CN110437882A - A kind of low-order coal based on chemical chain and biomass graded utilize device and method - Google Patents
A kind of low-order coal based on chemical chain and biomass graded utilize device and method Download PDFInfo
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- CN110437882A CN110437882A CN201910774593.XA CN201910774593A CN110437882A CN 110437882 A CN110437882 A CN 110437882A CN 201910774593 A CN201910774593 A CN 201910774593A CN 110437882 A CN110437882 A CN 110437882A
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- 239000003245 coal Substances 0.000 title claims abstract description 46
- 239000002028 Biomass Substances 0.000 title claims abstract description 42
- 239000000126 substance Substances 0.000 title claims abstract description 22
- 238000000034 method Methods 0.000 title claims abstract description 18
- 238000000197 pyrolysis Methods 0.000 claims abstract description 91
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 87
- 239000001301 oxygen Substances 0.000 claims abstract description 87
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 87
- 239000007789 gas Substances 0.000 claims abstract description 70
- 238000002309 gasification Methods 0.000 claims abstract description 56
- 238000006243 chemical reaction Methods 0.000 claims abstract description 39
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 37
- 230000003647 oxidation Effects 0.000 claims abstract description 31
- 239000007787 solid Substances 0.000 claims abstract description 17
- 239000002245 particle Substances 0.000 claims abstract description 12
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000002994 raw material Substances 0.000 claims abstract description 7
- 230000008569 process Effects 0.000 claims abstract description 6
- 238000002156 mixing Methods 0.000 claims abstract 2
- 239000012071 phase Substances 0.000 claims description 46
- 239000002131 composite material Substances 0.000 claims description 23
- 239000007788 liquid Substances 0.000 claims description 15
- 239000003077 lignite Substances 0.000 claims description 12
- 230000015572 biosynthetic process Effects 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 10
- 238000003786 synthesis reaction Methods 0.000 claims description 10
- 239000000571 coke Substances 0.000 claims description 8
- 239000011343 solid material Substances 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 6
- 239000007791 liquid phase Substances 0.000 claims description 6
- 239000011280 coal tar Substances 0.000 claims description 5
- 229910044991 metal oxide Inorganic materials 0.000 claims description 5
- 150000004706 metal oxides Chemical class 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- 230000003197 catalytic effect Effects 0.000 claims description 4
- 239000010813 municipal solid waste Substances 0.000 claims description 4
- 239000002802 bituminous coal Substances 0.000 claims description 3
- 230000008859 change Effects 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 230000036651 mood Effects 0.000 claims description 3
- 239000002893 slag Substances 0.000 claims description 3
- 238000005979 thermal decomposition reaction Methods 0.000 claims description 3
- 230000009471 action Effects 0.000 claims description 2
- 230000005587 bubbling Effects 0.000 claims description 2
- 229910052791 calcium Inorganic materials 0.000 claims description 2
- 229910052802 copper Inorganic materials 0.000 claims description 2
- 229910052742 iron Inorganic materials 0.000 claims description 2
- 229910052748 manganese Inorganic materials 0.000 claims description 2
- 229910052759 nickel Inorganic materials 0.000 claims description 2
- 238000007789 sealing Methods 0.000 claims description 2
- 239000010902 straw Substances 0.000 claims description 2
- 229910052723 transition metal Inorganic materials 0.000 claims description 2
- 229910000314 transition metal oxide Inorganic materials 0.000 claims description 2
- 150000003624 transition metals Chemical class 0.000 claims description 2
- 238000006555 catalytic reaction Methods 0.000 claims 1
- 238000006392 deoxygenation reaction Methods 0.000 claims 1
- 239000012263 liquid product Substances 0.000 abstract description 10
- 239000007795 chemical reaction product Substances 0.000 abstract description 3
- 229910014460 Ca-Fe Inorganic materials 0.000 description 21
- 241000195493 Cryptophyta Species 0.000 description 11
- 239000000203 mixture Substances 0.000 description 9
- 239000000047 product Substances 0.000 description 7
- 238000004458 analytical method Methods 0.000 description 4
- 238000000921 elemental analysis Methods 0.000 description 4
- 238000006722 reduction reaction Methods 0.000 description 4
- -1 vapor Chemical compound 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 230000008878 coupling Effects 0.000 description 3
- 238000010168 coupling process Methods 0.000 description 3
- 238000005859 coupling reaction Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 238000007233 catalytic pyrolysis Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 230000011218 segmentation Effects 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 230000004087 circulation Effects 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 238000009510 drug design Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000002905 metal composite material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 150000002927 oxygen compounds Chemical group 0.000 description 1
- 230000001869 rapid Effects 0.000 description 1
- 239000004449 solid propellant Substances 0.000 description 1
- 210000000952 spleen Anatomy 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000007039 two-step reaction Methods 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
-
- 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
- C10J2300/0983—Additives
- C10J2300/0986—Catalysts
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
- Industrial Gases (AREA)
Abstract
The invention belongs to the classified utilization technical fields of low-order coal and biomass; more particularly to a kind of low-order coal based on chemical chain and it is biomass graded utilize device and method; reduction-state oxygen carrier carries out fast pyrogenation with low order coal particle or biological particles mixing and reacts, and reduction-state oxygen carrier generates oxidation state oxygen carrier；Pyrolysis is burnt, oxidation state oxygen carrier is separated with pyrolysis gas liquid product in the close phase section of two-part pyrolysis reactor；Isolated pyrolysis is burnt and oxidation state oxygen carrier enters gasification reactor with the oxidation state oxygen carrier come from air reactor jointly and carries out gasification reaction, and oxidation state oxygen carrier is reduced to reduction-state oxygen carrier；Reduction-state oxygen carrier respectively enters two-part air reactor and two-part pyrolysis reactor by tripper；Whole process makes low-order coal, biomass etc. realize classification, high efficient resourcing containing the higher solid carbon raw material of volatile matter, while pyrolytic reaction regulation, cascaded utilization of energy, separating in reaction product.
Description
Technical field:
The invention belongs to the classified utilization technical fields of low-order coal and biomass, and in particular to a kind of based on the low of chemical chain
Rank coal and it is biomass graded utilize device and method, be suitable for including that the low-order coals such as lignite, bituminous coal and terrestrial organism matter, ocean are raw
The classified utilization process of the solid carbon raw material containing high volatile of the biomass such as substance.
Background technique:
The clean, efficient of the carbonic solid fuels such as coal, biomass, low-carbon conversion are China's energy and environment sustainable development
Certainty road.Since the degree of coalification of low price coal is low, calorific value is low, volatile matter content is high, directly burning or gasification efficiency are low,
And its resource value can not be fully utilized.Biomass equally exists the features such as calorific value is low, volatile matter is high, simple burning or
Gasification also cannot achieve its high efficient resourcing.Therefore, the composition and structure feature according to low-order coal or biomass, is classified it point
Matter conversion is the effective way realizing low-order coal clean and effective and utilizing.
The pyrolysis of low-order coal or biomass can get oil gas, chemicals and the semicoke of high added value, and gasification or burning can be with
Synthesis gas or heat are obtained, therefore, pyrolysis coupling char Gasification or burning are that it is classified the important channel that sub-prime utilizes.With tradition
Pyrolysis is compared, the quality of the adjustable thermal decomposition product of catalytic pyrolysis, hydropyrolysis, however, there are catalyst circulations for catalytic pyrolysis
Using difficulty, the problems such as hydropyrolysis is expensive there are hydrogen source, its industrial application is limited.Chemical chain (Chemical Looping)
Oxygen carrier there is oxygen carrier, heat-carrying and catalytic action simultaneously, not only adjustable gas-liquid product composition, but also can be realized catalyst and follow
Ring utilizes, and is the ideal heat carrier of low-order coal/biomass pyrolytic and potential catalyst.
Burning chemistry chains/gasification (Chemical Looping combustion/gasification, CLC/CLG) are benefits
Molecular oxygen is replaced with the Lattice Oxygen of oxygen carrier, traditional combustion or gasification reaction are decoupled as two-step reaction, i.e., in fuel reactor
The oxidation reaction of oxygen carrier in the reduction reaction and air reactor of oxygen carrier is a kind of novel burning/gasification mode, has
The advantages such as separation in cascaded utilization of energy, reaction product.Compared with coupling coal-char combustion, pyrolysis coupling char Gasification process can be with
Using the secondary pyrolytic reaction of gasification synthesis gas regulation volatile matter, promote the hydropyrolysis process of tar, and then improves liquid phase and produce
Rate and improvement liquid phase quality.
Summary of the invention:
It is that low-order coal, biomass etc. are higher containing volatile matter it is an object of the invention to overcome disadvantage of the existing technology
The transfer design of solid carbon raw material for a kind of low-order coal based on chemical chain and it is biomass graded utilize device and method so that
The higher solid carbon raw material containing volatile matter such as low-order coal, biomass realizes classification, high efficient resourcing, meanwhile, realization low-order coal,
The pyrolytic reaction regulation of the higher solids containing volatile matter such as biomass carbon raw material, cascaded utilization of energy separate in reaction product.
In order to achieve the above object, low-order coal of the present invention based on chemical chain and biomass graded apparatus main body is utilized
Structure includes that main structure includes cyclone separator I, gasification reactor, accumulator, material control valve, dipleg, jet pipe I, jet pipe
II, returning charge valve, flow control valve I, gas distribution grid I, gas distributing chamber I, solid slag-drip opening, cyclone separator III, whirlwind point
From device II, two-part air reactor fast lifting section, tripper, flow control valve II, the close phase section of two-part air reactor,
Gas distribution grid II, gas distributing chamber II, two-part pyrolysis reactor fast downlink section, the close phase section of two-part pyrolysis reactor,
Gas-liquid separator, rapid-cooling heat exchanger, gas distribution grid III and gas distributing chamber III；Accumulator passes through material control valve and jet pipe I
It is connected, jet pipe I and jet pipe II are symmetricly set on the top two sides of two-part pyrolysis reactor fast downlink section；Two-part heat
Solution reactor fast downlink section and the close phase section of two-part pyrolysis reactor are connected to form two-part pyrolysis reactor, two-part pyrolysis
The close phase section top of reactor is connected with gas-liquid separator, the close phase pars infrasegmentalis of two-part pyrolysis reactor by flow control valve I with
Gasification reactor is connected, and the bottom of the close phase section of two-part pyrolysis reactor is equipped with gas distributing chamber III, two-part pyrolysis reactor
Separated between close phase section and gas distributing chamber III by gas distribution grid III, the top of gasification reactor successively with cyclonic separation
Device II is connected with cyclone separator III, the bottom cyclone separator II be equipped with tripper, tripper respectively with jet pipe II and flowing
Control valve II is connected, and the solid material that cyclone separator II is obtained enters jet pipe II or flow control valve by tripper control
II；The control of tripper is realized by the tolerance of control jet pipe II jet media and the loosening general mood amount of flow control valve II；
The lower end of flow control valve II is connected with the close phase section of two-part air reactor, the close phase section top of two-part air reactor and two
Segmentation air reactor fast lifting section is connected to form two-part air reactor, two-part air reactor fast lifting section top
End is connected with cyclone separator I, and the bottom cyclone separator I connects dipleg, and gasification reactor is connect by returning charge valve with dipleg, revolves
The solid material that wind separator I is obtained passes sequentially through dipleg, returning charge valve enters the lower part of gasification reactor, and from flow control valve
The solid material that I is flowed into mixes；Solid slag-drip opening passes vertically through gas distributing chamber I and gas distribution grid I, is used for solid slag
Discharge, rapid-cooling heat exchanger is located at outside gas-liquid separator, makes into the gas-phase product generation gas-liquid two-phase of gas-liquid separator and real
Now separate.
Two-part air reactor of the present invention is two-section flowing bed, and the close phase section of lower section two-part air reactor is rapids
It is fluidized bed, upper section two-part air reactor fast lifting section be fast lifting pipe, the close phase section of two-part air reactor with
The diameter ratio of two-part air reactor fast lifting section is greater than 2；Two-part pyrolysis reactor is two-section flowing bed, upper section two
Segmentation pyrolysis reactor fast downlink section is descending-bed reactor, and the close phase section of lower section two-part pyrolysis reactor is bubbling fluidized bed
The diameter ratio of reactor, two-part pyrolysis reactor fast downlink section and the close phase section of two-part pyrolysis reactor is less than 0.5；Gas
Change reactor is fast lifting pipe reactor；Returning charge valve, flow control valve I and flow control valve II are loop sealing valve, U-shaped
One of valve, V valve, L valve；Gas distribution grid I, gas distribution grid II, gas distribution grid III are porous plate, blast cap plate, micropore
One of plate；Material control valve is one kind of screw-feeder, mechanical valve.
Low-order coal of the present invention based on chemical chain and biomass graded utilization device are in use, reduction-state oxygen carrier pair
The pyrolytic reaction of low-order coal or biomass plays the role of catalytic deoxidation, oxidation state oxygen carrier and pyrolysis coal tar or biomass char carries out
The oxidation reaction of gasification reaction, reduction-state oxygen carrier provides heat, gasified reverse for the gasification reaction of pyrolysis coal tar or biomass char
Reduction-state oxygen carrier after answering provides heat for the pyrolytic reaction of low-order coal or biomass, and detailed process is as follows:
(1) it is mixed to carry out jet stream for the low order coal particle and/or biological particles of reduction-state oxygen carrier and 0.01~5mm of partial size
It closes, low order coal particle or biological particles carry out fast pyrogenation reaction, and reduction-state oxygen carrier is to pyrolysis during pyrolytic reaction
The reactions such as product is catalyzed, deoxidation, reduction-state oxygen carrier generate oxidation state oxygen carrier；Pyrolysis coke, oxidation state oxygen carrier and heat
Liquid product of venting one's spleen is separated in the close phase section of two-part pyrolysis reactor；
(2) isolated pyrolysis is burnt and oxidation state oxygen carrier and the oxidation state oxygen carrier from air reactor jointly into
Enter gasification reactor and carry out gasification reaction, in gasifying agent CO2/H2Under the action of O, synthesis gas CO/H is generated2, oxidation state oxygen carrier
It is reduced to reduction-state oxygen carrier；
(3) reduction-state oxygen carrier respectively enters two-part air reactor and two-part pyrolysis reactor by tripper,
Reduction-state oxygen carrier into two-part pyrolysis reactor repeats step (1)；Reduction-state into two-part air reactor carries
Oxidation reaction occurs for oxysome, generates a large amount of heat, provides heat for the burnt gasification reaction of pyrolysis in gasification reactor, repeats step
(2)。
Superficial gas velocity in two-part air reactor and two-part pyrolysis reactor of the present invention is 0.01~0.5m/
S, the superficial gas velocity in gasification reactor are 1~5m/s, 1~7m/s of superficial gas velocity in jet pipe I and jet pipe II；Two-part
Pyrolysis reactor operation temperature is 550~750 DEG C, operating pressure 0.1-1Mpa；Two-part air reactor and gasification reaction
The operation temperature of device is 800~950 DEG C, operating pressure 0.1-1Mpa.
Reduction-state oxygen carrier of the present invention is the metal oxide of lower valency, and oxidation state oxygen carrier is the metal of high-valence state
Oxide, metal oxide include the transition metal oxides such as Ca, Fe, Ni, Cu, Mn, Co and any 2~4 kinds of transition metal
Composite oxides.
Low-order coal of the present invention includes mud coal, lignite, bituminous coal and bottle coal；Biomass includes the lands such as straw, timber
The marine organisms and kitchen garbage, municipal refuse etc. such as raw biomass, microalgae.
Loosening wind and jet media of the present invention include N2、CO2, vapor, carbon raw material pyrolysis gas or gasification gas in
It is one or more of.
Compared with prior art, the present invention have the advantage that first is that oxygen carrier while being also heat carrier, with pyrolysis it is burnt or
Coal ash does solid thermal carriers and compares, and oxygen carrier can reduce the dustiness of pyrolysis liquid product, improves the product of pyrolysis liquid product
Matter；Second is that oxygen carrier has catalytic action to the pyrolysis of low-order coal and biomass, by rational design to oxygen carrier and modification,
It can be realized the orientation regulation of pyrolysis gas liquid product；Third is that pyrolysis coke reacted with the Lattice Oxygen of oxygen carrier, not with air
It directly contacts, improves the quality of synthesis gas and pyrolysis gas.
Detailed description of the invention:
Fig. 1 is that the low-order coal of the present invention based on chemical chain and biomass graded utilization apparatus main body structural principle are illustrated
Figure.
Fig. 2 is the low-order coal and the biomass graded work original using device described in the embodiment of the present invention 1 based on chemical chain
Schematic block diagram is managed, wherein MeOxFor oxidation state oxygen carrier；MeOx-1For reduction-state oxygen carrier, wherein x >=1.
Fig. 3 is the liquid phase of pyrolytic reaction between reduction-state Ca-Fe composite oxygen carrier and micro- quasi- ball algae in the embodiment of the present invention 1
Product forms distribution map.
Fig. 4 is gasification reaction between 1 oxidation state Ca-Fe composite oxygen carrier of the embodiment of the present invention and micro- quasi- ball algae pyrolysis coke
Generate synthesis gas composition figure.
The liquid phase of Fig. 5 pyrolytic reaction between 2 reduction-state Ca-Fe composite oxygen carrier of the embodiment of the present invention and Zhaotong Brown Coal produces
Object forms distribution map.
The life of Fig. 6 gasification reaction between 2 oxidation state Ca-Fe composite oxygen carrier of the embodiment of the present invention and Zhaotong Brown Coal coal tar
It forms and schemes at synthesis gas.
Specific embodiment:
The invention will be further described by way of example and in conjunction with the accompanying drawings.
Embodiment 1:
Low-order coal and biomass graded utilization apparatus main body structure described in the present embodiment based on chemical chain include main body knot
Structure includes cyclone separator I 1, gasification reactor 2, accumulator 3, material control valve 4, dipleg 5, jet pipe I 6, jet pipe II 7, returns
Expect valve 8, flow control valve I 9, gas distribution grid I 10, gas distributing chamber I 11, solid slag-drip opening 12, cyclone separator III
13, cyclone separator II 14, two-part air reactor fast lifting section 15, tripper 16,17, two sections of flow control valve II
The close phase section 18 of formula air reactor, gas distribution grid II 19, gas distributing chamber II 20, two-part pyrolysis reactor fast downlink
Section 21, the close phase section 22 of two-part pyrolysis reactor, gas-liquid separator 23, rapid-cooling heat exchanger 24, gas distribution grid III 25 are gentle
Body distributing chamber III26；Accumulator 3 is connected by material control valve 4 with jet pipe I 6, and jet pipe I 6 and jet pipe II 7 are symmetrical arranged
In the top two sides of two-part pyrolysis reactor fast downlink section 21；Two-part pyrolysis reactor fast downlink section 21 and two-part
The close phase section 22 of pyrolysis reactor is connected to form two-part pyrolysis reactor, close 22 top of phase section of two-part pyrolysis reactor and gas-liquid
Separator 23 is connected, and close 22 lower part of phase section of two-part pyrolysis reactor is connected by flow control valve I 9 with gasification reactor 2,
The bottom of the close phase section 22 of two-part pyrolysis reactor is equipped with gas distributing chamber III 26, the close phase section of two-part pyrolysis reactor 22 with
Separated between gas distributing chamber III 26 by gas distribution grid III 25, the top of gasification reactor 2 successively with cyclonic separation
Device II 14 is connected with cyclone separator III 13,14 bottom cyclone separator II be equipped with tripper 16, tripper 16 respectively with
Jet pipe II 7 is connected with flow control valve II 17, and the solid material that cyclone separator II 14 is obtained is controlled by tripper 16
Into jet pipe II 7 or flow control valve II 17；The gas that the control of tripper 16 passes through control 7 jet media of jet pipe II
Amount and the loosening general mood amount of flow control valve II 17 are realized；The lower end of flow control valve II 17 and two-part air reactor are close
Phase section 18 is connected, and close 18 top of phase section of two-part air reactor is connected to form with two-part air reactor fast lifting section 15
Two-part air reactor, 15 top of two-part air reactor fast lifting section are connected with cyclone separator I 1, cyclonic separation
1 bottom device I connects dipleg 5, and gasification reactor 2 is connect by returning charge valve 8 with dipleg 5, the solid that cyclone separator I 1 is obtained
Material passes sequentially through dipleg 5, returning charge valve 8 enters the lower part of gasification reactor 2, with the solids flowed into from flow control valve I 9
Material mixes；Solid slag-drip opening 12 passes vertically through gas distributing chamber I 10 and gas distribution grid I 11, for solid slag to be discharged,
Rapid-cooling heat exchanger 24 is located at outside gas-liquid separator 23, and the gas-phase product into gas-liquid separator 23 is made to generate gas-liquid two-phase and real
Now separate.
The step of the present embodiment low-order coal and biomass graded utilization, is as follows:
(1) at 600 DEG C, reduction-state Ca-Fe composite oxygen carrier and the micro- quasi- ball algae particle of 0.01~5mm carry out jet stream and mix
It closes, micro- quasi- ball algae particle carries out fast pyrogenation reaction, and reduction-state oxygen carrier urges thermal decomposition product during pyrolytic reaction
The reaction such as change, deoxidation, reduction-state Ca-Fe composite oxygen carrier generate oxidation state Ca-Fe composite oxygen carrier；Pyrolysis coke, oxidation state Ca-
Fe composite oxygen carrier is separated with pyrolysis gas liquid product in the close phase section 22 of two-part pyrolysis reactor；
(2) isolated pyrolysis coke and oxidation state oxygen carrier and the oxidation state Ca-Fe next from two-part air reactor
Composite oxygen carrier enters gasification reactor 2 jointly and carries out gasification reaction, at 850 DEG C, cooks gasifying agent using vapor, generates and close
At gas CO/H2, oxidation state Ca-Fe composite oxygen carrier is reduced to reduction-state Ca-Fe composite oxygen carrier；
(3) reduction Ca-Fe composite oxygen carrier respectively enters two-part air reactor and two-part heat by tripper 16
Reactor is solved, the reduction Ca-Fe composite oxygen carrier into two-part pyrolysis reactor repeats step (1), into two-part air
Oxidation reaction occurs for the reduction Ca-Fe composite oxygen carrier of reactor, generates a large amount of heat, is that pyrolysis is burnt in gasification reactor 2
Gasification reaction provides heat, repeats step (2).
For the present embodiment using micro- quasi- ball algae as reactant, the Industrial Analysis and elemental analysis of micro- quasi- ball algae are shown in Table 1, use
Ca-Fe composite oxygen carrier is oxygen carrier, the liquid product of pyrolytic reaction between reduction-state Ca-Fe composite oxygen carrier and micro- quasi- ball algae
Fig. 3 is shown in composition distribution, the generation synthesis gas group of gasification reaction between oxidation state Ca-Fe composite oxygen carrier and micro- quasi- ball algae pyrolysis coke
At Fig. 4,
Table 1: the Industrial Analysis and elemental analysis (air-dried basis) of micro- quasi- ball algae
From the figure 3, it may be seen that the addition of oxygen carrier has the composition for adjusting pyrolytic behavior phase compared with conventional micro- quasi- ball algae pyrolysis
Important function reduces the relative amount of nitrogenous compound, increases the relative amount of aromatic hydrocarbon, phenol and alkene, and makes to contain
The main composition of oxygen compound becomes ketone compounds from carboxylic acid compound, reduces the oxygen content of liquid product；It can by Fig. 4
Know, the gasification of micro- quasi- ball algae pyrolysis char may be implemented in oxidation state Ca-Fe composite oxygen carrier, generates hydrogen-rich synthetic gas.
Embodiment 2:
The present embodiment uses 1 described device of embodiment and method, uses Ca-Fe composite oxygen carrier for oxygen carrier, use is clear
Lead to lignite as reactant, the Industrial Analysis and elemental analysis of Zhaotong Brown Coal are shown in Table 2, reduction-state Ca-Fe composite oxygen carrier with it is clear
The liquid product composition distribution of pyrolytic reaction is shown in that Fig. 5, oxidation state Ca-Fe composite oxygen carrier and Zhaotong Brown Coal are pyrolyzed between logical lignite
The generation synthesis gas of gasification reaction forms Fig. 6 between coke,
Table 2: the Industrial Analysis and elemental analysis (air-dried basis) of Zhaotong Brown Coal
As shown in Figure 5, compared with the pyrolysis of conventional lignite, the addition of oxygen carrier has the composition for adjusting pyrolytic behavior phase important
Effect considerably increases the relative amount of benzene,toluene,xylene (BTX) in pyrolysis liquid phase；It will be appreciated from fig. 6 that oxidation state Ca-Fe
The gasification of Zhaotong Brown Coal pyrolysis char may be implemented in composite oxygen carrier, generates co-rich synthesis gas.
Claims (7)
1. a kind of low-order coal based on chemical chain and biomass graded utilizing device, it is characterised in that main structure includes whirlwind point
From device I, gasification reactor, accumulator, material control valve, dipleg, jet pipe I, jet pipe II, returning charge valve, flow control valve I, gas
Distribution grid I, gas distributing chamber I, solid slag-drip opening, cyclone separator III, cyclone separator II, two-part air reactor are fast
Fast raising section, tripper, flow control valve II, the close phase section of two-part air reactor, gas distribution grid II, gas distributing chamber
II, two-part pyrolysis reactor fast downlink section, the close phase section of two-part pyrolysis reactor, gas-liquid separator, rapid-cooling heat exchanger, gas
Body distribution grid III and gas distributing chamber III；Accumulator is connected by material control valve with jet pipe I, jet pipe I and II pairs of jet pipe
Claim the top two sides that two-part pyrolysis reactor fast downlink section is set；Two-part pyrolysis reactor fast downlink section with two sections
The close phase section of formula pyrolysis reactor is connected to form two-part pyrolysis reactor, the close phase section top of two-part pyrolysis reactor and gas-liquid point
It is connected from device, the close phase pars infrasegmentalis of two-part pyrolysis reactor is connected by flow control valve I with gasification reactor, two-part pyrolysis
The bottom of the close phase section of reactor is equipped with gas distributing chamber III, between the close phase section of two-part pyrolysis reactor and gas distributing chamber III
It being separated by gas distribution grid III, the top of gasification reactor is successively connected with cyclone separator II and cyclone separator III,
The bottom cyclone separator II is equipped with tripper, and tripper is connected with jet pipe II and flow control valve II respectively, cyclone separator
The solid material that II is obtained enters jet pipe II or flow control valve II by tripper control；The control of tripper passes through control
The tolerance of jet pipe II jet media and the loosening general mood amount of flow control valve II are realized；The lower end of flow control valve II with two sections
The close phase section of formula air reactor is connected, the close phase section top of two-part air reactor and two-part air reactor fast lifting section
It is connected to form two-part air reactor, two-part air reactor fast lifting section top is connected with cyclone separator I, whirlwind
The bottom separator I connects dipleg, and gasification reactor is connect by returning charge valve with dipleg, the solid material that cyclone separator I is obtained
Pass sequentially through dipleg, returning charge valve enters the lower part of gasification reactor, mixed with the solid material flowed into from flow control valve I；
Solid slag-drip opening passes vertically through gas distributing chamber I and gas distribution grid I, and for solid slag to be discharged, rapid-cooling heat exchanger is located at gas
Outside liquid/gas separator, so that the gas-phase product into gas-liquid separator is generated gas-liquid two-phase and realize separation.
2. according to claim 1 the low-order coal based on chemical chain and it is biomass graded utilize device, it is characterised in that it is described
Two-part air reactor be two-section flowing bed, the close phase section of lower section two-part air reactor be turbulent fluidized bed, two sections of upper section
Formula air reactor fast lifting section is fast lifting pipe, and the close phase section of two-part air reactor and two-part air reactor are fast
The diameter ratio of fast raising section is greater than 2；Two-part pyrolysis reactor is two-section flowing bed, and upper section two-part pyrolysis reactor is quick
Downlink section is descending-bed reactor, and the close phase section of lower section two-part pyrolysis reactor is bubbling fluidized bed reactor, two-part pyrolysis
The diameter ratio of reactor fast downlink section and the close phase section of two-part pyrolysis reactor is less than 0.5；Gasification reactor is quickly to mention
Riser reactors；Returning charge valve, flow control valve I and flow control valve II are loop sealing valve, U-shaped valve, V valve, one in L valve
Kind；Gas distribution grid I, gas distribution grid II, gas distribution grid III are one of porous plate, blast cap plate, microwell plate；Material controlling
Valve is one kind of screw-feeder, mechanical valve.
3. it is a kind of using device as described in claim 1 realize low-order coal based on chemical chain and it is biomass graded utilize method,
It is characterized in that reduction-state oxygen carrier plays the role of catalytic deoxidation, oxidation state oxygen carrier to the pyrolytic reaction of low-order coal or biomass
Gasification reaction is carried out with pyrolysis coal tar or biomass char, the oxidation reaction of reduction-state oxygen carrier is pyrolysis coal tar or biomass char
Gasification reaction provides heat, and the reduction-state oxygen carrier after gasification reaction provides heat for the pyrolytic reaction of low-order coal or biomass,
Detailed process is as follows:
(1) the low order coal particle and/or biological particles of reduction-state oxygen carrier and 0.01~5mm of partial size carry out jet mixing, low
Rank coal particle or biological particles carry out fast pyrogenation reaction, during pyrolytic reaction reduction-state oxygen carrier to thermal decomposition product into
Row catalysis, deoxygenation, reduction-state oxygen carrier generate oxidation state oxygen carrier；Pyrolysis coke, oxidation state oxygen carrier and pyrolysis liquid phase
Product is separated in the close phase section of two-part pyrolysis reactor；
(2) the isolated burnt and oxidation state oxygen carrier that is pyrolyzed enters gas with from the next oxidation state oxygen carrier of air reactor jointly
Change reactor and carry out gasification reaction, in gasifying agent CO2/H2Under the action of O, synthesis gas CO/H is generated2, oxidation state oxygen carrier gone back
It originally was reduction-state oxygen carrier；
(3) reduction-state oxygen carrier respectively enters two-part air reactor and two-part pyrolysis reactor by tripper, enters
The reduction-state oxygen carrier of two-part pyrolysis reactor repeats step (1)；Into the reduction-state oxygen carrier of two-part air reactor
Oxidation reaction occurs, generates a large amount of heat, provides heat for the burnt gasification reaction of pyrolysis in gasification reactor, repeats step (2).
4. according to claim 3 the low-order coal based on chemical chain and it is biomass graded utilize method, it is characterised in that it is described
Superficial gas velocity in two-part air reactor and two-part pyrolysis reactor is 0.01~0.5m/s, the table in gasification reactor
Sight gas velocity is 1~5m/s, 1~7m/s of superficial gas velocity in jet pipe I and jet pipe II；Two-part pyrolysis reactor operation temperature
It is 550~750 DEG C, operating pressure 0.1-1Mpa；The operation temperature of two-part air reactor and gasification reactor be 800~
950 DEG C, operating pressure 0.1-1Mpa.
5. according to claim 3 the low-order coal based on chemical chain and it is biomass graded utilize method, it is characterised in that it is described
Reduction-state oxygen carrier is the metal oxide of lower valency, and oxidation state oxygen carrier is the metal oxide of high-valence state, metal oxide
Composite oxides including Ca, Fe, Ni, Cu, Mn, Co transition metal oxide and any 2~4 kinds of transition metal.
6. according to claim 3 the low-order coal based on chemical chain and it is biomass graded utilize method, it is characterised in that it is described
Low-order coal includes mud coal, lignite, bituminous coal and bottle coal；Biomass includes straw, timber, microalgae, kitchen garbage, city rubbish
Rubbish.
7. according to claim 3 the low-order coal based on chemical chain and it is biomass graded utilize method, it is characterised in that loosen
Wind and jet media include N2、CO2, vapor, carbon raw material pyrolysis gas or gasification one or more of gas.
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