CN104109543A - Powder pyrolysis method using circulating fluidized bed technology - Google Patents
Powder pyrolysis method using circulating fluidized bed technology Download PDFInfo
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Abstract
A powder pyrolysis method using a circulating fluidized bed technology is especially suitable for the pyrolysis of fine coal and other organic powders. The circulating fluidized bed pyrolysis method characteristics the following steps: a gas F14 discharged from the top of a fluidized bed pyrolysis chamber R1 of fine coal F11 is separated in a first separation part S1 to form first semi-coke S1S and a first gas S1V, and the first semi-coke S1S partially or completely returns to the lower portion of the fluidized bed pyrolysis chamber R1. The whole fluidized bed becomes an efficient heating chamber and a rapid pyrolysis chamber of the fine coal F11. Compared with routine semi-coke-free circulating technologies, the method has the advantages of fast pyrolysis speed, stable operation, flexible adjustment, increases of the tar output, and suitableness for large scale processing. The separation characteristic particle size of a first stage separation process is controlled when the discharged gas F14 undergoes tandem two-stage separation in order to make small grain semi-coke separated after second stage separation enter a stripping chamber for stripping, so the output of fine powder of semi-coke is lower than that of the return of the small grain semi-coke to the fluidized bed pyrolysis chamber R1.
Description
Technical field
The present invention relates to a kind of powder method for pyrolysis that uses Circulating Fluidized Bed Process; Say especially, the present invention relates to the combined method of a kind of gaseous heat-carrier (carbonized gas that the synthetic gas producing as gasification or carbonization process produce etc.) and the circulating fluidized bed pyrolysis oil preparation process of powder, for realizing powder as the clean and effective pyrolysis of coal, resinous shale, oil-sand etc.
Background technology
Powder pyrolysis of the present invention, is often referred to the process that powder decomposes is gas and solid.Powder of the present invention is generally organic powder that can produce hydrocarbon vapours under heating condition, comprises fine coal, coal gangue, resinous shale, oil-sand, biomass and waste or used plastics etc.
Pulverized coal pyrolysis of the present invention, refers to described fine coal is implemented heat treated, made it parse fugitive constituent to complete the hot procedure that partial gasification obtains pyrolysis gas and semicoke, and pyrolysis gas contains oil vapour and flammable non-condensable gas conventionally as H
2, CO, CH
4deng in a kind of, two or more components, pyrolysis gas can obtain conventional liq hydrocarbon after condensation.
Known PC-FB method for pyrolysis mostly is one way through type, its shortcoming is that fluidized bed pyrolysis chamber cannot provide the sufficiently long residence time cannot provide sufficiently long pyrolysis time, because the sufficiently long residence time mean low fluidizing velocity and or high fluidized-bed layer height, because the granularity of fine coal is confined to 0～13 millimeter, there is a critically limit low value in its fluidizing velocity, in order to guarantee the stable of fluidized-bed, fluidizing velocity must be higher than critically limit low value.Because fine coal exists certain particle size, distribute, the gas friction that in a through type PC-FB pyrolysis chamber, macroparticle specific surface area is little, be subject to and the ratio of deadweight are little, and in fluidized bed pyrolysis chamber, speed uplink is slow, and the residence time is long; Small-particle specific surface area gas friction large, that be subject to is large, and in fluidized bed pyrolysis chamber, speed uplink is fast, and the residence time is short.The residence time of different-size particles in fluidized bed pyrolysis chamber can be divided into pyrolysis before warm up time, pyrolysis time and semicoke escape the time, the semicoke escape time is less to improving the effect of pyrolysis effect, but its particle collision can the more most burnt fine powders of cracked generation.Clearly, under the certain condition of fluidized bed pyrolysis chamber height, if just guarantee the pyrolysis effect of maximum diameter coal dust particle, conventionally cause the pyrolysis effect of smaller particle size coal dust particle (namely most of coal dust particle) to reach in advance, the semicoke time of escaping is grown and manufactures how fine coke powder, and semicoke escape time while is longer, and the lost work that liquid agent is done particle is more, fine coke powder output is larger, separated just more difficult with coal gas.On the other hand, under the certain condition of fluidized bed pyrolysis chamber height, in order to reduce fine coke powder output, need to reduce the semicoke of most of particles escapes the time, if only guarantee a certain feature coal dust particle diameter (be greater than minimum grain size and be less than maximum particle diameter) and the pyrolysis effect of small-particle more thereof, conventionally cause the pyrolysis of the coal dust particle that is greater than feature coal dust particle diameter insufficient.That is to say, in fluidized bed pyrolysis chamber, have the contradiction of the pyrolysis degree of depth and the excessive fine coke powder of manufacture: wish guarantees the pyrolysis degree of depth, certainly leads to a large amount of fine coke powders; Wish reduces fine coke powder output, must reduce the pyrolysis degree of depth.Moreover because fluidized bed pyrolysis chamber does not have the back-mixing of macroparticle, the preheating of coal dust is mainly by gas-particle heat transfer, far beyond heat-transfer effect is poor admittedly, in order to guarantee the pyrolysis effect of maximum diameter coal dust particle, the height that needs to increase fluidized bed pyrolysis chamber, causes fluidized bed pyrolysis chamber height larger.This is a large shortcoming of a through type PC-FB pyrolysis chamber existence.
Known PC-FB method for pyrolysis mostly is one way through type, a kind of is air flow bed method for pyrolysis, be that the hot fine coal raw material that certain particle size distributes enters fluidized-bed bottom, under high temperature fluidized gas effect, self-fluidized type bed bottom moves up, in a through type PC-FB pyrolysis chamber, all discharge at top, semicoke product self-fluidized type bed pyrolysis chamber.As number of patent application 200310116687.7 oil shale material fluidized bed pyrolysis and decarbonization process and the disclosed content of number of patent application 200610151086.3 fluidization hydrogenation liquefaction method for coal, pulverized coal pyrolysis route is that one way is passed through, fluidized bed pyrolysis chamber does not arrange semicoke outer circulation, and inside also exists coal dust/semicoke internal recycle hardly.
Another kind of PC-FB method for pyrolysis is also one way through type, and coal charge adds fluidized bed pyrolysis chamber, and small-particle semicoke self-fluidized type bed pyrolysis chamber discharges with pyrolysis gas at top, and discharge bottom, macrobead semicoke self-fluidized type bed pyrolysis chamber.It is that 200910153522.4 circulating fluidized bed coals grading transform gas, tar, semi-coke multi-joint-production apparatus and method that these class methods have the application number of Zhejiang University, relate to a kind of pulverized coal pyrolysis technique, adopt the normal pressure fluidized bed pyrolysis oven, its fluidizing agent is the pyrolysis coal gas that returns confession.The gas-solid logistics that discharge at top, fluidized bed pyrolysis chamber, is separated into coal gas gas and ejects semicoke solid through separator, ejects semicoke solid and enters fluidized-bed gasification furnace, does not return to the semicoke recycle system of fluidized bed pyrolysis chamber.Cycle stock (being formed by semicoke, the circulating ash) solid thermal carriers that pyrolysis heat absorption produces for fluidized-bed gasification furnace, pyrolysis oven bottom is connected with thermal barrier and carrys out pipe material, and bottom is connected with conveying semicoke and coal ash to the charging line of vapourizing furnace.In combined system, pyrolytic process belongs to once generally by flow process, and the pyrolysis time of different-grain diameter fine coal is not controlled, and the semicoke that discharge at the semicoke that pyrolysis chamber is got rid of bottom and top is carried the inadequate green coke of partial thermal decomposition secretly, and tar yield is lower.The semicoke that does not complete the expection pyrolysis degree of depth directly enters vapourizing furnace, and its tar components direct gasification is synthetic gas, has reduced again oil product yield.
The patent CN100445351C double lift pipe circulation fluidized bed coal gasifying device of University of Petroleum China, comprises the pyrolysis fluidized-bed (pyrolysis) of fine coal, the ciculation fluidized burning bed (partial gasification under air atmosphere) of pyrolysis char, the bubbling fluidized bed of gasification char material (gasification char and ash) and the gasification circulating fluidized bed of gasification char material.Because char Gasification need at high temperature operate, seldom, the bubbling fluidized bed function of gasification char material (gasification char and ash) is mainly to adopt bubbling fluidized bed to mix with degassed two-way gasification char material to the fugitive constituent of the gasification char material solid interior after char Gasification.
The application number of Institute of Engineering Thernophysics, Academia Sinica is 200410081018.5 double-circulating fluid bed coal gas-steam combined production method and device, relate to a kind of pulverized coal pyrolysis technique, first coal dust enters circulating fluidized bed combustor, high-temperature lower part divided combustion at 800 ℃ to 1000 ℃, fugitive constituent after-flame substantially in combustion chamber, the ash-laden gas that discharge combustion chamber is separated into dedusting flue gas and circulating ash through separator.Circulating ash is divided into two-way, and first via circulating ash is returned to combustion chamber and formed circulation, and the second tunnel circulating ash enters fluidized-bed gasification chamber partial gasification, and as the thermal barrier of gasification, vaporizer service temperature is 700 ℃ to 950 ℃ simultaneously.Although the function of circulating fluidized bed vaporizer is gas making, in the fugitive constituent of the second tunnel circulating ash seldom, the coal gas that its pyrolysis produces is limited, and the accounting in total coal gas seldom.The essence of this technique is circulating fluidized bed combustion and the gasification of semicoke circulating fluidized bed.
Shortcoming for an above-mentioned through type PC-FB pyrolyzer, the present invention proposes a kind of pulverized coal circulating fluidized bed method for pyrolysis.The fine coal that enters pyrolyzer has certain size-grade distribution, and macroparticle coal dust falls along wall after colliding wall in fluidized gas uphill process, simultaneously cracked, forms internal recycle, and pyrolyzer internal temperature is reached unanimity.The gas-solid mixed phase logistics of pulverized coal circulating fluidized bed pyrolyzer is separated into first at the first cyclonic separator and revolves minute solid phase logistics and contain first of small particle size particle and revolve a minute gas-solid mixed phase logistics, the Semi Coke Particles that degree of pyrolysis is high enters first and revolves in minute gas-solid mixed phase logistics, completes pulverized coal pyrolysis process; At least a portion first is revolved a minute solid phase logistics and is returned in pyrolyzer and contact with coal dust particle as first and revolve a minute solid phase recycle stream, form the outer circulation back-mixing of large grain semicoke, between strengthening solid, conduct heat, shorten the heat-up time of coal dust, first of remainder revolves a minute solid phase logistics and can be used as semicoke product, finishes pulverized coal pyrolysis process, along with the increasing of recycle ratio, green coke ratio in semicoke product reduces, and has improved the pyrolysis degree of depth of large grain semicoke.First revolves a minute gas-solid mixed phase logistics can enter the second cyclonic separator, being separated into second revolves minute solid phase logistics and contains second of fine grain size particle and revolve a minute gas-solid mixed phase logistics, part as required, second revolves a minute solid phase logistics returns in pyrolyzer and contacts with coal dust particle as second and revolve a minute solid phase recycle stream, form the outer circulation back-mixing of granule semicoke, between strengthening solid, conduct heat, shorten the heat-up time of coal charge, second of remainder revolves minute solid phase logistics as granule semicoke product, finish pulverized coal pyrolysis process, increasing along with recycle ratio, green coke ratio in granule semicoke product reduces, improved the pyrolysis degree of depth of granule semicoke.The semicoke recycle ratio of sized particles all can regulate separately.
Major objective and the effect of technical solution of the present invention are:
1. reduce semicoke and escape the time, reduce fine silt suboutput, reduce the height of pulverized coal circulating fluidized bed pyrolyzer, the inner-outer circulation of strengthening pulverized coal circulating fluidized bed pyrolysis system, strengthens the heat-transfer capability of fluidized-bed, shortens coal dust heat-up time;
2. by improving working pressure, compressed gas volume, significantly improves device processing power;
3. can be combined as combined method with any suitable semicoke processing or the coal course of processing, not need to arrange dedicated stream agent system.
The circulating fluidized bed method for pyrolysis of fine coal of the present invention has no report.
The first object of the present invention is to propose a kind of powder method for pyrolysis that uses Circulating Fluidized Bed Process.
The second object of the present invention is to propose a kind of pulverized coal pyrolysis method that uses Circulating Fluidized Bed Process.
Summary of the invention
A kind of powder method for pyrolysis that uses Circulating Fluidized Bed Process of the present invention, is characterized in that:
1. in fluidized bed pyrolysis chamber R1 part, fluidized gas F13 enters the R1 of pyrolysis chamber from bottom, containing organic powder F11, enter the R1 of pyrolysis chamber and form fluidized under the effect of up gas, in the R1 of fluidized bed pyrolysis chamber, powder F11 is heated and carries out pyrolytic reaction by thermal barrier, the pyrolysis gas that generation comprises non-condensable gas and tar steam and semicoke, pyrolysis gas mixes with fluidized gas and carries Semi Coke Particles and discharge from R1 top, pyrolysis chamber, becomes and discharges gas F14;
2. at the first separate part S1, logistics F14 carries out the first semicoke S1S and the first gas S1V that gas solid separation obtains and leaves respectively the first separate part S1;
3. by circulation revert pipe XHG1, part or all of the first semicoke S1S returns to the R1 of pyrolysis chamber, forms the first semicoke recycle stream S1SR.
When a small amount of large-size particles of fluidized bed pyrolysis chamber R1 bottom accumulation, need to be interrupted or to discharge continuously, now feature of the present invention is further: 1. semicoke F18 is discharged in the R1 of pyrolysis chamber bottom.
The first semicoke recycle stream S1SR that the present invention exists returns to the lower region of the R1 of pyrolysis chamber conventionally.
The present invention can be separated into two groups by particle diameter by the semicoke of discharging in gas F14, and now feature of the present invention is further: 4. at the second separate part S2, logistics S1V carries out that gas solid separation obtains the second semicoke S2S and the second gas S2V leaves the second separate part S2; The second semicoke S2S enters stripping chamber K and adopts water vapor to complete stripping, obtains stripping gas KV and finished product semicoke KS.
Stripping of the present invention chamber K can be solid moving-bed or bubbling fluidized bed, in stripping chamber, the K semicoke residence time is generally 2 minutes～and 120 minutes.
Of the present invention containing organic powder F11, refer to the solid powder that produces hydrocarbon vapours under heating condition, be selected from fine coal, coal gangue, resinous shale, oil-sand, biomass and waste or used plastics.
The present invention, when the powder of processing is fine coal, at the R1 of PC-FB pyrolysis chamber, can arrange the entrance that adds of the second raw material of processing altogether with fine coal, and the second raw material of fluidized bed pyrolysis chamber R1 is the material that contains coal-tar pitch, carries out thermo-cracking or the fluid coking of coal-tar pitch; The second raw material is selected from following form: liquid coal-tar pitch sprays into fluidized-bed and contacts with powder, or the coal-tar pitch after gas atomization sprays into fluidized-bed and contact with powder, or the coal oil mixture mixture being comprised of coal-tar pitch and fine coal and/or semicoke; Pyrolysis chamber's the second raw material add the middle and lower part that entrance is generally positioned at fluidized bed pyrolysis chamber R1.
When the powder F11 of the present invention's processing is fine coal, the fluidizing agent of the R1 of PC-FB pyrolysis chamber, is coal gasification course synthetic gas or char Gasification process synthetic gas or semicoke carbonization process carbonized gas or pyrolysis coal gas or water vapor.
When the powder of the present invention's processing is fine coal, fluidized bed pyrolysis chamber R1, use the fluidized gas of hydrogen rich gas to form hydropyrolysis atmosphere, the working pressure of the R1 of PC-FB pyrolysis chamber is 1～8MPa, can in the raw material fine coal F11 of fluidized bed pyrolysis chamber R1, add hydropyrolysis metal catalyst, this catalyzer be selected from iron-based, molybdenum base, zinc-base, Ni-based, tinbase, cobalt-based metal catalyst a kind of, two or more, the addition of catalyzer is 0～15% of feed coal mass rate.
When the present invention processes fine coal, its operational condition scope is:
1. fine coal F11 is selected from: brown coal, long-flame coal, non-caking coal, weakly caking coal, bituminous coal; Pulverized coal particle size distribution range is generally 0.001～13 millimeter, is generally 0.001～8 millimeter, is preferably 0.001～6 millimeter; Fine coal F11 temperature is generally 100～450 ℃, is generally 200～350 ℃;
The R1 of PC-FB pyrolysis chamber operational condition: working pressure is generally normal pressure～8MPa, is generally normal pressure～2MPa, is preferably normal pressure～1MPa, service temperature is generally 400～1000 ℃, is generally 500～800 ℃, is 550～700 ℃ during middle low temperature pyrogenation;
2. the Action Target of the first separate part S1 is the macroparticle of isolating expection characteristic diameter, and characteristic diameter is generally 10～250 microns, is generally 50～200 microns, is preferably 100～150 microns.
3. part the first semicoke directly returns to the R1 of pyrolysis chamber and forms the first semicoke recycle stream S1SR, the mass rate of semicoke recycle stream S1SR is defined as semicoke recycle ratio with the ratio of the mass rate of raw material fine coal F11, this recycle ratio is generally 0.001～20, is generally 0.5～10, is preferably 3～8;
4. at stripping chamber K, the semicoke residence time is generally 2 minutes～and 120 minutes.
Accompanying drawing explanation
Accompanying drawing 1 is the schematic flow sheet of general planning of the present invention, and in accompanying drawing 1, major equipment has: the powders flowing purification Chuan Liu R1 of pyrolysis chamber, separate part S1, circulation revert pipe XHG1.The pipeline relevant to the powders flowing purification bed R1 of pyrolysis chamber: powder F11 input tube 11, the second raw material F12 input tube 12, vaporized chemical F13 input tube 13, pyrolysis chamber discharge gas F14 vent pipe 14, circulation revert pipe XHG1.The pipeline relevant to separate part S1: feed-pipe 14, gaseous stream S1V vent pipe 21, solid phase logistics S1S vent pipe 22.Separate part S1, selects cyclonic separator conventionally.In figure, BW represents lagging casing, utilizes gaseous stream S1V to be incubated separator S1.
Accompanying drawing 2 represents, on scheme basis shown in accompanying drawing 1, when a small amount of large particle diameter of fluidized bed pyrolysis chamber R1 bottom accumulation F18, needs to be interrupted or through pipeline 18, discharges continuously; When separate part S1, circulation revert pipe XHG1 system accumulation semicoke S1SP, need to be interrupted or through pipeline 32, discharge continuously.
Accompanying drawing 3 expressions, on scheme basis shown in accompanying drawing 2, logistics F14 is introduced into separator S1 and carries out separation, then enters separator S2 and carries out separation, separator S1 and the operation of separator S2 two-stage series connection; At the second separate part S2, logistics S1V carries out that gas solid separation obtains the second semicoke S2S and the second gas S2V leaves the second separate part S2; At stripping chamber K, water vapor F51 enters through pipeline 51, and the second semicoke S2S enters stripping chamber K through pipeline 42 and adopts water vapor F51 to complete stripping, and the stripping gas KV obtaining discharges through pipeline 52, and the finished product semicoke KS obtaining discharges through pipeline 53.
Accompanying drawing 4 is the separate part S1 of general planning of the present invention, the second form of circulation revert pipe XHG1, compares with scheme shown in accompanying drawing 1, and lagging casing BW is not set, and need to outer insulation be set to separator S1.
Accompanying drawing 5 is the separate part S1 of general planning of the present invention, the third form of circulation revert pipe XHG1, compare with scheme shown in accompanying drawing 1, the interface that circulation revert pipe XHG1 is set on the lagging casing BW arranging, separator S1 pneumatic outlet directly stretches out outside lagging casing BW.
Embodiment
Below describe the present invention in detail.
Pressure of the present invention, refers to absolute pressure.
Below in conjunction with accompanying drawing, take pulverized coal pyrolysis as example, describe technical solution of the present invention in detail.
Accompanying drawing is drawn for the present invention is described, but can not limit range of application of the present invention.
A kind of powder method for pyrolysis that uses Circulating Fluidized Bed Process of the present invention, is characterized in that:
1. in fluidized bed pyrolysis chamber R1 part, fluidized gas F13 enters the R1 of pyrolysis chamber from bottom, containing organic powder F11, enters the R1 of pyrolysis chamber, under the effect of up gas, forms fluidized.In the R1 of fluidized bed pyrolysis chamber, powder F11 is heated and carries out pyrolysis gas and the semicoke that pyrolytic reaction generation comprises non-condensable gas and tar steam by thermal barrier, pyrolysis gas mixes with fluidized-bed fluidized gas and carries Semi Coke Particles and discharge from R1 top, pyrolysis chamber, becomes and discharges gas F14;
2. at the first separate part S1, logistics F14 carries out the first semicoke S1S and the first gas S1V that gas solid separation obtains and leaves respectively the first separate part S1;
3. by circulation revert pipe XHG1, part or all of the first semicoke S1S returns to the R1 of pyrolysis chamber, forms the first semicoke recycle stream S1SR.
When a small amount of large-size particles of fluidized bed pyrolysis chamber R1 bottom accumulation, need to be interrupted or to discharge continuously, now feature of the present invention is further: 1. semicoke F18 is discharged in the R1 of pyrolysis chamber bottom.
The first semicoke recycle stream S1SR that the present invention exists returns to the lower region of the R1 of pyrolysis chamber conventionally.
The present invention can be separated into two groups by particle diameter by the semicoke of discharging in gas F14, and now feature of the present invention is further: 4., at the second separate part S2, logistics S1V carries out gas solid separation, obtains the second semicoke S2S and the second gas S2V leaves the second separate part S2; The second semicoke S2S enters stripping chamber K and adopts water vapor to complete stripping, obtains stripping gas KV and finished product semicoke KS.
Stripping of the present invention chamber K can be solid moving-bed or bubbling fluidized bed, in stripping chamber, the K semicoke residence time is generally 2 minutes～and 120 minutes.
Of the present invention containing organic powder F11, refer to the solid powder that produces hydrocarbon vapours under heating condition, be selected from fine coal, coal gangue, resinous shale, oil-sand, biomass and waste or used plastics.
The present invention, when the powder of processing is fine coal, at the R1 of PC-FB pyrolysis chamber, can arrange the entrance that adds of the second raw material of processing altogether with fine coal, and the second raw material of fluidized bed pyrolysis chamber R1 is the material that contains coal-tar pitch, carries out thermo-cracking or the fluid coking of coal-tar pitch; The second raw material is selected from following form: liquid coal-tar pitch sprays into fluidized-bed and contacts with powder, or the coal-tar pitch after gas atomization sprays into fluidized-bed and contact with powder, or the coal oil mixture mixture being comprised of coal-tar pitch and fine coal and/or semicoke; Pyrolysis chamber's the second raw material add the middle and lower part that entrance is generally positioned at fluidized bed pyrolysis chamber R1.
When the powder F11 of the present invention's processing is fine coal, the fluidizing agent of the R1 of PC-FB pyrolysis chamber, is coal gasification course synthetic gas or char Gasification process synthetic gas or semicoke carbonization process carbonized gas or pyrolysis coal gas or water vapor.
When the powder of the present invention's processing is fine coal, fluidized bed pyrolysis chamber R1, use the fluidized gas of hydrogen rich gas to form hydropyrolysis atmosphere, the working pressure of the R1 of PC-FB pyrolysis chamber is 1～8MPa, can in the raw material fine coal F11 of fluidized bed pyrolysis chamber R1, add hydropyrolysis metal catalyst, this catalyzer be selected from iron-based, molybdenum base, zinc-base, Ni-based, tinbase, cobalt-based metal catalyst a kind of, two or more, the addition of catalyzer is 0～15% of feed coal mass rate.
When the present invention processes fine coal, its operational condition scope is:
1. fine coal F11 is selected from: brown coal, long-flame coal, non-caking coal, weakly caking coal, bituminous coal; Pulverized coal particle size distribution range is generally 0.001～13 millimeter, is generally 0.001～8 millimeter, is preferably 0.001～6 millimeter; Fine coal F11 temperature is generally 100～450 ℃, is generally 200～350 ℃;
The R1 of PC-FB pyrolysis chamber operational condition: working pressure is generally normal pressure～8MPa, is generally normal pressure～2MPa, is preferably normal pressure～1MPa, service temperature is generally 400～1000 ℃, is generally 500～800 ℃, is 550～700 ℃ during middle low temperature pyrogenation;
2. the Action Target of the first separate part S1 is the macroparticle of isolating expection characteristic diameter, and characteristic diameter is generally 10～250 microns, is generally 50～200 microns, is preferably 100～150 microns.
3. part the first semicoke directly returns to the R1 of pyrolysis chamber, form the first semicoke recycle stream S1SR, the mass rate of semicoke recycle stream S1SR is defined as semicoke recycle ratio with the ratio of the mass rate of fine coal raw material F11, and this recycle ratio is generally 0.001～20, be generally 0.5～10, be preferably 3～8;
4. at stripping chamber K, the semicoke residence time is generally 2 minutes～and 120 minutes.
According to the present invention, as required, one of the steps such as desulfurization and deashing, drying and dehydrating, grain size distribution of fine coal F11, two or more; Various known feed way all can adopt; Typical fine coal raw material is: brown coal, long-flame coal, non-caking coal, weakly caking coal, bituminous coal etc., or the two or many persons' mixture in them.
The operational condition of the PC-FB of the present invention R1 of pyrolysis chamber, determines according to fine coal composition and pyrolysis target.
When the R1 of PC-FB pyrolysis chamber adopts low temperature, middle temperature or high temperature pyrolysis, the present invention can form low temperature, middle temperature or high temperature pyrolysis technique; By controlling pyrolysis time and pyrolysis temperature, when PC-FB pyrolysis chamber carries out at a slow speed, middling speed, fast and during flash pyrolysis, the present invention can form at a slow speed, middling speed, fast and flash pyrolytic process; In PC-FB of the present invention pyrolysis chamber, feed coal powder particles is pre-/and the hot body of heating can or be solid or be that thermal barrier is combined in gas-solid for gas; According to the composition of fluidizing agent, pyrolysis atmosphere of the present invention can form inert atmosphere pyrolysis, hydropyrolysis and catalytic hydropyrolysis, recommends hydropyrolysis and catalytic hydropyrolysis; According to pyrolysis operations pressure, the present invention can form normal pressure pyrolysis and pressurized pyrolysis.
The R1 of PC-FB pyrolysis chamber can be used any suitable fluidizing agent, recommends the high-temperature gas of hydrogen rich gas, preferably from high-temperature synthesis gas or the high temperature coke oven coal gas of gasification or char Gasification process; When using the gas stream agent of hydrogen rich gas, pyrolytic process forms hydropyrolysis atmosphere; For mild pyrolysis operational condition, can in feed coal, use hydropyrolysis metal catalyst, this catalyzer can be iron-based, molybdenum base, zinc-base, Ni-based, tinbase, cobalt-based metal catalyst a kind of, two or more, the quantity of adding catalyzer is 0～15% of feed coal flow.
The structure of gas solid separation part is unrestricted, according to the insulation classification of type of separator, substantially has three kinds, sees respectively shown in accompanying drawing 1, accompanying drawing 4, accompanying drawing 5.
It is that single-stage is separated, two-stage is separated, stage trapping that the technical process of gas solid separation part can be divided into three kinds.As shown in accompanying drawing 1, accompanying drawing 2, accompanying drawing 4, accompanying drawing 5, be single-stage separation, attachedly Figure 2 shows that two-stage is separated.
Stripping chamber K, the stripping chamber that can use any suitable form, can be moving-bed or bubbling fluidized bed, conventionally selects moving-bed; Stripping chamber interior can be divided into two or more powder flow passage formulas space; Gas distributor or distribution pipe or the compartment of delivering gas can be arranged in powder flow passage formula space, on sparger or distribution pipe or compartment's wall, ventilating pit is set, it outside sparger or distribution pipe or compartment, is solid flow space, sweeping gas can be introduced to Rapid replacement in powder passage and blow out intergranular semicoke parsing gas, to reduce the thermal condensation probability of oily vapour, stripping gas can be drawn to powder passage and shift out fast intergranular semicoke parsing gas.Sweeping gas can be returning to gas or being semicoke synthetic gas of water vapor, carbon dioxide gas, pyrolysis coal gas.At stripping chamber K, the semicoke residence time is generally 2 minutes～and 120 minutes, be generally 5 minutes～60 minutes, be preferably 10 minutes～30 minutes.
Service temperature and the working pressure of the first separate part S1, circulation revert pipe XHG1, stripping chamber K, determine according to service temperature and the working pressure of the R1 of PC-FB pyrolysis chamber discharge gas F14 conventionally.
Gaseous heat-carrier can be injected to the R1 of PC-FB pyrolysis chamber and discharge gas F14 and improve gas temperature, to prevent that gas its tar heavy constituent in separator from condensing.
The gaseous heat-carrier of hydrogen rich gas can be injected to the R1 of PC-FB pyrolysis chamber as secondary stream agent gas heating coal dust and multistage hydrogenation, the free radical that saturated and stable pyrolysis produces, suppress its polycondensation and generate semicoke, its opening for feed is positioned at the above position of fine coal opening for feed.
Claims (15)
1. a powder method for pyrolysis that uses Circulating Fluidized Bed Process, is characterized in that:
1. in fluidized bed pyrolysis chamber R1 part, fluidized gas F13 enters the R1 of pyrolysis chamber from bottom, containing organic powder F11, enter the R1 of pyrolysis chamber and form fluidized under the effect of up gas, in the R1 of fluidized bed pyrolysis chamber, powder F11 is heated and carries out fluidized bed pyrolysis reaction and produces the fluid bed heat that comprises non-condensable gas and tar steam and vent one's spleen and semicoke by thermal barrier, and fluid bed heat is vented one's spleen and mixed with fluidized-bed fluidized gas and carry Semi Coke Particles and from R1 top, pyrolysis chamber, discharge and become discharge gas F14;
2. at the first separate part S1, logistics F14 carries out the first semicoke S1S and the first gas S1V that gas solid separation obtains and leaves respectively the first separate part S1;
3. by circulation revert pipe XHG1, part or all of the first semicoke S1S returns to the R1 of pyrolysis chamber and forms the first semicoke recycle stream S1SR.
2. method according to claim 1, is characterized in that:
1. semicoke F18 is discharged in the R1 of pyrolysis chamber bottom.
3. method according to claim 1, is characterized in that:
3. part the first semicoke recycle stream S1SR is returned to the lower region of the R1 of pyrolysis chamber.
4. method according to claim 1, is characterized in that:
4. at the second separate part S2, logistics S1V carries out that gas solid separation obtains the second semicoke S2S and the second gas S2V leaves the second separate part S2; The second semicoke S2S enters stripping chamber K and adopts water vapor to complete stripping, obtains stripping gas KV and finished product semicoke KS.
5. method according to claim 4, is characterized in that:
4. stripping chamber K adopts solid moving-bed.
6. method according to claim 4, is characterized in that:
4. stripping chamber K adopts bubbling fluidized bed.
7. method according to claim 4, is characterized in that:
4. at stripping chamber K, the semicoke residence time is 2 minutes～120 minutes.
8. method according to claim 1, the powder of processing is while being fine coal, at the R1 of PC-FB pyrolysis chamber, the entrance that adds of the second raw material of processing altogether with fine coal is set, the second raw material of fluidized bed pyrolysis chamber R1 is the material that contains coal-tar pitch, carries out thermo-cracking or the fluid coking of coal-tar pitch; The second raw material is selected from following form: liquid coal-tar pitch sprays into fluidized-bed and contacts with powder, or the coal-tar pitch after gas atomization sprays into fluidized-bed and contact with powder, or the coal oil mixture mixture being comprised of coal-tar pitch and fine coal and/or semicoke; Pyrolysis chamber's the second raw material add the middle and lower part that entrance is positioned at fluidized bed pyrolysis chamber R1.
9. method according to claim 1, when the powder F11 of processing is fine coal, the fluidizing agent of the R1 of PC-FB pyrolysis chamber, is coal gasification course synthetic gas or char Gasification process synthetic gas or pyrolysis coal gas or water vapor.
10. method according to claim 1, when the powder of processing is fine coal, is characterized in that:
1. fluidized bed pyrolysis chamber R1, is used the fluidized gas of hydrogen rich gas to form hydropyrolysis atmosphere, and the working pressure of the R1 of PC-FB pyrolysis chamber is 1～8MPa.
11. methods according to claim 10, is characterized in that:
1. in the raw material fine coal F11 of fluidized bed pyrolysis chamber R1, add hydropyrolysis metal catalyst, this catalyzer be selected from iron-based, molybdenum base, zinc-base, Ni-based, tinbase, cobalt-based metal catalyst a kind of, two or more, the interpolation weight of catalyzer is 0～15% of feed coal weight.
12. methods according to claim 1, when the powder of processing is fine coal, is characterized in that:
1. fine coal F11 is selected from: brown coal, long-flame coal, non-caking coal, weakly caking coal, bituminous coal; Pulverized coal particle size distribution range is 0.001～13 millimeter; Fine coal F11 temperature is 100～450 ℃;
The R1 of PC-FB pyrolysis chamber operational condition: working pressure is that normal pressure～8MPa, service temperature are 400～1000 ℃;
2. the Action Target of the first separate part S1 is the macroparticle of isolating expection characteristic diameter, and characteristic diameter is 10～250 microns;
3. part the first semicoke directly returns to the R1 of pyrolysis chamber and forms the first semicoke recycle stream S1SR, and the mass rate of semicoke recycle stream S1SR is defined as semicoke recycle ratio N1 with the ratio of the mass rate of fine coal raw material F11, and this recycle ratio N1 is 0.001～20;
4. at stripping chamber K, the semicoke residence time is 2 minutes～120 minutes.
13. methods according to claim 12, when the powder of processing is fine coal, is characterized in that:
1. fine coal F11 particle size distribution is 0.001～8 millimeter; Fine coal F11 temperature is 200～350 ℃;
The R1 of PC-FB pyrolysis chamber operational condition: working pressure is that normal pressure～2MPa, service temperature are 500～800 ℃;
2. the Action Target of the first gas solid separation part S1 is the macroparticle of isolating expection characteristic diameter, and characteristic diameter is 50～200 microns.
3. recycle ratio N1 is 0.5～10.
14. methods according to claim 13, when the powder of processing is fine coal, is characterized in that:
1. fine coal F11 particle size distribution is 0.001～6 millimeter;
The R1 of PC-FB pyrolysis chamber operational condition: working pressure is that normal pressure～1MPa, service temperature are 550～700 ℃;
2. the Action Target of the first gas solid separation part S1 is the macroparticle of isolating expection characteristic diameter, and characteristic diameter is 100～150 microns;
3. recycle ratio N1 is 3～8.
15. methods according to claim 1, described containing organic powder F11, refer to the solid powder that produces hydrocarbon vapours under heating condition, be selected from coal, coal gangue, resinous shale, oil-sand, biomass and the waste or used plastics of powdery.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105779015A (en) * | 2016-01-29 | 2016-07-20 | 东南大学 | Device and method for preparing hydrogen-enriched syngas with lignite and biomass as fuels |
| CN105889906A (en) * | 2016-06-13 | 2016-08-24 | 合肥德博生物能源科技有限公司 | Thermal-pulverization high-efficiency combustion device and method for high-volatile-component carbon-containing fuel |
| WO2017132900A1 (en) * | 2016-02-03 | 2017-08-10 | 太原理工大学 | Composite catalyst for coal pyrolysis and using method therefor |
| CN108018055A (en) * | 2016-10-30 | 2018-05-11 | 何巨堂 | It is unconventional to contain solid oil plant fluid coking process and fluidization pyrolytic process combined method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1608972A (en) * | 2004-09-20 | 2005-04-27 | 东南大学 | Biomass-gasifying hydrogen generating serial fluid bed apparatus and method |
| CN1727750A (en) * | 2004-07-26 | 2006-02-01 | 中国科学院工程热物理研究所 | The CFBB of gas and steam co-production and band pyrolysis vaporizer |
-
2013
- 2013-04-16 CN CN201310129704.4A patent/CN104109543A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1727750A (en) * | 2004-07-26 | 2006-02-01 | 中国科学院工程热物理研究所 | The CFBB of gas and steam co-production and band pyrolysis vaporizer |
| CN1608972A (en) * | 2004-09-20 | 2005-04-27 | 东南大学 | Biomass-gasifying hydrogen generating serial fluid bed apparatus and method |
Non-Patent Citations (1)
| Title |
|---|
| DAVID A BELL: "《Coal Gasification and its Application》", 31 December 2011 * |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105779015A (en) * | 2016-01-29 | 2016-07-20 | 东南大学 | Device and method for preparing hydrogen-enriched syngas with lignite and biomass as fuels |
| CN105779015B (en) * | 2016-01-29 | 2018-05-15 | 东南大学 | The device and method of Hydrogen synthesis gas is rich in using lignite and biomass as preparation of fuel |
| WO2017132900A1 (en) * | 2016-02-03 | 2017-08-10 | 太原理工大学 | Composite catalyst for coal pyrolysis and using method therefor |
| US20190009256A1 (en) * | 2016-02-03 | 2019-01-10 | Taiyuan University Of Technology | Composite catalyst for coal depolymerization and using method therefor |
| US11110440B2 (en) | 2016-02-03 | 2021-09-07 | Taiyuan University Of Technology | Composite catalyst for coal depolymerization and using method therefor |
| CN105889906A (en) * | 2016-06-13 | 2016-08-24 | 合肥德博生物能源科技有限公司 | Thermal-pulverization high-efficiency combustion device and method for high-volatile-component carbon-containing fuel |
| CN108018055A (en) * | 2016-10-30 | 2018-05-11 | 何巨堂 | It is unconventional to contain solid oil plant fluid coking process and fluidization pyrolytic process combined method |
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