CN105238447A - Apparatus and method for preparing natural gas and light oil from coal - Google Patents

Apparatus and method for preparing natural gas and light oil from coal Download PDF

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CN105238447A
CN105238447A CN201510598202.5A CN201510598202A CN105238447A CN 105238447 A CN105238447 A CN 105238447A CN 201510598202 A CN201510598202 A CN 201510598202A CN 105238447 A CN105238447 A CN 105238447A
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gas
semicoke
logistics
gasification
oxygen
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CN105238447B (en
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李大鹏
刘国海
王宁波
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Abstract

The invention relates to an apparatus and a method for preparing natural gas and light oil from coal. The apparatus comprises an oxygen-steam gasification furnace, a primary hydrogenation gasification furnace, a catalytic hydrogenation gasification-hydrogenation pyrolysis integration device, a gas-solid separator and a coal gas purification system. The primary hydrogenation gasification furnace can trap all semi-coke and prolongs the stay time of semi-coke particles in a hydrogenation gasification segment; and the content of methane in a gas phase can reach or approach a balance concentration through prolonging the stay time of synthetic gas in a low temperature zone in the catalytic hydrogenation gasification process. Hydrogenation rapid pyrolysis of coal is convenient for producing an oil product. A pyrolysis gas output by a hydrogenation rapid pyrolysis segment is cooled through a chilling circulating gas to inhibit tar polymerization side reactions carried out under the catalysis of semi-coke. Dust-containing crude synthetic gas goes through a crude synthetic gas-fine particle separation and semi-coke return system to remove solid particles in the synthetic gas. The dedusted and purified synthetic gas goes through a gas-solid separation unit to further condense the oil product in the gas phase. Acidic gases and CO2 in the gas-liquid separated purified gas are further removed. The purified synthetic gas is processed through a methane separation technology to obtain methane.

Description

The device and method of a kind of coal preparing natural gas and light oil
Technical field
The present invention relates to a kind of device and method synthesizing gasification and fast pyrogenation integration, the particularly device and method of a kind of coal preparing natural gas and light oil.
Background technology
Integrated having it long ago is carried out in hydrogasification and oxygen-steam gasification technology, similar by hydropyrolysis and gasification integral process produce oil product, synthetic gas, Sweet natural gas technique be also well known.
In coal preparing natural gas field, once recommended in existing technical literature to adopt two-stage gasifier as unstripped gas device for making.Wherein representative is exactly the two stage pressurization airflow bed gasification furnace being called as Bi-gas technique.This vapourizing furnace is the technology developed by bituminous coal institute of the U.S. between 1960 ~ 1970 years.(referring to paper DOE/METC/SP-1DE858).In this technique, the semicoke particle of secondary reformer trapping returns primary reformer and water vapor and oxygen reaction for producing synthesis gas.The service temperature of one section of vapourizing furnace is about 3000 °F (1648.89 DEG C), and adopts slag deslagging.The synthetic gas that primary reformer produces is using the thermal source as secondary reformer.Coal and water vapor carry out hydrogasification to produce SNG after adding secondary reformer.The service temperature of secondary reformer is about 1700 °F (927 DEG C).Crude synthesis gas enters the separation carrying out gas-solid two-phase in cyclonic separator after being cooled to 800 °F (427 DEG C) again.Subsequently, synthetic gas carries out methanation again in order to produce SNG after purification, transformationreation.Synthetic gas after part purification also will circulate and return vapourizing furnace.Above-mentioned two-stage gasifier still has a lot of area for improvement.Such as: in entrained-flow reactor, the mixed effect of material is poor, under the temperature of reaction of 1700 °F (927 DEG C), mixing of materials poor effect may cause the generation of tar (about less than 1%), and in synthetic gas the tar of lower concentration substantially without recovery value.The value that its investment and running cost can be brought far above the so a small amount of tar of recovery.Because in coal gas, methane concentration is lower (being less than 10%), this technique must have synthetic gas methanator.
United States Patent (USP) 3,779,725 improve above-mentioned Bio-Gas technique.Technology disclosed in this patent attempts to save methanator.By from decontaminating syngas, isolate methane and by purification after effective gas (CO+H 2) loop back in secondary reformer and carry out hydrogasification reaction.Because the equilibrium methane concentration in synthetic gas reduces with the rising of temperature of reaction system.When reactor temperature is 1700 °F (927 DEG C), the methane concentration in synthetic gas is below 10%.In fact, according to " chemistry of coal utilization " (" chemistry of coal utilization-second edition additional issue ", editor MartinElliott) content disclosed by P1722 ~ 1723, the methane concentration in the Bi-Gas pilot plant institute production of synthetic gas of 5t/h coal feeding amount only has 4.3%.The methane content of lower concentration like this, is just needed to be separated with other synthesis gas componentses by methane by the mode of cryogenic condensation, then the synthetic gas after separation of methane is looped back vapourizing furnace.Thus one, what this technique just became in economy does not have feasibility.Meanwhile, also can containing a small amount of tar in the waste water that gasification produces, these waste water containing tar also need the flow process more grown to carry out subsequent disposal.
Another is exactly that to adopt take fluidized-bed reactor as the multi-stek hydrogenation gasifying process of core for effective trial that Bi-Gas gasifying process carries out improving, hydrogasification is coupled efficiently with steam gasification process, because the mixed effect of material is better than entrained-flow reactor in fluidized-bed reactor.Hydrogenation synthesis gasifying process as HYGAS gasifying process and synthetic gas company of Britain is exactly good example.Britain's synthetic gas metallization processes just comprises steam/oxygen gas and hydrogasification two gasification section.The hydrogen source of hydrogasification section is from steam/oxygen gas gasification section.But similar with other fluidized bed gasifying process, when gasified raw material is bituminous coal, total efficiency of carbon conversion is general lower.Lower total efficiency of carbon conversion just causes hydrogen yield lower, and the amounts of hydrogen therefore needed for hydrogasification reaction is just under-supply.
Be not described in this patent of invention in each section of gasification and how go equilibrium hydrogen productive rate and efficiency of carbon conversion problem.Sometimes on paper, draw bar line be easy to: such as, a side line drawn by one-level hydrogasification stove, the semicoke that one-level hydrogasification stove produces is sent to secondary hydrogenation vapourizing furnace gasify, the semicoke that secondary hydrogenation vapourizing furnace produces is sent to steam-oxygen vapourizing furnace again for hydrogen manufacturing.But since nineteen twenty-six, First fluidized-bed gasification furnace dropped into commercial operation, in fluidized-bed gasification furnace, the trapping of semicoke just never well solves.If semicoke granule capturing problem can not get solving, so all imaginations all cannot come true.This technique faces such problem equally: because last step gasifier operation temperature is 800 °F (426.67 DEG C), at this temperature, the methane equilibrium concentration in synthetic gas is lower than 15%.So, be just necessary after vapourizing furnace, set up the production of a methanator for SNG again.
Simultaneously another solution party's rule produces SNG and fuel oil by the synthesis gasification-dry distillation of coal or synthesis gasification-coal hydrogenation pyrolysis integrated technique.Representative technique is exactly the Coalcon technique grown up the sixties in 20th century and the seventies.In this technique, coal to be added in hydrotorting stove by hydropyrolysis in order to produce oil product and pyrolysis gas.Pyrolysis char to enter in vapourizing furnace gasification hydrogen-producing for pyrolysis oven provides hydrogen source.Although with synthesis gas washing purification and transformation system in Coalcon gasifying process, in theory the high-temperature synthesis gas produced in vapourizing furnace is directly inputted hydropyrolysis stove and should be not difficult to realize to realize the integration of synthesis gasification-hydropyrolysis.But in Coalcon technique and other similar technique for how oxygen-steam being gasified, hydrogasification and hydropyrolysis technique is coupled and is specifically described for SNG and high-quality Oil Production.All do not recognize in above-mentioned technique: hydrogasification needs material in reactive system, have the longer residence time, hydropyrolysis then needs material in reactive system, have the shorter residence time, to limit the contact of semicoke particle and tar to greatest extent, because the semicoke particle in synthetic gas is the catalyzer that tar component generation deep pyrolytic becomes light gas components.
Summary of the invention
The object of the present invention is to provide the device and method of a kind of coal preparing natural gas and light oil, produced the technique of Sweet natural gas, synthetic gas and fuel oil by synthesis gasification, hydrogasification, hydropyrolysis integrated technology, and always efficiency of carbon conversion close to 100%.
For achieving the above object, the inventive system comprises: comprise the shortening be made up of shortening gasification section and hydrogenation fast pyrogenation section be connected with feed coal pipeline gasify-hydropyrolysis integrated apparatus, oxygen-steam vapourizing furnace, one-level hydrogasification stove, crude synthesis gas-fine particle is separated and semicoke revert system, solution-air, liquid-liquid separation unit, gas treating system;
The semicoke logistics pipeline of shortening gasification-hydropyrolysis integrated apparatus is connected with one-level hydrogasification stove, the synthesis gas stream pipeline of one-level hydrogasification stove gasifies with shortening-and hydropyrolysis integrated apparatus is connected, the pyrolysis gas logistics that shortening gasification-hydropyrolysis integrated apparatus exports to be separated with crude synthesis gas-fine particle through pipeline and semicoke revert system is connected, crude synthesis gas-fine particle is separated and the synthesis gas stream of semicoke revert system is connected with solution-air and liquid-liquid separation unit by the road, the outlet of solution-air and liquid-liquid separation unit divides three tunnels, be respectively separating obtained water, the oil product reclaiming gained and the primary purifying synthesis gas stream be connected with gas treating system, through the CO of gas treating system purification separation gained 2, H 2s mixture flow continues to enter downstream and carries out being separated and advanced treatment, and the methane after separation and other gas phase alkane export as product, CO and H of gained after being separated 2return one-level hydrogasification stove as circulation gas to be separated and semicoke revert system with crude synthesis gas-fine particle, the macrobead lime-ash logistics of one-level hydrogasification stove is discharged through pipeline, semicoke logistics is connected with oxygen-steam vapourizing furnace through pipeline, the synthetic gas that oxygen-steam top of gasification furnace exports is connected with one-level hydrogasification stove through pipeline, primary purifying synthesis gas stream is also connected with the pipeline of synthetic gas through circulation gas logistics, the stove material that enters of oxygen-steam vapourizing furnace is respectively the semicoke logistics that steam stream, oxygen stream and crude synthesis gas-fine particle is separated and semicoke revert system is discharged, and the outlet of oxygen-steam vapourizing furnace is slag pipeline.
The gasification section of described oxygen-steam vapourizing furnace adopts the inclined structure that dips down, semicoke logistics, steam stream, oxygen stream tangentially enter gas-slag separating tank by the tangential gasification section mix products that injects, lime-ash enters the bottom of gas-slag separating tank, the grey solid impurity particle of gas-slag separating tank trapping gained flows downward along inwall, chilled water adds bottom gas-slag separating tank, the position added is below gas-slag mixture inlet, and the synthetic gas leaving separating tank enters one-level hydrogasification stove.
The gasification section of described oxygen-steam vapourizing furnace adopts direction vertically downward, semicoke logistics, steam stream, oxygen stream tangentially inject gasification section, linkage section is entered under gas phase and lime-ash also flow to, in the downward flow ipe bottom slag discharge gradually of linkage section slag, linkage section tangentially enters gas-slag separating tank, the grey solid impurity particle of gas-slag separating tank trapping gained flows downward along inwall, chilled water adds bottom gas-slag separating tank, the position added is below gas-slag mixture inlet, and the synthetic gas leaving separating tank enters one-level hydrogasification stove.
Described one-level hydrogasification stove comprises cone structure, the cylinder upper end of cone structure vertical direction be also provided with for connect body of heater cut sth. askew to cone, the bottom of cone structure and semicoke logistics pipeline, feed coal pipeline is connected, its profile is intilted eccentric cone, synthetic gas, circulation gas logistics enters one-level hydrogasification stove by centre, side bottom it, and the logistics of macrobead lime-ash, ash particle logistics then to be discharged and capable of circulation to hydrocracking section from the bottommost of opposite side cone, be positioned in body of heater directly over cone and be provided with emulsion zone, in emulsion zone, body of heater circumference is provided with several primary cyclones, the multicyclone be connected with the outlet pipe of primary cyclone is also provided with in primary cyclone upper end, the synthesis gas stream that multicyclone is separated is connected with synthesis gas stream transport pipe through diversion trench, the lower end of multicyclone is provided with dipleg, the whirlwind dipleg of multicyclone stretches in dipleg, the semicoke particle of an outlet of dipleg enters bed as circulating granular, the semicoke particle of an outlet of dipleg joins oxygen-steam vapourizing furnace as fuel.
Described cone structure discharges the logistics of macrobead lime-ash, the side of semicoke logistics also offers fluidized gas entrance; The sidewall of cone offers cone fluidized gas entrance, dipleg is connected with fluidized gas and passes into pipeline.
The diameter of described primary cyclone top cylindrical shell is 0.4-0.8m, the crude synthesis gas produced tangentially enters primary cyclone by entrance, the solid particulate of primary cyclone trapping returns bed by the dipleg of cyclonic separator, and the distance between the position of dipleg outlet and cone inwall is 2-4 times of whirlwind dipleg diameter.
Described multicyclone comprises some groups of small cyclones separator units, entered the gas inlet surge bunker of multicyclone by the outlet pipe at cyclonic separator top containing the fine grain crude synthesis gas of semicoke after primary cyclone gas-particle separation, primarily of semicoke composition fine particle trapped by multi-cyclone after be collected in granule capturing storehouse, enter dipleg by whirlwind dipleg subsequently.
In the hydropyrolysis section of described shortening gasification-hydropyrolysis integrated apparatus, the riser tube of pyrolysis oven is connected with feed coal, feed coal is carried by conveying gas, be divided into two branch roads, a branch road enters the hydrogenation fast pyrogenation section of shortening gasification-hydropyrolysis integrated apparatus, another branch road enters one-level hydrogasification stove, the pyrolysis gas that hydrogenation fast pyrogenation section top exports is connected with pyrolysis oven primary cyclone entrance, pyrolysis oven secondary cyclone is entered after leaving cyclonic separator from pyrolysis oven primary cyclone top, the gas-solid mixture flow that pyrolysis oven secondary cyclone exports to be separated with crude synthesis gas-fine particle through pipeline and semicoke revert system is connected, the semicoke logistics that pyrolysis oven secondary cyclone is caught enters dipleg rear portion and returns shortening gasification-hydropyrolysis integrated apparatus by solids stream channel cycle, the logistics of another part semicoke is connected with one-level hydrogasification stove entrance through pipeline, the isolated carbonaceous solid particulates of pyrolysis oven primary cyclone returns hydrogenation fast pyrogenation section through upright dipleg circulation, simultaneously, in order to ensure the circulation ratio of solid circle, the upright dipleg be connected with hydrogenation fast pyrogenation section also offers the entrance connected with loosening gas phase,
Shortening gasification section is fluidized-bed reactor, and in bed, material load has the particle of gasification catalysis active ingredient, and synthesis gas stream mixes mutually with the semicoke logistics returned from hydrogenation fast pyrogenation section, carries out gas phase and gas-solid two alternate hydrogenation methanation reactions simultaneously.
Described crude synthesis gas-fine particle is separated and semicoke revert system comprises the returning charge cyclonic separator be made up of several unit cyclonic separators be connected with pyrolysis gas logistics, circulation synthetic gas; The gas-solid hay tank of the built-in efficient filter core be connected with dust diversion trench; The hopper be connected with hay tank outlet at bottom thrust-augmenting nozzle, the synthesis gas stream exported bottom returning charge cyclonic separator is connected with gas-particle separation unit by the road, the dust that returning charge cyclonic separator is caught enters in the annular space region surrounded by the wall of hay tank and skirt by diversion trench, hay tank upper end is provided with filter core, lower end is cone, gas phase upwards flows into filter core and forms synthesis gas stream discharge, semicoke logistics enters hopper along thrust-augmenting nozzle, and the semicoke logistics formed in hopper enters oxygen-steam vapourizing furnace along pipeline.
Method of the present invention is as follows: by steam stream, oxygen stream composition vaporized chemical and semicoke logistics carry out gasification reaction in oxygen-steam vapourizing furnace, the lime-ash produced is discharged by oxygen-steam vapourizing furnace bottom ash discharging hole, one-level hydrogasification stove is advanced on the synthetic gas produced is direct, the descending oxygen-steam vapourizing furnace that returns of the semicoke logistics that one-level hydrogasification stove produces proceeds gasification reaction, the logistics of macrobead lime-ash is discharged by one-level hydrogasification furnace bottom, feed coal and circulation gas and the synthetic gas come from oxygen-steam vapourizing furnace react in one-level hydrogasification stove, the synthetic gas containing higher concentration methane that one-level hydrogasification stove produces is by synthesis gas stream pipeline being advanced into shortening gasification-hydropyrolysis integrated apparatus, after fresh feed coal enters shortening gasification-hydropyrolysis integrated apparatus, pyrolytic reaction is carried out with the high-temperature solid particle of sweeping along as thermal source using the synthetic gas containing higher concentration methane exported from one-level hydrogasification furnace roof portion, semicoke logistics pipeline of passing through under pyrolysis char and inert particle enters one-level hydrogasification stove, the pyrolysis gas logistics that shortening gasification-hydropyrolysis integrated apparatus exports enters crude synthesis gas-fine particle again and to be separated and semicoke revert system carries out the initial gross separation purifying treatment of synthetic gas after the cooling of Quench circulation gas, crude synthesis gas-fine particle is separated and the semicoke logistics circulation of semicoke revert system trapping returns oxygen-steam vapourizing furnace, synthesis gas stream enters gas-particle separation unit, separating obtained liquid product is respectively water and tar, gas-liquid separation unit export through oil removing, the primary purifying synthesis gas stream of processed is divided into two branch roads: circulation gas logistics returns as sharp circulating cold air the synthesis gas phase exported with oxygen-steam top of gasification furnace and mixes, remaining decontaminating syngas then enters gas treating system, the methane that gas treating system produces and other gas phase hydrocarbon are as output of products, CO and H 2return one-level hydrogasification stove as circulation gas to be separated and semicoke revert system with crude synthesis gas-fine particle, wherein return the Quench gas of circulation gas for pyrolysis gas logistics of crude synthesis gas-fine particle separation and semicoke revert system, separating obtained CO 2, H 2s mixture flow continues to enter downstream and carries out being separated and advanced treatment.
The present invention comprises a gasification section, hydrogenation fast pyrogenation section and two-stage hydrogasification section.
The present invention comprises oxygen-steam vapourizing furnace, one-level hydrogasification stove, shortening gasification-hydropyrolysis integrated apparatus, gas-particle separation and gas cleaning system
All semicokes can trap and extend the residence time of hydrogasification section semicoke particle by one-level hydrogasification stove, have two objects like this: one is improve in the residence time of cold zone the content that vapourizing furnace exports methane in synthetic gas gas phase by increasing hydrogasification synthetic gas.Two is improve tar yield by the hydrogenation fast pyrogenation of coal, is convenient to follow-up oil manufacture.First thin ash contained in the pyrolysis gas that quick hot arc exports is recycled below ash fusion point temperature that synthetic gas is cooled to thin ash particle, on tar condensing dew-point temperature.Dust-laden crude synthesis gas will realize the removal of solid particulate in synthetic gas by crude synthesis gas-fine particle separation and semicoke revert system.The tar of synthetic gas after udst separation again in solution-air, liquid-liquid separation unit further condensation removal gas phase.Purge gas after gas-liquid separation also needs to remove wherein contained sour gas and CO further 2.Decontaminating syngas removes the methane in synthetic gas more further by methane separation technique.Unreacted CO and H 2recirculation is returned secondary shortening gasification section and is participated in hydrogasification reaction.
Accompanying drawing explanation
Fig. 1 is feel flow draw of block of the present invention;
Fig. 2 is the structure iron of oxygen-steam vapourizing furnace in the present invention;
Fig. 3 is the structure iron of the another kind of oxygen-steam vapourizing furnace of the present invention;
Fig. 4 is the structure iron of one-level hydrogasification stove of the present invention;
Fig. 5 is the structure iron of secondary catalytic gasification of the present invention and pyrolysis oven integrated apparatus;
Fig. 6 is the structure iron of crude synthesis gas of the present invention-fine particle separation and semicoke revert system.
In figure, conveying gas 1, feed coal 2, shortening 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, synthetic gas 9, steam stream 10, oxygen stream 11, oxygen-steam vapourizing furnace 12, slag 13, pyrolysis gas logistics 14, Quench circulation gas 15, ash particle logistics 16, macrobead lime-ash logistics 17, semicoke logistics 18, semicoke logistics 19, crude synthesis gas-fine particle is separated and semicoke revert system 20, synthesis gas stream 21, solution-air, liquid-liquid separation unit 22, water 23, oil product 24, primary purifying synthesis gas stream 25, circulation gas 26, gas treating system 27, CO 2, H 2s mixture flow 28, decontaminating syngas product 29, gasification section 30, gas-slag separating tank 31, chilled water 32, ash solid impurity particle 33, lime-ash 34, linkage section 35, body of heater 36, cone 37, cone structure 38, circulation gas logistics 39, cylinder 40, solid particulate logistics 41, dipleg 42, emulsion zone 43, primary cyclone 44, cylindrical shell 45, outlet pipe 46, crude synthesis gas 47, multicyclone 48, diversion trench 49, outer wall 50, small cyclones separator unit 51, gas inlet surge bunker 52, the fine particle 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, solids stream passage 61, fluidized gas entrance 62, solid circle logistics 63, bed material material level line 64, upright dipleg 65, solid circle logistics 66, pyrolysis oven primary cyclone 67, unit cyclonic separator 68, filter core 69, hay tank 70, skirt 71, wall 72, cone 73, diversion trench 74, anti-material cyclonic separator 75, annular space 76, gas phase 77, semicoke logistics 78, thrust-augmenting nozzle 79, hopper 80, circulation gas 81, cone fluidized gas entrance 82, circulation synthetic gas pipeline 83, loosen gas 84, synthesis gas stream 85, shortening gasification-hydropyrolysis integrated apparatus 86.
Embodiment
Below in conjunction with accompanying drawing, the present invention is described in further detail.
See Fig. 1, the inventive system comprises the shortening be made up of shortening gasification section 3 and hydrogenation fast pyrogenation section 4 be connected with feed coal pipeline gasify-hydropyrolysis integrated apparatus 86, oxygen-steam vapourizing furnace 12, one-level hydrogasification stove 8, crude synthesis gas-fine particle is separated and semicoke revert system 20, solution-air, liquid-liquid separation unit 22, gas treating system 27.
Wherein, one-level hydrogasification stove 8 is connected with feed coal pipeline, shortening gasification-hydropyrolysis integrated apparatus 86 is made up of shortening gasification section 3 and hydrogenation fast pyrogenation section 4, the semicoke logistics pipeline 6 of shortening gasification-hydropyrolysis integrated apparatus 86 is connected with one-level hydrogasification stove 8, the synthesis gas stream pipeline 5 of one-level hydrogasification stove 8 gasifies with shortening-and hydropyrolysis integrated apparatus 86 is connected, the pyrolysis gas logistics 14 that shortening gasification-hydropyrolysis integrated apparatus 86 exports enters crude synthesis gas-fine particle again and to be separated and semicoke revert system 20 carries out the initial gross separation purifying treatment of synthetic gas after Quench circulation gas 15 cools, crude synthesis gas-fine particle be separated and semicoke revert system 20 synthesis gas stream 21 by the road with solution-air, liquid-liquid separation unit 22 is connected, solution-air, the outlet of liquid-liquid separation unit 22 divides three tunnels, be respectively separating obtained water 23, the oil product 24 reclaiming gained and the primary purifying synthesis gas stream 25 be connected with gas treating system 27, through the CO of gas treating system 27 purification separation gained 2, H 2s mixture flow 28 continues to enter downstream and carries out being separated and advanced treatment, and the methane produced and gas phase hydrocarbon export as final product 29, CO and H 2return one-level hydrogasification stove 8 as circulation gas to be separated and semicoke revert system 20 with crude synthesis gas-fine particle, , the macrobead lime-ash logistics 17 of one-level hydrogasification stove 8 is discharged through pipeline, semicoke logistics 18 is connected with oxygen-steam vapourizing furnace 12 through pipeline, the synthetic gas 9 of oxygen-steam vapourizing furnace 12 is connected with one-level hydrogasification stove 8 through pipeline, primary purifying synthesis gas stream 25 is also connected through the pipeline of circulation gas logistics 39 with synthetic gas 9, the stove material that enters of oxygen-steam vapourizing furnace 12 is respectively steam stream 10, oxygen stream 11 and the semicoke logistics 19 that crude synthesis gas-fine particle is separated and semicoke revert system 20 is discharged, the bottom of oxygen-steam vapourizing furnace 12 is provided with slag 13 Residue extraction pipeline.
The effect of secondary shortening gasification section 3 is the katalysis by basic metal or alkaline-earth metal, and the semicoke particle that synthetic gas and pyrolysis oven are produced carries out reacting to produce methane, CO and H in crude synthesis gas 2also there is gas phase methanation reaction simultaneously.The gas of secondary shortening gasification section 3 directly on be advanced into fast pyrogenation section 4 as the fluidized gas of pyrolysis section and thermal source.
Crude synthesis gas-fine particle is separated and the effect of semicoke revert system 20 is most of semicoke particles of escaping in trapping pyrolysis oven, and the semicoke particles circulating of trapping is returned oxygen-steam vapourizing furnace 12.The effect of solution-air, liquid-liquid separation unit 22 is the thin ash removing trace, can be trapped oils and the water of most of condensable separation by oil wash or washing.Gas treating system 27 comprises following part: realize CO 2and H 2the sour gas separation system that S is separated with synthetic gas; CO shift-converter; Methane separation system, described methane separation system is separated by cryogenic condensation and realizes methane and to be separated with synthetic gas and unreacted hydrogen, synthetic gas to be looped back reactor simultaneously, is delivered to pipeline after being compressed by SNG.
In most preferred embodiment of the present invention, oxygen-steam vapourizing furnace 12 is slag deslagging airflow bed gasification furnaces.The stove logistics that enters of oxygen-steam vapourizing furnace 12 is respectively steam stream 10, oxygen stream 11 and semicoke logistics 19.Semicoke logistics 19 comprises conveying gas, superheated vapour.According to the reactive behavior of semicoke and the difference of ash fusion point, oxygen-steam vapourizing furnace 12 service temperature is 1300-1900 DEG C of variation.In semicoke, ash is finally converted to slag 13, and discharges with the form of slag.
The hydrogen source that the synthetic gas 9 that oxygen-steam vapourizing furnace 12 generates will directly be sent to as hydrogasification reaction in one-level hydrogasification stove 8.In oxygen-steam vapourizing furnace 12, gas phase and lime-ash flow in the opposite direction, and lime-ash flows downward, and synthetic gas upwards flows.Inevitably, the slag particles of part can enter in one-level hydrogasification stove 8 with synthetic gas 9, and the bed material finally in these slags and one-level hydrogasification stove 8 aggregates into particle.But the slag entering one-level hydrogasification stove 8 with synthetic gas 9 is more few better, most slag should trap by the lime-ash trapping system of oxygen-steam vapourizing furnace 12.
Although oxygen-steam vapourizing furnace 12 can be any one airflow bed gasification furnace, and gas phase and slag are without Quench refrigerated separation, optimal situation is exactly reclaimed by the sensible heat entrained by gas, instead of takes this part sensible heat out of vapourizing furnace by chilled water cooling.Most of thermal source in the present invention needed for one-level hydrogasification stove 8 is that the sensible heat entrained by synthetic gas produced by oxygen-steam vapourizing furnace 12 provides, and sub-fraction provided by hydrogasification reaction heat.Therefore, chilled water of the present invention is only for solidifying agent cooling lime-ash.
See Fig. 2, the gasification section 30 of oxygen-steam vapourizing furnace 12 of the present invention adopts the inclined structure that dips down, semicoke logistics 19 and steam stream 10, oxygen stream 11 enter the vapourizing furnace perpendicular with gasification section 30 furnace wall by tangential injection, mix products tangentially enters gas-slag separating tank 31, lime-ash 34 enters the bottom of gas-slag separating tank 31, most lime-ash can enter the bottom of gas-slag separating tank 31 under gravity, the lime-ash 34 namely in figure; In the process that the crude synthesis gas having carried grey solid impurity particle secretly rises at gas-slag separating tank 31 internal screw at this gas-solid mixture, realize the separation of gas-solid two-phase under the influence of centrifugal force.The grey solid impurity particle that gas-slag separating tank 31 traps gained will flow downward along inwall, and this is grey solid impurity particle 33.Chilled water 32 adds bottom gas-slag separating tank 31, and the position added is below gas-slag separating tank 31 mixture inlet.Lime-ash after Quench will be discharged into the conventional dregs breaker of most of airflow bed gasification furnace and lock hopper system.
See Fig. 3, in this structure, gasification section 30 is directions vertically downward.With the similar in Fig. 2, semicoke logistics 19, steam stream 10, oxygen stream 11 are all tangentially inject gasification section 30.The slag formed can flow along gasification section inwall, and can form one deck falling liquid film, and the barrier film formed can play the effect well protecting the refractory liner in gasification section 30.Gas phase and lime-ash also enter linkage section 35 under flowing to, will flow ipe bottom slag discharge gradually downwards at the most of slag of linkage section 35.Linkage section 35 tangentially enters synthetic gas-slag separating tank 31.As mentioned above, most of slag stream 34 will flow to bottom gas-slag separating tank 31 under gravity.The crude synthesis gas carrying little slag particles will rise along the spiral inner wall of separating tank 31, in the process slag solid particulate will be deposited on gas-slag separating tank 31 inwall on and along the fire-resistant formation falling liquid film 33 on wall, thus and gas phase separation.After being separated, the slag of gained is cooled by chilled water 32, and the synthetic gas 9 leaving gas-slag separating tank 31 enters one-level hydrogasification stove 8.
Pattern in moulder moisture Fig. 2 or Fig. 3 of oxygen-steam vapourizing furnace 12, depends on the service temperature of oxygen-steam vapourizing furnace 12, and the service temperature of oxygen-steam vapourizing furnace 12 then depends on the ash fusion point of adopted feed coal.When the initial deformation temperature of coal ash is on 1300 DEG C, oxygen-steam gasification furnace structure adopts structure as shown in Figure 3, otherwise then adopts structure as shown in Figure 2.When the ash fusion point temperature of feed coal is higher than 1300 DEG C, the service temperature of vapourizing furnace will higher than 1500 DEG C or its service temperature higher than T 250, T 250refer under this service temperature, the viscosity of liquid lime-ash equals 250poise.The catadromous slag fluid matasomatism of vapourizing furnace gasification section 30 inwall can play as sealing coat the object well protecting the refractory liner in gasification section 30.In addition, spiral coil cooling tube can be installed in the flame retardant coating of gasification section 30 to extend the life-span of flame retardant coating.When the initial deformation temperature of coal ash is under 1300 DEG C, the vapourizing furnace shown in Fig. 2 is more applicable, because its internal structure is relatively simple.
See Fig. 4, one-level hydrogasification stove 8 of the present invention comprises cone structure 38, cylinder 40 upper end of cone structure 38 vertical direction be also provided with for connect body of heater 36 cut sth. askew to cone 37, the bottom of cone structure 38 and semicoke logistics pipeline 6, feed coal pipeline 7 is connected, its profile is the eccentric cone internally tilted, synthetic gas 9, circulation gas logistics 39 enters one-level hydrogasification stove 8 by centre, side bottom it, and macrobead lime-ash logistics 17, ash particle logistics 16 capable of circulation time hydrogenation fast pyrogenation sections, be positioned in body of heater 36 directly over cone 37 and be provided with emulsion zone 43, in emulsion zone, body of heater 36 circumference is provided with some groups of primary cyclones 44, the multicyclone 48 be connected with the outlet pipe 46 of primary cyclone 44 is also provided with in the body of heater 36 of the upper end of primary cyclone 44, the synthesis gas stream that multicyclone 48 is separated is connected with synthesis gas stream pipeline 5 through diversion trench 49, the lower end of multicyclone 48 is provided with dipleg 58, the whirlwind dipleg 56 of multicyclone 48 stretches in dipleg 58, the semicoke particle 57 that dipleg 58 1 outlet exports enters bed as circulating granular.The semicoke particle 18 that another outlet of dipleg 58 exports adds oxygen-steam vapourizing furnace 12 as reactant.
Wherein, cone structure 38 discharges macrobead lime-ash logistics 17.Ash particle logistics 16 capable of circulation time hydrogenation fast pyrogenation sections 4.Macrobead logistics 17 and ash particle logistics 16 realize being separated under the effect of fluidized gas 62; The sidewall of cone 37 offers cone fluidized gas entrance 82, dipleg 58 is connected with circulation synthetic gas pipeline 83;
The diameter of primary cyclone 44 top cylindrical shell 45 is 0.4-0.8m, crude synthesis gas enters primary cyclone 44 by entrance 55, the solid particulate logistics 41 trapped through primary cyclone 44 returns bed by the dipleg 42 of cyclonic separator, and the distance between the position of dipleg 42 outlet and cone 37 inwall is 2-4 times of whirlwind dipleg 42 diameter;
Multicyclone 48 comprises some groups of small cyclones separator units 51, the crude synthesis gas 47 after semicoke fine particle to enter multicyclone 48 gas inlet surge bunker 52 by the outlet pipe 46 at cyclonic separator 44 top is removed through primary cyclone 44, primarily of semicoke composition fine particle 53 trapped by multi-cyclone after be collected in granule capturing storehouse 54, enter whirlwind dipleg 56 subsequently.The coal gas of low particle concentration is then exported from one-level hydrogenator by pipeline 49.
Be under the condition of 1300-1900 DEG C in service temperature, through sufficient gasification reaction, the synthetic gas 9 that oxygen-steam vapourizing furnace 12 top exports enters one-level hydrogasification stove 8.Crude synthesis gas 9 after entering one-level hydrogasification stove 8, can be cooled by the semicoke logistics containing inert particle from shortening gasification section 3 inputted through semicoke logistics pipeline 6; Also can be cooled by circulation synthetic gas 39 as shown in Figure 4 after crude synthesis gas 9 exports one-level hydrogasification stove 8.Before entering one-level hydrogasification stove 8, lower than 1200 DEG C, 1100 DEG C to be preferably lower than through the cooled temperature of the cooled crude synthesis gas of circulation synthetic gas 39 9.Although crude synthesis gas 9 is through the cooled temperature of circulation synthetic gas 39 lower than ash fusion point, the slag particles entrained by crude synthesis gas 9 still can not solidify completely.
Carrying out pre-cooled object to crude synthesis gas 9 is generate larger clinker in order to prevent when the crude synthesis gas 9 of temperatures as high 1900 DEG C contacts with the Solid Bed material in one-level hydrogasification stove.By cooling, what the mixture flow formed by circulation synthetic gas 39 and crude synthesis gas 9 just can be safe enters one-level hydrogasification stove 8.
The ingress of one-level hydrogasification stove 8, crude synthesis gas 9 can mix with the semicoke logistics containing inert particle inputted through semicoke logistics pipeline 6 further.After these two bursts of logistics mixing, the temperature of mixture will be consistent with the temperature of reactor bed, is all 800-950 DEG C.According to the difference of the temperature of circulation synthetic gas 39 and the mixed mixture flow of crude synthesis gas 9, one-level hydrogasification furnace operating temperature and pyrolysis oven service temperature, the mass ratio of semicoke logistics and said mixture stream changes in the scope of 0.4-5.Feed coal 7 also can be added by synthetic gas entrance, like this can rapidly by the service temperature of the heating temperatures hydrogasification section of feed coal, at utmost to improve the yield of methane and other hydrocarbon products and tar.Because main products of the present invention is exactly tar, therefore the productive rate of tar is more high better.
If raw material coal is caking coal, then in advance coal be mixed with the semicoke 6 from hydrogenation fast pyrogenation section before one-level hydrogasification stove coal, the mass ratio of semicoke and fresh feed in mixture is 10 ~ 20, can prevent the coking of viscous materials coal so to greatest extent.In this case, the circulation ratio of the solid particulate come from hydropyrolysis stove is just determined by following several factors: one is by the largest loop amount of solid entering the decision of coal speed; Two is the solid circle amounts needed for the service temperature in order to be cooled to hydrogasification stove from oxygen-steam vapourizing furnace 12 gaseous mixture.When the normal running temperature of bed temperature after solid circle particle mixes with feed coal lower than vapourizing furnace, the amount of recycle gas will be cut down, and the temperature entering the crude synthesis gas in hydrogasification stove so is just approximately about 1000-1200 DEG C.
The slag that synthetic gas 9 carries can be wrapped in the outside surface of bed material particle, and this will cause the particle diameter ratio ideal dimensions of part bed material large.These become macrobead lime-ash logistics 17 later greatly and will be discharged from bed.Any other bed material entering bed along with solid circle material can be drawn out of together with above-mentioned macrobead lime-ash logistics 17 from same nozzle, but needs afterwards to be separated with macrobead lime-ash logistics 17 by screening or fluid suspended mode.Ash particle logistics 16 is delivered to by circulation gas the pyrolysis that hydrogenation fast pyrogenation section 4 is coal and provides heat.Feed coal 2 also using circulation synthetic gas as carrier gas, need be delivered to hydrogenation fast pyrogenation section 4.
The cone structure 38 of one-level hydrogasification stove 8 bottom, its profile is the eccentric cone to lopsidedness.Synthetic gas 9 enters vapourizing furnace from its bottom left centre, and the bottommost that lime-ash and grey melt body particle are then positioned at cone from opposite side is discharged, so that be separated with normal bed material by grey melt body particle.After synthetic gas 9 enters one-stage hydrogenation vapourizing furnace 8 together with circulation gas logistics 39, the jet logistics that said two devices is formed will multilated after mixing with solid materials, and this structure design is relatively suitable for for one-level hydrogasification stove.
Fluidized gas also enters vapourizing furnace from cone 37 through cone fluidized gas entrance 82, and its effect is the fluidisation promoting position, tapering material.
The working pressure of one-level hydrogasification stove 8 is also at 40-100bar (4.0-10.0MPa), and object is the equilibrium concentration in order to improve methane in synthetic gas.Operating temperature range is 800-950 DEG C, selects this operating temperature range to be consideration based on the equilibrium concentration of methane in synthetic gas and the reaction kinetics equilibrium constant of methanation reaction.The gas phase superfacial velocity of cone 37 is 0.3-0.7m/s, and best superfacial velocity is 0.3-0.5m/s.Superficial gas flow velocity in the body of heater 36 that broken-line expands is about 0.1-0.5m/s, and above-mentioned two-part cross-sectional area ratio is between 1.5 to 3.
In one-level hydrogasification stove, the reactive behavior of semicoke directly determines the height of emulsion zone 43 and fluidized-bed bed, and the height of bed can affect the residence time of semicoke in vapourizing furnace and concrete operations temperature (temperature range must between 800-950 DEG C).In one-level vapourizing furnace, the residence time of semicoke particle should control within 15min, preferably controls within 10min.Gasification reaction in vapourizing furnace (as hydrogasification, steam and CO 2gasification reaction etc.) to carry out will ensureing that the charcoal percent conversion contained by semicoke particle is greater than 65% completely, optimal conversion is 75%.
When crude synthesis gas exports from one-level hydrogasification stove 8, gas phase can carry a part of bed material.Crude synthesis gas enters primary cyclone 44 by entrance 55.Only demonstrating in Fig. 4 and only have two primary cyclones, in actual design process, in order to improve the collection efficiency of solid particulate, often designing multiple primary cyclone.In order to balance particle capture efficiency and the crude synthesis gas treatment capacity of primary cyclone 44, the diameter of the cylindrical shell 45 that one cyclonic divides is advisable with 0.4-0.8m.Dipleg 42 by cyclonic separator is returned bed by the solid particulate logistics 41 trapped through primary cyclone 44.
In most preferred embodiment of the present invention, the position that solid particulate logistics 41 circulation that primary cyclone dipleg 42 traps returns bed has also given indicating in the diagram.The solid particulate logistics of primary cyclone trapping will return the bed at cone 37 position, distance optimum value dipleg returned between the position of the outlet of solid and cone inwall is 2-4 times of cyclone dip-leg diameter, only in this way just can ensure that the output of dipleg position solid materials is more steady.Because the superfacial velocity of bed central section gas is higher than solid materials, cause the tap density of bed central section bed material lower thus.Under gravity, the solid materials that internal recycling returns will flow to bed center along cone 37 inwall.Avoid synthetic gas to flow to whirlwind dipleg with this, thus overcome because gas upwards flows the cyclonic separator operation troubles that causes in dipleg.
The crude synthesis gas 47 exported by primary cyclone 44 can carry the semicoke fine particle of some collection at large, and the outlet pipe 46 by cyclonic separator top is entered the gas inlet surge bunker 52 of multicyclone 48 by these fine particles.Multicyclone 48 is containing the small cyclones separator unit 51 being much usually used in thin ash trapping.To be collected in granule capturing storehouse 54 by unified after being trapped by multi-cyclone primarily of the fine particle 53 of semicoke composition, enter whirlwind dipleg 56 more subsequently.Whirlwind dipleg 56 stretches in dipleg 58 to prevent gas backwash from entering cyclone dip-leg.As shown in Figure 4, the semicoke particle 57 that multicyclone 48 traps enters one-level hydrogasification stove 8 using finally unified as circulating granular.
Even if extend the residence time, the carbon contained by semicoke is still difficult to be converted completely, and as shown in Figure 4, the semicoke logistics 18 of part is extracted out by the material sealing that it may be necessary multicyclone.In order to ensure the stable output of solids stream, add loosening gas by circulation synthetic gas pipeline 83 to dipleg 58.Oxygen-steam vapourizing furnace is entered together after the semicoke logistics 18 of being extracted out by dipleg 58 and the solid particulate that crude synthesis gas-fine particle is separated and semicoke revert system 20 traps converge.Decontaminating syngas leaves multi-cyclone separation system by the diversion trench 49 at multi-cyclone top, and one-level hydrogasification stove is left in final logistics 5.Whole cyclone separation system and vapourizing furnace are became one by the connection between the outer wall 50 of diversion trench 49 and gasification stove internal wall 36.Space between multi-cyclone system 48 and gasification stove internal wall 36 suppresses the accumulation of dust by the purging of circulation synthetic gas.
See Fig. 5, the riser tube of the hydrogenation fast pyrogenation section 4 of shortening gasification-hydropyrolysis integrated apparatus 86 of the present invention is connected with feed coal 2, pyrolysis section outlet is connected with pyrolysis oven primary cyclone 67 entrance, pyrolysis oven secondary cyclone 59 is entered after the pyrolysis gas exported leaves cyclonic separator from primary cyclone 67 top, the isolated pyrolysis gas logistics 14 of pyrolysis oven secondary cyclone 59 to be separated with crude synthesis gas-fine particle through pipeline and semicoke revert system 20 is connected, the semicoke logistics that pyrolysis oven secondary cyclone 59 is caught enters dipleg 60 rear portion and enters hydrogenation fast pyrogenation section 4 by solids stream passage 61, another part semicoke logistics pipeline 6 is connected with one-level hydrogasification stove 8, the logistics of pyrolysis oven primary cyclone 67 isolated solid circle through upright dipleg 65 respectively with shortening gasification section 3, hydrogenation fast pyrogenation section 4 is connected, and also offer on upright dipleg 65 and loosening gas 84, the entrance that 87 line of pipes are connected.
From the change of bed material material level line 64, the solid circle logistics 63 entered bottom bed is taken out of bed again by upstream.In bed, being coupled of the mixing of material or fluidized-bed and fixed bed is that control by bed material particle diameter and gas phase apparent velocity realizes.Optimal support of the catalyst is metallurgical coke, and the active ingredient of catalyzer is basic metal or alkaline-earth metal, and its median size is 3-6mm.Why coke is suitable support of the catalyst, is because itself have higher intensity, good wear resisting property and thermostability.Meanwhile, the fine particle produced due to the wearing and tearing of coke granule can gasify and can not produce solid waste in oxygen-steam vapourizing furnace.Other inert particle also can be used as the carrier of catalyzer.
The median size of carrying out the solid particulate circulated by upright dipleg 65 is 80-100 μm.In bed, the apparent velocity of gas phase is 0.3-0.7m/s, and in shortening gasification-hydropyrolysis integrated apparatus 86 emulsion zone bed, the residence time of gas phase is 10-30s.Selecting the superficial gas velocity of this scope, is because granules of catalyst can not be only had solid circle particle to be taken out of bed by taking bed out of.
The operating temperature range of shortening gasification-hydropyrolysis integrated apparatus 86 is 550-700 DEG C, and optimum operating temperature is 550-650 DEG C.Under the working pressure and lower operational temperature conditions of 40-100bar (4.0-10.0MPa), under the katalysis of catalyzer, the equilibrium concentration of methane can reach 20-35mol%.Operating pressure is higher, and in synthetic gas, methane concentration is also higher.As shown in Figure 5, the circulation ratio of solid circle logistics 63 can be regulated by controlling loosening gas 84 flow, finally can realize the effective control to shortening gasification-hydropyrolysis integrated apparatus 86 temperature.Pyrolysis oven is entered after leaving shortening gasification-hydropyrolysis integrated apparatus 86 containing the synthetic gas of higher concentration methane.This synthetic gas first mixes mutually with the solids stream 66 from the upright dipleg of primary cyclone, and the solids stream 61 of the mixture flow formed dipleg upright with secondary cyclone again mixes mutually.The temperature of above-mentioned solids stream and autocatalysis hydrogasification stove and the gas-solid mixture that comes is roughly the same.
As shown in Figure 5, fresh feed coal 2 adds from the riser tube of pyrolysis oven.The particle diameter of fresh feed coal 2 is less than 800 μm, and median size is 150-200 μm.If using caking coal as charging, then charging and pyrolysis siege material need be pre-mixed in another one tank body, require that the concentration of inert particle in mixture is between 90-95%, to prevent pyrolytic process coking.Described pyrolysis oven is a circulating fluid bed reactor with higher bed material density preferably.The mass flux ratio scope of the solid circle circulated by riser tube and feed coal is 100-200, can ensure that in pyrolysis oven riser tube, material has higher temperature rise rate with this.In pyrolysis oven riser tube, the apparent velocity scope of gas phase is 6-15m/s, and the residence time of gas phase is 1-10s, and the best residence time is 2-4s.To be rapidly heated and under hydrogen atmosphere condition, by pyrolytic reaction, coal particle will be converted into the lighter hydrocarbons product of tar steam and gaseous state as methane, ethane etc.The residence time keeping shorter can avoid pyrolysis product that polymerization coking reaction occurs.As everyone knows, the semicoke that pyrolytic reaction produces is the catalyzer of pyrolysis product tar polymerization reaction take place and then coking.Although there is the gas of gasification reactivity as CO 2, H 2o, H 2can passivation semicoke to the catalytic activity of tar polyreaction.The present invention adopts the circulation dilution effect of the solid particulate be made up of inert component in coal ash in a large number to reduce semicoke concentration in solid circle further.
Being separated of nearly all inert particle and gas phase can be realized after the gas-solid mixture flow leaving hydrogenation fast pyrogenation section 4 riser tube enters vapourizing furnace primary cyclone 67.The semicoke particle only having particle diameter to be greater than 30 μm just can catch by primary cyclone.Although the average particle size range of pyrolysis oven feed coal is 150-200 μm, the particle diameter of the semicoke particle of the 40-50% that pyrolysis oven produces but is less than 30 μm.Inert particle and the larger semicoke particle of part particle diameter will circulate along upright dipleg 65 points of two-way under gravity: circulate to return and urge secondary to gasify hydrogasification stove 3 in a road, one tunnel circulation returns to the bottom of pyrolysis oven 4, and above-mentioned circulation returning charge route and equipment are shown in Fig. 5.
Carry the fine grain synthetic gas of part, enter secondary cyclone 59 from top after leaving cyclonic separator, the semicoke particle that most of particle diameter is greater than 10 μm in cyclonic separator will be captured.The semicoke particle that secondary cyclone is caught falls under gravity and enters dipleg 60.As shown in Figure 5, circulation is returned the riser tube of hydrogenation fast pyrogenation section 4 by the logistics of small portion semicoke granulometric composition through solids stream passage 61.Circulation is returned one-level hydrogasification stove through semicoke logistics pipeline 6 by most semicoke logistics.Although Fig. 5 only shows a primary cyclone and a secondary cyclone, give also the schematic diagram of dipleg and uprise dipleg simultaneously.But the engineering technical personnel being familiar with this technique list can also set up several cyclonic separators in every one-level cyclonic separation workshop section.In addition, all cyclonic separators can also be fixed in same pressurized vessel, and allow solid particulate from then on assemble in pressurized vessel and to be circulated by dipleg.
See Fig. 6, crude synthesis gas of the present invention-fine particle is separated and semicoke revert system 20 comprises and pyrolysis gas logistics 14, the anti-material cyclonic separator 75 be made up of several unit cyclonic separators 68 that circulation gas is connected, the isolated synthesis gas stream 21 of anti-material cyclonic separator 75 by the road with solution-air, liquid-liquid separation unit 22 is connected, the wall 72 that the dust that anti-material cyclonic separator 75 is caught enters hay tank 70 by diversion trench 74 encloses in 71 annular spaces surrounded 76 with skirt, hay tank 70 upper end is provided with filter core 69, lower end is cone 73, gas phase 77 upwards flows into filter core 69 and forms synthesis gas stream 85 and discharge, semicoke logistics 78 enters hopper 80 along thrust-augmenting nozzle 79, the semicoke logistics 19 formed in hopper 80 sends into oxygen-steam vapourizing furnace 12 along pipeline.
Pyrolysis oven heat outputting cracked gas stream 14 will first cool by Quench circulation gas 15, Quench circulation gas described herein 15 with loosen the circulation gas of gas from same recycle gas compressor as other equipment, it is emphasized that pyrolysis gas logistics 14 just should be cooled before not entering the unit cyclonic separator 68 in crude synthesis gas-fine particle separation and semicoke revert system herein.The cooled optimum temperature range of synthetic gas is 400-450 DEG C, and at this temperature, the polymerization coking reaction of tar component can be prevented from completely, can also stop the condensation of coal-tar middle oil and other oils products of gas phase simultaneously.Prevent tar condensing from being the lower limit of synthetic gas cooling temperature.
Gravity and carrier gas down direction sweep along the acting in conjunction of power under, hay tank 70 will be entered by diversion trench 74 by the dust that the anti-material cyclonic separator 75 set up separately is caught.Dust logistics enters through diversion trench 74 is enclosed in 71 annular spaces surrounded with skirt by the wall 72 of hay tank 70.The dust of entrainment portions gas will flow downward and enter above-mentioned annular space region.At cone 73 position, gas phase 77 will upwards flow into filter core 69, and the material that filter core described herein is comparatively suitable for is pottery or sintering metal.Synthetic gas after dedusting by the secondary washing tower in synthetic gas cleaning system, or mixes with synthesis gas phase for reaching in gas-liquid separation system that synthesis gas stream 85 washing, purifying object sets up separately.The synthetic gas removed after tar will enter gas treating system.Semicoke logistics 78 enters hopper 80 along thrust-augmenting nozzle 79 under gravity.
Under usual conditions, hopper 80 needs preparation two cover: one of them normal charging operating mode, another then receives the semicoke from hay tank.In addition, two hoppers also can at right angle setting: one be lock hopper another be hopper.Can adopt superheated vapour or circulation gas 81 that semicoke is delivered into oxygen-steam vapourizing furnace 12.
After gas-particle separation, in synthesis gas stream 21, the content of semicoke is less than 100ppm and enters solution-air, liquid-liquid separation device 22.In most preferred embodiment of the present invention, enter solution-air, liquid-liquid separation device 22 has two-stage washing device, and one-level is traditional Venturi scrubber, and one-level is as packing tower for the gas-liquid contact apparatus of condensation separation tar and water from gas phase in addition.The operating temperature range of one-level washer is 375-400 DEG C, and main purpose removes dust entrained by gas phase and heavy oil component.Secondary washing tower is then remove the most of tar and moisture that carry in synthetic gas.The typical operating temperature scope of secondary washing tower is 25-40 DEG C.
Solution-air, product liquid separating obtained in liquid-liquid separation system 22 also can carry out isolation of purified further.Oil-water separation realizes mainly through the mode of gravity settling.Different components in tar proceeds to be separated by common rectifying mode.Heavy oil containing dust can be sent to gasification in oxygen-steam vapourizing furnace and produce synthetic gas.Light oil entrained in synthetic gas after rectifying tower is separated carries out solution-air two-phase laminated flow by other common modes such as activated carbon adsorption bed.The oil product 24 of recovery gained as shown in Figure 1 mainly comprises aromatic hydrocarbons and light-end products as diesel oil and kerosene component.Separating obtained water 23 as refrigeration agent, as process cooling water, can also can be used as the chilled water of lime-ash on the one hand in addition on the one hand.The ammonia dissolved in separating obtained water 23 and phenols can be reclaimed by the mode of multistage flash evaporation or air lift.Chemical such as ammonia and phenols that aforesaid method reclaims can also be processed as Chemicals further.Or without the need to purification, these Chemicals can directly be vaporized to produce synthetic gas in oxygen-steam vapourizing furnace.
As shown in Figure 1, the primary purifying synthetic gas 2 after removing tar will enter in gas treating system 27 and reclaim CO further 2with H 2s.The CO that gas treating system reclaims 2with H 2may be used for producing highly purified CO after downstream processes further after S leaves gas treating system 27 2level Containing Sulfur chemical product.In most cases, without the need to CO being converted into CO by synthetic gas transformationreation 2, because 550-700 DEG C of synthetic gas transformationreation reaches chemical equilibrium.In other words, in secondary hydrogenation gasification and hydropyrolysis reactor, synthetic gas transformationreation reaches balance.And a large amount of CO is converted into methane in secondary hydrogenation vapourizing furnace.Therefore without the need to setting up a synthetic gas shift-converter again.Synthetic gas after purification finally also will enter cryogenic condensation separation system with light hydrocarbon products 29 such as further separation of methane, ethane.Main containing H 2and the synthetic gas 26 of CO will loop back hydrogasification stove as vaporized chemical and loosening gas.
The method of coal preparing natural gas of the present invention and light oil is as follows: by steam stream 10, oxygen stream 11 forms vaporized chemical and semicoke logistics 19 carries out gasification reaction in oxygen-steam vapourizing furnace 12, the lime-ash 13 produced is discharged by oxygen-steam vapourizing furnace 12 bottom ash discharging hole, one-level hydrogasification stove 8 is advanced on the synthetic gas 9 produced is direct, the descending oxygen-steam vapourizing furnace 12 that returns of the semicoke logistics 18 that one-level hydrogasification stove 8 produces proceeds gasification reaction, macrobead lime-ash logistics 17 is discharged by bottom one-level hydrogasification stove 8, ash particle logistics 16 capable of circulation times hydrogenation fast pyrogenation sections 4, feed coal 7 reacts in one-level hydrogasification stove 8 with circulation gas 26 and the synthetic gas 9 next from oxygen-steam vapourizing furnace 12, the synthetic gas containing higher concentration methane that one-level hydrogasification stove 8 produces is by synthesis gas stream pipeline 5 being advanced into shortening gasification-hydropyrolysis integrated apparatus 86, after fresh feed coal 2 enters shortening gasification-hydropyrolysis integrated apparatus 86, pyrolytic reaction is carried out with the high-temperature solid particle of sweeping along as thermal source using the synthetic gas containing higher concentration methane exported from one-level hydrogasification stove 8 top, semicoke logistics pipeline 6 of passing through under pyrolysis char and inert particle enters one-level hydrogasification stove 8, the pyrolysis gas logistics 14 that shortening gasification-hydropyrolysis integrated apparatus 86 exports enters crude synthesis gas-fine particle again and to be separated and semicoke revert system 20 carries out the initial gross separation purifying treatment of synthetic gas after Quench circulation gas 15 cools, semicoke logistics 19 circulation that crude synthesis gas-fine particle is separated and semicoke revert system 20 traps returns oxygen-steam vapourizing furnace 12, synthesis gas stream 21 enters solution-air, liquid-liquid separation unit 22, separating obtained liquid product is respectively water 23 and tar 24, solution-air, liquid-liquid separation unit 22 export through oil removing, the primary purifying synthesis gas stream 25 of processed is divided into two branch roads: circulation gas logistics 39 returns as sharp circulating cold air the synthetic gas 9 exported with oxygen-steam vapourizing furnace 12 top and mixes mutually, remaining decontaminating syngas then enters gas treating system 27, the purified gas that gas treating system 27 produces is divided into two bursts of outputs, one returns one-level hydrogasification stove 8 as circulation gas 26 and is separated and semicoke revert system 20 with crude synthesis gas-fine particle, wherein return the Quench gas of circulation gas for pyrolysis gas logistics 14 of crude synthesis gas-fine particle separation and semicoke revert system 20, the gas phase hydrocarbon of another strand based on methane then exports as the finished product 29, separating obtained CO 2, H 2s mixture flow 28 continues to enter downstream and carries out being separated and advanced treatment.

Claims (10)

1. a device for coal preparing natural gas and light oil, is characterized in that: comprise with feed coal pipeline be connected the shortening be made up of shortening gasification section (3) and hydrogenation fast pyrogenation section (4) gasify-hydropyrolysis integrated apparatus (86), oxygen-steam vapourizing furnace (12), one-level hydrogasification stove (8), crude synthesis gas-fine particle is separated and semicoke revert system (20), solution-air, liquid-liquid separation unit (22), gas treating system (27);
The semicoke logistics pipeline (6) of shortening gasification-hydropyrolysis integrated apparatus (86) is connected with one-level hydrogasification stove (8), the synthesis gas stream pipeline (5) of one-level hydrogasification stove (8) gasifies with shortening-and hydropyrolysis integrated apparatus (86) is connected, the pyrolysis gas logistics (14) that shortening gasification-hydropyrolysis integrated apparatus (86) exports to be separated with crude synthesis gas-fine particle through pipeline and semicoke revert system (20) is connected, crude synthesis gas-fine particle is separated and the synthesis gas stream (21) of semicoke revert system (20) is connected with solution-air and liquid-liquid separation unit (22) by the road, the outlet of solution-air and liquid-liquid separation unit (22) divides three tunnels, be respectively separating obtained water (23), the oil product (24) reclaiming gained and the primary purifying synthesis gas stream (25) be connected with gas treating system (27), through the CO of gas treating system (27) purification separation gained 2, H 2s mixture flow (28) continues to enter downstream and carries out being separated and advanced treatment, and the methane after separation and other gas phase alkane export as product (29), CO and H of gained after being separated 2return one-level hydrogasification stove (8) as circulation gas to be separated and semicoke revert system (20) with crude synthesis gas-fine particle, the macrobead lime-ash logistics (17) of one-level hydrogasification stove (8) is discharged through pipeline, semicoke logistics (18) is connected with oxygen-steam vapourizing furnace (12) through pipeline, the synthetic gas (9) that oxygen-steam vapourizing furnace (12) top exports is connected with one-level hydrogasification stove (8) through pipeline, primary purifying synthesis gas stream (25) is also connected through the pipeline of circulation gas logistics (39) with synthetic gas (9), the stove material that enters of oxygen-steam vapourizing furnace (12) is respectively steam stream (10), oxygen stream (11) and the semicoke logistics (19) that crude synthesis gas-fine particle is separated and semicoke revert system (20) is discharged, the outlet of oxygen-steam vapourizing furnace (12) is slag (13) pipeline.
2. the device of coal preparing natural gas according to claim 1 and light oil, it is characterized in that: the gasification section (30) of described oxygen-steam vapourizing furnace (12) adopts the inclined structure that dips down, semicoke logistics (19), steam stream (10), oxygen stream (11) tangentially enters gas-slag separating tank (31) by tangentially injecting gasification section (30) mix products, lime-ash (34) enters the bottom of gas-slag separating tank (31), the grey solid impurity particle (33) of gas-slag separating tank (31) trapping gained flows downward along inwall, chilled water (32) adds from gas-slag separating tank (31) bottom, the position added is below gas-slag mixture inlet, the synthetic gas (9) leaving separating tank (31) enters one-level hydrogasification stove (8).
3. the device of coal preparing natural gas according to claim 1 and light oil, it is characterized in that: the gasification section (30) of described oxygen-steam vapourizing furnace (12) adopts direction vertically downward, semicoke logistics (19), steam stream (10), oxygen stream (11) tangentially injects gasification section (30), linkage section (35) is entered under gas phase and lime-ash also flow to, in the downward flow ipe bottom slag discharge gradually of linkage section (35) slag (34), linkage section (35) tangentially enters gas-slag separating tank (31), the grey solid impurity particle (33) of gas-slag separating tank (31) trapping gained flows downward along inwall, chilled water (32) adds from gas-slag separating tank (31) bottom, the position added is below gas-slag mixture inlet, the synthetic gas (9) leaving separating tank (31) enters one-level hydrogasification stove (8).
4. the device of coal preparing natural gas according to claim 1 and light oil, it is characterized in that: described one-level hydrogasification stove (8) comprises cone structure (38), cylinder (40) upper end of cone structure (38) vertical direction be also provided with for connect body of heater (36) cut sth. askew to cone (37), the bottom of cone structure (38) and semicoke logistics pipeline (6), feed coal pipeline (7) is connected, its profile is intilted eccentric cone, synthetic gas (9), circulation gas logistics (39) enters one-level hydrogasification stove (8) by centre, side bottom it, and macrobead lime-ash logistics (17), ash particle logistics (16) then to be discharged and capable of circulation to hydrocracking section (4) from the bottommost of opposite side cone, be positioned in body of heater (36) directly over cone (37) and be provided with emulsion zone (43), in emulsion zone, body of heater (36) circumference is provided with several primary cyclones (44), the multicyclone (48) be connected with the outlet pipe of primary cyclone (44) (46) is also provided with in primary cyclone (44) upper end, the synthesis gas stream that multicyclone (48) is separated is connected with synthesis gas stream transport pipe (5) through diversion trench (49), the lower end of multicyclone (48) is provided with dipleg (58), the whirlwind dipleg (56) of multicyclone (48) stretches in dipleg (58), the semicoke particle (57) of an outlet of dipleg (58) enters bed as circulating granular, the semicoke particle (18) of an outlet of dipleg (58) joins oxygen-steam vapourizing furnace (12) as fuel.
5. the device of coal preparing natural gas according to claim 4 and light oil, is characterized in that: described cone structure (38) discharges macrobead lime-ash logistics (17), the side of semicoke logistics (18) also offers fluidized gas entrance (62); The sidewall of cone (37) offers cone fluidized gas entrance (82), dipleg (58) is connected with fluidized gas and passes into pipeline (83).
6. the device of coal preparing natural gas according to claim 4 and light oil, it is characterized in that: the diameter on described primary cyclone (44) top cylindrical shell (45) is 0.4-0.8m, the crude synthesis gas produced tangentially enters primary cyclone (44) by entrance (55), the solid particulate (41) that primary cyclone (44) traps returns bed by the dipleg (42) of cyclonic separator, and the distance between the position that exports of dipleg (42) and cone (37) inwall be the 2-4 of whirlwind dipleg (42) diameter doubly.
7. the device of coal preparing natural gas according to claim 4 and light oil, it is characterized in that: described multicyclone (48) comprises some groups of small cyclones separator units (51), entered the gas inlet surge bunker (52) of multicyclone (48) by the outlet pipe (46) at cyclonic separator top containing the fine grain crude synthesis gas of semicoke (47) after primary cyclone gas-particle separation, primarily of semicoke composition fine particle (53) trapped by multi-cyclone after be collected in granule capturing storehouse (54), dipleg (58) is entered subsequently by whirlwind dipleg (56).
8. the device of coal preparing natural gas according to claim 1 and light oil, it is characterized in that: the riser tube of hydropyrolysis section (4) the interior pyrolysis oven of described shortening gasification-hydropyrolysis integrated apparatus (86) is connected with feed coal (2), feed coal (2) is carried by conveying gas (1), be divided into two branch roads, a branch road enters the hydrogenation fast pyrogenation section (4) of shortening gasification-hydropyrolysis integrated apparatus (86), another branch road enters one-level hydrogasification stove (8), the pyrolysis gas that hydrogenation fast pyrogenation section (4) top exports is connected with pyrolysis oven primary cyclone (67) entrance, pyrolysis oven secondary cyclone (59) is entered after leaving cyclonic separator from pyrolysis oven primary cyclone (67) top, the gas-solid mixture flow (14) that pyrolysis oven secondary cyclone (59) exports to be separated with crude synthesis gas-fine particle through pipeline and semicoke revert system (20) is connected, the semicoke logistics that pyrolysis oven secondary cyclone (59) is caught enters dipleg (60) rear portion and returns shortening gasification-hydropyrolysis integrated apparatus (86) by solids stream passage (61) circulation, the logistics of another part semicoke is connected with one-level hydrogasification stove (8) entrance through pipeline (6), pyrolysis oven primary cyclone (67) isolated carbonaceous solid particulates (63) returns hydrogenation fast pyrogenation section (4) through upright dipleg (65) circulation, simultaneously, in order to ensure the circulation ratio of solid circle, the upright dipleg (65) be connected with hydrogenation fast pyrogenation section (4) also offers the entrance be connected with loosening gas (84),
Shortening gasification section (3) is fluidized-bed reactor, in bed, material load has the particle of gasification catalysis active ingredient, synthesis gas stream (5) mixes mutually with the semicoke logistics (63) returned from hydrogenation fast pyrogenation section, carries out gas phase and gas-solid two alternate hydrogenation methanation reactions simultaneously.
9. the device of coal preparing natural gas according to claim 1 and light oil, is characterized in that: described crude synthesis gas-fine particle is separated and semicoke revert system (20) comprises the returning charge cyclonic separator (75) be made up of several unit cyclonic separators (68) be connected with pyrolysis gas logistics (14), circulation synthetic gas (26), the gas-solid hay tank (70) of the built-in efficient filter core be connected with dust diversion trench (74), the hopper (80) be connected with hay tank (70) outlet at bottom thrust-augmenting nozzle (69), the synthesis gas stream (21) that returning charge cyclonic separator (75) bottom exports is connected with gas-particle separation unit (22) by the road, the dust that returning charge cyclonic separator (75) is caught enters in the annular space region (76) surrounded by the wall of hay tank (70) (72) and skirt (71) by diversion trench (74), hay tank (70) upper end is provided with filter core (69), lower end is cone (73), gas phase (77) upwards flows into filter core (69) and forms synthesis gas stream (85) discharge, semicoke logistics (78) enters hopper (80) along thrust-augmenting nozzle (79), the semicoke logistics (19) formed in hopper (80) enters oxygen-steam vapourizing furnace (12) along pipeline.
10. one kind as the coal preparing natural gas of any one device in claim 1-10 and the method for light oil, it is characterized in that: by steam stream (10), oxygen stream (11) composition vaporized chemical and semicoke logistics (19) carry out gasification reaction in oxygen-steam vapourizing furnace (12), the lime-ash (13) produced is discharged by oxygen-steam vapourizing furnace (12) bottom ash discharging hole, one-level hydrogasification stove (8) is advanced on the synthetic gas (9) produced is direct, the descending oxygen-steam vapourizing furnace (12) that returns of the semicoke logistics (18) that one-level hydrogasification stove (8) produces proceeds gasification reaction, macrobead lime-ash logistics (17) is discharged by one-level hydrogasification stove (8) bottom, feed coal (7) reacts in one-level hydrogasification stove (8) with circulation gas (26) and the synthetic gas (9) next from oxygen-steam vapourizing furnace (12), the synthetic gas containing higher concentration methane that one-level hydrogasification stove (8) produces is by synthesis gas stream pipeline (5) is advanced into shortening gasification-hydropyrolysis integrated apparatus (86), after fresh feed coal (2) enters shortening gasification-hydropyrolysis integrated apparatus (86), pyrolytic reaction is carried out with the high-temperature solid particle of sweeping along as thermal source using the synthetic gas containing higher concentration methane exported from one-level hydrogasification stove (8) top, semicoke logistics pipeline (6) of passing through under pyrolysis char and inert particle enters one-level hydrogasification stove (8), the pyrolysis gas logistics (14) that shortening gasification-hydropyrolysis integrated apparatus (86) exports enters crude synthesis gas-fine particle again and to be separated and semicoke revert system (20) carries out the initial gross separation purifying treatment of synthetic gas after Quench circulation gas (15) cooling, semicoke logistics (19) circulation that crude synthesis gas-fine particle is separated and semicoke revert system (20) traps returns oxygen-steam vapourizing furnace (12), 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) export through oil removing, the primary purifying synthesis gas stream (25) of processed is divided into two branch roads: circulation gas logistics (39) returns as sharp circulating cold air the synthetic gas (9) exported with oxygen-steam vapourizing furnace (12) top and mixes mutually, remaining decontaminating syngas then enters gas treating system (27), the methane that gas treating system (27) produces and other gas phase hydrocarbon are as output of products, CO and H 2return one-level hydrogasification stove (8) as circulation gas to be separated and semicoke revert system (20) with crude synthesis gas-fine particle, the circulation gas wherein returning crude synthesis gas-fine particle separation and semicoke revert system (20) is used for the Quench gas of pyrolysis gas logistics (14), separating obtained CO 2, H 2s mixture flow (28) continues to enter downstream and carries out being separated and advanced treatment.
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CN107099319A (en) * 2017-05-27 2017-08-29 李大鹏 The device and method of methane rich synthesis gas and light tar is produced in a kind of synchronization
CN107353936A (en) * 2017-09-04 2017-11-17 东华工程科技股份有限公司 The purification separation system and its technique of a kind of hydrogasification synthesis gas
CN109453824A (en) * 2018-11-15 2019-03-12 新奥科技发展有限公司 Catalyst carrying method and catalytic hydrogenation gasification process
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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
CN109054903B (en) * 2018-08-24 2021-04-16 新奥科技发展有限公司 Coal hydro-gasification method and device
CN115261079A (en) * 2022-08-25 2022-11-01 西安交通大学 Circulating fluidization device and method for preparing synthesis gas
CN117106489A (en) * 2023-10-23 2023-11-24 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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CN107099319A (en) * 2017-05-27 2017-08-29 李大鹏 The device and method of methane rich synthesis gas and light tar is produced in a kind of synchronization
CN107353936A (en) * 2017-09-04 2017-11-17 东华工程科技股份有限公司 The purification separation system and its technique of a kind of hydrogasification synthesis gas
CN107353936B (en) * 2017-09-04 2019-12-24 东华工程科技股份有限公司 Purification and separation system and process for hydro-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
CN110467943A (en) * 2018-05-11 2019-11-19 成都聚实节能科技有限公司 A kind of natural gas from coal, alkene and coal tar method
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
CN109453824A (en) * 2018-11-15 2019-03-12 新奥科技发展有限公司 Catalyst carrying method and catalytic hydrogenation gasification process
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
CN115261079A (en) * 2022-08-25 2022-11-01 西安交通大学 Circulating fluidization device and method for preparing synthesis gas
CN115261079B (en) * 2022-08-25 2023-08-15 西安交通大学 Circulating fluidization device and method for preparing synthesis gas
CN117106489A (en) * 2023-10-23 2023-11-24 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
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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