CN105238447B - A kind of device and method of natural gas from coal and light oil - Google Patents
A kind of device and method of natural gas from coal and light oil Download PDFInfo
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- CN105238447B CN105238447B CN201510598202.5A CN201510598202A CN105238447B CN 105238447 B CN105238447 B CN 105238447B CN 201510598202 A CN201510598202 A CN 201510598202A CN 105238447 B CN105238447 B CN 105238447B
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 116
- 239000003245 coal Substances 0.000 title claims abstract description 65
- 238000000034 method Methods 0.000 title claims abstract description 38
- 239000003345 natural gas Substances 0.000 title claims abstract description 18
- 239000007789 gas Substances 0.000 claims abstract description 333
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 217
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 212
- 238000002309 gasification Methods 0.000 claims abstract description 160
- 239000002245 particle Substances 0.000 claims abstract description 98
- 238000000926 separation method Methods 0.000 claims abstract description 95
- 238000000197 pyrolysis Methods 0.000 claims abstract description 67
- 239000007787 solid Substances 0.000 claims abstract description 64
- 238000009903 catalytic hydrogenation reaction Methods 0.000 claims abstract description 46
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 40
- 239000007788 liquid Substances 0.000 claims abstract description 29
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 19
- 239000001301 oxygen Substances 0.000 claims abstract description 19
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000000746 purification Methods 0.000 claims abstract description 16
- 238000010791 quenching Methods 0.000 claims abstract description 15
- 239000002893 slag Substances 0.000 claims description 58
- 239000002956 ash Substances 0.000 claims description 53
- 238000006243 chemical reaction Methods 0.000 claims description 34
- 239000000463 material Substances 0.000 claims description 28
- 239000000047 product Substances 0.000 claims description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 25
- 229910052739 hydrogen Inorganic materials 0.000 claims description 23
- 239000001257 hydrogen Substances 0.000 claims description 20
- 238000010926 purge Methods 0.000 claims description 19
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 16
- 238000002156 mixing Methods 0.000 claims description 15
- 239000000203 mixture Substances 0.000 claims description 15
- 238000001914 filtration Methods 0.000 claims description 14
- 230000005532 trapping Effects 0.000 claims description 14
- 230000008859 change Effects 0.000 claims description 13
- 239000000428 dust Substances 0.000 claims description 12
- 239000000839 emulsion Substances 0.000 claims description 9
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 claims description 9
- 239000008187 granular material Substances 0.000 claims description 8
- 239000012535 impurity Substances 0.000 claims description 8
- 238000006555 catalytic reaction Methods 0.000 claims description 7
- 229930195733 hydrocarbon Natural products 0.000 claims description 7
- 150000002430 hydrocarbons Chemical class 0.000 claims description 7
- 239000003795 chemical substances by application Substances 0.000 claims description 6
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 3
- 239000010882 bottom ash Substances 0.000 claims description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 239000012263 liquid product Substances 0.000 claims description 3
- 238000004517 catalytic hydrocracking Methods 0.000 claims description 2
- 239000000446 fuel Substances 0.000 claims description 2
- 150000001875 compounds Chemical class 0.000 claims 1
- 230000018044 dehydration Effects 0.000 claims 1
- 238000006297 dehydration reaction Methods 0.000 claims 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 abstract description 10
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 230000003197 catalytic effect Effects 0.000 abstract description 4
- 238000004140 cleaning Methods 0.000 abstract description 4
- 238000006116 polymerization reaction Methods 0.000 abstract description 3
- 238000007086 side reaction Methods 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 19
- 230000008569 process Effects 0.000 description 12
- 230000000694 effects Effects 0.000 description 10
- 238000001816 cooling Methods 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 239000003054 catalyst Substances 0.000 description 7
- 230000005484 gravity Effects 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 239000012530 fluid Substances 0.000 description 5
- 230000004927 fusion Effects 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 238000005979 thermal decomposition reaction Methods 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 4
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 229910001882 dioxygen Inorganic materials 0.000 description 4
- 239000000295 fuel oil Substances 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 230000010354 integration Effects 0.000 description 4
- 239000011343 solid material Substances 0.000 description 4
- 230000002194 synthesizing effect Effects 0.000 description 4
- 239000010883 coal ash Substances 0.000 description 3
- 239000000571 coke Substances 0.000 description 3
- 238000004939 coking Methods 0.000 description 3
- 230000009257 reactivity Effects 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000005201 scrubbing Methods 0.000 description 3
- 239000008247 solid mixture Substances 0.000 description 3
- RNFJDJUURJAICM-UHFFFAOYSA-N 2,2,4,4,6,6-hexaphenoxy-1,3,5-triaza-2$l^{5},4$l^{5},6$l^{5}-triphosphacyclohexa-1,3,5-triene Chemical compound N=1P(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP=1(OC=1C=CC=CC=1)OC1=CC=CC=C1 RNFJDJUURJAICM-UHFFFAOYSA-N 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- 229910052783 alkali metal Inorganic materials 0.000 description 2
- 150000001340 alkali metals Chemical class 0.000 description 2
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 2
- 150000001342 alkaline earth metals Chemical class 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 239000002802 bituminous coal Substances 0.000 description 2
- 239000012159 carrier gas Substances 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 239000011248 coating agent Substances 0.000 description 2
- 238000000576 coating method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000003063 flame retardant Substances 0.000 description 2
- 239000002010 green coke Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 150000002989 phenols Chemical class 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 208000035126 Facies Diseases 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
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- 239000012895 dilution Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
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- 238000004064 recycling Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000011345 viscous material Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Landscapes
- Industrial Gases (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The device and method of a kind of natural gas from coal and light oil, includes steam oxygen gasification furnace, one-level hydrogasification stove, catalytic hydrogenation gasification hydropyrolysis integrated apparatus, gas solid separation and gas cleaning system.All semicokes can be trapped and increase the residence time of hydrogasification section semicoke particle by one-level hydrogasification stove；Catalytic hydrogenation gasification makes the content of methane in gas phase reach or close to equilibrium concentration by extending synthesis gas in the residence time of low-temperature space.The hydrogenation fast pyrogenation of coal is easy to the production of oil product.The pyrolysis gas of hydrogenation fast pyrogenation section output is cooled by Quench circulating air first, suppresses the generation of tar polymerization side reaction under semicoke catalytic action with this.Dust-laden crude synthesis gas will be separated by crude synthesis gas fine grained and semicoke revert system realizes the removal of solid particle in synthesis gas.Synthesis gas after udst separation further condenses the oil product removed in gas phase by gas solid separation unit again.Purification gas after gas-liquid separation further removes sour gas and CO contained therein2.Decontaminating syngas obtains methane by methane separation technique again.
Description
Technical field
The present invention relates to a kind of device and method for synthesizing gasification and fast pyrogenation integration, more particularly to a kind of coal system day
The device and method of right gas and light oil.
Background technology
By hydrogasification and oxygen-steam gasification technology carry out it is integrated have it long ago, it is similar to pass through hydropyrolysis and gas
Change integral process next life oil-producing product, synthesis gas, the technique of natural gas to be also well known.
Once recommended to produce dress as unstripped gas using two stage gasifier in natural gas from coal field, existing technical literature
Put.The wherein representative two stage pressurization airflow bed gasification furnace for being just known as Bi-gas techniques.The gasification furnace is
The technology developed between 1960~1970 years by bituminous coal research institute of the U.S..(referring to paper DOE/METC/SP-1DE858).
In the technique, the semicoke particle of secondary reformer trapping, which returns to primary reformer and water vapour and oxygen reaction, is used for producing synthesis gas.One section
The operation temperature of gasification furnace is about 3000 °F (1648.89 DEG C), and uses slag deslagging.The synthesis gas that primary reformer is produced will be made
For the thermal source of secondary reformer.Coal and water vapour, which are added after secondary reformer, to carry out hydrogasification to produce SNG.The operation temperature of secondary reformer is about
For 1700 °F (927 DEG C).Crude synthesis gas, which is cooled to enter back into after 800 °F (427 DEG C), carries out gas-solid two-phase in cyclone separator
Separation.Then, synthesis gas carries out methanation to produce SNG again after purification, transformationreation.Conjunction after part purification
Gasification furnace is also recycled back into gas.Above-mentioned two-stage gasifier still has many areas for improvement.For example：Air flow bed
The mixed effect of material is poor in reactor, under the reaction temperature of 1700 °F (927 DEG C), the not good possibility of material mixed effect
The generation (about less than 1%) of tar can be caused, and the basic non-recovery of the tar of low concentration is worth in synthesis gas.It is invested and transported
The value that row cost can be brought far above the so a small amount of tar of recovery.Because methane concentration is relatively low in coal gas (being less than 10%),
The technique must have synthesis gas methanator.
United States Patent (USP) 3,779,725 is improved above-mentioned Bio-Gas techniques.Technology disclosed in the patent attempts
Save methanator.By isolating methane from decontaminating syngas and by effective gas (CO+H after purification2) be recycled back to
Hydrogasification reaction is carried out in secondary reformer.Because the equilibrium methane concentration in synthesis gas drops with the rise of temperature of reaction system
It is low.When reactor temperature is 1700 °F (927 DEG C), the methane concentration in synthesis gas is below 10%.In fact, according to
《Chemistry of coal utilization》(《Chemistry of coal utilization-second edition additional issue》, editor Martin Elliott) and disclosed by P1722~1723
Content, the methane concentration in the Bi-Gas pilot-plants institute production of synthetic gas of 5t/h coal feeding amounts only has 4.3%.Such low concentration
Methane content, it is necessary to separated methane with other synthesis gas componentses by way of cryogenic condensation, then by separation of methane
Synthesis gas afterwards is recycled back to gasification furnace.Thus one, what the technique just became in economy does not have feasibility.At the same time,
Also a small amount of tar can be contained in the waste water that gasification is produced, these waste water containing tar are also required to after the progress of longer flow
Continuous processing.
Another effective trial being improved for Bi-Gas gasification process be exactly use using fluidized-bed reactor as
The multi-stek hydrogenation gasification process of core, hydrogasification is efficiently coupled with steam gasification process, because fluidized-bed reaction
The mixed effect of material is better than entrained-flow reactor in device.Hydrogenation such as HYGAS gasification process and synthesis gas company of Britain is closed
It is exactly good example into gasification process.Britain's synthesis gasification process just includes steam/oxygen gas and two gasification sections of hydrogasification.
The hydrogen source of hydrogasification section comes from steam/oxygen gas gasification section.However, it is similar with other fluidized bed gasifying process, work as gasification
When raw material is bituminous coal, total efficiency of carbon con version is typically relatively low.It is relatively low that relatively low total efficiency of carbon con version results in hydrogen yield, therefore hydrogenation
Amounts of hydrogen needed for changing reaction is just insufficient.
It is not described in the patent of invention in each section of gasification and how removes equilibrium hydrogen yield and efficiency of carbon con version problem.Sometimes
Bar line is drawn on paper to be easy to：For example, drawing a side line on one-level hydrogasification stove, one-level hydrogasification stove is produced
Semicoke is sent to secondary hydrogenation gasification furnace and gasified, and the semicoke that secondary hydrogenation gasification furnace is produced is sent to steam-oxygen gasification furnace again
For hydrogen manufacturing.But, since the input commercial operation of nineteen twenty-six First fluidized-bed gasification furnace, half in fluidized-bed gasification furnace
Burnt trapping is just never solved well.If semicoke granule capturing problem cannot be solved, then all imaginations all can not
Come true.The problem of technique equally faces such：Because afterbody gasifier operation temperature is 800 °F (426.67
DEG C), at this temperature, the methane equilibrium concentration in synthesis gas is less than 15%.So, it is therefore necessary to set up again after gasification furnace
One methanator is used for SNG production.
Another solution party's rule is by synthesizing gasification-dry distillation of coal or the integrated skill of synthesis gasification-coal hydrogenation pyrolysis
Art produces SNG and fuel oil simultaneously.Representative technique is exactly 1960s with growing up the seventies
Coalcon techniques.In this technique, coal is added into hydrotoring stove by hydropyrolysis to produce oil product and pyrolysis gas.Heat
Solution semicoke enters gasification hydrogen-producing in gasification furnace and provides hydrogen source for pyrolysis oven.Although with synthesis air purge in Coalcon gasification process
Purification and transformation system are washed, directly inputs hydropyrolysis stove to realize conjunction by high-temperature synthesis gas produced in gasification furnace in theory
It should be not difficult to realize into gasification-hydropyrolysis integration.But for how by oxygen in Coalcon techniques and other similar techniques
Gas-steam gasification, hydrogasification and hydropyrolysis technique are coupled and be specifically described for SNG and high-quality Oil Production.
All do not recognize in above-mentioned technique：Hydrogasification needs the material to have the longer residence time in reaction system, and heat from hydrogenation
Xie Ze needs the material to have the shorter residence time in reaction system, to limit connecing for semicoke particle and tar to greatest extent
Touch, because the semicoke particle in synthesis gas, which is tar component, occurs the catalyst that deep pyrolytic becomes light gas components.
The content of the invention
It is an object of the invention to provide a kind of natural gas from coal and the device and method of light oil, by synthesizing gasification, adding
Hydrogen, hydropyrolysis integrated technology produce natural gas, synthesis gas and the technique of fuel oil, and total efficiency of carbon con version approaches
100%.
To reach above-mentioned purpose, the inventive system comprises：Gasified including what is be connected with raw coal conduit by catalytic hydrogenation
Section and hydrogenation fast pyrogenation section constituted catalytic hydrogenation gasification-hydropyrolysis integrated apparatus, oxygen-steam gasification furnace, one
Level hydrogasification stove, crude synthesis gas-fine grained separation and semicoke revert system, solution-air, liquid-liquid separation unit, gas purification system
System；
The semicoke logistics pipeline of catalytic hydrogenation gasification-hydropyrolysis integrated apparatus is connected with one-level hydrogasification stove,
The synthesis gas stream pipeline of one-level hydrogasification stove is connected with catalytic hydrogenation gasification-hydropyrolysis integrated apparatus, and catalysis adds
The pyrolysis gas logistics of hydrogen-hydropyrolysis integrated apparatus output is separated through pipeline with crude synthesis gas-fine grained and semicoke is returned
Material system is connected, the synthesis gas stream of the separation of crude synthesis gas-fine grained and semicoke revert system by the road with solution-air and liquid-
Liquid separative element is connected, three tunnels of the outlet of solution-air and liquid-liquid separation unit point, respectively separating obtained water, reclaims gained
Oil product and the primary purifying synthesis gas stream that is connected with gas purge system, through obtained by gas purge system purification separation
CO2、H2S mixing logistics goes successively to downstream and separated and advanced treating, the methane after separation and other gas phase alkane conducts
Product is exported, the CO and H of gained after separation2One-level hydrogasification stove and crude synthesis gas-fine grained separation are returned as circulating air
And semicoke revert system；The bulky grain soot object of one-level hydrogasification stove flows through pipeline discharge, semicoke logistics through pipeline and oxygen-
Steam gasification stove is connected, and the synthesis gas of oxygen-steam top of gasification furnace output is connected through pipeline with one-level hydrogasification stove,
Primary purifying synthesis gas stream is also connected through circulating air logistics with the pipeline of synthesis gas, and oxygen-steam gasification furnace enters stove thing
Material is respectively the semicoke logistics of steam stream, oxygen stream and crude synthesis gas-fine grained separation and the discharge of semicoke revert system, oxygen
The outlet of gas-steam gasification stove is slag pipeline.
The gasification section of described oxygen-steam gasification furnace is using dip down inclined structure, semicoke logistics, steam stream, oxygen
Gas logistics tangentially enters gas-slag knockout drum by being injected tangentially gasification section mix products, and lime-ash enters the bottom of gas-slag knockout drum
Portion, the grey solid impurity particle obtained by gas-slag knockout drum trapping flows downward along inwall, and chilled water adds from gas-slag knockout drum bottom
Enter, the position of addition is below gas-slag mixture inlet, and the synthesis gas for leaving knockout drum enters one-level hydrogasification stove.
The gasification section of described oxygen-steam gasification furnace is using direction vertically downward, semicoke logistics, steam stream, oxygen
Gas logistics is injected tangentially gasification section, and gas phase is downwardly into linkage section with lime-ash cocurrent, pipe is gradually flowed into downwards in linkage section slag
Road bottom slag discharge, linkage section tangentially enters gas-slag knockout drum, and the grey solid impurity particle obtained by gas-slag knockout drum trapping is along inwall
Flow downward, chilled water is added from gas-slag knockout drum bottom, and the position of addition is left below gas-slag mixture inlet
The synthesis gas of knockout drum enters one-level hydrogasification stove.
Described one-level hydrogasification stove includes cone structure, and the cylinder upper end of cone structure vertical direction is additionally provided with use
In connection body of heater beveling to cone, the bottom of cone structure is connected with semicoke logistics pipeline, raw coal conduit, its profile
For intilted eccentric cone, synthesis gas, circulating air logistics enter one-level hydrogasification stove by its bottom side centre,
And the logistics of bulky grain lime-ash, ash particle logistics are then discharged from the bottommost of opposite side cone and can be recycled to hydrocracking section,
Emulsion zone is arranged above positioned at cone in body of heater, body of heater circumference is provided with several one cyclonics point in emulsion zone
From device, the multi-cyclone being connected with the outlet of primary cyclone is additionally provided with primary cyclone upper end and is separated
Device, the synthesis gas stream of multicyclone separation is connected through guiding gutter with synthesis gas stream conveyance conduit, in multi-cyclone
The lower end of separator is provided with dipleg, and the whirlwind dipleg of multicyclone is stretched into dipleg, and one of dipleg goes out
The semicoke particle of mouth enters bed as circulating granular, and the semicoke particle of the one outlet of dipleg is added to oxygen as fuel
Gas-steam gasification stove.
Described cone structure discharges the logistics of bulky grain lime-ash, the side of semicoke logistics and is further opened with fluidized gas entrance；Cone
Offered on the side wall of body and be connected with fluidized gas on cone fluidized gas entrance, dipleg and be passed through pipeline.
A diameter of 0.4-0.8m of described primary cyclone top cylinder, the crude synthesis gas of generation is tangential by entrance
Into primary cyclone, the solid particle of primary cyclone trapping returns to bed by the dipleg of cyclone separator,
And the distance between position and the cone inwall of dipleg outlet is 2-4 times of whirlwind dipleg diameter.
Described multicyclone includes some groups of small cyclones separator units, through primary cyclone gas-
Gu multicyclone is entered by the outlet at the top of cyclone separator containing semicoke fine grain crude synthesis gas after separation
Gas access surge bunker, the fine grained being mainly made up of semicoke is collected after being trapped by multi-cyclone in granule capturing storehouse, then
Dipleg is entered by whirlwind dipleg.
The riser and original of pyrolysis oven in the hydropyrolysis section of described catalytic hydrogenation gasification-hydropyrolysis integrated apparatus
Expect coal facies connection, feed coal is conveyed by conveying gas, be divided into two branch roads, a branch road enters catalytic hydrogenation and gasifies-add
The hydrogenation fast pyrogenation section that the makeup of hydrogen thermal decomposition integrated is put, another branch road enters one-level hydrogasification stove, hydrogenation fast pyrogenation section
The pyrolysis gas of top output is connected with pyrolysis oven primary cyclone entrance, is left from pyrolysis oven primary cyclone top
Enter pyrolysis oven secondary cyclone, the gas-solid mixing logistics of pyrolysis oven secondary cyclone output after cyclone separator
Separated through pipeline with crude synthesis gas-fine grained and semicoke revert system is connected, the half of the capture of pyrolysis oven secondary cyclone
Burnt logistics enters dipleg rear portion and returns to catalytic hydrogenation gasification-hydropyrolysis integrated apparatus by solids stream channel cycle,
The logistics of another part semicoke is connected through pipeline with one-level hydrogasification stove entrance, and pyrolysis oven primary cyclone is isolated
Carbonaceous solid particulates are recycled back into hydrogenation fast pyrogenation section through upright dipleg, meanwhile, in order to ensure the circulating ratio of solid circle,
It is further opened with the upright dipleg being connected with hydrogenation fast pyrogenation section with loosening the entrance of gas phase even；
Catalytic hydrogenation gasification section is the particle that material is loaded with gasification catalysis active component in fluidized-bed reactor, bed, is closed
The semicoke logistics returned into gas logistics and from hydrogenation fast pyrogenation section is mixed, at the same carry out gas phase and it is gas-solid two it is alternate plus
Hydrogen methanation reaction.
Described crude synthesis gas-fine grained separation and semicoke revert system include and pyrolysis gas logistics, circulation synthesis gas phase
The returning charge cyclone separator being made up of several unit cyclone separators even；The built-in high-efficient filter being connected with dust guiding gutter
The gas-solid filtering tank of core；The hopper being connected with filtering tank outlet at bottom mozzle, the conjunction of returning charge cyclone separator bottom output
Be connected by the road with gas-particle separation unit into gas logistics, returning charge cyclone separator capture dust by guiding gutter enter by
In the annular space region that the wall of filtering tank is surrounded with skirt, it is cone that filtering tank upper end, which is provided with filter core, lower end, and gas phase is upward
Filter core formation synthesis gas stream discharge is flowed into, semicoke logistics enters feed hopper along mozzle, half formed in feed hopper
Burnt logistics enters oxygen-steam gasification furnace along pipeline.
The method of the present invention is as follows：Gasifying agent and semicoke logistics are constituted in oxygen-steam gas by steam stream, oxygen stream
Change and gasification reaction is carried out in stove, produced lime-ash is discharged by oxygen-steam gasification furnace bottom ash discharging hole, produced synthesis gas
One-level hydrogasification stove is advanced on directly, the semicoke logistics produced by one-level hydrogasification stove is descending to return to oxygen-steam gas
Change stove and proceed gasification reaction, the logistics of bulky grain lime-ash is discharged by one-level hydrogasification furnace bottom, feed coal and circulating air and
The synthesis gas come from oxygen-steam gasification furnace is reacted in one-level hydrogasification stove, produced by one-level hydrogasification stove
The methane containing higher concentration synthesis gas by being advanced into catalytic hydrogenation gasification-hydropyrolysis integration on synthesis gas stream pipeline
Device, fresh feed coal enters after catalytic hydrogenation gasification-hydropyrolysis integrated apparatus, with defeated from one-level hydrogasification furnace roof portion
The synthesis gas of the methane containing higher concentration gone out and the high-temperature solid particle swept along carry out pyrolytic reaction as thermal source, pyrolysis char and
Semicoke logistics pipeline of being passed through under inert particle enters one-level hydrogasification stove, catalytic hydrogenation gasification-hydropyrolysis integrated apparatus
The pyrolysis gas logistics of output enters back into crude synthesis gas-fine grained separation after circulating air cooling through Quench and semicoke revert system is carried out
The semicoke logistics circulation of the initial gross separation purified treatment of synthesis gas, crude synthesis gas-fine grained separation and the trapping of semicoke revert system
Return oxygen-steam gasification furnace, synthesis gas stream enter gas-particle separation unit, separating obtained liquid product be respectively water and
Tar, the primary purifying synthesis gas stream through oil removing, dewater treatment of gas-liquid separation unit output is divided into two branch roads：Circulation
Gas logistics is recycled back into the synthesis gas exported with oxygen-steam top of gasification furnace as Quench gas and mixed, and remaining purification is closed
Then enter gas purge system into gas, methane and other gas phase hydrocarbons produced by gas purge system are used as output of products；CO
And H2One-level hydrogasification stove and crude synthesis gas-fine grained separation and semicoke revert system are returned to as circulating air, wherein returning
The circulating air of crude synthesis gas-fine grained separation and semicoke revert system is used for the Quench gas of pyrolysis gas logistics；Separating obtained
CO2、H2S mixing logistics goes successively to downstream and separated and advanced treating.
The present invention includes a gasification section, hydrogenation fast pyrogenation section and two-stage hydrogasification section.
The present invention includes oxygen-steam gasification furnace, one-level hydrogasification stove, catalytic hydrogenation gasification-hydropyrolysis integration
Device, gas-particle separation and gas cleaning system
All semicokes can be trapped and extend the residence time of hydrogasification section semicoke particle by one-level hydrogasification stove, so
There are two purposes：One is to improve gasification furnace output synthesis gas by increasing hydrogasification synthesis gas in the residence time of low-temperature space
The content of methane in gas phase.Two be to improve tar yield by the hydrogenation fast pyrogenation of coal, is easy to the production of follow-up oil product.Quickly
Fine ash contained by the pyrolysis gas of hot arc output is cooled to below the ash fusion point temperature of fine ash particle by circulation synthesis gas first, Jiao
Oil cooling is coagulated on dew-point temperature.Dust-laden crude synthesis gas will be realized and closed by crude synthesis gas-fine grained separation and semicoke revert system
The removal of solid particle into gas.Synthesis gas after udst separation is further cold by solution-air, liquid-liquid separation unit again
The solidifying tar removed in gas phase.Purification gas after gas-liquid separation also need further to remove sour gas contained therein and
CO2.Decontaminating syngas further removes the methane in synthesis gas by methane separation technique again.Unreacted CO and H2Recycling
Return two grades of catalytic hydrogenation gasification sections and participate in hydrogasification reaction.
Brief description of the drawings
Fig. 1 is the block flow diagram of the present invention；
Fig. 2 is the structure chart of oxygen-steam gasification furnace in the present invention；
Fig. 3 is the structure chart of another oxygen-steam gasification furnace of the invention；
Fig. 4 is the structure chart of one-level hydrogasification stove of the present invention；
Fig. 5 is the structure chart of two grades of catalytic gasifications of the invention and pyrolysis oven integrated apparatus；
Fig. 6 is the structure chart of crude synthesis gas of the present invention-fine grained separation and semicoke revert system.
In figure, conveying gas 1, feed coal 2, catalytic hydrogenation gasification section 3, hydrogenation fast pyrogenation section 4, synthesis gas stream pipeline 5,
Semicoke logistics pipeline 6, feed coal 7, one-level hydrogasification stove 8, synthesis gas 9, steam stream 10, oxygen stream 11, oxygen-steam
Gasification furnace 12, slag 13, pyrolysis gas logistics 14, Quench circulating air 15, ash particle logistics 16, bulky grain lime-ash logistics 17, semicoke
The separation of logistics 18, semicoke logistics 19, crude synthesis gas-fine grained and semicoke revert system 20, synthesis gas stream 21, solution-air, liquid-
Liquid separative element 22, water 23, oil product 24, primary purifying synthesis gas stream 25, circulating air 26, gas purge system 27, CO2、H2S
Mix logistics 28, decontaminating syngas product 29, gasification section 30, gas-slag knockout drum 31, chilled water 32, grey solid impurity particle 33, lime-ash
34th, linkage section 35, body of heater 36, cone 37, cone structure 38, circulating air logistics 39, cylinder 40, solid particle logistics 41, dipleg
42nd, emulsion zone 43, primary cyclone 44, cylinder 45, outlet 46, crude synthesis gas 47, multicyclone 48, water conservancy diversion
Groove 49, outer wall 50, small cyclones separator unit 51, gas access surge bunker 52, the fine grained 53 of semicoke composition, granule capturing
Storehouse 54, entrance 55, whirlwind dipleg 56, semicoke particle 57, dipleg 58, pyrolysis oven secondary cyclone 59, dipleg 60, solid
Logistics corridor 61, fluidized gas entrance 62, solid circle logistics 63, bed material position line 64, upright dipleg 65, solid circle logistics
66th, pyrolysis oven primary cyclone 67, unit cyclone separator 68, filter core 69, filtering tank 70, skirt 71, wall 72, cone
73rd, guiding gutter 74, anti-material cyclone separator 75, annular space 76, gas phase 77, semicoke logistics 78, mozzle 79, feed hopper 80, circulation
Gas 81, cone fluidized gas entrance 82, circulation synthesis gas pipeline 83, loosening gas 84, synthesis gas stream 85, catalytic hydrogenation gasification-add
The makeup of hydrogen thermal decomposition integrated puts 86.
Embodiment
The present invention is described in further detail below in conjunction with the accompanying drawings.
It is quick by catalytic hydrogenation gasification section 3 and hydrogenation the inventive system comprises being connected with raw coal conduit referring to Fig. 1
Catalytic hydrogenation gasification-hydropyrolysis integrated apparatus 86 that pyrolysis section 4 is constituted, oxygen-steam gasification furnace 12, one-level hydrogenation
Change stove 8, crude synthesis gas-fine grained separation and semicoke revert system 20, solution-air, liquid-liquid separation unit 22, gas purge system
27。
Wherein, one-level hydrogasification stove 8 is connected with raw coal conduit, catalytic hydrogenation gasification-hydropyrolysis integrated apparatus
86 are made up of catalytic hydrogenation gasification section 3 and hydrogenation fast pyrogenation section 4, catalytic hydrogenation gasification-hydropyrolysis integrated apparatus 86
Semicoke logistics pipeline 6 be connected with one-level hydrogasification stove 8, the synthesis gas stream pipeline 5 of one-level hydrogasification stove 8 and catalysis
Hydrogasification-hydropyrolysis integrated apparatus 86 is connected, the heat that catalytic hydrogenation gasification-hydropyrolysis integrated apparatus 86 is exported
Cracked gas stream 14 enters back into crude synthesis gas-fine grained separation after being cooled down through Quench circulating air 15 and semicoke revert system 20 is closed
Into the initial gross separation purified treatment of gas, the synthesis gas stream 21 of crude synthesis gas-fine grained separation and semicoke revert system 20 is through pipe
Road is connected with solution-air, liquid-liquid separation unit 22, solution-air, three tunnels of outlet point of liquid-liquid separation unit 22, respectively separates
The water 23 of gained, reclaim obtained by oil product 24 and the primary purifying synthesis gas stream 25 that is connected with gas purge system 27,
Through the CO obtained by the purification separation of gas purge system 272、H2S mixing logistics 28 goes successively to downstream and separated and advanced treating,
Produced methane and gas phase hydrocarbon is exported as final product 29；CO and H2One-level hydrogasification stove 8 is returned as circulating air
Separated with crude synthesis gas-fine grained and semicoke revert system 20；, the bulky grain lime-ash logistics 17 of one-level hydrogasification stove 8 is through pipe
Road is discharged, and semicoke logistics 18 is connected through pipeline with oxygen-steam gasification furnace 12, and the synthesis gas 9 of oxygen-steam gasification furnace 12 is passed through
Pipeline is connected with one-level hydrogasification stove 8, pipe of the primary purifying synthesis gas stream 25 also through circulating air logistics 39 Yu synthesis gas 9
Road is connected, and the stove material that enters of oxygen-steam gasification furnace 12 is respectively steam stream 10, oxygen stream 11 and crude synthesis gas-thin
The semicoke logistics 19 that particle is separated and semicoke revert system 20 is discharged, the bottom of oxygen-steam gasification furnace 12 is provided with the row of slag 13
Slag pipeline.
The effect of two grades of catalytic hydrogenation gasification sections 3 is the catalytic action by alkali metal or alkaline-earth metal, makes synthesis gas
The semicoke particle produced with pyrolysis oven is reacted to produce the CO and H in methane, crude synthesis gas2Also gas phase methane occurs simultaneously
Change reaction.Fluidized gas and heat of the fast pyrogenation section 4 as pyrolysis section are advanced on the gas of two grades of catalytic hydrogenation gasification sections 3 is direct
Source.
Crude synthesis gas-fine grained separation and the effect of semicoke revert system 20 are to trap most of half escaped in pyrolysis oven
Burnt particle, and the semicoke particle of trapping is recycled back into oxygen-steam gasification furnace 12.The work of solution-air, liquid-liquid separation unit 22
With the fine ash for being removal trace, the oils and water of most of condensable separation can be trapped by oil wash or washing.Gas purification
System 27 includes following part：Realize CO2And H2The sour gas piece-rate system that S is separated with synthesis gas；CO shift-converters；
Methane separation system, described methane separation system realizes that methane is separated with synthesis gas while will be not anti-by cryogenic condensation separation
The hydrogen answered, synthesis gas are recycled back to reactor, and pipeline is delivered to after SNG is compressed.
In highly preferred embodiment of the present invention, oxygen-steam gasification furnace 12 is slag deslagging airflow bed gasification furnace.Oxygen-
The stove logistics that enters of steam gasification stove 12 is respectively steam stream 10, oxygen stream 11 and semicoke logistics 19.Semicoke logistics 19 includes
Convey gas, superheated steam.According to the reactivity of semicoke and the difference of ash fusion point, the operation temperature of oxygen-steam gasification furnace 12 exists
1300-1900 DEG C of variation.Ash is finally converted to slag 13 in semicoke, and is discharged in the form of slag.
The synthesis gas 9 that oxygen-steam gasification furnace 12 is generated, which will be directly sent in one-level hydrogasification stove 8, is used as hydrogenation
Change the hydrogen source of reaction.Gas phase flows in the opposite direction with lime-ash in oxygen-steam gasification furnace 12, and lime-ash flows downward, synthesis
Gas is flowed up.Inevitably, the slag particles of part can enter in one-level hydrogasification stove 8 with synthesis gas 9, finally
These slags aggregate into particle with the bed in one-level hydrogasification stove 8.But, enter one-level hydrogenation with synthesis gas 9
The slag for changing stove 8 is more few better, and most slag should be trapped by the lime-ash trapping system of oxygen-steam gasification furnace 12.
Although oxygen-steam gasification furnace 12 can be any airflow bed gasification furnace, and gas phase with slag without too drastic
Cold refrigerated separation, optimal situation is exactly to be reclaimed the sensible heat entrained by gas, rather than will by Quench water cooling
This part sensible heat takes gasification furnace out of.Most of thermal source in the present invention needed for one-level hydrogasification stove 8 is gasified by oxygen-steam
What the sensible heat entrained by the synthesis gas produced by stove 12 was provided, sub-fraction is provided by hydrogasification reaction heat.Therefore, this hair
Bright described chilled water is served only for curing agent cooling lime-ash.
Referring to Fig. 2, the gasification section 30 of oxygen-steam gasification furnace 12 of the invention uses dip down inclined structure, semicoke thing
Stream 19 enters the gasification furnace perpendicular with the furnace wall of gasification section 30, mixing production by tangential injection with steam stream 10, oxygen stream 11
Thing tangentially enters gas-slag knockout drum 31, and lime-ash 34 enters the bottom of gas-slag knockout drum 31, work of the most lime-ash in gravity
It can enter the bottom of gas-slag knockout drum 31, i.e., the lime-ash 34 in figure with lower；Carried secretly the crude synthesis gas of grey solid impurity particle the gas-
Solid mixture realizes point of gas-solid two-phase under the influence of centrifugal force during gas-inside spin of slag knockout drum 31 rises
From.Grey solid impurity particle obtained by gas-trapping of slag knockout drum 31 will flow downward along inwall, and this is grey solid impurity particle 33.Chilled water 32
Added from gas-bottom of slag knockout drum 31, the position of addition is below gas-mixture inlet of slag knockout drum 31.Lime-ash after Quench
The conventional slag breaker of most of airflow bed gasification furnaces and lock hopper system will be discharged into.
Referring to Fig. 3, in this structure, gasification section 30 is direction vertically downward.It is similar with the structure in Fig. 2, semicoke thing
Stream 19, steam stream 10, oxygen stream 11 are all injected tangentially gasification section 30.The slag of formation can be along gasification section inwall stream
It is dynamic, and one layer of falling liquid film can be formed, the barrier film formed can play the refractory liner in protection gasification section 30 well
Effect.Gas phase is downwardly into linkage section 35 with lime-ash cocurrent, and pipeline will be gradually flowed into downwards in the most of slag of linkage section 35
Bottom slag discharge.Linkage section 35 tangentially enters synthesis gas-slag knockout drum 31.As described above, most of slag stream 34 is in weight
Gas-bottom of slag knockout drum 31 will be flowed in the presence of power.The crude synthesis gas for carrying small slag particles will be along knockout drum
31 spiral inner wall rises, in the process slag solid particle will be deposited on the inwall of gas-slag knockout drum 31 and along
Fire resisting on wall forms falling liquid film 33, so as to be separated with gas phase.The slag of gained is cooled down by chilled water 32 after separation, from
The synthesis gas 9 for driving gas-slag knockout drum 31 then enters one-level hydrogasification stove 8.
Pattern in moulder moisture Fig. 2 or Fig. 3 of oxygen-steam gasification furnace 12, depends on the behaviour of oxygen-steam gasification furnace 12
Make temperature, and the operation temperature of oxygen-steam gasification furnace 12 then depends on the ash fusion point of used feed coal.At the beginning of coal ash
When beginning deformation temperature is on 1300 DEG C, oxygen-steam gasification furnace structure uses structure as shown in Figure 3, otherwise then using such as
Structure shown in Fig. 2.When the ash fusion point temperature of feed coal is higher than 1300 DEG C, the operation temperature of gasification furnace will be above 1500 DEG C or
Its operation temperature is higher than T250,T250Refer under this operation temperature, the viscosity of liquid lime-ash is equal to 250poise.Gasify furnace gas
It is that can play resistance in protection gasification section 30 well as separation layer to change the catadromous slag fluid matasomatism of the inwall of section 30
The purpose of fiery lining.In addition, cooling coil can be installed in the flame retardant coating of gasification section 30 to extend the life-span of flame retardant coating.Work as coal ash
Initial deformation temperature under 1300 DEG C when, gasification furnace shown in Fig. 2 is relatively applicable, because its internal structure is relatively simple
It is single.
Referring to Fig. 4, one-level hydrogasification stove 8 of the invention includes cone structure 38, the post of the vertical direction of cone structure 38
The upper end of body 40 be additionally provided with for connect the beveling of body of heater 36 to cone 37, bottom and the semicoke logistics pipeline of cone structure 38
6th, raw coal conduit 7 is connected, and its profile is internally inclined eccentric cone, and synthesis gas 9, circulating air logistics 39 are by its bottom
Portion side centre enters one-level hydrogasification stove 8, and bulky grain lime-ash logistics 17, ash particle logistics 16 are then recycled into and added
Hydrogen fast pyrogenation section, is arranged above emulsion zone 43 positioned at cone 37 in body of heater 36, justifies in emulsion zone along body of heater 36
It is provided with some groups of primary cyclones 44 week, is additionally provided with the body of heater 36 of the upper end of primary cyclone 44 and one
The multicyclone 48 that the outlet 46 of level cyclone separator 44 is connected, the synthesis gas that multicyclone 48 is separated
Logistics is connected through guiding gutter 49 with synthesis gas stream pipeline 5, and dipleg 58 is provided with the lower end of multicyclone 48, many
The whirlwind dipleg 56 of pipe cyclone separator 48 is stretched into dipleg 58, the one outlet of dipleg 58 output semicoke particle 57 as
Circulating granular enters bed.The semicoke particle 18 of another outlet output of dipleg 58 adds oxygen-steam gas as reactant
Change stove 12.
Wherein, the discharge bulky grain lime-ash of cone structure 38 logistics 17.Ash particle logistics 16 is then recycled into the fast speed heat of hydrogenation
Solve section 4.Separation is realized in bulky grain logistics 17 and ash particle logistics 16 in the presence of fluidized gas 62；Opened up on the side wall of cone 37
Having be connected with cone fluidized gas entrance 82, dipleg 58 circulation synthesis gas pipeline 83；
A diameter of 0.4-0.8m of the top cylinder 45 of primary cyclone 44, crude synthesis gas enters one-level by entrance 55 and revolved
Wind separator 44, the solid particle logistics 41 trapped through primary cyclone 44 returns to bed by the dipleg 42 of cyclone separator
Layer, and the distance between dipleg 42 position and the inwall of cone 37 that export are 2-4 times of the diameter of whirlwind dipleg 42；
Multicyclone 48 includes some groups of small cyclones separator units 51, is removed through primary cyclone 44
Crude synthesis gas 47 after semicoke fine grained enters multicyclone 48 by the outlet 46 at the top of cyclone separator 44
Gas access surge bunker 52, the fine grained 53 being mainly made up of semicoke is collected in granule capturing storehouse 54 after being trapped by multi-cyclone
It is interior, subsequently enter whirlwind dipleg 56.The coal gas of low dust content is then exported by pipeline 49 from one-level hydrogenation reactor.
Under conditions of operation temperature is 1300-1900 DEG C, by sufficient gasification reaction, oxygen-steam gasification furnace 12
The synthesis gas 9 of top output enters one-level hydrogasification stove 8.Crude synthesis gas 9 can enter one-level hydrogasification stove 8 after,
Cooled down by the semicoke logistics containing inert particle from catalytic hydrogenation gasification section 3 inputted through semicoke logistics pipeline 6；
It can be cooled down after the output one-level hydrogasification of crude synthesis gas 9 stove 8 by circulation synthesis gas 39 as shown in Figure 4.Entering
Enter before one-level hydrogasification stove 8, the temperature after the crude synthesis gas 9 after circulation synthesis gas 39 is cooled down is cooled down will be less than 1200
DEG C, preferably lower than 1100 DEG C.Although temperature of the crude synthesis gas 9 after circulation synthesis gas 39 is cooled down is less than ash fusion point, thick to close
Still it will not be fully cured into the slag particles entrained by gas 9.
It is to prevent when temperature is up to 1900 DEG C of crude synthesis gas 9 and one to the purpose that crude synthesis gas 9 is precooled
Solid bed in level hydrogasification stove generates larger clinker when contacting.By cooling, by circulation synthesis gas 39 and slightly
The mixing logistics that synthesis gas 9 is formed can be with the entrance one-level hydrogasification stove 8 of safety.
The porch of one-level hydrogasification stove 8, crude synthesis gas 9 can further with containing for being inputted through semicoke logistics pipeline 6
The semicoke logistics mixing of inert particle.After the mixing of this two streams, the temperature that the temperature of mixed material will be with reactor bed
Unanimously, all it is 800-950 DEG C.According to the temperature of the mixed mixing logistics of circulation synthesis gas 39 and crude synthesis gas 9, one-level hydrogenation
The mass ratio of the difference of gasifier operation temperature and pyrolysis oven operation temperature, semicoke logistics and said mixture stream is 0.4-5's
In the range of change.Feed coal 7 can also be added by synthesis gas entrance, rapidly can so be added the temperature heating of feed coal
The operation temperature of hydrogen gasification section, at utmost to improve the yield of methane and other hydrocarbon products and tar.Because the present invention's
Major product is exactly tar, therefore the higher the better for the yield of tar.
It is in advance that coal is quick with coming from hydrogenation before one-level hydrogasification stove coal if raw material coal is caking coal
The semicoke 6 of pyrolysis section is mixed, and semicoke and the mass ratio of fresh feed are 10~20 in mixture, so can be to greatest extent
Prevent the coking of viscous materials coal.In this case, from hydropyrolysis stove and come solid particle circulating ratio just by
Following several factors are determined：One is by entering the largest loop amount of solid that coal speed is determined；Two be to will come from oxygen-steam
The admixture of gas of gasification furnace 12 is cooled to the solid circle amount needed for the operation temperature of hydrogasification stove.When solid circle particle with
When bed temperature is less than the normal running temperature of gasification furnace after feed coal mixing, the amount of recyclegas will be cut down, so
Temperature into the crude synthesis gas in hydrogasification stove is about just 1000-1200 DEG C or so.
The slag that synthesis gas 9 is carried can be wrapped in the outer surface of bed particle, and this will cause the particle diameter of part bed than managing
Think that size is big.These, which will become big later bulky grain lime-ash logistics 17, to be discharged from bed.Any other is with solid circle
The bed that material enters bed can be extracted from same nozzle together with above-mentioned bulky grain lime-ash logistics 17, but be needed afterwards
Separated by screening or fluid suspended mode with bulky grain lime-ash logistics 17.Ash particle logistics 16 is delivered to by circulating air to be added
Hydrogen fast pyrogenation section 4 provides heat for the pyrolysis of coal.Feed coal 2 need to be also transported to and add to circulate synthesis gas as carrier gas
Hydrogen fast pyrogenation section 4.
The cone structure 38 of the bottom of one-level hydrogasification stove 8, its profile is to the inclined eccentric cone in side.Synthesis gas 9
Enter gasification furnace from its bottom left centre, and the bottommost that lime-ash and grey melt body particle are then located at cone from opposite side is arranged
Go out, in order to which grey melt body particle is separated with normal bed.When synthesis gas 9 enters one section together with circulating air logistics 39
After hydrogasification stove 8, the jet logistics of said two devices formation after being mixed with solid material will multilated, and this structure is set
Meter is that comparison is applicable for one-level hydrogasification stove.
Fluidized gas through cone fluidized gas entrance 82 also from cone 37 enter gasification furnace in, its act on be promote tapering position material
Fluidisation.
The operating pressure of one-level hydrogasification stove 8 is also at 40-100bar (4.0-10.0MPa), in order to improves and closes
The equilibrium concentration of methane into gas.Operating temperature range is 800-950 DEG C, and selecting this operating temperature range is based in synthesis gas
The consideration of the equilibrium concentration of methane and the kinetics equilibrium constant of methanation reaction.The gas phase superficial velocity of cone 37 is
0.3-0.7m/s, optimal superficial velocity is 0.3-0.5m/s.Superficial gas flow velocity in the body of heater 36 that broken-line expands is about
For 0.1-0.5m/s, above-mentioned two-part cross-sectional area ratio is between 1.5 to 3.
The reactivity of semicoke directly determines the height of emulsion zone 43 and fluid bed bed in one-level hydrogasification stove, and
The height of bed can influence residence time and concrete operations temperature of the semicoke in gasification furnace again, and (temperature range have to be between 800-
Between 950 DEG C).The residence time of semicoke particle should be controlled within 15min in one-level gasification furnace, be preferably controlled in 10min
Within.Gasification reaction (such as hydrogasification, steam and CO in gasification furnace2Gasification reaction etc.) carry out completely after to ensure semicoke
Charcoal percent conversion contained by grain is more than 65%, and optimal conversion is 75%.
When crude synthesis gas is exported from one-level hydrogasification stove 8, gas phase can carry a part of bed.Crude synthesis gas is by entrance
55 enter primary cyclone 44.Only shown in Fig. 4 in only two primary cyclones, actual design process,
In order to improve the arresting efficiency of solid particle, multiple primary cyclones are often designed.In order to balance one cyclonic separation
The particle capture efficiency of device 44 and crude synthesis gas treating capacity, the diameter of the cylinder 45 of one cyclonic point are advisable with 0.4-0.8m.Through
The solid particle logistics 41 that primary cyclone 44 is trapped will return to bed by the dipleg 42 of cyclone separator.
In highly preferred embodiment of the present invention, the solid particle logistics 41 trapped on primary cyclone dipleg 42 is circulated
The position for returning to bed has also given indicating in Fig. 4.The solid particle logistics of primary cyclone trapping will return to cone
It is cyclone separator that the distance between position and the cone inwall of the outlet of solid optimum value is returned on the bed at 37 positions, dipleg
2-4 times of dipleg diameter, only in this way can just ensure that the output of dipleg position solid material is more steady.Due to bed center
The superficial velocity of area's gas is higher than solid material, thus causes the bulk density of bed center bed relatively low.In gravity
Under effect, the solid material that inner loop is returned will flow to bed center along the inwall of cone 37.Avoid synthesizing air-flow with this
To whirlwind dipleg, so as to overcome the cyclone separator operation troubles caused by gas is flowed up in dipleg.
The crude synthesis gas 47 exported by primary cyclone 44 can carry the semicoke fine grained of some collection at large, these
Fine grained will enter the gas access surge bunker 52 of multicyclone 48 by the outlet 46 at the top of cyclone separator.It is many
Pipe cyclone separator 48 contains the small cyclones separator unit 51 for being much usually used in fine ash trapping.It is main by semicoke constitute it is thin
Particle 53 will be collected uniformly in granule capturing storehouse 54 after being trapped by multi-cyclone, then enter back into whirlwind dipleg 56.Whirlwind
Dipleg 56 stretches into dipleg 58 to prevent that gas backwash from entering cyclone dip-leg.As shown in figure 4, multicyclone
The semicoke particle 57 of 48 trappings final will enter one-level hydrogasification stove 8 collectively as circulating granular.
Even if extending the residence time, the carbon contained by semicoke is still difficult to be converted completely, as shown in Figure 4, it is necessary to pass through
The semicoke logistics 18 of part is extracted in the material sealing of multicyclone out.In order to ensure the stable output of solids stream, pass through
Circulate synthesis gas pipeline 83 and added to dipleg 58 and loosen gas.The semicoke logistics 18 and crude synthesis gas extracted out by dipleg 58-thin
The solid particle that particle is separated and semicoke revert system 20 is trapped enters oxygen-steam gasification furnace together after converging.Purification synthesis
Gas leaves multi-cyclone piece-rate system by the guiding gutter 49 at the top of multi-cyclone, and one-level hydrogasification stove is left in final logistics 5.It is whole
Connection between outer wall 50 and gasification stove internal wall 36 that individual cyclone separation system and gasification furnace pass through guiding gutter 49 and became one.
Space between multi-cyclone system 48 and gasification stove internal wall 36 suppresses the accumulation of dust by circulating the purging of synthesis gas.
Referring to Fig. 5, the hydrogenation fast pyrogenation section 4 of catalytic hydrogenation gasification-hydropyrolysis integrated apparatus 86 of the invention
Riser is connected with feed coal 2, and pyrolysis section outlet is connected with the entrance of pyrolysis oven primary cyclone 67, the pyrolysis gas of output
Left from the top of primary cyclone 67 and enter pyrolysis oven secondary cyclone 59 after cyclone separator, two grades of rotations of pyrolysis oven
The pyrolysis gas logistics 14 that wind separator 59 is isolated is separated through pipeline with crude synthesis gas-fine grained and semicoke revert system 20 is connected
Logical, the semicoke logistics that pyrolysis oven secondary cyclone 59 is captured is entered into the rear portion of dipleg 60 by solids stream passage 61
Fast pyrogenation section 4 is hydrogenated with, another part semicoke logistics pipeline 6 is connected with one-level hydrogasification stove 8, pyrolysis oven one cyclonic point
The solid circle logistics isolated from device 67 through upright dipleg 65 respectively with catalytic hydrogenation gasification section 3, hydrogenation fast pyrogenation 4 phases of section
Even, and on upright dipleg 65 it is further opened with the entrance with loosening gas 84,87 feed-lines are connected.
From the point of view of the change of bed material position line 64, the solid circle logistics 63 into bed bottom is raised air-flow band again
Go out bed.The coupling of the mixing of material or fluid bed and fixed bed is by bed particle diameter and gas phase apparent velocity in bed
Control to realize.Optimal catalyst carrier is metallurgical coke, and the active component of catalyst is alkali metal or alkaline-earth metal,
Its average grain diameter is 3-6mm.Why coke is suitable catalyst carrier, be because itself have higher intensity, it is good
Good anti-wear performance and heat endurance.At the same time, due to the fine grained produced by the abrasion of coke granule can oxygen-
Gasify in steam gasification stove without producing solid waste.Other inert particles also can as catalyst carrier.
The average grain diameter for the solid particle being circulated by upright dipleg 65 is 80-100 μm.Gas phase is apparent in bed
Flow velocity is the residence time of gas phase in 0.3-0.7m/s, the emulsion zone bed of catalytic hydrogenation gasification-hydropyrolysis integrated apparatus 86
For 10-30s.The superficial gas velocity of this scope is selected, is because catalyst granules will not be carried over bed and only solid circle
Grain can be carried over bed.
The operating temperature range of catalytic hydrogenation gasification-hydropyrolysis integrated apparatus 86 is 550-700 DEG C, optimum operation temperature
Spend for 550-650 DEG C.40-100bar (4.0-10.0MPa) operating pressure with relatively low operational temperature conditions, in catalysis
Under the catalytic action of agent, the equilibrium concentration of methane can reach 20-35mol%.Operating pressure is higher, methane in synthesis gas
Concentration is also higher.As shown in figure 5, the circulating ratio of solid circle logistics 63 can be adjusted by controlling the loosening flow of gas 84, most
Effective control to catalytic hydrogenation gasification-temperature of hydropyrolysis integrated apparatus 86 can be realized eventually.The methane containing higher concentration
Synthesis gas, which leaves, enters pyrolysis oven after catalytic hydrogenation gasification-hydropyrolysis integrated apparatus 86.The synthesis gas from one-level first with revolving
The upright dipleg of wind separator and come solids stream 66 mix, the mixing logistics formed is upright with secondary cyclone again
The solids stream 61 of dipleg is mixed.The temperature of above-mentioned solids stream and self-catalysis hydrogasification stove and the gas-solid mixture come
Material is roughly the same.
As shown in figure 5, fresh feed coal 2 is added from the riser of pyrolysis oven.The particle diameter of fresh feed coal 2 is less than 800 μm,
Average grain diameter is 150-200 μm.If using binding coal as charging, charging need to be in another tank body with pyrolysis oven bed
It is pre-mixed, it is desirable to which the concentration of inert particle is between 90-95% in mixture, to prevent pyrolytic process coking.Described
Pyrolysis oven, which is preferably one, has the circulating fluid bed reactor of higher bed density.The solid circle circulated by riser with
The mass flow ratio scope of feed coal is 100-200, can ensure that material has higher heating in pyrolysis oven riser with this
Speed.The apparent velocity scope of gas phase is 6-15m/s in pyrolysis oven riser, and the residence time of gas phase is 1-10s, and optimal stops
It is 2-4s to stay the time.Be rapidly heated and hydrogen atmosphere under the conditions of, by pyrolytic reaction, coal particle will be converted into tar steam
And gaseous lighter hydrocarbons product such as methane, ethane etc..Kept for the shorter residence time thermal decomposition product can be avoided to occur polymerization green coke anti-
Should.It is well known that the semicoke that pyrolytic reaction is produced is the catalyst that polymerisation and then coking occur for thermal decomposition product tar.Although
Gas with gasification reactivity such as CO2,H2O、H2Catalytic activity of the semicoke to tar polymerisation can be passivated.The present invention is adopted
With largely further reducing by half in solid circle by the circulation dilution effect for the solid particle that inert component is constituted in coal ash
Burnt concentration.
The gas-solid mixture stream for leaving hydrogenation fast pyrogenation 4 risers of section enters after gasification furnace primary cyclone 67
The separation of almost all of inert particle and gas phase can be achieved.Only semicoke particle of the particle diameter more than 30 μm just can be by one cyclonic
Separator is captured.Although the average particle size range of pyrolysis oven feed coal is 150-200 μm, the 40- produced by pyrolysis oven
The particle diameter of 50% semicoke particle is less than 30 μm.Inert particle and the larger semicoke particle of part particle diameter are under gravity
It will be circulated along upright 65 points of two-way of dipleg：It is recycled back into all the way and urges two grades of gasification hydrogasification stoves 3, pyrolysis is recycled back into all the way
The bottom of stove 4, above-mentioned circulation returning charge route and equipment are shown in Fig. 5.
The fine grain synthesis gas in part is carried, is left from top and enters secondary cyclone 59 after cyclone separator,
Semicoke particle of most of particle diameters more than 10 μm will be captured in cyclone separator.The semicoke that secondary cyclone is captured
Drop enters dipleg 60 to grain under gravity.As shown in figure 5, the logistics of fraction semicoke particle composition is through solids stream passage
61 will be recycled back into the riser of hydrogenation fast pyrogenation section 4.Most semicoke logistics will be recycled back into one-level through semicoke logistics pipeline 6
Hydrogasification stove.Although Fig. 5 only shows a primary cyclone and a secondary cyclone, while also providing
The schematic diagram of dipleg and upright materials in the tube leg.But the engineers and technicians for being familiar with this technique list can also be in every one cyclonic
Several cyclone separators are set up in centrifugal station.Further, it is also possible to which all cyclone separators are fixed on into same pressure
In container, and solid particle is allowed to assemble out of this pressure vessel and be circulated by dipleg.
Referring to Fig. 6, crude synthesis gas-fine grained separation of the invention and semicoke revert system 20 include and pyrolysis gas logistics
14th, the connected anti-material cyclone separator 75 being made up of several unit cyclone separators 68 of circulating air, counter to expect cyclone separator
75 synthesis gas streams 21 isolated by the road with solution-air, liquid-liquid separation unit 22 is connected, and anti-material cyclone separator 75 is caught
The dust obtained enters the wall 72 of filtering tank 70 by guiding gutter 74 and skirt is enclosed in 71 annular spaces 76 surrounded, the upper end of filtering tank 70
It is cone 73 to be provided with filter core 69, lower end, and gas phase 77 flows up into the formation synthesis gas stream 85 of filter core 69 and discharged, semicoke thing
Stream 78 enters feed hopper 80 along mozzle 79, and the semicoke logistics 19 formed in feed hopper 80 sends into oxygen-steam gas along pipeline
Change stove 12.
Pyrolysis oven heat outputting cracked gas stream 14 will be quenched circulating air 15 first and be cooled down, Quench circulating air described herein
15 come from same recycle gas compressor with loosening the circulating air of gas as other equipment, herein it is emphasized that pyrolysis gas
Logistics 14 just should before the unit cyclone separator 68 being introduced into crude synthesis gas-fine grained separation and semicoke revert system
It is cooled.It is 400-450 DEG C to synthesize the optimum temperature range after air cooling, and at this temperature, the polymerization green coke of tar component is anti-
It is able to should be completely prevented, while the condensation of tar and other oils products in gas phase can also be prevented.Preventing tar condensing is
The lower limit of synthesis gas chilling temperature.
Gravity and carrier gas down direction sweep along the collective effect of power under, the anti-material cyclone separator 75 individually set up
The dust of capture will enter filtering tank 70 by guiding gutter 74.Dust logistics enters the wall by filtering tank 70 by guiding gutter 74
72 enclose in 71 annular spaces surrounded with skirt.The dust of entrainment portions gas will flow downward into above-mentioned annular space region.In cone
73 positions, gas phase 77 will flow up into filter core 69, and filter core described herein more suitable material is ceramics or sintered gold
Category.Synthesis gas after dedusting is by two grades of scrubbing towers in synthetic gas cleaning system, or is to reach that synthesis gas stream 85 is washed
Mixed in the gas-liquid separation system for purifying purpose and individually setting up with synthesis gas.The synthesis gas gone after tar removing will enter gas
Body cleaning system.Semicoke logistics 78 enters feed hopper 80 along mozzle 79 under gravity.
Under usual conditions, feed hopper 80 needs to prepare two sets：One of them normal charging operating mode, and another is then received and
The semicoke of inherent filtration tank.In addition, two feed hoppers can also right angle setting：One be lock hopper another be feed hopper.It can use
Superheated steam or circulating air 81 convey semicoke into oxygen-steam gasification furnace 12.
The content of semicoke enters solution-air, liquid-liquid separation less than 100ppm in synthesis gas stream 21 after gas-particle separation
Device 22.In highly preferred embodiment of the present invention, into solution-air, liquid-liquid separation device 22 has two-stage wash mill, and one-level is
Traditional Venturi scrubber, one-level is such as filled out for the gas-liquid contact apparatus of condensation separation tar and water from gas phase in addition
Expect tower.The operating temperature range of one-level washer is 375-400 DEG C, and main purpose is to remove the dust and heavy oil entrained by gas phase
Component.Two grades of scrubbing towers are then to remove the most of tar and moisture carried in synthesis gas.The typical operation temperature of two grades of scrubbing towers
It is 25-40 DEG C to spend scope.
Separating obtained product liquid can also further carry out isolation of purified in solution-air, liquid-liquid separation system 22.Oil-water
Separation is mainly realized by way of gravitational settling.Different component in tar can be proceeded point by common rectifying mode
From.Heavy oil containing dust can be sent to gasification in oxygen-steam gasification furnace and produce synthesis gas.The synthesis gas after rectifying column is separated
In entrained light oil can pass through such as the activated carbon adsorption bed progress vapor-liquid two phases separation of other common modes.As shown in Figure 1
Oil product 24 obtained by recovery mainly includes aromatic hydrocarbons and light-end products such as diesel oil and kerosene component.Separating obtained water 23 can conduct
Refrigerant, on the one hand can be as process cooling water, and still further aspect is alternatively arranged as the chilled water of lime-ash.Separating obtained water 23
The ammonia and phenols of middle dissolving can be reclaimed by way of multistage flash evaporation or air lift.The chemicals that the above method is reclaimed is such as
Ammonia and phenols can also be further processed into chemical products.Or, without purification, these chemical products can directly oxygen-
Gasified to produce synthesis gas in steam gasification stove.
Further reclaimed in gas purge system 27 as shown in figure 1, going the primary purifying synthesis gas 2 after tar removing to enter
CO2With H2S.The CO that gas purge system is reclaimed2With H2S leaves further handled through downstream after gas purge system 27 after can be with
CO for producing high-purity2Level sulfur-bearing chemical products.In most cases, without being converted CO by synthesis gas transformationreation
For CO2, because 550-700 DEG C of synthesis gas transformationreation has reached chemical balance.In other words, gasify and add in secondary hydrogenation
In hydrogen pyrolysis reactor, synthesis gas transformationreation has reached balance.And substantial amounts of CO quilts in secondary hydrogenation gasification furnace
It is converted into methane.Therefore without setting up a synthesis gas shift-converter again.Synthesis gas after purification finally will also enter low temperature
Condensate separation system is with the light hydrocarbon products such as further separation of methane, ethane 29.Mainly contain H2And CO synthesis gas 26 will be recycled back to
Hydrogasification stove is as gasifying agent and loosens gas.
Natural gas from coal of the present invention and the method for light oil are as follows：By steam stream 10, oxygen stream 11 constitute gasifying agent with
Semicoke logistics 19 carries out gasification reaction in oxygen-steam gasification furnace 12, and produced lime-ash 13 is by oxygen-steam gasification furnace 12
Bottom ash discharging hole is discharged, produced synthesis gas 9 directly on be advanced into one-level hydrogasification stove 8, one-level hydrogasification stove 8 is produced
The descending oxygen-steam gasification furnace 12 that returns of raw semicoke logistics 18 proceeds gasification reaction, and the logistics 17 of bulky grain lime-ash is by one
The bottom discharge of level hydrogasification stove 8, ash particle logistics 16 is recycled into hydrogenation fast pyrogenation section 4, feed coal 7 and circulating air 26 and
The synthesis gas 9 come from oxygen-steam gasification furnace 12 is reacted in one-level hydrogasification stove 8, the institute of one-level hydrogasification stove 8
The synthesis gas of the methane containing higher concentration produced is by being advanced into catalytic hydrogenation gasification-hydropyrolysis on synthesis gas stream pipeline 5
Integrated apparatus 86, fresh feed coal 2 enters after catalytic hydrogenation gasification-hydropyrolysis integrated apparatus 86, to be hydrogenated with from one-level
The synthesis gas of the methane containing higher concentration of the top of gasification furnace 8 output and the high-temperature solid particle swept along carry out being pyrolyzed instead as thermal source
Should, semicoke logistics pipeline 6 of being passed through under pyrolysis char and inert particle enters one-level hydrogasification stove 8, catalytic hydrogenation gasification-hydrogenation
The pyrolysis gas logistics 14 that 86 outputs are put in thermal decomposition integrated makeup enters back into crude synthesis gas-fine grained point after the cooling of Quench circulating air 15
From and semicoke revert system 20 carry out the initial gross separation purified treatment of synthesis gas, the separation of crude synthesis gas-fine grained and semicoke returning charge
The semicoke logistics 19 that system 20 is trapped is recycled back into oxygen-steam gasification furnace 12, and synthesis gas stream 21 enters solution-air, liquid-liquid point
From unit 22, separating obtained liquid product is respectively water 23 and tar 24, and solution-air, the warp that liquid-liquid separation unit 22 is exported is removed
Oil, 25 points of the primary purifying synthesis gas stream of dewater treatment are two branch roads：Circulating air logistics 39 is recycled back into as Quench gas
Mixed with the synthesis gas 9 of the top of oxygen-steam gasification furnace 12 output, remaining decontaminating syngas then enters gas purge system
27, the purified gas produced by gas purge system 27 is divided into two bursts of outputs, and one returns to one-level hydrogasification as circulating air 26
Stove 8 and crude synthesis gas-fine grained separation and semicoke revert system 20, wherein returning, crude synthesis gas-fine grained is separated and semicoke is returned
The circulating air of material system 20 is used for the Quench gas of pyrolysis gas logistics 14；And gas phase hydrocarbon of another stock based on methane is then as most
Finished product 29 is exported, separating obtained CO2、H2S mixing logistics 28 goes successively to downstream and separated and advanced treating.
Claims (10)
1. the device of a kind of natural gas from coal and light oil, it is characterised in that：Including being connected with raw coal conduit by catalytic hydrogenation
Gasification section (3) and hydrogenation fast pyrogenation section (4) constituted catalytic hydrogenation gasification-hydropyrolysis integrated apparatus (86), oxygen-
The separation of steam gasification stove (12), one-level hydrogasification stove (8), crude synthesis gas-fine grained and semicoke revert system (20), solution-air,
Liquid-liquid separation unit (22), gas purge system (27)；
The semicoke logistics pipeline (6) of catalytic hydrogenation gasification-hydropyrolysis integrated apparatus (86) and one-level hydrogasification stove (8) phase
Connection, synthesis gas stream pipeline (5) and the catalytic hydrogenation gasification-hydropyrolysis integrated apparatus of one-level hydrogasification stove (8)
(86) it is connected, the pyrolysis gas logistics (14) that catalytic hydrogenation gasification-hydropyrolysis integrated apparatus (86) is exported is through pipeline and slightly
Synthesis gas-fine grained separation and semicoke revert system (20) are connected, crude synthesis gas-fine grained separation and semicoke revert system
(20) synthesis gas stream (21) is connected with solution-air and liquid-liquid separation unit (22) by the road, solution-air and liquid-liquid separation list
Three tunnels of outlet point of first (22), respectively separating obtained water (23), reclaim obtained by oil product (24) and with gas purification system
The primary purifying synthesis gas stream (25) that system (27) is connected, through the CO obtained by gas purge system (27) purification separation2、H2S is mixed
Compound stream (28) goes successively to downstream and separated and advanced treating, and the methane after separation and other gas phase alkane are used as product
(29) export, the CO and H of gained after separation2One-level hydrogasification stove (8) and crude synthesis gas-fine grained point are returned as circulating air
From and semicoke revert system (20)；The bulky grain lime-ash logistics (17) of one-level hydrogasification stove (8) is discharged through pipeline, semicoke logistics
(18) it is connected through pipeline with oxygen-steam gasification furnace (12), the synthesis gas (9) of output at the top of oxygen-steam gasification furnace (12)
It is connected through pipeline with one-level hydrogasification stove (8), primary purifying synthesis gas stream (25) is also through circulating air logistics (39) with closing
Pipeline into gas (9) is connected, and the stove material that enters of oxygen-steam gasification furnace (12) is respectively steam stream (10), oxygen stream
And crude synthesis gas (11)-fine grained separation and the semicoke logistics (19) of semicoke revert system (20) discharge, oxygen-steam gasification furnace
(12) outlet is slag (13) pipeline.
2. the device of natural gas from coal according to claim 1 and light oil, it is characterised in that：Described oxygen-steam gas
Change the gasification section (30) of stove (12) using dip down inclined structure, semicoke logistics (19), steam stream (10), oxygen stream (11)
Tangentially enter gas-slag knockout drum (31) by being injected tangentially gasification section (30) mix products, lime-ash (34) enters gas-slag knockout drum
(31) bottom, the grey solid impurity particle (33) obtained by the trapping of gas-slag knockout drum (31) flows downward along inwall, chilled water (32) from
Gas-slag knockout drum (31) bottom is added, and knockout drum (31) is left in the position of addition below gas-slag mixture inlet
Synthesis gas (9) enters one-level hydrogasification stove (8).
3. the device of natural gas from coal according to claim 1 and light oil, it is characterised in that：Described oxygen-steam gas
Change the gasification section (30) of stove (12) using direction vertically downward, semicoke logistics (19), steam stream (10), oxygen stream (11)
Gasification section (30) is injected tangentially, gas phase is downwardly into linkage section (35) with lime-ash cocurrent, in linkage section (35) slag (34) downwards
Duct bottom slag-drip opening is gradually flowed into, linkage section (35) tangentially enters gas-slag knockout drum (31), gas-slag knockout drum (31) trapping
The grey solid impurity particle (33) of gained is flowed downward along inwall, and chilled water (32) is added from gas-slag knockout drum (31) bottom, is added
Position below gas-slag mixture inlet, leave knockout drum (31) synthesis gas (9) enter one-level hydrogasification stove (8).
4. the device of natural gas from coal according to claim 1 and light oil, it is characterised in that：Described one-level hydrogasification
Stove (8) includes cone structure (38), and cylinder (40) upper end of cone structure (38) vertical direction is additionally provided with for connecting body of heater
(36) beveling to cone (37), the bottom of cone structure (38) is connected with semicoke logistics pipeline (6), raw coal conduit (7)
Logical, its profile is intilted eccentric cone, and synthesis gas (9), circulating air logistics (39) are entered by its bottom side centre
Enter one-level hydrogasification stove (8), and bulky grain lime-ash logistics (17), ash particle logistics (16) are then from the bottommost of opposite side cone
Discharge and can be recycled to hydrocracking section (4), emulsion zone (43) is arranged above positioned at cone (37) in body of heater (36),
Body of heater (36) circumference is provided with several primary cyclones (44) in emulsion zone, on primary cyclone (44)
End is additionally provided with the multicyclone (48) being connected with the outlet (46) of primary cyclone (44), multi-cyclone point
The synthesis gas stream separated from device (48) is connected through guiding gutter (49) with synthesis gas stream conveyance conduit (5), in multi-cyclone point
Lower end from device (48) is provided with dipleg (58), and the whirlwind dipleg (56) of multicyclone (48) stretches into dipleg (58)
In, the semicoke particle (57) of the one outlet of dipleg (58) enters bed as circulating granular, and one of dipleg (58) goes out
The semicoke particle (18) of mouth is added to oxygen-steam gasification furnace (12) as fuel.
5. the device of natural gas from coal according to claim 4 and light oil, it is characterised in that：Described cone structure (38)
Discharge bulky grain lime-ash logistics (17), the side of semicoke logistics (18) are further opened with fluidized gas entrance (62)；The side of cone (37)
Offered on wall and be connected with fluidized gas on cone fluidized gas entrance (82), dipleg (58) and be passed through pipeline (83).
6. the device of natural gas from coal according to claim 4 and light oil, it is characterised in that：Described one cyclonic separation
A diameter of 0.4-0.8m of device (44) top cylinder (45), the crude synthesis gas of generation tangentially enters one cyclonic point by entrance (55)
From device (44), the solid particle (41) of primary cyclone (44) trapping returns to bed by the dipleg (42) of cyclone separator
Layer, and the distance between position and cone (37) inwall of dipleg (42) outlet are 2-4 times of whirlwind dipleg (42) diameter.
7. the device of natural gas from coal according to claim 4 and light oil, it is characterised in that：Described multi-cyclone separation
Device (48) includes some groups of small cyclones separator units (51), and thin of semicoke is contained after primary cyclone gas-particle separation
The gas that the crude synthesis gas (47) of grain enters multicyclone (48) by the outlet (46) at the top of cyclone separator enters
Mouth surge bunker (52), the fine grained being mainly made up of semicoke (53) is collected after being trapped by multi-cyclone in granule capturing storehouse (54)
It is interior, dipleg (58) is then entered by whirlwind dipleg (56).
8. the device of natural gas from coal according to claim 1 and light oil, it is characterised in that：Described catalytic hydrogenation gas
The riser of hydropyrolysis section (4) interior pyrolysis oven of change-hydropyrolysis integrated apparatus (86) is connected with feed coal (2), former
Material coal (2) is conveyed by conveying gas (1), is divided into two branch roads, and a branch road enters catalytic hydrogenation gasification-hydropyrolysis one
The hydrogenation fast pyrogenation section (4) of (86) is put in body makeup, and another branch road enters one-level hydrogasification stove (8), is hydrogenated with fast pyrogenation
The pyrolysis gas of output is connected with pyrolysis oven primary cyclone (67) entrance at the top of section (4), from the separation of pyrolysis oven one cyclonic
Left at the top of device (67) and enter pyrolysis oven secondary cyclone (59), pyrolysis oven secondary cyclone after cyclone separator
(59) the gas-solid mixing logistics (14) of output separates through pipeline with crude synthesis gas-fine grained and semicoke revert system (20) is connected
Logical, the semicoke logistics of pyrolysis oven secondary cyclone (59) capture enters dipleg (60) rear portion by solids stream passage
(61) catalytic hydrogenation gasification-hydropyrolysis integrated apparatus (86) is recycled back into, the logistics of another part semicoke is through pipeline (6) and one
Level hydrogasification stove (8) entrance is connected, carbonaceous solid particulates (63) warp that pyrolysis oven primary cyclone (67) is isolated
Upright dipleg (65) is recycled back into hydrogenation fast pyrogenation section (4), meanwhile, in order to ensure the circulating ratio of solid circle, with adding
It is further opened with the upright dipleg (65) that hydrogen fast pyrogenation section (4) is connected with loosening the entrance that gas (84) is connected；
Catalytic hydrogenation gasification section (3) is the particle that material is loaded with gasification catalysis active component in fluidized-bed reactor, bed, synthesis
Gas logistics (5) and the semicoke logistics (63) returned from hydrogenation fast pyrogenation section are mixed, while carrying out gas phase and gas-solid two alternate
Hydrogenation methanation reaction.
9. the device of natural gas from coal according to claim 1 and light oil, it is characterised in that：Described crude synthesis gas-thin
Particle is separated and semicoke revert system (20) with pyrolysis gas logistics (14), circulation synthesis gas (26) including being connected by several lists
The returning charge cyclone separator (75) of first cyclone separator (68) composition；The built-in efficient filter core being connected with dust guiding gutter (74)
Gas-solid filtering tank (70)；The hopper (80) being connected with filtering tank (70) outlet at bottom mozzle (69), returning charge cyclonic separation
The synthesis gas stream (21) of device (75) bottom output is connected with gas-particle separation unit (22) by the road, returning charge cyclone separator
(75) dust of capture enters the annular space surrounded by the wall (72) of filtering tank (70) with skirt (71) by guiding gutter (74)
In region (76), it is cone (73) that filtering tank (70) upper end, which is provided with filter core (69), lower end, and gas phase (77) flows up into filter
Core (69) formation synthesis gas stream (85) discharge, semicoke logistics (78) enters feed hopper (80) along mozzle (79), in feed hopper
(80) the semicoke logistics (19) formed in enters oxygen-steam gasification furnace (12) along pipeline.
10. it is a kind of such as the method for the natural gas from coal and light oil of any one device in claim 1-9, it is characterised in that：By
Steam stream (10), oxygen stream (11) composition gasifying agent and semicoke logistics (19) are carried out in oxygen-steam gasification furnace (12)
Gasification reaction, produced lime-ash (13) is discharged by oxygen-steam gasification furnace (12) bottom ash discharging hole, produced synthesis gas
(9) directly on be advanced into one-level hydrogasification stove (8), the semicoke logistics (18) produced by one-level hydrogasification stove (8) is descending to be returned
Return oxygen-steam gasification furnace (12) and proceed gasification reaction, bulky grain lime-ash logistics (17) is by one-level hydrogasification stove (8) bottom
Portion is discharged, and with circulating air (26) and from oxygen-steam gasification furnace (12), next synthesis gas (9) is hydrogenated with feed coal (7) in one-level
Reacted in gasification furnace (8), the synthesis gas of the methane containing higher concentration produced by one-level hydrogasification stove (8) passes through synthesis gas
Catalytic hydrogenation gasification-hydropyrolysis integrated apparatus (86) is advanced on logistics pipeline (5), fresh feed coal (2) enters catalysis
After hydrogasification-hydropyrolysis integrated apparatus (86), with the first containing higher concentration of the output from the top of one-level hydrogasification stove (8)
The synthesis gas of alkane and the high-temperature solid particle swept along carry out passing through under pyrolytic reaction, pyrolysis char and inert particle partly as thermal source
Burnt logistics pipeline (6) enters one-level hydrogasification stove (8), catalytic hydrogenation gasification-hydropyrolysis integrated apparatus (86) output
Pyrolysis gas logistics (14) enters back into crude synthesis gas-fine grained separation and semicoke revert system after being cooled down through Quench circulating air (15)
(20) the initial gross separation purified treatment of synthesis gas is carried out, what crude synthesis gas-fine grained separation and semicoke revert system (20) were trapped
Semicoke logistics (19) is recycled back into oxygen-steam gasification furnace (12), and synthesis gas stream (21) enters gas-particle separation unit (22),
Separating obtained liquid product is respectively water (23) and tar (24), gas-liquid separation unit (22) output through oil removing, dehydration at
The primary purifying synthesis gas stream (25) of reason is divided into two branch roads：Circulating air logistics (39) is recycled back into and oxygen as Quench gas
The synthesis gas (9) of output is mixed at the top of gas-steam gasification stove (12), and remaining decontaminating syngas then enters gas purge system
(27), the methane and other gas phase hydrocarbons produced by gas purge system (27) are used as output of products；CO and H2It is used as circulating air
Return to one-level hydrogasification stove (8) to separate with crude synthesis gas-fine grained and semicoke revert system (20), wherein returning to thick synthesis
The circulating air of gas-fine grained separation and semicoke revert system (20) is used for the Quench gas of pyrolysis gas logistics (14)；Separating obtained
CO2、H2S mixing logistics (28) goes successively to downstream and separated and advanced treating.
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| CN107099319B (en) * | 2017-05-27 | 2018-09-28 | 李大鹏 | It is a kind of to synchronize the device and method for producing methane rich synthesis gas and light tar |
| CN107353936B (en) * | 2017-09-04 | 2019-12-24 | 东华工程科技股份有限公司 | A purification and separation system and process for hydrogenation gasification synthesis gas |
| CN110467943B (en) * | 2018-05-11 | 2022-04-15 | 成都聚实节能科技有限公司 | Method for preparing natural gas, olefin and coal tar from coal |
| CN109054903B (en) * | 2018-08-24 | 2021-04-16 | 新奥科技发展有限公司 | Coal hydro-gasification method and device |
| CN109453824B (en) * | 2018-11-15 | 2021-09-10 | 新奥科技发展有限公司 | Catalyst loading method and catalytic hydro-gasification method |
| CN112625757B (en) * | 2019-09-24 | 2025-07-25 | 中国石油化工股份有限公司 | Device and method for fluidized catalytic gasification of pulverized coal |
| CN110921626A (en) * | 2019-12-04 | 2020-03-27 | 上海浦江特种气体有限公司 | Oil removing and filtering system for gas |
| CN112646609B (en) * | 2021-02-02 | 2025-03-18 | 上海浦合绿碳清洁能源科技有限公司 | A device and method for producing hydrogen by biomass gasification |
| CN115261079B (en) * | 2022-08-25 | 2023-08-15 | 西安交通大学 | A circulating fluidization device and method for preparing synthesis gas |
| CN117106489B (en) * | 2023-10-23 | 2024-02-20 | 西子清洁能源装备制造股份有限公司 | Device and method for producing synthetic gas by three-stage pyrolysis and gasification of organic solid waste |
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