CN108504394A - It is catalyzed pyrolysis-gasification integrated reacting device and method - Google Patents
It is catalyzed pyrolysis-gasification integrated reacting device and method Download PDFInfo
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- CN108504394A CN108504394A CN201710099832.7A CN201710099832A CN108504394A CN 108504394 A CN108504394 A CN 108504394A CN 201710099832 A CN201710099832 A CN 201710099832A CN 108504394 A CN108504394 A CN 108504394A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/02—Multi-step carbonising or coking processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
Abstract
The present invention relates to a kind of catalytic pyrolysis gasification integrated reacting device and method, solves the problems, such as existing gasification technology there are reaction temperatures that high, flow rate is low, makes a low multiple use.The present invention is mainly by conical fluidized bed, efficient cyclone device, the quick response proportioning valve of shock chamber and tape control unit forms, signal generator controls quick response proportioning valve and generates dither air-flow, the carbonic solid fuels of different-grain diameter are made to be rapidly achieved in conical fluidized bed in the thin layer distributed of the thick top particle of bottom particles, it burns in conical fluidized bed bottom, middle and upper part carries out catalytic gasification and pyrolysis, fine grained continues that pyrolytic reaction occurs in efficient cyclone device, synthesis gas is carried out in shock chamber, the separation of tar and lime-ash, obtain the technical solution of high heating value synthesis gas and high-quality tar, it can be applied to derived energy chemical field.
Description
Technical field
The present invention relates to a kind of carbonic solid fuels to be catalyzed pyrolysis-gasification integrated reacting device and method, belongs to the energy
Chemical field.
Background technology
The low-order coals rich reserves such as China's lignite, and producing level is gradually increased, since low-order coal volatile matter is high, moisture
Height, calorific value are low, therefore unsuitable long-distance transportation, can only generally be consumed in locality.In addition, biomass and part carbonaceous solids waste material
Fugitive constituent it is also higher.If being used for direct combustion power generation, serious environmental pollution and a large amount of greenhouse gas emissions can be caused, and
Generating efficiency is low, and comprehensive resource utilization rate is relatively low.By classified utilization by the organic matter volatile matter in above-mentioned carbonic solid fuels
It is efficiently separated with fixed carbon, carries out comprehensive processing and utilization, obtained the chemicals of tar, synthesis gas and high added value, meet China
The strategic importance of energy diversification has very strong competitiveness.
The gasification temperature of the gasification process of current comparative maturity is generally at 1000 DEG C or more, and there is reaction temperature height, energy
The shortcomings of consumption is big, difficult to the purification of synthesis gas, synthesis gas intensity of cooling is big and equipment requirement is stringent.As chemical industry goes out
What version society published for 2010《Coal gasification》Air-flow bed technique (such as Texaco, Shell, OMB) described in page 26~45,
Have many advantages, such as that vaporization ability is big, carbon conversion efficiency is high, be current advanced Coal Gasification Technology, development is very fast in recent years, but reacts
Temperature is high, energy consumption is big, coal comprehensive utilization ratio is relatively low, and is also deposited in colms such as applicable high moisture content, ash-rich, high ash melting points
In problems.
Catalytic gasification can reduce reaction temperature while not influencing reaction rate, reduce energy consumption and equipment requirement,
Desulfuration in furnace, dedusting can be achieved, be conducive to environmental protection.On the other hand, since gasification temperature reduces, so as to effectively have adjusted outlet
The composition of gaseous product is distributed, to H in synthesis gas2And CH4The selectivity of product is more preferable, can be carried out at the same time many building-up processes.With
It is compared than conventional pyrolysis, the tar that catalysis pyrolysis acquires, yield higher, quality are more preferable.
Invention content
Present invention mainly solves the technical issues of one of be existing gasification technology there are reaction temperatures high, flow rate
It is low, comprehensive utilization ratio is relatively low, the present invention proposes a kind of carbonic solid fuels catalysis integrated reaction unit of pyrolysis-gasification,
It will be pyrolyzed and gasification reaction efficient coupling is in a reactor, and realize high-effective classifying utilization, reduce reaction temperature, improve
Flow rate, while obtaining more and quality better tar and high added value chemicals.
The technical problems to be solved by the invention two are to provide a kind of catalysis pyrolysis-corresponding with one of technical problem is solved
Gasify integrated reacting method.
One of to solve above-mentioned technical problem, the technical solution adopted by the present invention is as follows：A kind of catalysis pyrolysis-gasification one
Change reaction unit, including conical fluidized bed, material inlet pipe, gas distributor, gasification agent inlet pipe, oxidant inlet pipe, gas
Body distributing chamber, center scum pipe, quick response proportioning valve, solenoid valve, outlet elbow, efficient cyclone device, returning charge valve, Quench
Room, spray thrower, synthesis gas distributor, deduster；
The material inlet pipe is located at conical fluidized bed middle and lower part, and gas distributor and gas distributing chamber are located at taper fluidisation
Bed bottom, gasification agent inlet pipe are connected with gas distributing chamber, and quick response proportioning valve I is mounted in gasification agent inlet pipe, in
Heart scum pipe is connected with gas distributor, and oxidant inlet tube inlet pipe is connected with center scum pipe, quick response ratio
Valve II is mounted in oxidant inlet pipe, and efficient cyclone device is connected by outlet elbow with conical fluidized bed, and returning charge valve connects
It is connected between efficient cyclone device and conical fluidized bed, spray thrower is housed at the top of shock chamber, inside is equipped with synthesis gas distributor, closes
It is connected with efficient cyclone device at gas distributor, deduster is connected with shock chamber.
The conical fluidized bed upper end diameter is 2~8 times of lower end diameter, and preferred scope is 4~6 times, due to difference
Gas flow rate on section is different, and it is in that the thick top particle of bottom particles is thin in the conical fluidized bed that can make carbonic solid fuels
Layer distributed achievees the purpose that layering catalysis pyrolysis-gasification to optimize residence time of the variable grain in the fluid bed,
Improve the efficiency of carbon con version of carbonic solid fuels.
The gas distributor is located at conical fluidized bed bottom, and the conical opening angle of gas distributor is 30 °~150 °,
It is preferred that 60 °~120 °, the gas distributor conical surface is equipped with stomata, is equipped with 5~40 circles, percent opening 1~10%, stomata is circumferentially equal
Even arrangement often encloses hole diameter along distributor radially increase, and the stomata close to center scum pipe is minimum, and minimum stomata is 0.5~
1mm, maximum stomata are 2~10mm, using the particle being so designed with conducive to different thicknesses in conical fluidized bed layer distributed,
Strengthen gas-solid mixing, is also beneficial to the discharge of lime-ash.
The response time of the quick response proportioning valve I and quick response proportioning valve II is less than 5 milliseconds, to make ratio
Valve can rapidly change aperture according to the signal that signal generator generates, and generate pulse pneumatic.
The efficient cyclone device is equipped with outer barrel and inner cylinder is set there are two cylinder, and a diameter of outer barrel of inner cylinder is straight
0.3~0.8 times of diameter, preferably 0.5~0.7 times；Air slit diameter is 0.2~0.7 times of inner cylinder diameter, preferably 0.4~0.6
Times；Using such design can by coarse granule and fine grained respectively outer tube in respectively be isolated by, have and efficiently detach
Efficiency.
Spray thrower is housed, inside is equipped with synthesis gas distributor, and the spray thrower uses taper at the top of the shock chamber
Design, base diameter are 2~8 times of top diameter, and preferably 4~6 times, bottom bulkhead is equipped with aperture, is equipped with 5~20 circles, trepanning
Rate 1~10%, stomata is circumferentially evenly arranged；It is that top is straight that the synthesis gas distributor, which uses conical design, base diameter,
2~6 times of diameter, preferably 3~5 times increase the contact area of synthesis gas and cooling water using such design, and will not be because of tar
Presence, so that synthesis gas distributor is blocked, improve the separative efficiency of synthesis gas, tar and fine ash.
In order to solve the above problem two, the technical solution adopted by the present invention is as follows：A kind of catalysis pyrolysis-gasification integration is anti-
Induction method, it is characterised in that mainly comprise the following steps, taper is entered by material inlet pipe after carbonic solid fuels and catalyst mixing
In fluid bed, oxidant enters conical fluidized bed by quick response proportioning valve II from oxidant inlet pipe from center scum pipe
In, gasifying agent enters taper after quick response proportioning valve I and gas distributing chamber from gasification agent inlet pipe from gas distributor
In fluid bed, quick response proportioning valve I is controlled by signal generator, dither air-flow is generated, makes different-grain diameter
Carbonic solid fuels be rapidly achieved in conical fluidized bed in the thin layer distributed of the thick top particle of bottom particles, in taper flow
Change bed bottom to burn, middle and upper part carries out catalytic gasification and pyrolysis, and bulky grain lime-ash is discharged from center scum pipe；One generated
Grade synthesis gas and fine-grained mixture enter efficient cyclone device by outlet elbow, and fine grained continues in efficient cyclone device
Pyrolytic reaction occurs, then reaches returning charge valve, is passed through oxidant in returning charge valve bottom, carries out low-temperature burning, finally enter taper
The bottom of fluid bed, the two level synthesis gas at the top of efficient cyclone device out enters shock chamber by synthesis gas distributor, cold
But water enters through spray thrower at the top of shock chamber, and after two level synthesis gas washs separation in shock chamber, ash is discharged in bottom, tar
It is discharged from middle part, three-level synthesis gas is discharged through deduster from top.
The carbonic solid fuels include：Various types of coals, petroleum coke, biomass, carbonaceous solids waste material or its
The high solid waste of mixture, preferably low-order coal, biomass, fugitive constituent or its mixture.
The oxidant refers to air, oxygen, oxygen-enriched air；The gasifying agent refer to vapor, carbon dioxide or
The mixture of itself and oxygen.
The catalyst includes alkali metal, alkaline-earth metal, transition metal or its mixture, and preferred technical solution is
Catalyst includes in potassium carbonate, sodium carbonate, potassium hydroxide, sodium hydroxide, calcium hydroxide, calcium oxide, ferric nitrate or nitric acid molybdenum
At least one；
The catalyst is supported in a manner of infusion process, dry pigmentation or ion-exchange on carbonic solid fuels；Institute
The load capacity for the catalyst stated accounts for the 0.1~30% of carbonic solid fuels quality.
The signal generator includes：The equipment and energy of outputs level signals are controlled by oscillograph, computer software
Various frequencies, the equipment of waveform and output level electric signal are provided.
It is described quick response proportioning valve is controlled by signal generator after generate pulse pneumatic, the waveform of pulse pneumatic can
To be any type of wave, preferably square wave and sine wave, keep control more convenient.
The oxidant generates pulse pneumatic from oxidant inlet pipe by the II controls of quick response proportioning valve, sets center
Scum pipe upper end spout mean flow rate is 1~50m/s, preferably 10-25m/s；In fluidization period, ripple frequency is 0.5~
100Hz, preferably 5~25Hz, pulse amplitude are the 1%~100% of mean flow rate, preferably 10%~50%；In the deslagging stage, root
It is opened and closed according to deslagging situation, it is 0.01~0.1Hz to be preferably opened and closed frequency.
The gasifying agent carries out control to quick response proportioning valve I by signal generator and generates pulse pneumatic, pulsation frequency
Rate is 0.5~100Hz, and preferably 5~25Hz, pulse amplitude is the 0%~100% of mean flow rate, preferably 10%~50%.
The conical fluidized bed bottom interface superficial velocity ranging from 1~30m/s, preferably 5~20m/s.
The conical fluidized bed bottom temp control is 900~1100 DEG C, and middle portion temperature control is 700~900 DEG C, top
Temperature control is 400~700 DEG C, and the carbon ratio control range of conical fluidized bed is 0.5~0.7mol/mol, and steam/hydrocarbons ratio controls model
It encloses for 1~2mol/mol, operating pressure ranging from 0.5~3MPa.
The efficient cyclone unit temp control is 300~700 DEG C.
The returning charge valve temperature control is 400~800 DEG C, and carbon ratio control range is 0.6~0.8mol/mol.
Technical solution using the present invention is carried out by being catalyzed pyrolysis-gasification integrated reacting in conical fluidized bed bottom
Burning, middle and upper part carry out catalytic gasification and pyrolysis, and fine grained continues that pyrolytic reaction occurs in efficient cyclone device, is closed
At gas and tar.Realize carbonic solid fuels high-effective classifying utilize, reduce reaction temperature, improve flow rate with
And the yield and quality of tar, it has a good application prospect.
Description of the drawings
1, Fig. 1 is the flow diagram for being catalyzed pyrolysis-gasification integrated reacting device：
In Fig. 1,1 is conical fluidized bed；2 be material inlet pipe；3 be gas distributor；4 be gasification agent inlet pipe；5 be oxygen
Agent inlet tube；6 be gas distributing chamber；Scum pipe centered on 7；8 (a) is quick response proportioning valve I, 8 (b) is quick response ratio
Example valve II；9 (a), 9 (b), 9 (c), 9 (d), 9 (e) are quick response solenoid valve；10 be outlet elbow；11 fill for efficient cyclone
It sets；11 (a) is the outer barrel of efficient cyclone device；11 (b) is the inner cylinder of efficient cyclone device；12 be returning charge valve；13 be sharp
Cold house；14 be synthesis gas distributor；15 be spray thrower；16 be deduster.
A is carbonic solid fuels；B is catalyst；C is gasifying agent；D is oxidant；E is bulky grain lime-ash；F closes for level-one
At gas and fine-grained mixture；G is oxidant；H is two level synthesis gas；I is cooling water；J is tar；K is ash；L closes for three-level
At gas.
Entered in conical fluidized bed (1) by material inlet pipe (2) after carbonic solid fuels A and catalyst B mixing, oxidation
Agent D enters conical fluidized bed (1) by quick response proportioning valve II (8b) from oxidant inlet pipe (5) from center scum pipe (7)
In, gasifying agent C is distributed after quick response proportioning valve I (8a) and gas distributing chamber (6) from gas from gasification agent inlet pipe (4)
Device (3) enters in conical fluidized bed (1), is controlled quick response proportioning valve I (8a) by signal generator, generates high frequency
Pulse pneumatic makes the carbonic solid fuels A of different-grain diameter be rapidly achieved in the thick top of bottom particles in conical fluidized bed (1)
The thin layer distributed of grain, burns in conical fluidized bed (1) bottom, and middle and upper part carries out catalytic gasification and pyrolysis, bulky grain ash
Slag E is discharged from center scum pipe (7)；The level-one synthesis gas and fine-grained mixture F of generation enter high by outlet elbow (10)
Cyclone (11) is imitated, fine grained gives birth to pyrolytic reaction in efficient cyclone device (11) relaying supervention, then reaches returning charge valve (12),
It is passed through oxidant G in returning charge valve (12) bottom, low-temperature burning is carried out, the bottom of conical fluidized bed (1) is finally entered, from efficient rotary
Two level synthesis gas H at the top of wind apparatus (11) out enters shock chamber (13) by synthesis gas distributor (14), and cooling water I is through spray
It drenches device (15) at the top of shock chamber (13) to enter, in shock chamber (13) after washing separation, grey K is arranged two level synthesis gas H in bottom
Go out, tar J is discharged from middle part, and three-level synthesis gas L is discharged through deduster (16) from top.
The present invention will be further described below by way of examples, but is not limited only to the present embodiment.
Specific implementation mode
【Embodiment 1】
A kind of catalysis pyrolysis-gasification integrated reacting device, conical fluidized bed bottom diameter are 0.5m, upper end maximum inner diameter
It is highly 5m for 1m, barrel diameter ratio is 0.6 inside and outside efficient cyclone device.
The lignite of 0-10mm and 10% potassium carbonate mixing after entered in conical fluidized bed by material inlet pipe, oxidant from
Oxidant inlet pipe enters from center scum pipe in conical fluidized bed by quick response proportioning valve II, and gasifying agent enters from gasifying agent
Mouth pipe enters from gas distributor in conical fluidized bed after quick response proportioning valve I and gas distributing chamber, is sent out by signal
Raw device controls quick response proportioning valve I, generates dither air-flow, makes the lignite of different-grain diameter in conical fluidized bed
It is rapidly achieved in the thin layer distributed of the thick top particle of bottom particles, burns in conical fluidized bed bottom, middle and upper part carries out
Catalytic gasification and pyrolytic reaction, control conical fluidized bed middle portion temperature be about 800 DEG C, conical fluidized bed pressure be 1MPa, big
Grain lime-ash is discharged from center scum pipe；The level-one synthesis gas and fine-grained mixture of generation enter efficient cyclone by outlet elbow
Device, for the control of efficient cyclone unit temp at 500 DEG C or so, fine grained gives birth to pyrolytic reaction in efficient cyclone device relaying supervention,
Then returning charge valve is reached, oxidant is passed through in returning charge valve bottom, carries out low-temperature burning, finally enter the bottom of conical fluidized bed,
Two level synthesis gas at the top of from efficient cyclone device out enters shock chamber by synthesis gas distributor, cooling water through spray thrower from
Enter at the top of shock chamber, after two level synthesis gas washs separation in shock chamber, ash is discharged in bottom, and tar is discharged from middle part, burnt
Oil mass is about into the 8.4% of coal quality, and three-level synthesis gas is discharged through deduster from top, and three-level syngas product carbon monoxide contains
Amount is 23%, hydrogen content 35.3%, carbon dioxide content 2.8%, methane content 8.9%, CnHmContent be
0.9%, coal gas high heating value is 13.6MJ/m3, total efficiency of carbon con version is 96%.
【Embodiment 2】
A kind of catalysis pyrolysis-gasification integrated reacting device, conical fluidized bed bottom diameter are 0.5m, upper end maximum inner diameter
It is highly 5m for 2.5m, barrel diameter ratio is 0.6 inside and outside efficient cyclone device.
The lignite of 0-10mm and 10% potassium carbonate mixing after entered in conical fluidized bed by material inlet pipe, oxidant from
Oxidant inlet pipe enters from center scum pipe in conical fluidized bed by quick response proportioning valve II, and gasifying agent enters from gasifying agent
Mouth pipe enters from gas distributor in conical fluidized bed after quick response proportioning valve I and gas distributing chamber, is sent out by signal
Raw device controls quick response proportioning valve I, generates dither air-flow, makes the lignite of different-grain diameter in conical fluidized bed
It is rapidly achieved in the thin layer distributed of the thick top particle of bottom particles, burns in conical fluidized bed bottom, middle and upper part carries out
Catalytic gasification and pyrolytic reaction, control conical fluidized bed middle portion temperature be about 800 DEG C, conical fluidized bed pressure be 1MPa, big
Grain lime-ash is discharged from center scum pipe；The level-one synthesis gas and fine-grained mixture of generation enter efficient cyclone by outlet elbow
Device, for the control of efficient cyclone unit temp at 500 DEG C or so, fine grained gives birth to pyrolytic reaction in efficient cyclone device relaying supervention,
Then returning charge valve is reached, oxidant is passed through in returning charge valve bottom, carries out low-temperature burning, finally enter the bottom of conical fluidized bed,
Two level synthesis gas at the top of from efficient cyclone device out enters shock chamber by synthesis gas distributor, cooling water through spray thrower from
Enter at the top of shock chamber, after two level synthesis gas washs separation in shock chamber, ash is discharged in bottom, and tar is discharged from middle part, burnt
Oil mass is about into the 12% of coal quality, and three-level synthesis gas is discharged through deduster from top, and three-level syngas product carbon monoxide contains
Amount is 21%, hydrogen content 35.3%, carbon dioxide content 3.5%, methane content 12%, CnHmContent be
2.1%, coal gas high heating value is 15.6MJ/m3, total efficiency of carbon con version is 98%.
【Embodiment 3】
A kind of catalysis pyrolysis-gasification integrated reacting device, conical fluidized bed bottom diameter are 0.5m, upper end maximum inner diameter
It is highly 5m for 4m, barrel diameter ratio is 0.6 inside and outside efficient cyclone device.
The lignite of 0-10mm and 10% potassium carbonate mixing after entered in conical fluidized bed by material inlet pipe, oxidant from
Oxidant inlet pipe enters from center scum pipe in conical fluidized bed by quick response proportioning valve II, and gasifying agent enters from gasifying agent
Mouth pipe enters from gas distributor in conical fluidized bed after quick response proportioning valve I and gas distributing chamber, is sent out by signal
Raw device controls quick response proportioning valve I, generates dither air-flow, makes the lignite of different-grain diameter in conical fluidized bed
It is rapidly achieved in the thin layer distributed of the thick top particle of bottom particles, burns in conical fluidized bed bottom, middle and upper part carries out
Catalytic gasification and pyrolytic reaction, control conical fluidized bed middle portion temperature be about 800 DEG C, conical fluidized bed pressure be 1MPa, big
Grain lime-ash is discharged from center scum pipe；The level-one synthesis gas and fine-grained mixture of generation enter efficient cyclone by outlet elbow
Device, for the control of efficient cyclone unit temp at 500 DEG C or so, fine grained gives birth to pyrolytic reaction in efficient cyclone device relaying supervention,
Then returning charge valve is reached, oxidant is passed through in returning charge valve bottom, carries out low-temperature burning, finally enter the bottom of conical fluidized bed,
Two level synthesis gas at the top of from efficient cyclone device out enters shock chamber by synthesis gas distributor, cooling water through spray thrower from
Enter at the top of shock chamber, after two level synthesis gas washs separation in shock chamber, ash is discharged in bottom, and tar is discharged from middle part, burnt
Oil mass is about into the 8.2% of coal quality, and three-level synthesis gas is discharged through deduster from top, and three-level syngas product carbon monoxide contains
Amount is 25.2%, hydrogen content 41.3%, carbon dioxide content 1.5%, methane content 5.8%, CnHmContent be
0.5%, coal gas high heating value is 11.6MJ/m3, total efficiency of carbon con version is 99%.
【Embodiment 4】
A kind of catalysis pyrolysis-gasification integrated reacting device, conical fluidized bed bottom diameter are 0.5m, upper end maximum inner diameter
It is highly 5m for 2.5m, barrel diameter ratio is 0.3 inside and outside efficient cyclone device.
The lignite of 0-10mm and 10% potassium carbonate mixing after entered in conical fluidized bed by material inlet pipe, oxidant from
Oxidant inlet pipe enters from center scum pipe in conical fluidized bed by quick response proportioning valve II, and gasifying agent enters from gasifying agent
Mouth pipe enters from gas distributor in conical fluidized bed after quick response proportioning valve I and gas distributing chamber, is sent out by signal
Raw device controls quick response proportioning valve I, generates dither air-flow, makes the lignite of different-grain diameter in conical fluidized bed
It is rapidly achieved in the thin layer distributed of the thick top particle of bottom particles, burns in conical fluidized bed bottom, middle and upper part carries out
Catalytic gasification and pyrolytic reaction, control conical fluidized bed middle portion temperature be about 800 DEG C, conical fluidized bed pressure be 1MPa, big
Grain lime-ash is discharged from center scum pipe；The level-one synthesis gas and fine-grained mixture of generation enter efficient cyclone by outlet elbow
Device, for the control of efficient cyclone unit temp at 500 DEG C or so, fine grained gives birth to pyrolytic reaction in efficient cyclone device relaying supervention,
Then returning charge valve is reached, oxidant is passed through in returning charge valve bottom, carries out low-temperature burning, finally enter the bottom of conical fluidized bed,
Two level synthesis gas at the top of from efficient cyclone device out enters shock chamber by synthesis gas distributor, cooling water through spray thrower from
Enter at the top of shock chamber, after two level synthesis gas washs separation in shock chamber, ash is discharged in bottom, and tar is discharged from middle part, burnt
Oil mass is about into the 9.2% of coal quality, and three-level synthesis gas is discharged through deduster from top, and three-level syngas product carbon monoxide contains
Amount is 20.8%, hydrogen content 38.3%, carbon dioxide content 2.5%, methane content 9.2%, CnHmContent be
1.8%, coal gas high heating value is 12.2MJ/m3, total efficiency of carbon con version is 95%.
【Embodiment 5】
A kind of catalysis pyrolysis-gasification integrated reacting device, conical fluidized bed bottom diameter are 0.5m, upper end maximum inner diameter
It is highly 5m for 2.5m, barrel diameter ratio is 0.5 inside and outside efficient cyclone device.
The lignite of 0-10mm and 10% potassium carbonate mixing after entered in conical fluidized bed by material inlet pipe, oxidant from
Oxidant inlet pipe enters from center scum pipe in conical fluidized bed by quick response proportioning valve II, and gasifying agent enters from gasifying agent
Mouth pipe enters from gas distributor in conical fluidized bed after quick response proportioning valve I and gas distributing chamber, is sent out by signal
Raw device controls quick response proportioning valve I, generates dither air-flow, makes the lignite of different-grain diameter in conical fluidized bed
It is rapidly achieved in the thin layer distributed of the thick top particle of bottom particles, burns in conical fluidized bed bottom, middle and upper part carries out
Catalytic gasification and pyrolytic reaction, control conical fluidized bed middle portion temperature be about 800 DEG C, conical fluidized bed pressure be 1MPa, big
Grain lime-ash is discharged from center scum pipe；The level-one synthesis gas and fine-grained mixture of generation enter efficient cyclone by outlet elbow
Device, for the control of efficient cyclone unit temp at 500 DEG C or so, fine grained gives birth to pyrolytic reaction in efficient cyclone device relaying supervention,
Then returning charge valve is reached, oxidant is passed through in returning charge valve bottom, carries out low-temperature burning, finally enter the bottom of conical fluidized bed,
Two level synthesis gas at the top of from efficient cyclone device out enters shock chamber by synthesis gas distributor, cooling water through spray thrower from
Enter at the top of shock chamber, after two level synthesis gas washs separation in shock chamber, ash is discharged in bottom, and tar is discharged from middle part, burnt
Oil mass is about into the 9.6% of coal quality, and three-level synthesis gas is discharged through deduster from top, and three-level syngas product carbon monoxide contains
Amount is 20.2%, hydrogen content 37.2%, carbon dioxide content 2.8%, methane content 10.8%, CnHmContent be
1.4%, coal gas high heating value is 14.4MJ/m3, total efficiency of carbon con version is 98%.
【Embodiment 6】
A kind of catalysis pyrolysis-gasification integrated reacting device, conical fluidized bed bottom diameter are 0.5m, upper end maximum inner diameter
It is highly 5m for 2.5m, barrel diameter ratio is 0.7 inside and outside efficient cyclone device.
The lignite of 0-10mm and 10% potassium carbonate mixing after entered in conical fluidized bed by material inlet pipe, oxidant from
Oxidant inlet pipe enters from center scum pipe in conical fluidized bed by quick response proportioning valve II, and gasifying agent enters from gasifying agent
Mouth pipe enters from gas distributor in conical fluidized bed after quick response proportioning valve I and gas distributing chamber, is sent out by signal
Raw device controls quick response proportioning valve I, generates dither air-flow, makes the lignite of different-grain diameter in conical fluidized bed
It is rapidly achieved in the thin layer distributed of the thick top particle of bottom particles, burns in conical fluidized bed bottom, middle and upper part carries out
Catalytic gasification and pyrolytic reaction, control conical fluidized bed middle portion temperature be about 800 DEG C, conical fluidized bed pressure be 1MPa, big
Grain lime-ash is discharged from center scum pipe；The level-one synthesis gas and fine-grained mixture of generation enter efficient cyclone by outlet elbow
Device, for the control of efficient cyclone unit temp at 500 DEG C or so, fine grained gives birth to pyrolytic reaction in efficient cyclone device relaying supervention,
Then returning charge valve is reached, oxidant is passed through in returning charge valve bottom, carries out low-temperature burning, finally enter the bottom of conical fluidized bed,
Two level synthesis gas at the top of from efficient cyclone device out enters shock chamber by synthesis gas distributor, cooling water through spray thrower from
Enter at the top of shock chamber, after two level synthesis gas washs separation in shock chamber, ash is discharged in bottom, and tar is discharged from middle part, burnt
Oil mass is about into the 10.8% of coal quality, and three-level synthesis gas is discharged through deduster from top, three-level syngas product carbon monoxide
Content is 21.8%, hydrogen content 33.1%, carbon dioxide content 3.1%, methane content 10.6%, CnHmContent
It is 1.8%, coal gas high heating value is 13.8MJ/m3, total efficiency of carbon con version is 97%.
【Embodiment 7】
A kind of catalysis pyrolysis-gasification integrated reacting device, conical fluidized bed bottom diameter are 0.5m, upper end maximum inner diameter
It is highly 5m for 2.5m, barrel diameter ratio is 0.8 inside and outside efficient cyclone device.
The lignite of 0-10mm and 10% potassium carbonate mixing after entered in conical fluidized bed by material inlet pipe, oxidant from
Oxidant inlet pipe enters from center scum pipe in conical fluidized bed by quick response proportioning valve II, and gasifying agent enters from gasifying agent
Mouth pipe enters from gas distributor in conical fluidized bed after quick response proportioning valve I and gas distributing chamber, is sent out by signal
Raw device controls quick response proportioning valve I, generates dither air-flow, makes the lignite of different-grain diameter in conical fluidized bed
It is rapidly achieved in the thin layer distributed of the thick top particle of bottom particles, burns in conical fluidized bed bottom, middle and upper part carries out
Catalytic gasification and pyrolytic reaction, control conical fluidized bed middle portion temperature be about 800 DEG C, conical fluidized bed pressure be 1MPa, big
Grain lime-ash is discharged from center scum pipe；The level-one synthesis gas and fine-grained mixture of generation enter efficient cyclone by outlet elbow
Device, for the control of efficient cyclone unit temp at 500 DEG C or so, fine grained gives birth to pyrolytic reaction in efficient cyclone device relaying supervention,
Then returning charge valve is reached, oxidant is passed through in returning charge valve bottom, carries out low-temperature burning, finally enter the bottom of conical fluidized bed,
Two level synthesis gas at the top of from efficient cyclone device out enters shock chamber by synthesis gas distributor, cooling water through spray thrower from
Enter at the top of shock chamber, after two level synthesis gas washs separation in shock chamber, ash is discharged in bottom, and tar is discharged from middle part, burnt
Oil mass is about into the 9.2% of coal quality, and three-level synthesis gas is discharged through deduster from top, and three-level syngas product carbon monoxide contains
Amount is 27.8%, hydrogen content 33.3%, carbon dioxide content 1.5%, methane content 7.2%, CnHmContent be
0.8%, coal gas high heating value is 11.8MJ/m3, total efficiency of carbon con version is 94%.
【Embodiment 8】
A kind of catalysis pyrolysis-gasification integrated reacting device, conical fluidized bed bottom diameter are 0.5m, upper end maximum inner diameter
It is highly 5m for 2.5m, barrel diameter ratio is 0.6 inside and outside efficient cyclone device.
The lignite of 0-10mm and 10% calcium oxide mixing after entered in conical fluidized bed by material inlet pipe, oxidant from
Oxidant inlet pipe enters from center scum pipe in conical fluidized bed by quick response proportioning valve II, and gasifying agent enters from gasifying agent
Mouth pipe enters from gas distributor in conical fluidized bed after quick response proportioning valve I and gas distributing chamber, is sent out by signal
Raw device controls quick response proportioning valve I, generates dither air-flow, makes the lignite of different-grain diameter in conical fluidized bed
It is rapidly achieved in the thin layer distributed of the thick top particle of bottom particles, burns in conical fluidized bed bottom, middle and upper part carries out
Catalytic gasification and pyrolytic reaction, control conical fluidized bed middle portion temperature be about 800 DEG C, conical fluidized bed pressure be 1MPa, big
Grain lime-ash is discharged from center scum pipe；The level-one synthesis gas and fine-grained mixture of generation enter efficient cyclone by outlet elbow
Device, for the control of efficient cyclone unit temp at 500 DEG C or so, fine grained gives birth to pyrolytic reaction in efficient cyclone device relaying supervention,
Then returning charge valve is reached, oxidant is passed through in returning charge valve bottom, carries out low-temperature burning, finally enter the bottom of conical fluidized bed,
Two level synthesis gas at the top of from efficient cyclone device out enters shock chamber by synthesis gas distributor, cooling water through spray thrower from
Enter at the top of shock chamber, after two level synthesis gas washs separation in shock chamber, ash is discharged in bottom, and tar is discharged from middle part, burnt
Oil mass is about into the 7.4% of coal quality, and three-level synthesis gas is discharged through deduster from top, and three-level syngas product carbon monoxide contains
Amount is 28.1%, hydrogen content 39.3%, carbon dioxide content 0.8%, methane content 5.2%, CnHmContent be
0.4%, coal gas high heating value is 10.6MJ/m3, total efficiency of carbon con version is 98%.
【Comparative example 1】
Using gray melting poly-fluid bed coal gasification reaction device, select the lignite of 0-6mm for raw material, operating pressure 0.04MPa,
1000 DEG C of average operating temperature, it is 21.9% to obtain syngas product carbon monoxide content, hydrogen content 38.6%, methane
4.3%, carbon dioxide content 22%, nitrogen content 7.11%, gas heating value 9.4MJ/m3, efficiency of carbon con version is only 90%.
Embodiment 1-8 and comparative example 1 are summarized as shown in table 1.
Table 1
From the comparison of the technic index of table 1, it can be deduced that, catalysis pyrolysis-gasification integration described in patent of the present invention is anti-
Device is answered, using 2 best results of embodiment, improves nearly 8 percentage points compared with the efficiency of carbon con version of comparative example 1, methane content improves
Nearly 8 percentage points, while calorific value of gas is improved, obtain the tar of high yield.
Claims (10)
1. a kind of catalysis pyrolysis-gasification integrated reacting device, which is characterized in that including conical fluidized bed (1), material inlet pipe
(2), gas distributor (3), gasification agent inlet pipe (4), oxidant inlet pipe (5), gas distributing chamber (6), center scum pipe
(7), quick response proportioning valve, solenoid valve, outlet elbow (10), efficient cyclone device (11), returning charge valve (12), shock chamber
(13), synthesis gas distributor (14), spray thrower (15), deduster (16)；
It is characterized in that material inlet pipe (2) is located at conical fluidized bed (1) middle and lower part, gas distributor (3) and gas distributing chamber
(6) it is located at conical fluidized bed (1) bottom, gasification agent inlet pipe (4) is connected with gas distributing chamber (6), quick response proportioning valve I
(8a) is mounted in gasification agent inlet pipe (4), and center scum pipe (7) is connected with gas distributor (3), oxidant inlet pipe
(5) it is connected with center scum pipe (7), quick response proportioning valve II (8b) is mounted in oxidant inlet pipe (5), efficient cyclone
Device (11) is connected by outlet elbow (10) with conical fluidized bed (1), and returning charge valve (12) is connected to efficient cyclone device
(11) between conical fluidized bed (1), spray thrower (15) is housed at the top of shock chamber (13), inside is equipped with synthesis gas distributor
(14), synthesis gas distributor (14) is connected with efficient cyclone device (11), and deduster (16) is connected with shock chamber (13).
2. catalysis pyrolysis according to claim 1-gasification integrated reacting device, it is characterised in that the taper fluidisation
Bed (1) upper end diameter is 2~8 times of lower end diameter.
3. catalysis pyrolysis according to claim 1-gasification integrated reacting device, it is characterised in that the gas distribution
Device (3) is located at conical fluidized bed (1) bottom, and the conical opening angle of gas distributor (3) is 30 °~150 °, gas distributor (3)
The conical surface is equipped with stomata, is equipped with 5~40 circles, and percent opening 1~10%, stomata is circumferentially evenly arranged, and often encloses hole diameter edge point
Cloth device radially increase, the stomata close to center scum pipe (7) is minimum, and minimum stomata is 0.5~1mm, and maximum stomata is 2~
10mm。
4. catalysis pyrolysis according to claim 1-gasification integrated reacting device, it is characterised in that the quick response
Proportioning valve I (8a), quick response proportioning valve II (8b) response time be less than 5 milliseconds.
5. catalysis pyrolysis according to claim 1-gasification integrated reacting device, it is characterised in that the efficient cyclone
Device (11) be equipped with outer barrel (11a) and inner cylinder (11b), inner cylinder diameter (11b) for outer barrel diameter (11a) 0.3~
0.8 times.
6. catalysis pyrolysis according to claim 1-gasification integrated reacting device, it is characterised in that the shock chamber
(13) top is equipped with spray thrower (15), and inside is equipped with synthesis gas distributor (14), and the spray thrower (15) uses conical design,
Base diameter is 2~8 times of top diameter, and bottom bulkhead is equipped with aperture, is equipped with 5~20 circles, percent opening 1~10%, stomata edge
Even circumferential is arranged；It is 2~6 times of top diameter that the synthesis gas distributor (14), which uses conical design, base diameter,.
7. a kind of catalysis pyrolysis-gasification integrated reacting method, using any catalysis pyrolysis-gas described in claim 1~6
Change integrated reacting device, it is characterised in that mainly comprise the following steps：After carbonic solid fuels A and catalyst B mixing by raw material into
Mouthful pipe (2) enter conical fluidized bed (1) in, oxidant D from oxidant inlet pipe (5) by quick response proportioning valve II (8b) from
Center scum pipe (7) enters in conical fluidized bed (1), and gasifying agent C passes through quick response proportioning valve I from gasification agent inlet pipe (4)
Enter in conical fluidized bed (1) from gas distributor (3) after (8a) and gas distributing chamber (6), by signal generator to quick
Response proportioning valve I (8a) is controlled, and dither air-flow is generated, and the carbonic solid fuels A of different-grain diameter is made to be fluidized in taper
It is rapidly achieved in the thin layer distributed of the thick top particle of bottom particles in bed (1), burns in conical fluidized bed (1) bottom,
Middle and upper part carries out catalytic gasification and pyrolysis, and bulky grain lime-ash E is discharged from center scum pipe (7)；The level-one synthesis gas of generation and thin
Granulate mixture F enters efficient cyclone device (11) by outlet elbow (10), and fine grained is relayed in efficient cyclone device (11)
Supervention gives birth to pyrolytic reaction, then reaches returning charge valve (12), is passed through oxidant G in returning charge valve (12) bottom, carries out low-temperature burning, most
The bottom for entering conical fluidized bed (1) afterwards, from efficient cyclone device (11) top, two level synthesis gas H out, which passes through, synthesizes qi leel
Cloth device (14) enters shock chamber (13), and cooling water I enters through spray thrower (15) at the top of shock chamber (13), and two level synthesis gas H exists
In shock chamber (13) after washing separation, grey K is discharged in bottom, and tar J is discharged from middle part, and three-level synthesis gas L is through deduster (16)
It is discharged from top.
8. catalysis pyrolysis according to claim 7-gasification integrated reacting method, it is characterised in that the gasifying agent C is logical
It crosses signal generator and control generation pulse pneumatic is carried out to quick response proportioning valve I (8a), ripple frequency is 0.5~100Hz, arteries and veins
Dynamic amplitude is the 0%~100% of mean flow rate.
9. catalysis pyrolysis according to claim 7-gasification integrated reacting method, it is characterised in that the oxidant D from
Oxidant inlet pipe (5) generates pulse pneumatic by quick response proportioning valve II (8b) controls, and in fluidization period, ripple frequency is
0.5~100Hz, pulse amplitude are the 1%~100% of mean flow rate；In the deslagging stage, it is opened and closed according to deslagging situation.
10. catalysis pyrolysis according to claim 7-gasification integrated reacting method, it is characterised in that the taper fluidisation
Bed (1) bottom temp control is 900~1100 DEG C, and middle portion temperature control is 700~900 DEG C, upper temp control for 400~
700 DEG C, the carbon ratio control range of conical fluidized bed (1) is 0.5~0.7mol/mol, and steam/hydrocarbons ratio control range is 1~2mol/
Mol, operating pressure ranging from 0.5~3MPa；
Efficient cyclone device (11) the temperature control is 300~700 DEG C；
Returning charge valve (12) the temperature control is 400~800 DEG C, and carbon ratio control range is 0.6~0.8mol/mol.
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