CN1240810C - Four coproduction process and equipment for circular fluiding carbon-hydrogen solid fuel - Google Patents
Four coproduction process and equipment for circular fluiding carbon-hydrogen solid fuel Download PDFInfo
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Abstract
The present invention relates to a four-coproduction technique for circulating fluidized carbon-hydrogen solid fuel. Powdery solid fuel is rapidly mixed with fed hot ash in a solid-solid mixer; after temperature rises, the mixture pyrolyzes when downwards moving through a downstream pipe, volatile components are separated out, and a gas-solid mixture produced after pyrolysis is completed is sent to a gas-solid separator to be separated; separated oil gas and fuel gas are respectively collected after cooled by a condenser; separated solid semi coke and circulating hot ash continuously and downwards move to return to a circulating fluidized bed boiler to be burned for heat supply, and the heat transfer surface in the boiler absorbs heat to generate steam in order to supply heat/ generate electricity; high-temperature hog ash is fed to the solid-solid mixer again to newly be in circulation to realize the four coproduction of oil, gas, heat and electricity.
Description
The invention belongs to solid-fuelled technology of fast pyrogenation and device, particularly a kind of circulating fluidization solid fuel, to extract oil fuel, combustion gas, coal-char combustion produces the hydrocarbon solid-fuelled tetrad production art of circulating fluidization and the device of heat/electricity subsequently.Here the solid fuel of indication can be coal, resinous shale, biomass, Tar sands etc., also can be their mixture.
Carbonic solid fuels is handled through various thermal chemical reactions (as gasification, liquefaction, pyrolysis and burning etc.) can obtain heat energy, electric energy, chemical or fuel, existing thermal processing method mostly is the material that carbon raw materials such as coal, biomass is considered as single property, by single process it all is converted into single product.With the coal is example, in the combustion processes, with the carbon in the fuel, the whole oxidations of hydrogen, with extraction heat energy, and then produces electric energy, and this thermal processing method is not only wasted resource, and damage ratio is more serious;
Coal direct liquefaction is transformed into hydrocarbon fuel oil, need be under the condition of high temperature, high pressure and catalyzer, and also process yield is lower, up to the present still rests on the laboratory test stage;
Coal is carried out indirect liquefaction, need the higher hydrocarbons in the strong broken ring coal, coal is degraded into gas phase CO and H
2, make intermediate hydrocarbon-type oil or other chemical by synthetic gas again; This obtains the technology of oil product, and coal is had relatively high expectations, and needs a large amount of facility investments, and the operation and maintenance of device also needs the expense of writing, and therefore development still rarely has application so far;
With coal be gasified totally need be comparatively strict condition because semicoke inactivation under the high-temperature atmosphere causes incomplete conversion, so gasification furnace structure complexity, cost height, coal is had certain requirement;
Above-mentioned technology mainly is to obtain a kind of purpose product, and obtains the process more complicated of oil, coal gas, and the condition harshness is invested higher.
Some fundamental researchs show, are the solid fuel of representative with the coal, mostly are organic and mixture mineral compound, pyrolysis can take place in heat-processed to be transformed, some hydro carbons and the organic compound that comprise in the coal can produce cracking, form gas or liquid and overflow, simultaneously residual semicoke and ash content.If adopt rapid heating technology, it is the scope that the heating rate of material reaches 1000～10000 ℃ of per seconds, make material in less than 1 second time, reach 400～750 ℃ temperature of reaction, complex organic compound in the solid fuel can resolve into the good component of chemical activity in a large number, these components mainly form by depolymerization and distillation at first, and these elementary products can keep original nonequilibrium situations through after the Quench.Can be selectively and obtain valuable chemical intermediate, high-grade fuel oil or high-quality combustion gas as much as possible by controlling suitable operational condition, and avoid generating too much the solid semicoke and the heavy tar of low value.
There has been the history of decades in China to the research of pyrolytic technique, and a large amount of laboratory studyes was done at the aspects such as low-temperature pyrolysis, hydropyrolysis and biomass fast pyrogenation of coal by units such as Shanxi Inst. of Coal Chemistry, Chinese Academy of Sciences, Beijing Coal Chemistry Inst., Coal Sciences General Inst., Dalian University of Technology, Chemical Industry ﹠ Metallrygy Research Office of CAS, East China University of Science.For achievement in research being pushed to industrial application, domestic expanding test even the type approval test that has carried out some Poly-generation.For example: three jointly-supplying technologies that domestic how tame institute and boiler factory are are researching and developing, its process characteristic is: circulating fluidized bed combustion coal boiler and producer gas generator are organically combined, 850 ℃～900 ℃ high-temp circulating ash with circular fluid bed are thermal barrier, it is sent into cycling hot coal gas do in the bubbling fluidized bed gasification of coal device of fluidizing medium, the broken coal of granularity 6～13mm reaches about 800 ℃ being heated in the gasifier, partial gasification takes place, and the generation calorific value is 10.5～12.5MJ/Mm
3About coal gas can be for output, the semicoke after the gasification is got back in the boiler furnace with circulating ash and is burnt, heat production generating, thereby realize the combination producing of coal gas, heating power and electric power.This technology lab scale is finished at present, and has carried out the design of 75t/h Poly-generation demonstration unit.But do not see relevant three coproduction results' report as yet.This technology is the output oil product not, but slow because of the material heat-up rate, gasification temperature is not high enough, could use after contained heavy tar need clean in the coal gas, and the coal gas aftertreatment technology is complicated, easily causes new pollution.
With tar, coal gas, semicoke is that the multi-joint confession technology of purpose product also has two kinds of technologies to carry out type approval test at home.A kind ofly be made up of 3 placed in-line Roarykilns for the pyrolysis of coal technology of MRF (multi-stage rotary stove), raw coal size 3～25mm adopts external-heat to be heated to 550～700 ℃ of temperature of reaction in a rotary kiln, and semicoke reaches 60% in the product, coal gas 250～300m
3/ t coal, tar yield are 60～70% of theoretical amount.Because tar yield is on the low side, and viscosity is big, process energy consumption is higher, and the semicoke purposes is indeterminate, and test stops; Another kind is " a brown coal solid thermal carriers distillation process ", the use raw material is the fine coal less than 8mm, its main pyrolytic process equipment has mixing tank, pyrolysis reactor, semicoke heating riser tube, fluidized bed combustion stove etc., dry coal mixes at mechanical mixer with 800 ℃ of hot coke powders, temperature rise to 550～650 ℃, enter moving-burden bed reactor and carry out pyrolytic reaction, separate out the destructive distillation gaseous product, discharge semicoke, wherein the semicoke of about 600 ℃ of parts is by partial combustion and heating up in the heating riser tube reaches again about 800 ℃ from 800～900 ℃ of oxygen gas of fluidized bed combustion stove, reenter mixing tank and mix with dry coal again, repeat the pyrolysis circulation; This process solids thermal barrier is a semicoke, and product is based on cooled semicoke, in dried brown coal per ton, and output semicoke 0.3～0.45t, tar 0.02～0.03t, coal gas 200m
3About.Because this technology coal grain is thicker, the solid particulate heating rate is slower, and tar content is few and matter sticking, influence operation direct motion, and the semicoke purposes is not smooth again, has stopped test after identifying.
Above-mentioned multi-production process, also there is more problem in the technology of not promotion and application, especially coproducing oil product as yet.
The object of the present invention is to provide hydrocarbon solid-fuelled tetrad production art of a kind of circulating fluidization and device, make powdered solid fuel in several specific equipments of reactive system, progressively realize the abundant burning of rapid heating, gas-solid sharp separation, gas-phase product rapid condensation and solid semicoke, thus the more oil product of output, medium calorific value gas and produce heat energy and then can be for generating.
Embodiment of the present invention is as follows:
The hydrocarbon solid-fuelled tetrad production art of circulating fluidization provided by the invention, its processing step is as follows:
1) will contain hydrocarbon solid fuel through pulverizing, screening powdering material, and after carrying out drying treatment, send into a non-pressurized mixing tank admittedly, in mixing tank admittedly, pulverulent material mixes intensification simultaneously rapidly with heat ash from circular fluid bed, afterwards, be admitted to a quick down pipe;
2) pulverulent material with from the mixture of the heat ash of circular fluid bed in down pipe fast, limit descending limit pyrolysis; The descending time by quick down pipe of mixture is 0.5-1.5 second, separates out volatilizable branch during pyrolysis, when pyrolysis is finished gas-solid mixture is sent into quick gas-solid separator;
3) sharp separation gas-solid mixture in quick gas-solid separator, disengaging time is 0.02-0.2 second, a rapid condensation device is sent in isolated oil gas and combustion gas rapidly, and the 0.1-1 time internal cooling to 0 of second～30 ℃, uncondensable gas phase fuel gas product is collected after the condenser cooling; The cold circulating liquid rapid cooling transformation of condensable oil gas in the rapid condensation device becomes the liquid phase oil product to be collected; Isolated solid phase semicoke and cycling hot ash continue descending, send into the bottom of rapid circulating fluidized bed boiler by a solid returning charge mechanism, in the rapid circulating fluidized bed boiler, semicoke and air fully burn with heat supply, heat-transfer surface in the boiler absorbs heat and produces steam, but draws not only heat supply but also can generate electricity of steam;
Cycling hot ash after burning heats up is entrained to furnace roof by the rising flue gas, carry out gas solid separation, hot flue gas is discharged after by the heat-transfer surface absorbing and cooling temperature, the hot ash of collecting of high temperature circulation enters deposits ash bucket, through a high-temp solid material valve, quantitatively add mixing reactor admittedly, participate in circulation again and carry out pyrolysis, burning, obtain oil, gas, heat, electricity, realize that tetrad produces;
The granularity of pulverulent material is the 0.03-0.3 millimeter in the described step 1);
The temperature of heat ash is 800～900 ℃ in the described step 1), and pulverulent material and hot grey blended weight part proportioning are 1: 6-1: 10;
Temperature rise rate in the described step 1) is 1000～5000 ℃ of per seconds, and heating up in the time of second at 0.1-1 reaches 450～700 ℃;
Pulverulent material in the step 1) is with the blended time is 0.1-1 second rapidly in mixing tank admittedly from the heat ash of circular fluid bed;
Described step 2) temperature in the quick down pipe is 400～650 ℃.
The hydrocarbon solid-fuelled tetrad of circulating fluidization provided by the invention produces device, it is characterized in that, comprise admittedly mixing tank 2, adjustable solid material valve 3, fast down pipe 4, fast gas-solid separator 5, rapid condensation device 6, fast fluidized bed burner 8 and powder feed device 1, smoke separator 9, deposit grey hopper 10 and returning charge U valve 7;
According to circulating path, these parts ordering from top to bottom are: smoke separator 9 is positioned at the top, its underpart connects deposits grey hopper 10, the lower end of depositing grey hopper 10 connects adjustable solid material valve 3, adjustable solid material valve 3 connects mixing tank 2 admittedly, admittedly Gu the side of mixing tank 2 is installed feeder 1, admittedly Gu the lower end of mixing tank 2 connects quick down pipe 4, down pipe 4 lower ends connect quick gas-solid separator 5 fast, the side of gas-solid separator 5 connects rapid condensation device 6 fast, the lower end of gas-solid separator 5 connects returning charge U valve 7 fast, and the drainage conduit of returning charge U valve 7 connects the lower end of fast fluidized bed burner 8, and fast fluidized bed burner 8 upper ends link to each other with smoke separator 9;
Described mixing tank 2 admittedly comprises a cavity, its top is cylinder barrel shaped cavity 221, the bottom is turbination cavity 222 or cylinder barrel shaped concentrated phase fluidized-bed 27, the upper end of this cavity is connected with the material valve outlet port pipe 24 of solid material valve 3, a conical distributor 29 is installed on top cylinder barrel shaped cavity 221 cavity inner axes lines, when the cavity bottom is turbination cavity 222, conical cavity 222 bottoms are shrunk to blanking pipe 25 and are connected with quick down pipe 4, and the inlet pipe 21 that vertical central lines tangentially is blown into is installed on the cylinder wall of top cylinder barrel shaped cavity 221; When the cavity bottom was cylinder barrel shaped concentrated phase fluidized-bed 27, the sidewall of the air compartment 26 of its grid distributor below was provided with inlet pipe 28, and the blanking pipe 25 of concentrated phase fluidized-bed 27 is connected with quick down pipe 4;
Described quick down pipe 4 is the circular section long tube of a vertical installation, and its upper end is connected with the outlet of consolidating mixing tank 2, and its lower end is communicated with the inlet tube of quick gas-solid separator 5;
Described quick gas-solid separator 5 comprises a cylinder barrel shaped cavity 59, a nozzle 52 that inwardly shrinks is installed in its center, top, nozzle 52 is connected with quick down pipe 4 outlets, at the middle part of cylinder barrel shaped cavity 59 axis arc surfaced cone shape separator 53 is installed, be respectively equipped with two cambered surface flow deflectors 54 that cambered surface intersects on the cylinder barrel shaped cavity 59 both sides inner-wall surfaces, the height of its intersecting lens in the center of gravity of separator 53 between the bottom surface, cylinder barrel shaped cavity 59 bottoms are shrunk to inverted cone, and be connected with the standpipe 55 of returning charge U-shaped valve 7 inlet, the top of cylinder barrel shaped cavity 59 is connected with the inlet pipe 64 of fast quench device 6 near the escape pipe of installing on the vertical sidewall 56; The cambered surface radian of described arc surfaced cone shape separator 53 is 60-90 °; The cambered surface radian of described pair of cambered surface flow deflector 54 is 60-90 °;
The reverse jet tube 62 of described rapid condensation device 6 is a cylindrical blank pipe, perforate communicates with the escape pipe 56 of gas-solid separator 5 on the reverse jet tube 62 vertical sidewalls, its underpart is vertical to be installed on the top cover of cylindrical cooling chamber 65, and communicate with cylindrical cooling chamber 65, single-hole nozzle 63 is vertical to be installed on the axis of reverse jet tube 62 bottoms, open the inlet pipe that a circular hole is communicated with secondary condenser 68 on the cooling room 65 top top boards, cooling room 65 bottoms are shrunk to turbination, its lower end connects liquid discharge pipe 66, a tubing is installed on cylindrical cooling chamber's 65 lower sides to be communicated with liquid pump 11, liquid pump 11 is connected with single-hole nozzle 63, cooling room 65 inside are by being equipped with the metal cools dish, and water coolant flows in the coolship.
The tetrad production art and the device of circulating fluidization carbonic solid fuels provided by the invention, fast pyrogenation reaction, fast quench and circulating fluidized bed combustion are organically combined, realized the pyrolysis of fuel elder generation, the semicoke afterfire, with solid fuel at normal pressure, need not to change into oil fuel, combustion gas, heat energy under the condition of catalyzer and extraneous hydrogen supply.
Its characteristics are as follows:
1. its granularity of the solid fuel of Cai Yonging is the 0.03-0.3 millimeter, experiment and calculating show, under certain external heat transfer condition, the particulate heat-up rate is subjected to the obvious influence of particle diameter, the technology of more aforementioned coproducing oil products, pyrolytic external heat transfer condition is relatively poor, and adopt the solids of greater particle size again, be subjected to the control of transmittance process, finishing the required time of pyrolysis may reach 10～30 minutes, causes the condition that can not satisfy fast pyrogenation, causes liquid oil product output not high, second-rate, even influence the continuous operation of equipment;
2. fast pyrolysis reactor of the present invention is mainly by mixing tank, quick down pipe, gas-solid separator constitute admittedly, under normal pressure, can realize the rapid heating of raw material, reach the heating rate of 1000～5000 ℃ of per seconds, heating up in less than 1 second time reaches 450～700 ℃, simultaneously gas-phase product the residence time in the reactor less than 1.5 seconds about:
3. in technology of the present invention, pyrolysis institute produce oil gas is usually less than below 1 second the time internal cooling to 30 ℃;
4. the major equipment of realizing technology of the present invention have mixing tank admittedly, fast the solid material valve of down pipe, gas-solid separator, rapid condensation device, fast fluidized bed burner and Control Circulation multiplying power and efflux of solids to returning charge U valve.The constitutional features of these equipment is as follows:
1.. the solid mixing tank of tachy steroling soon is a visual plant of realizing the carbonaceous material fast pyrogenation.Powdery carbonaceous solids raw material is sneaked into solid thermal carriers (cycling hot ash) fast, and make it instantaneous cracking;
Fig. 2 and Fig. 3 show the structural representation of two kinds of solid mixing tanks of tachy steroling soon respectively, and their common feature is the technology that all adopts strength control, do not have machinery sealing or whipping appts;
As shown in Figure 2, in cylindrical vessel,, reach the purpose of powdery carbonaceous solids raw material and hot grey short mix by the stirring action of the swirling eddy of coming in from peripheral jet.Mixed fuel and heat ash transfer to quick down pipe 4 with gas by blanking pipe 25;
As shown in Figure 3, the carbonaceous solids raw material is directly sprayed in the dense-phase fluidization bed 27, hot ash also enters in the concentrated phase sulfuration bed 27, and heat ash and powder fluidized gas fluidisation are Gu solid mixture transfers to quick down pipe 4 by blanking pipe 25;
2.. the present invention proposes a kind of down pipe of circular section, as the conversion zone of finishing fast pyrogenation, reaches the solid fuel of about 600 ℃ of temperature of reaction through mixing, and the residence time through about 1 second is finished fast pyrogenation by down pipe.Because the gas-solid turbulence is strong in the down pipe, rate of mass transfer is fast, and gas-solid two phase concentration radial distribution are even, and the back-mixing degree is little, makes the residence time distribution of fuel pellet and gas-phase product approach piston flow, is unlikely to generate too much heavy tar series products;
3.. the invention provides the quick gas-solid separating device 5 of a kind of low pressure drop, short residence time(SRT), as shown in Figure 4, rely on the dual pushing effect of self gravitation and gas differential pressure to enter a kind of nozzle 52 of internal diameter convergent from the effusive gas-solid two-phase mixture of quick down pipe, solid jet flow after process is quickened is thrown to the arc separator 53 (radian is 60-90 °) in downstream, owing to gas, solid two alternate inertia differences reach isolating purpose.Carried secretly by exit flow once more under the effect of air-flow drag force for preventing the solids that eject from the arc blade face, be provided with flow deflector 54 along the separator inwall, this structure has improved gas, solid primary separation effect effectively, can reduce the gas-solid in exit and disturb, and prevents the particle re-entrainment.The solid particulate semicoke that separates slips into down in the standpipe 55 that connects along flow deflector 54.Isolated oil gas leads to condenser rapidly through escape pipe 56;
4.. the invention provides the directly reverse spray type rapid condensation device 6 of contact of a kind of gas-liquid, as shown in Figure 5, through overcooled circulating liquid (liquid phase that this technology produces or with the mixture of certain suitable liquid solvent), from being installed in 63 li upwards ejections at a high speed of single-hole nozzle that reverse jet tube 62 is transferred, with the reverse collision of oil gas that comes from separator, violent turbulence makes the condensable gas quenching of heat become liquid, flow into 65 li of cooling rooms downwards, because the effect of cool metal wall internal cooling heat transfer water, circulating liquid is cooled to below 30 ℃ with the new liquid that produces, partially liq is extracted out from water cooler as elementary oil plant, send downstream processing, partially liq sprays into reverse jet tube 62 again through liquid pump 11 pressurizations, so circulation.The entrained steam that is not condensed in the condenser enters secondary condenser 68 (with frozen water refrigerative dividing wall type cooling tower) and continues cooling, and liquid returns cooling room, does not coagulate dry gas and exports as combustion gas;
5.. the present invention utilizes circular fluid bed 8 as quick coal-char combustion device, extracts heat energy and 600 ℃ of left and right sides solid thermal carriers are heated to about 850 ℃.The present invention uses the flow rate of high-temp solid material valve 3 Control Circulation heat ash in the reinforced rate of 6～10 times solid fuel.The present invention also uses returning charge U type valve 7 to make that semicoke and solid thermal carriers flow to fluidized bed combustor 8 in the concentrated phase mode from quick gas-solid separator 5 after the pyrolysis, realizes the safe separating of pyrolysis air-flow and combustion gas flowing.
Further describe the present invention below in conjunction with drawings and Examples:
Accompanying drawing 1 is a structural representation of the present invention;
Accompanying drawing 2 is a structural representation of consolidating mixing tank 2;
Accompanying drawing 3 is a structural representation of consolidating mixing tank 2;
Accompanying drawing 4 is the structural representation of gas-solid separator 5;
Accompanying drawing 5 is the structural representation of rapid condensation device 6;
Wherein: admittedly consolidate mixing tank 2 inlet pipe 21 circular cylindrical cavities 221
Material valve outlet port pipe 24 blanking pipes 25 air compartments 26
Concentrated phase fluidized-bed 27 inlet pipe 28 distributors 29
Quick down pipe 4 quick gas-solid separator 5 nozzles 52
Separate 53 flow deflectors, 54 pipes 55
Single-hole nozzle 63 cooling rooms 65 liquid discharge pipes 66
Adjustable solid material valve 3 feeders 1 smoke separator 9
Deposit grey hopper 10 liquid pumps 11 condenser inlet pipe 64
Cylinder barrel shaped cavity 59 feed-pipes 23
Embodiment 1, the tetrad production art of the hydrocarbon solid fuel of a kind of circulating fluidization (Datong District's coal):
Fig. 1 is for realizing the device of the hydrocarbon solid fuel of circulating fluidization (Datong District's coal) tetrad production art, and its step is as follows:
With volatile content is 24.6%, Datong District's coal of water content 2.3% is crushed to the 0.03-0.3 millimeter, be added to overflow type gas control feeder 1, in feeder 1 exit, coal dust is tangentially sent into the mixing tank 2 admittedly of an atmospheric operation with carrier gas, this is the structure employing structure shown in Figure 2 of mixing tank 2 admittedly, in mixing tank 2 admittedly coal dust with mix rapidly by about 850 ℃-900 ℃ heat of solid material valve 3 is grey from circular fluid bed, heat exchange, its heat ash amount is 10 times of coal dust amount, coal dust is heated to that (its heating rate is 1000 ℃ of per seconds about 600 ℃-650 ℃,), can regulate degree of mixing by changing carrier gas flux; Afterwards, the mixture of coal dust and heat ash enters quick down pipe 4, leaning on gravity descending in the down pipe 4 fast, limit descending limit pyrolysis, its temperature is that coal dust generation fast pyrogenation is separated out volatile matter about 600 ℃-650 ℃, entered the mouth control of export gas mean residence time about 1 second from down pipe, and the gas-solid mixture when pyrolysis is finished is sent into gas-solid separator 5; Gas-solid mixture separates rapidly in gas-solid separator 5, disengaging time is 0.02-0.2 second, isolated about 550 ℃ gaseous product enters rapid condensation device 6, and about 20 ℃ the circulating liquid of being made from liquid pump 11 is cooled to obtain tar, pyrolysis water and coal gas about 30 ℃; Pyrogenous origin semicoke and circulating ash enter circulating fluidized bed combustion device 8 through returning charge U type valve 7, semicoke air combustion, 850～900 ℃ of controlled temperature; Circulating ash after the heating falls into after smoke separator 9 (present embodiment adopts the efficient cyclone smoke separator) separates and deposits grey hopper 10, and flowing into admittedly through solid material valve 3 again, mixing tank 2 uses with dry coal powder mixed cycle; Hot flue gas heating water generates steam after separate on burner 8 tops; In this embodiment, the main component of the dry gas of acquisition is hydrogen, methane, carbon monoxide, carbonic acid gas, ethane, ethene and propylene; Productive rate is about 10%, caloric power of gas 20MJ/Nm
3About, oil yield rate is about 7%, and pyrolysis of coal devolatilization degree is about 70%.
Fig. 1 produces device for the present invention realizes the hydrocarbon solid-fuelled tetrad of circulating fluidization of the hydrocarbon solid-fuelled tetrad production art of circulating fluidization;
With the corn stalk powder is raw material, use the reinforced rate of screw feeder control instead, corn stalk powder is carried adding mixing tank 2 admittedly by feed-pipe 23 usefulness carrier gas, in mixing tank 2 admittedly straw powder with mix rapidly from about 800 ℃ the thermal cyclic carrier sand of circular fluid bed by solid material valve, be heated to about 460-520 ℃ (heating rate be 2500 ℃ of per seconds or 5000 ℃), send into quick down pipe 4, the weight part proportioning when straw powder is mixed with thermal barrier sand is 1: 6 (also can be 1: 8);
Mixture is descending by gravity in down pipe, the pyrolysis of biomass takes place in descending limit, limit, outlet by quick down pipe 4 subsequently is admitted to realization gas solid separation in the gas-solid separator 5 (present embodiment is an inertial separator), disengaging time is 0.2 second, isolated about 450 ℃ gaseous product enters condenser 6, can coagulate component and generate pyrolysis oil and pyrolysis water, noncondensable gas is exported as combustion gas; Pyrogenous origin semicoke and thermal barrier sand enter fast fluidized bed burner 8 by U type valve 7, use air combustion, 800～850 ℃ of controlled temperature, thermal barrier after the heating falls into hot ash bucket 10 after gas solid separation, enter admittedly through solid material valve 3 that mixing tank 2 mixes with straw powder again, realized circulating fluidization pyrolysis and burning.The isolated hot flue gas in burning back is used for taking place steam.In this embodiment, obtaining gas yield is about 24%, caloric power of gas 12MJ/Nm
3About, liquid yield about 55%, char yeild about 20%, hot obvious heat of smoke reclaims the back and produces steam.
The hydrocarbon solid-fuelled tetrad of circulating fluidization provided by the invention produces the embodiment of device, see shown in Fig. 1-5, as seen from the figure, the hydrocarbon solid-fuelled tetrad of this circulating fluidization produces device, comprise admittedly mixing tank 2, adjustable solid material valve 3, fast down pipe 4, fast gas-solid separator 5, rapid condensation device 6, fast fluidized bed burner 8 and powder feed device 1, smoke separator 9, deposit grey hopper 10 and returning charge U valve 7;
According to circulating path, these parts ordering from top to bottom are: smoke separator 9 is positioned at the top, its underpart connects deposits grey hopper 10, the lower end of depositing grey hopper 10 connects adjustable solid material valve 3, adjustable solid material valve 3 connects mixing tank 2 admittedly, admittedly Gu the side of mixing tank 2 is installed feeder 1, admittedly Gu the lower end of mixing tank 2 connects quick down pipe 4, down pipe 4 lower ends connect quick gas-solid separator 5 fast, the side of gas-solid separator 5 connects fast quench device 6 fast, the lower end of gas-solid separator 5 connects returning charge U valve 7 fast, and the drainage conduit of returning charge U valve 7 connects the lower end of fast fluidized bed burner 8, and fast fluidized bed burner 8 upper ends link to each other with smoke separator 9;
Gu admittedly the structure of mixing tank 2 has two kinds of structure formations.One is: admittedly mixing tank 2 comprises a cavity admittedly, its top is cylinder barrel shaped cavity 221, the bottom is a turbination cavity 222, the upper end of this cavity is connected with the material valve outlet port pipe 24 of solid material valve 3, a conical distributor 29 is installed on cylinder barrel shaped cavity 221 upper cavity inner axes lines, conical cavity 222 bottoms are shrunk to pipe 25 and are connected with quick down pipe 4, the inlet pipe 21 that vertical central lines tangentially is blown into is installed on the cylinder wall of cylinder barrel shaped cavity 221, and what embodiment 1 used is the mixing tank admittedly of this structure; It two is: admittedly mixing tank 2 comprises a cavity admittedly, its top is cylinder barrel shaped cavity 221, the bottom is a cylinder barrel shaped concentrated phase fluidized-bed 27, the sidewall of the air compartment 26 of the grid distributor below of cylinder barrel shaped concentrated phase fluidized-bed 27 is provided with inlet pipe 28, the tremie pipe 25 of concentrated phase fluidized-bed 27 is connected with quick down pipe 4, and what embodiment 2 used is the mixing tank admittedly of this structure;
Described quick down pipe 4 is the circular section long tube of a vertical installation, and its upper end is connected with the outlet of consolidating mixing tank 2, and its lower end is communicated with the inlet tube of quick gas-solid separator 5;
Described quick gas-solid separator 5 comprises a cylinder barrel shaped cavity 59, a nozzle 52 that inwardly shrinks is installed in its center, top, nozzle 52 is connected with quick down pipe 4 outlets, arc surfaced cone shape separator 53 (its cambered surface radian is 60-90 °) are installed at the middle part of cylinder barrel shaped cavity 59 axis, be respectively equipped with two cambered surface flow deflectors 54 (its cambered surface radian is 60-90 °) that cambered surface intersects on the cylinder barrel shaped cavity 59 both sides inner-wall surfaces, the height of its intersecting lens in the center of gravity of separator 53 between the bottom surface, cylinder barrel shaped cavity 59 bottoms are shrunk to inverted cone, and be connected with the standpipe 55 of returning charge U-shaped valve 7 inlet, the top of cylinder barrel shaped cavity 59 is connected with the inlet pipe 64 of rapid condensation device 6 near the escape pipe of installing on the vertical sidewall 56;
The reverse jet tube 62 of described rapid condensation device 6 is a cylindrical blank pipe, perforate communicates with the escape pipe 56 of gas-solid separator 5 on the reverse jet tube 62 vertical sidewalls, its underpart is vertical to be installed on the top cover of cylindrical cooling chamber 65, and communicate with cylinder item cooling room 65, single-hole nozzle 63 is vertical to be installed on the axis of reverse jet tube 62 bottoms, open the inlet pipe 64 that a circular hole is communicated with secondary condenser 68 on the cooling room 65 top top boards, cooling room 65 bottoms are shrunk to turbination, its lower end connects liquid discharge pipe 66, a tubing is installed on cylindrical cooling chamber's 65 lower sides to be communicated with liquid pump 11, liquid pump 11 is connected with single-hole nozzle 63, cooling room 65 inside are by being equipped with the metal cools dish, and water coolant flows in the coolship.
Claims (5)
1. hydrocarbon solid-fuelled tetrad production art of circulating fluidization, its processing step is as follows:
1) will contain hydrocarbon solid fuel through pulverizing, screening powdering material, and after carrying out drying treatment, send into a non-pressurized mixing tank admittedly, in mixing tank admittedly, pulverulent material mixes intensification simultaneously rapidly with heat ash from circular fluid bed, afterwards, be admitted to a quick down pipe;
2) pulverulent material with from the mixture of the heat ash of circular fluid bed in down pipe fast, limit descending limit pyrolysis; The descending time by quick down pipe of mixture is 0.5-1.5 second, separates out volatilizable branch during pyrolysis, when pyrolysis is finished gas-solid mixture is sent into quick gas-solid separator;
3) sharp separation gas-solid mixture in quick gas-solid separator, disengaging time is 0.02-0.2 second, a rapid condensation device is sent in isolated oil gas and combustion gas rapidly, and the 0.1-1 time internal cooling to 0 of second～30 ℃, uncondensable gas phase fuel gas product is collected after the condenser cooling; The cold circulating liquid rapid cooling transformation of condensable oil gas in the rapid condensation device becomes the liquid phase oil product to be collected; Isolated solid phase semicoke and cycling hot ash continue descending, send into the bottom of rapid circulating fluidized bed boiler by a solid returning charge mechanism, in the rapid circulating fluidized bed boiler, semicoke and air fully burn with heat supply, heat-transfer surface in the boiler absorbs heat and produces steam, but draws not only heat supply but also can generate electricity of steam;
Cycling hot ash after burning heats up is entrained to furnace roof by the rising flue gas, carry out gas solid separation, hot flue gas is discharged after by the heat-transfer surface absorbing and cooling temperature, the hot ash of collecting of high temperature circulation enters deposits ash bucket, through a high-temp solid material valve, quantitatively add mixing reactor admittedly, participate in circulation again and carry out pyrolysis, burning, obtain oil, gas, heat, electricity, realize that tetrad produces;
The temperature of heat ash is 800～900 ℃ in the described step 1), and pulverulent material and hot grey blended weight part proportioning are 1: 6-1: 10; Pulverulent material in the step 1) is with the blended time is 0.1-1 second rapidly in mixing tank admittedly from the heat ash of circular fluid bed; Described step 2) temperature in the quick down pipe is 400～650 ℃.
2. by the hydrocarbon solid-fuelled tetrad production art of the described circulating fluidization of claim 1, it is characterized in that the granularity of pulverulent material is the 0.03-0.3 millimeter in the described step 1).
3. the hydrocarbon solid-fuelled tetrad of circulating fluidization produces device, it is characterized in that, comprise admittedly mixing tank (2), adjustable solid material valve (3), fast down pipe (4), fast gas-solid separator (5), rapid condensation device (6), fast fluidized bed burner (8) and powder feed device (1), smoke separator (9), deposit grey hopper (10) and returning charge U valve (7);
According to circulating path, these parts ordering from top to bottom are: smoke separator (9) is positioned at the top, its underpart connects deposits grey hopper (10), the lower end of depositing grey hopper (10) connects adjustable solid material valve (3), adjustable solid material valve (3) connects mixing tank (2) admittedly, admittedly Gu the side of mixing tank (2) is installed feeder (1), admittedly Gu the lower end of mixing tank (2) connects quick down pipe (4), down pipe (4) lower end connects quick gas-solid separator (5) fast, the side of gas-solid separator (5) connects rapid condensation device (6) fast, the lower end of gas-solid separator (5) connects returning charge U valve (7) fast, the drainage conduit of returning charge U valve (7) connects the lower end of fast fluidized bed burner (8), and fast fluidized bed burner (8) upper end links to each other with smoke separator (9);
Described mixing tank (2) admittedly comprises a cavity, its top is cylinder barrel shaped cavity (221), the bottom is turbination cavity (222) or cylinder barrel shaped concentrated phase fluidized-bed (27), the upper end of this cavity is connected with the material valve outlet port pipe (24) of solid material valve (3), a conical distributor (29) is installed on top cylinder barrel shaped cavity (221) cavity inner axes line, when the cavity bottom is turbination cavity (222), conical cavity (222) bottom is shrunk to blanking pipe (25) and is connected with quick down pipe (4), and the inlet pipe (21) that vertical central lines tangentially is blown into is installed on the cylinder wall of top cylinder barrel shaped cavity (221); When the cavity bottom was cylinder barrel shaped concentrated phase fluidized-bed (27), the sidewall of the air compartment (26) of its grid distributor below was provided with inlet pipe (28), and the blanking pipe (25) of concentrated phase fluidized-bed (27) is connected with quick down pipe (4);
Described quick down pipe (4) is the circular section long tube of a vertical installation, and its upper end is connected with the outlet of consolidating mixing tank (2), and its lower end is communicated with the inlet tube of quick gas-solid separator (5);
Described quick gas-solid separator (5) comprises a cylinder barrel shaped cavity (59), a nozzle (52) that inwardly shrinks is installed in its center, top, nozzle (52) is connected with quick down pipe (4) outlet, arc surfaced cone shape separator (53) is installed at middle part at cylinder barrel shaped cavity (59) axis, be respectively equipped with two cambered surface flow deflectors (54) that cambered surface intersects on the inner-wall surface of cylinder barrel shaped cavity (59) both sides, the height of its intersecting lens in the center of gravity of separator (53) between the bottom surface, cylinder barrel shaped cavity (59) bottom is shrunk to inverted cone, and be connected with the standpipe (55) of returning charge U-shaped valve (7) inlet, the top of cylinder barrel shaped cavity (59) is connected with the inlet pipe (64) of fast quench device (6) near the escape pipe of installing on the vertical sidewall (56);
The reverse jet tube (62) of described rapid condensation device (6) is a cylindrical blank pipe, perforate communicates with the escape pipe (56) of gas-solid separator (5) on the vertical sidewall of reverse jet tube (62), its underpart is vertical to be installed on the top cover of cylindrical cooling chamber (65), and communicate with cylindrical cooling chamber (65), a single-hole nozzle (63) is vertical to be installed on the axis of reverse jet tube (62) bottom, open the inlet pipe (64) that a circular hole is communicated with secondary condenser (68) on the top board of cooling room (65) top, cooling room (65) bottom is shrunk to turbination, its lower end connects liquid discharge pipe (66), a tubing is installed on cylindrical cooling chamber (65) lower sides to be communicated with liquid pump (11), liquid pump (11) is connected with single-hole nozzle (63), cooling room (65) inside is equipped with the metal cools dish, and water coolant flows in the coolship.
4. produce device by the hydrocarbon solid-fuelled tetrad of the described circulating fluidization of claim 1, it is characterized in that the cambered surface radian of described arc surfaced cone shape separator (53) is 60-90 °.
5. produce device by the hydrocarbon solid-fuelled tetrad of the described circulating fluidization of claim 1, it is characterized in that the cambered surface radian of described pair of cambered surface flow deflector (54) is 60-90 °.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01110152 CN1240810C (en) | 2001-03-30 | 2001-03-30 | Four coproduction process and equipment for circular fluiding carbon-hydrogen solid fuel |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN 01110152 CN1240810C (en) | 2001-03-30 | 2001-03-30 | Four coproduction process and equipment for circular fluiding carbon-hydrogen solid fuel |
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| CN1377938A CN1377938A (en) | 2002-11-06 |
| CN1240810C true CN1240810C (en) | 2006-02-08 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 01110152 Expired - Lifetime CN1240810C (en) | 2001-03-30 | 2001-03-30 | Four coproduction process and equipment for circular fluiding carbon-hydrogen solid fuel |
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Families Citing this family (16)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1318796C (en) * | 2004-07-26 | 2007-05-30 | 中国科学院工程热物理研究所 | Method for producing both gas and steam, and boiler of circulating fluid bed with pyrolysis vaporizer |
| EP3252128B1 (en) | 2006-04-03 | 2019-01-02 | Pharmatherm Chemicals Inc. | Thermal extraction method for producing a taxane extract |
| US7905990B2 (en) * | 2007-11-20 | 2011-03-15 | Ensyn Renewables, Inc. | Rapid thermal conversion of biomass |
| US20110284359A1 (en) | 2010-05-20 | 2011-11-24 | Uop Llc | Processes for controlling afterburn in a reheater and for controlling loss of entrained solid particles in combustion product flue gas |
| US8499702B2 (en) | 2010-07-15 | 2013-08-06 | Ensyn Renewables, Inc. | Char-handling processes in a pyrolysis system |
| US9441887B2 (en) | 2011-02-22 | 2016-09-13 | Ensyn Renewables, Inc. | Heat removal and recovery in biomass pyrolysis |
| US9347005B2 (en) | 2011-09-13 | 2016-05-24 | Ensyn Renewables, Inc. | Methods and apparatuses for rapid thermal processing of carbonaceous material |
| US10041667B2 (en) | 2011-09-22 | 2018-08-07 | Ensyn Renewables, Inc. | Apparatuses for controlling heat for rapid thermal processing of carbonaceous material and methods for the same |
| US9044727B2 (en) | 2011-09-22 | 2015-06-02 | Ensyn Renewables, Inc. | Apparatuses and methods for controlling heat for rapid thermal processing of carbonaceous material |
| US10400175B2 (en) | 2011-09-22 | 2019-09-03 | Ensyn Renewables, Inc. | Apparatuses and methods for controlling heat for rapid thermal processing of carbonaceous material |
| US9109177B2 (en) | 2011-12-12 | 2015-08-18 | Ensyn Renewables, Inc. | Systems and methods for renewable fuel |
| US9670413B2 (en) | 2012-06-28 | 2017-06-06 | Ensyn Renewables, Inc. | Methods and apparatuses for thermally converting biomass |
| WO2014210150A1 (en) | 2013-06-26 | 2014-12-31 | Ensyn Renewables, Inc. | Systems and methods for renewable fuel |
| US10337726B2 (en) | 2015-08-21 | 2019-07-02 | Ensyn Renewables, Inc. | Liquid biomass heating system |
| MY193949A (en) | 2016-12-29 | 2022-11-02 | Ensyn Renewables Inc | Demetallization Of Liquid Biomass |
| CN109401788B (en) * | 2017-08-17 | 2020-07-03 | 中国石油化工股份有限公司 | Combined fluidized bed reaction device and reaction method for catalytic gasification coupled pyrolysis |
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