
Ratio 1 and comparative example 2 all increase, and the productivity of the tar especially obtained in embodiment 1 to 4 relatively comparative example 1 improves about
20%, relatively comparative example 2 improves about 30%, and, can be had by the heat supply ratio controlling solid thermal carriers and gas heat carrier
Effect improves the calorific value of the coal gas of gained, and the calorific value of the coal gas obtained by such as embodiment 1 to 4 is all at 2000Kcal/Nm3Above.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for the skill of this area
For art personnel, the present invention can have various modifications and variations.All within the spirit and principles in the present invention, that is made any repaiies
Change, equivalent, improvement etc., should be included within the scope of the present invention.
Claims (24)
1. the system being used for being pyrolyzed carbonic solid fuels, it is characterised in that described system includes:
Pyrolysis installation (4), utilizes the heat of solid thermal carriers and gas heat carrier to carry out pyrolysis in wherein carbonic solid fuels and produces
Raw thick pyrolysis gas and solid product, the introduction volume of described solid thermal carriers and gas heat carrier makes described solid thermal carriers and institute
The heat stating gas heat carrier is all not enough to be supplied separately to the net quantity of heat needed for the pyrolysis of described carbonic solid fuels；
Solid product recovery unit, connects with described pyrolysis installation (4), for by the cooling of described solid product and/or passivation；
Liquid product recovery unit (10), gas phase connects described pyrolysis installation (4), and receive that described pyrolysis installation (4) produces is thick
Pyrolysis gas, and described thick pyrolysis gas is condensed, to obtain liquid product and fuel gas；With
Heat carrier feeding unit, connects with described pyrolysis installation (4), and exports described gas heat carrier and solid thermal carriers to institute
State in pyrolysis installation (4).
System the most according to claim 1, it is characterised in that described solid product recovery unit returns with described liquid product
Receiving unit (10) connection, the part fuel gas from described liquid product recovery unit (10) reclaims single at described solid product
With the mixture heat exchange of described solid product and/or solid product with solid thermal carriers in unit.
System the most according to claim 2, it is characterised in that described solid product recovery unit includes:
First solid separator (7), connects with described pyrolysis installation (4), is used for separating described solid product and described solid thermal
Carrier, described fuel gas from the bottom of described first solid separator (7) introduce, by purging with described solid product and consolidate
The mixture heat exchange of body heat carrier, and solid product described in idetified separation and solid thermal carriers；With
Chiller (11), cooling and/be passivated described isolated solid product.
System the most according to claim 2, it is characterised in that described heat carrier feeding unit includes:
Burner (6), the fuel gas after a part of described heat exchange of wherein burning produces combustion tail gas, at least part of described combustion
Burn tail gas to introduce in described pyrolysis installation (4) as described gas heat carrier；With
Solid thermal carriers heating unit (5), connects with described solid product recovery unit, is used for making described solid thermal carriers heat
It is delivered in described pyrolysis installation (4) for high-temp solid heat carrier and by described high-temp solid heat carrier.
System the most according to claim 4, it is characterised in that the fuel gas after a part of described heat exchange is admitted to described
In burner (6), burning produces combustion tail gas, the fuel gas after heat exchange described in another part and a part of described combustion tail gas
Described pyrolysis installation (4) is entered as described gas heat carrier after mixing.
System the most according to claim 5, it is characterised in that described system also includes exsiccator (1), in described solid thermal
In carrier heating unit (5), described solid thermal carriers and/or external fuel combustion produce high-temp solid heat carrier and heat smoke,
Described heat smoke, another part of described combustion tail gas and dry tail gas are together as being dried medium introducing and described pyrolysis dress
Put in the described exsiccator (1) that (4) connect.
System the most according to claim 6, it is characterised in that described system also includes being located at described exsiccator (1) and heat
Solve the blender (3) between device (4), in wherein mixing the described carbonic solid fuels from exsiccator (1) and carrying out self-heating load
The high-temp solid heat carrier of body feeding unit.
System the most according to any one of claim 1 to 7, it is characterised in that the introduction volume of described solid thermal carriers makes
Obtaining it is heat that heat that pyrolysis provides is more than or equal to that gas heat carrier is pyrolysis offer,
Described solid thermal carriers can provide 50～the heat of 95% for the pyrolysis of described carbonic solid fuels；
Described gas heat carrier can provide 5～the heat of 50% for the pyrolysis of described carbonic solid fuels.
System the most according to any one of claim 1 to 7, it is characterised in that the introduction volume of described solid thermal carriers makes
Obtaining it is heat that heat that pyrolysis provides is more than or equal to that gas heat carrier is pyrolysis offer,
Described solid thermal carriers can provide 55～the heat of 90% for the pyrolysis of described carbonic solid fuels；
Described gas heat carrier can provide 10～the heat of 45% for the pyrolysis of described carbonic solid fuels.
System the most according to any one of claim 1 to 7, it is characterised in that the introduction volume of described solid thermal carriers makes
Obtaining it is heat that heat that pyrolysis provides is more than or equal to that gas heat carrier is pyrolysis offer,
Described solid thermal carriers can provide 70～the heat of 85% for the pyrolysis of described carbonic solid fuels；
Described gas heat carrier can provide 10～the heat of 30% for the pyrolysis of described carbonic solid fuels.
11. systems according to claim 8, it is characterised in that described solid thermal carriers and described gas heat carrier enter
The temperature of described pyrolysis installation (4) is 500～800 DEG C.
12. 1 kinds of methods being pyrolyzed carbonic solid fuels, including:
Under the heat effect of solid thermal carriers and gas heat carrier, carbonic solid fuels is made to be pyrolyzed, described solid thermal carriers
The heat of described solid thermal carriers and described gas heat carrier is made all to be not enough to be supplied separately to the introduction volume of gas heat carrier
Net quantity of heat needed for the pyrolysis of described carbonic solid fuels；
The thick pyrolysis gas that condensation pyrolysis produces, to obtain fluid oil and fuel gas；And
Solid product is cooled down and/or is passivated.
13. methods according to claim 12, described method also include making described fuel gas and described solid product and
The mixture heat exchange of solid thermal carriers.
14. methods according to claim 13, described method also includes separating described solid product and described solid thermal carries
Body, and in separation process, it is passed through fuel gas to carry out solid product and solid thermal carriers described in heat exchange and idetified separation.
15. methods according to claim 13, described method also includes burning the fuel gas after a part of described heat exchange
Produce combustion tail gas, be used as described after the fuel gas mixing after heat exchange described at least part of described combustion tail gas and another part
Gas heat carrier.
16. methods according to claim 15, described method also includes directly using clean pyrolysis gas to heat as air heat
Carrier.
17. methods according to claim 15, described gas heat carrier is vented one's spleen, no selected from high temperature inert gas, high-temperature hot
Participate in the high-temperature tail gas of carbonic solid fuels solution thermal response, high-temp waste gas and one or more in the group of high-temperature tail gas composition.
18. methods according to claim 15, described method also includes burn described solid thermal carriers and/or external fuel
To produce high-temp solid heat carrier and heat smoke, and described high-temp solid heat carrier is delivered in pyrolysis installation (4).
19. methods according to claim 18, described method also includes another portion mixing described heat smoke, combustion tail gas
Divide and dry tail gas forms the dry medium being used for dried carbonaceous solids fuel.
20. according to the method according to any one of claim 12 to 19, solid thermal carriers be the heat that provides of pyrolysis more than or
The heat provided for pyrolysis equal to gas heat carrier,
Described solid thermal carriers can provide 50～the heat of 95% for the pyrolysis of described carbonic solid fuels；
Described gas heat carrier can provide 5～the heat of 50% for the pyrolysis of described carbonic solid fuels.
21. according to the method according to any one of claim 12 to 19, solid thermal carriers be the heat that provides of pyrolysis more than or
The heat provided for pyrolysis equal to gas heat carrier,
Described solid thermal carriers can provide 55～the heat of 90% for the pyrolysis of described carbonic solid fuels；
Described gas heat carrier can provide 10～the heat of 45% for the pyrolysis of described carbonic solid fuels.
22. according to the method according to any one of claim 12 to 19, solid thermal carriers be the heat that provides of pyrolysis more than or
The heat provided for pyrolysis equal to gas heat carrier,
Described solid thermal carriers can provide 70～the heat of 85% for the pyrolysis of described carbonic solid fuels；
Described gas heat carrier can provide 10～the heat of 30% for the pyrolysis of described carbonic solid fuels.
23. methods according to claim 20, it is characterised in that described solid thermal carriers and described gas heat carrier enter
The temperature of pyrolysis installation (4) is 500～800 DEG C.
24. methods according to claim 20, it is characterised in that described pyrolysis temperature controls to obtain half at 400～700 DEG C
Jiao, coalite tar and medium calorific value gas product.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| GB747061A (en) * | 1953-04-25 | 1956-03-28 | Union Rheinische Braunkohlen | Production of gases of high and low calorific value |
| US4078973A (en) * | 1976-07-12 | 1978-03-14 | Occidental Petroleum Corporation | Loop pyrolysis process for organic solid wastes |
| CN102297431A (en) * | 2010-06-24 | 2011-12-28 | 中国科学院过程工程研究所 | Method and device for decoupling and burning solid waste with high water content |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB747061A (en) * | 1953-04-25 | 1956-03-28 | Union Rheinische Braunkohlen | Production of gases of high and low calorific value |
| US4078973A (en) * | 1976-07-12 | 1978-03-14 | Occidental Petroleum Corporation | Loop pyrolysis process for organic solid wastes |
| CN102297431A (en) * | 2010-06-24 | 2011-12-28 | 中国科学院过程工程研究所 | Method and device for decoupling and burning solid waste with high water content |
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