CN103436278A - Combined process for pressurized gasification and pressurized pyrolysis of broken carbon material - Google Patents
Combined process for pressurized gasification and pressurized pyrolysis of broken carbon material Download PDFInfo
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- CN103436278A CN103436278A CN2013103503402A CN201310350340A CN103436278A CN 103436278 A CN103436278 A CN 103436278A CN 2013103503402 A CN2013103503402 A CN 2013103503402A CN 201310350340 A CN201310350340 A CN 201310350340A CN 103436278 A CN103436278 A CN 103436278A
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Abstract
The invention relates to a combined process for the pressurized gasification and pressurized pyrolysis of a broken carbon material, in particular to a combined process for broken semi-coke movable bed pressurized gasification and pressurized pyrolysis of a carbon material. A semi-coke-prepared coal gas pressurization gasification furnace and a carbon material pressurization pyrolysis furnace are connected in series for use, partial or all gasification furnace coal gas flows into a pyrolysis furnace system and is used as pyrolysis heat carrying gas, such as pyrolysis heat source gas and pyrolysis coke quenching gas; the hydropyrolysis and inner hole processing of the pyrolysis furnace carbon material can be completed under the condition of pressurization and under a strong reduction atmosphere within appropriate pyrolysis time, so that the pyrolysis oil yield is improved, the semi-coke specific surface area is improved, partial or all pyrolysis furnace semi-coke enters the gasification furnace for producing gas, gasification furnace coal gas and/or pyrolysis furnace coal gas are/is used for producing compound products, as a result, the integral and efficient coal gas production oil process is realized, and both the pyrolysis furnace and the gasification furnace can work under the optimal operation conditions.
Description
Technical field
The present invention relates to a kind of broken carbon material pressurized gasification and carbon material pressurized pyrolysis combination process; Say especially, the present invention relates to a kind of broken semicoke moving-bed pressurized gasification and carbon material pressurized pyrolysis combination process.
Background technology
The utilization of coal, mainly be divided into heat energy utilization and chemical utilization.Coal Chemical Industry, mainly be divided into coal gas and turn to basic Coal Chemical Industry, take the coal partial gasification as basic Coal Chemical Industry and DCL/Direct coal liquefaction Coal Chemical Industry, the invention belongs to and take the coal partial gasification as basic Coal Chemical Industry.
Carbon material pyrolytic process of the present invention, comprise dry distillation of coal process, semicoke hot-work reaming process.
Broken carbon material pressurized gasification process of the present invention, the broken carbon material of use, from coal or semicoke or Jiao, is preferably semicoke.
Carbon material pressurized pyrolysis process of the present invention, the carbon material of use, from coal or semicoke or Jiao, is generally and is preferably coal or semicoke.
Along with the semicoke industrial expansion, China has formed the semicoke industry, but coal semicoke technique processed be take the upright pyrolysis oven technique of internal heat type normal pressure as main at present, this technique floor space is large, energy consumption is high, the coal gas nitrogen gas concn is high, the tar yield is low, blue charcoal needs to improve as sorbent material and vaporized carbon material activity, its major product semicoke is limited and cheap as the consumption of reductive agent, can't support the benign development of semicoke industry, geographical position, semicoke source causes the concentrated Xinjiang that is distributed in of semicoke factory, Inner Mongol, northerns Shensi etc. are away from the water-deficient area of China consumer center, be badly in need of the feature of environmental protection that has both that transforms semicoke, water saving ability, energy saving, the conversion route of the production high-value product of economy, be badly in need of in other words the feature of environmental protection that has both that transforms coal, water saving ability, energy saving, the conversion route of the production high-value product of economy, purpose of the present invention just is to propose one and meets the coal of above-mentioned requirements or the conversion route of semicoke.
The unavoidable shortcoming that independently coal of the upright pyrolysis oven of internal heat type normal pressure semicoke technique processed exists is:
1. because working pressure low causes the particle size diameter of pyrolysis oven feed coal large, pyrolysis time is long, the pyrolysis oven floor space is large, pyrolysis oven gas phase H
2minute force down thus the tar yield is low, pyrolysis oven gas phase CO divide force down thereby the phenol yield low;
2. pyrolysis coal gas utilizes process to pressurize and consumes a large amount of compression works;
, 3. because thereby pyrolysis oven need to consume a large amount of pyrolysis coal gas to be made thermal source fuel gas and prepare hot flue gas and serve as pyrolysis thermal source gas and reduced the pyrolysis gas productive rate, exist pyrolysis coal gas to return the stove recycle system and cause system complex, investment large;
4. pyrolysis coal gas is made thermal source fuel gas combustion processes and is used air to cause the nitrogenous gas of pyrolysis coal gas to be difficult to utilize more, uses air separation facility and uses the carbonic acid gas circulation technology to realize the denitrogenation gas of pyrolysis coal gas, must cause construction investment significantly to raise.
The unavoidable shortcoming that independently the strange gas maked coal technique in broken coal pressurization moving-bed Shandong exists is:
1. in order to improve gasification intensity, improve working pressure, reduced the rate of decomposition of water, increased containing tar sewage output;
2. being limited by carbon material bed height can not be too high, and its pyrolysis section residence time is shorter, and the tar yield is lower;
3. the speed that gasification consumes the charcoal material has determined bed of material lowering speed, and pyrolysis section bed of material lowering speed determines thereupon, and pyrolysis section bed of material lowering speed can not independently be regulated, and coal charge can not independently be regulated in the residence time of pyrolysis section;
4. the temperature of pyrolysis section thermal source gas, by the Exhaust Gas decision of the methane layer from bottom, can not independently regulate;
5. be difficult to take out pyrolysis section half Jiaozhuo product and use, because can affect the distributing homogeneity of the bed of material in vapourizing furnace greatly, and, because the pyrolysis section bottom is methane layer, responding layer, internals are set extremely difficult;
6. the variation of ature of coal, cause the operation of vapourizing furnace to regulate more responsive.
In coal semicoke industry processed or gasification industry, usually there is the decontamination process containing tar sewage, this process is used the carbon material sorbent material of adsorbed oil usually, if use semicoke, because of the less large usage quantity of semicoke specific surface area, in order to reduce carbon material sorbent material consumption, need to use the larger high reactivity semicoke of specific surface area.Because the pressurization lurgi gasifier is worked under higher pressure, the H of high partial pressures
2o, CO, CO
2, H
2component possesses the ability of deep reaction to semicoke, extend the pyrolysis section residence time under other operational condition permanence condition, can prepare the semicoke that porosity is higher, can improve semicoke to oily adsorptive power, can improve the reducing activity of semicoke.
The current coal of China semicoke process processed and semicoke Gas-making carry out two independent systems respectively, the blue charcoal by-product oil of the coal system process of take is example, in order to pursue high tar yield and low construction investment, the pyrolytic process of the blue charcoal liquefaction of coal system should be at suitable low temperature, the longer residence time completes pyrolysis; Pressurized operation can improve pyrolysis efficiency, but reduces tar yield, increase construction investment.And blue charcoal pure oxygen gasification process pursues that high steam resolution ratio is appropriate to the occasion under low pressure completes gasification, pursue that high gasification intensity is appropriate to the occasion to be completed gasification and reduced steam resolution ratio simultaneously, increased construction investment under pressurized conditions.
In order to solve above-mentioned contradiction, the present invention proposes a kind of broken semicoke moving-bed pressurized gasification and carbon material pressurized pyrolysis combination process, hydropyrolysis stove and the semicoke pressurized-gasification furnace series connection of pressurizeing is used, partly or entirely gasifier gas reduces phlegm and internal heat and separates furnace system and make the pyrolysis heat-carrying gas such as making pyrolysis thermal source gas, pyrolysis quenching gas, partly or entirely the pyrolysis oven semicoke enters vapourizing furnace gas making, after the sewage purification that the sepn process of pyrolysis oven coal gas produces, generating steam enters vapourizing furnace gas making, semicoke Cheng Fenhou forms the absorption of absorbing and filtering bed and realizes sewage preliminary cleaning containing the organism in tar sewage, gasifier gas and or pyrolysis oven coal gas manufacture synthetics, pyrolysis oven and vapourizing furnace are all worked under its optimized operational condition, thereby realized integrated energy-conservation, water saving, environmental protection, efficiently, the coal generating gas produce oil technique of low investment.
With existing independence two cover systems, compare, advantage is:
1. pyrolysis oven operates under pressurized conditions, and pyrolysis time and pyrolysis temperature all can realize optimizing, and the coal maceral hydrogenation reaction causes the tar yield to significantly improve, H
2dividing potential drop is high, CO significantly
2significantly high, the yield of tar and phenol significantly improves, and colloid, bituminous matter are produced and reacted suppressed;
2. pyrolysis oven operation under pressurization, have strong reaming ability to the carbon material, high reactivity semicoke that can the output high-specific surface area;
When pyrolysis oven material carbon material is the granule half-angle, high reactivity semicoke that can output extra-high-speed specific surface area;
3. gasifier gas enters pyrolysis oven as pyrolysis thermal source gas, quenching gas, has significantly reduced the recycle gas quantity of returning to pyrolysis oven of half coke installation pyrolyzing coal gas, decrease investment and the energy consumption of half coke installation pyrolyzing coal gas circulation route;
4. pyrolysis oven adopts Dry Quenching Technology, the char Gasification stove does not need dryer section, the top of gasification furnace temperature can be higher, the high-temperature gasification producer gas enters the pyrolysis oven system and uses as pyrolysis thermal source gas, significantly reduced the fuel gas quantity that the pyrolysis oven combustion chamber consumes, decrease investment and the energy consumption of half coke installation firing system, improved the pyrolysis gas yield;
When 5. the vapourizing furnace oxygenant adopts pure oxygen, gasifier gas, for low nitrogen gas, enters the pyrolysis oven system and makes the pyrolysis heat-carrying gas such as making pyrolysis thermal source gas, pyrolysis quenching gas, can avoid pyrolysis coal gas containing a large amount of nitrogen problems, need not increase empty minute scale simultaneously;
6. gasifier gas enters pyrolysis oven, the H in gasification gas
2o, CO
2contact with hot charcoal further and decompose, improved rate of decomposition, increased production synthetic gas quantity;
7. low nitrogen gasifier gas enters the pyrolysis oven system and makes the pyrolysis heat-carrying gas such as making pyrolysis thermal source gas, pyrolysis quenching gas, can reduce pyrolytic process prussiate output, can reduce cyanogen hydrogen radical amount in sewage;
8. utilize self-produced high reactivity semicoke as containing tar sewage sorbent material, removing oil purification, the oil suction powder coke adsorbent is made fuel, or the oil suction coke breeze becomes after piece to enter pyrolysis oven or the vapourizing furnace secondary processing reclaims tar or partial gasification tar, do not need ad hoc adsorbent reactivation or conversion system, systematic collaboration is respond well; Sewage vaporescence recovery plant Low Temperature Thermal after purification is vaporizated into steam, enters the vapourizing furnace major part and is converted into the coal gas active principle, has realized that reusing sewage and Low Temperature Thermal reclaim;
9. adopting coal is gasified raw material, and half Jiaozhuo its stable in properties of vapourizing furnace raw material is better, can improve the operational stability of vapourizing furnace;
10. the operation flexible adjustment of pyrolysis oven, vapourizing furnace is large, and restriction each other is little, is beneficial to and realizes the optimization of operational condition separately, such as the top temperature of carbon material in pyrolysis oven, lower than at least 100 ℃ of the temperature of the outlet coal gas of vapourizing furnace.
Contain a large amount of tar in coal gas due to the coal charge gasification, adopt the tar in gasification gas when of the present invention that pyrolysis to a certain degree can occur in pyrolysis oven, be condensed into the reaction of resin and asphalt, reduce tar total recovery and the quality of coal charge, this is not wish to occur.Therefore, the present invention recommends gasification to adopt broken semicoke moving-bed pressurized gasification.
A kind of prior art similar to the present invention is two-stage gasifier as Italian IGC company two-stage gasifier, Polish two-stage gasifier, is normal pressure or low pressure process, and its advantage is to have obtained pyrolysis section coal gas and two gas products of gasification section coal gas; One of its shortcoming is, the pyrolysis section spatial volume is too little, can't expand the pyrolysis section spatial volume that the blue charcoal stove of pure pyrolysis oven possesses to, and the residence time of pyrolysis of coal far is shorter than the blue charcoal stove of pure pyrolysis oven; Two of its shortcoming is that the temperature section of the being vaporized temperature restriction of two-stage gasifier pyrolysis section, can't realize optimized lower pyrolysis terminal temperature.The pyrolysis section of two-stage gasifier, temperature and the residence time can't optimizations, therefore the tar yield of two-stage gasifier is far below the blue charcoal stove of pure pyrolysis oven.Therefore, when the high non-caking coal of processing oil length or weakly caking coal are pursued high tar yield, two stage gasification coke oven tar yield is too low becomes fatal shortcoming.But the gasification gas of two-stage gasifier, as the pyrolysis section heat air, has been simplified flow process, has reduced investment, is its advantage.
Another kind of prior art similar to the present invention is broken coal moving-bed pressurization Lurgi gasifier, with the blue charcoal stove of pure pyrolysis oven, compare, same because the temperature of pyrolysis section and the residence time can't optimizations, therefore the tar yield of the broken coal moving-bed Lurgi gasifier of low pressure or atmospheric operation is lower than the blue charcoal stove of pure pyrolysis oven.But the gasification gas of broken coal moving-bed Lurgi gasifier, as the pyrolysis section heat air, has been simplified flow process, has reduced investment, is its advantage.When broken coal moving-bed Lurgi gasifier adopts pressurized operation, dividing potential drop due to the hydrogen of having strengthened reducing atmosphere, carbon monoxide, methane etc., the tar yield has been brought up to the degree that can compare with the blue charcoal stove of pure pyrolysis oven, but invest too high, the water decomposition rate is too low, the water consumption is too high, needs the huge Sewage treatment systems of configuration.
The present invention possesses the prior art advantage that is beyond one's reach, and therefore, the present invention possesses novelty.
Combination process of the present invention has no report.
The first purpose of the present invention is to propose a kind of broken carbon material pressurized gasification and carbon material pressurized pyrolysis combination process.
The second purpose of the present invention is to propose a kind of broken semicoke moving-bed pressurized gasification and carbon material pressurized pyrolysis combination process, can realize the operational condition optimization of pyrolysis oven and vapourizing furnace, and flow process is simple simultaneously, and less investment, energy consumption are low.
Summary of the invention
A kind of broken carbon material pressurized gasification and carbon material pressurized pyrolysis combination process is characterized in that comprising following steps: use that carbon material F1 pressurized pyrolysis stove R1 is connected with broken carbon material F2 pressurization moving-bed gasification stove R2, and partly or entirely gasifier gas PV2 removes pyrolysis oven R1; Pyrolysis oven R1, working pressure is greater than normal pressure, and carbon material F1 enters pyrolysis oven R1 and has contacted pyrolysis with pyrolysis thermal source gas, and carbon material pyrolysis solid product is semicoke BJ, and carbon material pyrolysis gas product enters in coal gas PV1, and semicoke BJ discharges pyrolysis oven R1; The coal gas PV1 that pyrolysis oven is discharged is separated into coal gas P1, contains tar sewage P2 and coal tar P3 through the refrigerated separation process; Vapourizing furnace R2, working pressure is greater than normal pressure.
Feature of the present invention further is: partly or entirely gasifier gas PV2 goes pyrolysis oven R1 to do the use of pyrolysis thermal source gas, and pyrolysis thermal source gas provides heat for coal charge F1 pyrolytic process; Pyrolysis oven R1, working pressure is greater than 1.0MPa, and pyrolysis thermal source gas adds from pyrolysis oven R1 bottom charging opening, and coal gas PV1 discharges from pyrolysis oven R1 top; Vapourizing furnace R2, be broken semicoke pressurization moving-bed gasification stove, and working pressure is greater than 1.0MPa, and slag is discharged in bottom, and coal gas PV2 is discharged on top.
Feature of the present invention further is: pyrolysis oven R1, and working pressure is greater than 2.5MPa; Carbon material vapourizing furnace R2, working pressure is greater than 2.5MPa, the H of gasifier gas PV2
2dividing potential drop is greater than 0.40MPa, and the CO dividing potential drop of gasifier gas PV2 is greater than 0.25MPa.
Feature of the present invention further is: pyrolysis oven R1, and working pressure is greater than 4.0MPa; Carbon material vapourizing furnace R2, working pressure is greater than 4.0MPa, the H of gasifier gas PV2
2dividing potential drop is greater than 0.60MPa, and the CO dividing potential drop of gasifier gas PV2 is greater than 0.40MPa.
Feature of the present invention further is: carbon material F1 is coal charge, and partly or entirely pyrolysis oven R1 semicoke BJ enters vapourizing furnace R2 gas making.
Feature of the present invention further is: the steam occurred after the sewage purification that pyrolysis oven R1 coal gas PV1 sepn process produces enters vapourizing furnace R2 gas making.
Feature of the present invention further is: after at least a portion semicoke BJ becomes powder, the absorption of composition filter bed realizes sewage P2 preliminary cleaning containing the organism in tar sewage P2.
Feature of the present invention further is: vapourizing furnace R2 coal gas PV2 and or pyrolysis oven R1 coal gas PV1 manufacture synthetics.
Feature of the present invention further is: vapourizing furnace R2 coal gas PV2 enters pyrolysis oven R1 quenching section bottom and contacts with hot semicoke as quenching gas, and quenching gas and semicoke counter current contact absorb the cooling semicoke of heat.
Feature of the present invention further is: the vapourizing furnace R1 coal gas PV21 of normal temperature state enters pyrolysis oven R1 quenching section bottom and contacts with hot semicoke as quenching gas.
Feature of the present invention further is: vapourizing furnace R2 coal gas PV22 enters pyrolysis oven R2 pyrolysis section bottom and uses as pyrolysis thermal source gas.
Feature of the present invention further is: high-temperature gasification stove R2 coal gas PV22 enters pyrolysis oven R1 pyrolysis section bottom as pyrolysis thermal source gas contact coal charge.
Feature of the present invention further is: the carbon material vapourizing furnace R2 part that gasifies, use the gasified boiler system of two kinds of operational conditions, and produce respectively normal temperature gasification gas PV21 and coal gas of high temperature PV22; Coal gas of high temperature PV22 enters pyrolysis oven R1 pyrolysis section bottom and uses as whole pyrolysis thermal source gas, and the gas of normal temperature gasification simultaneously PV21 enters pyrolysis oven R1 quenching section bottom and contacts with hot semicoke as quenching gas.
Feature of the present invention further is: the carbon material vapourizing furnace R2 part that gasifies, use the gasified boiler system of two kinds of operational conditions, and produce respectively normal temperature gasification gas PV21 and coal gas of high temperature PV22; First via normal temperature gasification gas PV211 enters pyrolysis oven R2 quenching section bottom and contacts with hot semicoke as quenching gas, it is high-temperature flue gas that the second road normal temperature gasification gas PV212 enters combustion chambers burn, high-temperature flue gas with enter pyrolysis oven R1 pyrolysis section bottom after coal gas of high temperature PV22 Mixed adjustment temperature and contact with the charing feed coal as part or all of pyrolysis thermal source gas use.
Feature of the present invention further is: pyrolysis oven R1 service temperature, top is that 60～800 ℃, charing section are that 550～800 ℃, bottom coke outlet are 50～800 ℃.
Feature of the present invention further is: when carbon material F1 is coal charge, and pyrolysis oven R1 service temperature, top is that 60～150 ℃, bottom coke outlet are 50～90 ℃.
Feature of the present invention further is: vapourizing furnace R2 burning zone service temperature, lower than 50～120 ℃ of ash fusion points; Air outlet, vapourizing furnace R2 top service temperature is 180～800 ℃; Vapourizing furnace R2 oxygenant, be selected from air, oxygen-rich air and purity oxygen, is preferably as purity oxygen; The non-oxygen gasified gas of vapourizing furnace R2, be selected from water vapor and or carbon dioxide gas.
Feature of the present invention further is: described synthetics is selected from methane, methyl alcohol, synthetic oil, is preferably synthetic oil.
Feature of the present invention further is: broken carbon material pressurized gasification process water steam, the steam that the water produced for described carbon material pressurized pyrolysis process and broken carbon material pressurized gasification process or synthetics building-up process occurs.
Feature of the present invention further is: pyrolysis oven R1 row semicoke section is used normal temperature carbonic acid gas rare gas element for isolation gas, has a rest during coke discharging and blows or blow continuously in production phase, and isolation gas enters in pyrolysis oven coal gas.
Feature of the present invention further is: in order to reduce the entrained foreign gas of carbon material F1 that enters pyrolysis oven, use the hopper of coalingging that possesses ventilatory, displacement gas is carbon dioxide.
Feature of the present invention further is: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal or semicoke or Jiao; The broken carbon material of described broken carbon material vapourizing furnace R2 processing is from coal or semicoke or Jiao.
Feature of the present invention further is: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal, and the broken carbon material of described broken carbon material vapourizing furnace R2 processing, from semicoke, forms coal charge pressurization hydropyrolysis and broken semicoke pressurized gasification process combination process.
Feature of the present invention further is: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from semicoke; The broken carbon material of described broken carbon material vapourizing furnace R2 processing, from semicoke, forms semicoke pressurization activation and broken semicoke pressurized gasification process combination process, the semicoke of pyrolysis oven R1 output high-specific surface area.
Feature of the present invention further is: described carbon material pyrolysis oven R1, and carbon material move mode is the downflow system moving-bed, and gas and the solid way of contact are adverse current, and the material carbon material adds from pyrolysis oven R1 top charging opening, and the product semicoke flows out from pyrolysis oven R1 bottom; Described carbon material pyrolysis oven R1, the carbon material semicoke granularity of processing is generally 3.0～60.0mm, is generally 3.0～10.0mm, and the pyrolysis section service temperature is 600～1000 ℃.
Feature of the present invention further is: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal, carbon material move mode is the downflow system moving-bed, gas and the solid way of contact are adverse current, and the material carbon material adds from pyrolysis oven R1 top charging opening, and the product semicoke flows out from pyrolysis oven R1 bottom; Described carbon material pyrolysis oven R1, the granularity of carbon material F1 is generally 3.0～60.0mm: pyrolysis oven R1 service temperature, top is that 60～200 ℃, charing section bottom are 550～800 ℃.
Feature of the present invention further is: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal, carbon material move mode is the downflow system expanded bed, gas and the solid way of contact are adverse current, and the material carbon material adds from pyrolysis oven R1 top charging opening, and the product semicoke flows out from pyrolysis oven R1 bottom; Described carbon material pyrolysis oven R1, the granularity of carbon material F1 is generally 0.001～8.0mm, is generally 0.1～5.0mm, and the pyrolysis section service temperature is 500～800 ℃.
Feature of the present invention further is: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal, carbon material move mode is the upflowing fluidized-bed, gas and the solid way of contact are and flow, material carbon material and pyrolysis thermal source gas add from pyrolysis oven R1 bottom, and pyrolysis product enters gas-solid separator from the outflow of pyrolysis oven R1 top and is separated into semicoke and pyrolysis gas; Described carbon material pyrolysis oven R1, the granularity of carbon material F1 is generally 0.001～8.0mm, is generally 0.001～5.0mm, and the pyrolysis section service temperature is 500～800 ℃.
Feature of the present invention further is: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal, and carbon material move mode is the upflowing ebullated bed, and the material carbon material adds from pyrolysis oven R1 bottom charging opening, and the product semicoke is collected a mouthful discharge pyrolysis oven R1 from semicoke; Described carbon material pyrolysis oven R1, the granularity of carbon material F1 is generally 0.001～8.0mm, is generally 0.001～5.0mm, and the pyrolysis section service temperature is 500～800 ℃.
Feature of the present invention further is: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal; The top temperature of carbon material in pyrolysis oven R1, lower than the temperature of the outlet coal gas of vapourizing furnace R2 such as at least 100 ℃ of the temperature of the outlet coal gas lower than vapourizing furnace R2.
Gasification of the present invention, therefore working pressure is determined not restriction according to vapor pressure, working pressure generally lower than 2.0MPa, be usually less than 1.0MPa, be preferably lower than 0.5MPa to utilize as far as possible factory's low-pressure steam or Low Temperature Thermal, improve the rate of decomposition of water.
Synthetics of the present invention, can be any one synthetics, usually is selected from methane, methyl alcohol, synthetic oil, synthetic oil preferably, because it only contains hydrogen charcoal atom, hydrogen/the charcoal atomic ratio is little, unit price is high, therefore it is long low apart from freight charges, be convenient to realize scale processing and scale sale.
The steam that sewage treatment process of the present invention produces, comprise the steam of the water generation that the processes such as described coal semicoke process processed, char Gasification process, building-up process produce.
A kind of the present invention processes the moving bed pyrolysis stove R1 of coal charge, and structure comprises pyrolysis section and quenching section, and pyrolysis section is positioned at the top of quenching section, and the semicoke of discharge is the low temperature semicoke, and its structure is: body of heater adopts water wall structure or heat-resistant lining structure; Coal charge enters furnace apparatus and adopts the material lock, and the similar lurgi gasifier coal of material lock construction is locked, and is positioned at top or the top of pyrolysis oven body of heater, with the top of pyrolysis oven body of heater or the Link Port on top, is connected; Carbon material distributor and agitator, coal charge distributor and the agitator of similar lurgi gasifier, be positioned at the top of pyrolysis oven furnace inner space; Pyrolysis thermal source gas, entering the pyrolytic layer bottom by thermal source gas inlet pipe contacts with the carbon material, preferably by thermal source gas inlet pipe, entering thermal source gas sparger then enters pyrolytic layer bottom and contacts with the carbon material, thermal source gas inlet pipe is arranged in bottom or the bottom of pyrolysis oven body of heater usually, also can be arranged in the middle part of pyrolysis oven body of heater; Thermal source gas sparger is arranged in the top of the quenching section of pyrolysis oven furnace inner space usually; The effect of thermal source gas sparger is that thermal source gas is evenly distributed in co-altitude carbon material bed; Quenching gas, enter quenching layer bottom by quenching gas inlet pipe and contact with the carbon material, preferably by quenching gas inlet pipe, enters quenching gas sparger and then enter bottom the quenching layer and contact with the carbon material, and quenching gas inlet pipe is arranged in bottom or the bottom of pyrolysis oven body of heater usually; Quenching gas sparger is arranged in the bottom of the quenching section of pyrolysis oven furnace inner space usually; The effect of quenching gas sparger is that quenching gas is evenly distributed in co-altitude carbon material bed; The semicoke discharge port is positioned at bottom or the bottom of pyrolysis oven body of heater, and the semicoke discharge port of separate unit pyrolysis oven can be 1 or 2 or a plurality of, can control co-altitude carbon material, evenly drops to Action Target; The semicoke discharging device adopts burnt lock, and the similar lurgi gasifier coal of burnt lock construction is locked, and is positioned at bottom or the bottom of pyrolysis oven body of heater, with the bottom of pyrolysis oven body of heater or the Link Port of bottom, is connected.
Embodiment
Pressure of the present invention is absolute pressure.
Below describe the present invention in detail.
A kind of broken carbon material pressurized gasification and carbon material pressurized pyrolysis combination process is characterized in that comprising following steps: use that carbon material F1 pressurized pyrolysis stove R1 is connected with broken carbon material F2 pressurization moving-bed gasification stove R2, and partly or entirely gasifier gas PV2 removes pyrolysis oven R1; Pyrolysis oven R1, working pressure is greater than normal pressure, and carbon material F1 enters pyrolysis oven R1 and has contacted pyrolysis with pyrolysis thermal source gas, and carbon material pyrolysis solid product is semicoke BJ, and carbon material pyrolysis gas product enters in coal gas PV1, and semicoke BJ discharges pyrolysis oven R1; The coal gas PV1 that pyrolysis oven is discharged is separated into coal gas P1, contains tar sewage P2 and coal tar P3 through the refrigerated separation process; Vapourizing furnace R2, working pressure is greater than normal pressure.
Feature of the present invention further is: partly or entirely gasifier gas PV2 goes pyrolysis oven R1 to do the use of pyrolysis thermal source gas, and pyrolysis thermal source gas provides heat for coal charge F1 pyrolytic process; Pyrolysis oven R1, working pressure is greater than 1.0MPa, and pyrolysis thermal source gas adds from pyrolysis oven R1 bottom charging opening, and coal gas PV1 discharges from pyrolysis oven R1 top; Vapourizing furnace R2, be broken semicoke pressurization moving-bed gasification stove, and working pressure is greater than 1.0MPa, and slag is discharged in bottom, and coal gas PV2 is discharged on top.
Feature of the present invention further is: pyrolysis oven R1, and working pressure is greater than 2.5MPa; Carbon material vapourizing furnace R2, working pressure is greater than 2.5MPa, the H of gasifier gas PV2
2dividing potential drop is greater than 0.40MPa, and the CO dividing potential drop of gasifier gas PV2 is greater than 0.25MPa.
Feature of the present invention further is: pyrolysis oven R1, and working pressure is greater than 4.0MPa; Carbon material vapourizing furnace R2, working pressure is greater than 4.0MPa, the H of gasifier gas PV2
2dividing potential drop is greater than 0.60MPa, and the CO dividing potential drop of gasifier gas PV2 is greater than 0.40MPa.
Feature of the present invention further is: carbon material F1 is coal charge, and partly or entirely pyrolysis oven R1 semicoke BJ enters vapourizing furnace R2 gas making.
Feature of the present invention further is: the steam occurred after the sewage purification that pyrolysis oven R1 coal gas PV1 sepn process produces enters vapourizing furnace R2 gas making.
Feature of the present invention further is: after at least a portion semicoke BJ becomes powder, the absorption of composition filter bed realizes sewage P2 preliminary cleaning containing the organism in tar sewage P2.
Feature of the present invention further is: vapourizing furnace R2 coal gas PV2 and or pyrolysis oven R1 coal gas PV1 manufacture synthetics.
Feature of the present invention further is: vapourizing furnace R2 coal gas PV2 enters pyrolysis oven R1 quenching section bottom and contacts with hot semicoke as quenching gas, and quenching gas and semicoke counter current contact absorb the cooling semicoke of heat.
Feature of the present invention further is: the vapourizing furnace R1 coal gas PV21 of normal temperature state enters pyrolysis oven R1 quenching section bottom and contacts with hot semicoke as quenching gas.
Feature of the present invention further is: vapourizing furnace R2 coal gas PV22 enters pyrolysis oven R2 pyrolysis section bottom and uses as pyrolysis thermal source gas.
Feature of the present invention further is: high-temperature gasification stove R2 coal gas PV22 enters pyrolysis oven R1 pyrolysis section bottom as pyrolysis thermal source gas contact coal charge.
Feature of the present invention further is: the carbon material vapourizing furnace R2 part that gasifies, use the gasified boiler system of two kinds of operational conditions, and produce respectively normal temperature gasification gas PV21 and coal gas of high temperature PV22; Coal gas of high temperature PV22 enters pyrolysis oven R1 pyrolysis section bottom and uses as whole pyrolysis thermal source gas, and the gas of normal temperature gasification simultaneously PV21 enters pyrolysis oven R1 quenching section bottom and contacts with hot semicoke as quenching gas.
Feature of the present invention further is: the carbon material vapourizing furnace R2 part that gasifies, use the gasified boiler system of two kinds of operational conditions, and produce respectively normal temperature gasification gas PV21 and coal gas of high temperature PV22; First via normal temperature gasification gas PV211 enters pyrolysis oven R2 quenching section bottom and contacts with hot semicoke as quenching gas, it is high-temperature flue gas that the second road normal temperature gasification gas PV212 enters combustion chambers burn, high-temperature flue gas with enter pyrolysis oven R1 pyrolysis section bottom after coal gas of high temperature PV22 Mixed adjustment temperature and contact with the charing feed coal as part or all of pyrolysis thermal source gas use.
Feature of the present invention further is: pyrolysis oven R1 service temperature, top is that 60～800 ℃, charing section are that 550～800 ℃, bottom coke outlet are 50～800 ℃.
Feature of the present invention further is: when carbon material F1 is coal charge, and pyrolysis oven R1 service temperature, top is that 60～150 ℃, bottom coke outlet are 50～90 ℃.
Feature of the present invention further is: vapourizing furnace R2 burning zone service temperature, lower than 50～120 ℃ of ash fusion points; Air outlet, vapourizing furnace R2 top service temperature is 180～800 ℃; Vapourizing furnace R2 oxygenant, be selected from air, oxygen-rich air and purity oxygen, is preferably as purity oxygen; The non-oxygen gasified gas of vapourizing furnace R2, be selected from water vapor and or carbon dioxide gas.
Feature of the present invention further is: described synthetics is selected from methane, methyl alcohol, synthetic oil, is preferably synthetic oil.
Feature of the present invention further is: broken carbon material pressurized gasification process water steam, the steam that the water produced for described carbon material pressurized pyrolysis process and broken carbon material pressurized gasification process or synthetics building-up process occurs.
Feature of the present invention further is: pyrolysis oven R1 row semicoke section is used normal temperature carbonic acid gas rare gas element for isolation gas, has a rest during coke discharging and blows or blow continuously in production phase, and isolation gas enters in pyrolysis oven coal gas.
Feature of the present invention further is: in order to reduce the entrained foreign gas of carbon material F1 that enters pyrolysis oven, use the hopper of coalingging that possesses ventilatory, displacement gas is carbon dioxide.
Feature of the present invention further is: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal or semicoke or Jiao; The broken carbon material of described broken carbon material vapourizing furnace R2 processing is from coal or semicoke or Jiao.
Feature of the present invention further is: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal, and the broken carbon material of described broken carbon material vapourizing furnace R2 processing, from semicoke, forms coal charge pressurization hydropyrolysis and broken semicoke pressurized gasification process combination process.
Feature of the present invention further is: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from semicoke; The broken carbon material of described broken carbon material vapourizing furnace R2 processing, from semicoke, forms semicoke pressurization activation and broken semicoke pressurized gasification process combination process, the semicoke of pyrolysis oven R1 output high-specific surface area.
Feature of the present invention further is: described carbon material pyrolysis oven R1, and carbon material move mode is the downflow system moving-bed, and gas and the solid way of contact are adverse current, and the material carbon material adds from pyrolysis oven R1 top charging opening, and the product semicoke flows out from pyrolysis oven R1 bottom; Described carbon material pyrolysis oven R1, the carbon material semicoke granularity of processing is generally 3.0～60.0mm, is generally 3.0～10.0mm, and the pyrolysis section service temperature is 600～1000 ℃.
Feature of the present invention further is: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal, carbon material move mode is the downflow system moving-bed, gas and the solid way of contact are adverse current, and the material carbon material adds from pyrolysis oven R1 top charging opening, and the product semicoke flows out from pyrolysis oven R1 bottom; Described carbon material pyrolysis oven R1, the granularity of carbon material F1 is generally 3.0～60.0mm; Pyrolysis oven R1 service temperature, top is that 60～200 ℃, charing section bottom are 550～800 ℃.
Feature of the present invention further is: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal, carbon material move mode is the downflow system expanded bed, gas and the solid way of contact are adverse current, and the material carbon material adds from pyrolysis oven R1 top charging opening, and the product semicoke flows out from pyrolysis oven R1 bottom; Described carbon material pyrolysis oven R1, the granularity of carbon material F1 is generally 0.001～8.0mm, is generally 0.1～5.0mm, and the pyrolysis section service temperature is 500～800 ℃.
Feature of the present invention further is: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal, carbon material move mode is the upflowing fluidized-bed, gas and the solid way of contact are and flow, material carbon material and pyrolysis thermal source gas add from pyrolysis oven R1 bottom, and pyrolysis product enters gas-solid separator from the outflow of pyrolysis oven R1 top and is separated into semicoke and pyrolysis gas; Described carbon material pyrolysis oven R1, the granularity of carbon material F1 is generally 0.001～8.0mm, is generally 0.001～5.0mm, and the pyrolysis section service temperature is 500～800 ℃.
Feature of the present invention further is: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal, and carbon material move mode is the upflowing ebullated bed, and the material carbon material adds from pyrolysis oven R1 bottom charging opening, and the product semicoke is collected a mouthful discharge pyrolysis oven R1 from semicoke; Described carbon material pyrolysis oven R1, the granularity of carbon material F1 is generally 0.001～8.0mm, is generally 0.001～5.0mm, and the pyrolysis section service temperature is 500～800 ℃.
Feature of the present invention further is: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal; The top temperature of carbon material in pyrolysis oven R1, lower than the temperature of the outlet coal gas of vapourizing furnace R2 such as at least 100 ℃ of the temperature of the outlet coal gas lower than vapourizing furnace R2.
Pyrolytic process in pyrolysis oven R1 of the present invention and the gasification in vapourizing furnace R2, working pressure is not specifically limited, working pressure generally higher than 1.0MPa, usually above 2.5MPa, preferably higher than 4.5MPa, to improve as far as possible hydrogen partial pressure, the CO dividing potential drop in pyrolyzer, improve the tar yield, suppress the condensation reaction of tar.
Synthetics of the present invention, can be any one synthetics, usually is selected from methane, methyl alcohol, synthetic oil, synthetic oil preferably, because it only contains hydrogen charcoal atom, hydrogen/the charcoal atomic ratio is little, unit price is high, therefore it is long low apart from freight charges, be convenient to realize scale processing and scale sale.
The steam that sewage treatment process of the present invention produces, comprise the steam of the water generation that the processes such as described coal semicoke process processed, char Gasification process, building-up process produce.
Apply when of the present invention, as required, may need to logistics heated, the step such as pressurization, purification, these are knowledge well known by persons skilled in the art, this paper is not described in detail.
The vapourizing furnace R2 that the present invention uses, can be the vapourizing furnace of any suitable construction, such as lurgi gasifier and various follow-on broken coal pressurization moving-bed gasification stove of typical structure.
The pyrolysis oven R1 that the present invention uses, can be the pyrolysis oven of any suitable construction, can be the pyrolysis oven that adopts water wall structure, can be the pyrolysis oven that adopts the heat-resistant lining structure.
The present invention processes the moving bed pyrolysis stove R1 of coal charge, and the first structure comprises pyrolysis section and quenching section, and pyrolysis section is positioned at the top of quenching section, and the semicoke of discharge is the low temperature semicoke, and its structure is: body of heater adopts water wall structure or heat-resistant lining structure; Coal charge enters furnace apparatus and adopts the material lock, and the similar lurgi gasifier coal of material lock construction is locked, and is positioned at top or the top of pyrolysis oven body of heater, with the top of pyrolysis oven body of heater or the Link Port on top, is connected; Carbon material distributor and agitator, coal charge distributor and the agitator of similar lurgi gasifier, be positioned at the top of pyrolysis oven furnace inner space; Pyrolysis thermal source gas, entering the pyrolytic layer bottom by thermal source gas inlet pipe contacts with the carbon material, preferably by thermal source gas inlet pipe, entering thermal source gas sparger then enters pyrolytic layer bottom and contacts with the carbon material, thermal source gas inlet pipe is arranged in bottom or the bottom of pyrolysis oven body of heater usually, also can be arranged in the middle part of pyrolysis oven body of heater; Thermal source gas sparger is arranged in the top of the quenching section of pyrolysis oven furnace inner space usually; The effect of thermal source gas sparger is that thermal source gas is evenly distributed in co-altitude carbon material bed; Quenching gas, enter quenching layer bottom by quenching gas inlet pipe and contact with the carbon material, preferably by quenching gas inlet pipe, enters quenching gas sparger and then enter bottom the quenching layer and contact with the carbon material, and quenching gas inlet pipe is arranged in bottom or the bottom of pyrolysis oven body of heater usually; Quenching gas sparger is arranged in the bottom of the quenching section of pyrolysis oven furnace inner space usually; The effect of quenching gas sparger is that quenching gas is evenly distributed in co-altitude carbon material bed; The semicoke discharge port is positioned at bottom or the bottom of pyrolysis oven body of heater, and the semicoke discharge port of separate unit pyrolysis oven can be 1 or 2 or a plurality of, can control co-altitude carbon material, evenly drops to Action Target; The semicoke discharging device adopts burnt lock, and the similar lurgi gasifier coal of burnt lock construction is locked, and is positioned at bottom or the bottom of pyrolysis oven body of heater, with the bottom of pyrolysis oven body of heater or the Link Port of bottom, is connected.
The present invention processes the moving bed pyrolysis stove R1 of coal charge, while adopting the first structure, it is the cold pyrolysis oven that discharges of the coke, the mode of operation of pyrolysis oven R1 has multiple, can be as follows: after the ventilation of coal lock, coal is locked the top of coalingging and coal being discharged into to the bed of material in pyrolyzer, the coal charge distributor is evenly distributed coal charge, uses as required agitator to improve the coal charge distributing homogeneity; Pyrolysis section in pyrolyzer R1, coal charge moves down, pyrolysis thermal source gas upwards flows, gas and solid counter current contact complete heat transfer, part water and partial CO 2 in pyrolysis thermal source gas are further decomposed, the coal charge pyrolysis produces pyrolysis gas, and all gas product of pyrolysis oven is discharged from the gas exit on pyrolyzer top; Quenching section in pyrolyzer R1, burnt material moves down, and quenching gas upwards flows, and gas and solid counter current contact complete heat absorption and heat up, part water and partial CO 2 in quenching gas are further decomposed, and the quenching gas after intensification enters the coal charge heat transfer of pyrolysis section to pyrolysis section; Pyrolysis char enters burnt lock from the semicoke outlet of pyrolyzer bottom, locks the coke discharging program through Jiao and discharges.In order to reduce dust content in coal gas, in pyrolyzer R1, bed of material top retains certain gas-phase space usually, and in pyrolyzer R1, bed of material top retains certain spacing apart from gas exit.
The coal latching segment program behavior step of coalingging is described as follows:
1. the ventilation of coal lock, step-down: the first step A1 are the venting of coal lock, open the displacement gas purging valve gas in the coal lock is put into to the displacement gas gas holder, and making coal lock pressure is normal pressure or pressure-fired, then closes the displacement gas purging valve; Second step A2, for being filled with displacement gas, opens the displacement gas inflation valve, is filled with gas to coal lock to be feeded and replaces and boost to 0.5～1.0MPa as carbon dioxide gas, closes the displacement gas inflation valve after boosting; The 3rd step A3 is displacement gas, opens the displacement gas purging valve displacement gas is put into to the displacement gas gas holder, and making coal lock pressure is normal pressure or pressure-fired, then closes the displacement gas purging valve, and wait is coaling; Steps A 2 and A3 can carry out twice or repeatedly;
2. the coal lock is coaling and is unloaded coal: the first step B1, and to open coal and lock the valve of coalingging, coal charge enters in the coal lock, after coal capacity reaches requirement, closes coal and locks the valve of coalingging; Second step B2, open the displacement gas inflation valve, is filled with gas to the coal of full material lock and boosts to 0.5～1.0MPa as carbon dioxide gas, closes the displacement gas inflation valve after boosting, and keeps pressure 2 minutes; The 3rd step B3, open displacement gas blow-off valve K9 displacement gas put into to the gas holder of dropping a hint, and making coal lock pressure is normal pressure or pressure-fired, completes the displacement of the interior foreign gas of coal lock and coal charge adsorbed gas, then closes displacement gas blow-off valve K9; Step B2 and B3 can carry out twice or repeatedly; The 4th step B4 inflation is boosted, and opens the displacement gas inflation valve, is filled with gas to the coal lock of full material and equates as carbon dioxide gas boosts to the pyrolysis oven top pressure, then closes the displacement gas inflation valve; The 5th step B5, open coal and lock the valve of unloading coal, and in the coal lock, coal charge enters pyrolysis oven, after the coal lock is unsnatched coal charge, closes coal and lock the valve of unloading coal; Wait for the program of next time coalingging.
Burnt latching segment unloads burnt program behavior step and is described as follows:
1. burnt lock ventilation, boost: the first step S1 is burnt lock venting, opens the displacement gas purging valve and Jiao is locked to interior gas puts into the displacement gas gas holder, and making burnt lock pressure is normal pressure or pressure-fired, then closes the displacement gas purging valve; Second step S2, for being filled with displacement gas, opens the displacement gas inflation valve, is filled with gas to Jiao's lock to be feeded and replaces and boost to 0.5～1.0MPa as carbon dioxide gas, closes the displacement gas inflation valve after boosting; The 3rd step S3 is displacement gas, opens the displacement gas purging valve displacement gas is put into to the displacement gas gas holder, and making burnt lock pressure is normal pressure or pressure-fired, then closes the displacement gas purging valve; Step S2 and S3 can carry out twice or repeatedly; The 4th step S4 boosts for inflation, opens the displacement gas inflation valve, is filled with gas to Jiao to be feeded lock and replace boosting to the pyrolysis oven bottom as carbon dioxide gas and discharge of the coke and locate pressure and equate, closes the displacement gas inflation valve after boosting, and waits Jiao to be installed;
2. burnt lock fills burnt and unloads Jiao: the first step T1, opens burnt lock and fills burnt valve, and Jiao's material enters in burnt lock, after dress Jiao amount reaches requirement, closes burnt lock and fills burnt valve; Second step T2 is burnt lock venting, opens the displacement gas purging valve and Jiao is locked to interior gas puts into the displacement gas gas holder, and making burnt lock pressure is normal pressure or pressure-fired, then closes the displacement gas purging valve; The 3rd step T3, for being filled with displacement gas, opens the displacement gas inflation valve, is filled with gas to Jiao of full material lock and replaces and boost to 0.5～1.0MPa as carbon dioxide gas, closes the displacement gas inflation valve after boosting; The 4th step T4 is displacement gas, opens the displacement gas purging valve displacement gas is put into to the displacement gas gas holder, and making burnt lock pressure is normal pressure or pressure-fired, then closes the displacement gas purging valve; Step T3 and T4 can carry out twice or repeatedly; The 5th step T5, for unloading Jiao, opens burnt lock and unloads burnt valve, Jiao is locked to interior semicoke and be discharged into Chu Jiaoqi, after burnt lock is unsnatched burnt material, closes burnt lock and unloads burnt valve; The 6th step T6, for being filled with displacement gas, opens the displacement gas inflation valve, is filled with gas to Jiao of cavity lock and replaces and boost to 0.5～1.0MPa as carbon dioxide gas, closes the displacement gas inflation valve after boosting; The 7th step T7 is displacement gas, open displacement gas blow-off valve KT9 by Jiao the air composition in locking put into the gas holder of dropping a hint, making burnt lock pressure is normal pressure or pressure-fired, then closes the displacement gas blow-off valve; Step T6 and T7 can carry out twice or repeatedly; The next one of waiting for burnt latching segment unloads burnt program.
The present invention processes the moving bed pyrolysis stove R1 of coal charge, and the second structure only comprises pyrolysis section, and the semicoke of discharge is hot semicoke, and its structure is: body of heater adopts water wall structure or heat-resistant lining structure; Coal charge enters furnace apparatus and adopts the material lock, and the similar lurgi gasifier coal lock of material lock construction, be connected with the top of pyrolysis oven body of heater or the Link Port on top; Carbon material sparger distributor and agitator, coal charge distributor and the agitator of similar lurgi gasifier, be positioned at the top of pyrolysis oven furnace inner space; Pyrolysis thermal source gas, entering the pyrolytic layer bottom by inlet pipe contacts with the carbon material, preferably by inlet pipe, entering thermal source gas sparger then enters pyrolytic layer bottom and contacts with the carbon material, the inlet pipe of pyrolysis thermal source gas is arranged in bottom or the bottom of pyrolysis oven body of heater usually, and the sparger of pyrolysis thermal source gas is arranged in bottom or the bottom of pyrolysis oven furnace inner space usually; The semicoke discharge port is positioned at bottom or the bottom of pyrolysis oven body of heater, and the semicoke discharge port of separate unit pyrolysis oven can be 1 or 2 or a plurality of, can control co-altitude carbon material, evenly drops to Action Target; The semicoke discharging device adopts burnt lock, and the similar lurgi gasifier coal lock of material lock construction, be connected with the bottom of pyrolysis oven body of heater or the Link Port of bottom.
The present invention processes the moving bed pyrolysis stove R1 of coal charge, it while adopting the second structure, is the heat pyrolysis oven that discharges of the coke, heat is burnt must be through the oke-quenching device cooling, the mode of operation of pyrolysis oven R1 has multiple, can be as follows: after the ventilation of coal lock, the coal lock is coaling and is unloaded coal and enters the pyrolyzer top, and the coal charge distributor is evenly distributed coal charge, uses as required agitator to improve the coal charge distributing homogeneity; In pyrolyzer R1, coal charge moves down, pyrolysis thermal source gas upwards flows, gas and solid counter current contact complete heat transfer, part water and partial CO 2 in pyrolysis thermal source gas are further decomposed, the coal charge pyrolysis produces pyrolysis gas, and all gas product of pyrolysis oven is discharged from the gas exit on pyrolyzer top; Pyrolysis char is discharged from the semicoke outlet of pyrolyzer bottom.
The present invention processes the moving bed pyrolysis stove R1 of coal charge, while adopting the second structure, is the heat pyrolysis oven that discharges of the coke, and hot Jiao can directly enter vapourizing furnace R2, and hot Jiao also can draw off storage after the ventilation of oke-quenching device H1 decrease temperature and pressure.
Claims (42)
1. a broken carbon material pressurized gasification and carbon material pressurized pyrolysis combination process is characterized in that comprising following steps: by carbon material F1 pressurized pyrolysis stove R1 and the broken carbon material F2 pressurization moving-bed gasification stove R2 use of connect, part or all of gasifier gas PV2 removes pyrolysis oven R1; Pyrolysis oven R1, working pressure is greater than normal pressure, and carbon material F1 enters pyrolysis oven R1 and has contacted pyrolysis with destructive distillation thermal source gas, and carbon material pyrolysis solid product is semicoke BJ, and carbon material pyrolysis gas product enters in coal gas PV1, and semicoke BJ discharges pyrolysis oven R1; The coal gas PV1 that pyrolysis oven is discharged is separated into coal gas P1, contains tar sewage P2 and coal tar P3 through the refrigerated separation process; Vapourizing furnace R2, working pressure is greater than normal pressure.
2. method according to claim 1 is characterized in that: partly or entirely gasifier gas PV2 goes pyrolysis oven R1 to make destructive distillation thermal source gas to use, and destructive distillation thermal source gas provides heat for coal charge F1 retort process; Pyrolysis oven R1, working pressure is greater than 1.0MPa, and destructive distillation thermal source gas adds from pyrolysis oven R1 bottom charging opening, and coal gas PV1 discharges from pyrolysis oven R1 top; Vapourizing furnace R2, be broken semicoke pressurization moving-bed gasification stove, and working pressure is greater than 1.0MPa, and slag is discharged in bottom, and coal gas PV2 is discharged on top.
3. method according to claim 2 is characterized in that: pyrolysis oven R1, and working pressure is greater than 2.5MPa; Carbon material vapourizing furnace R2, working pressure is greater than 2.5MPa, the H of gasifier gas PV2
2dividing potential drop is greater than 0.40MPa, and the CO dividing potential drop of gasifier gas PV2 is greater than 0.25MPa.
4. according to claim 2 or described method, it is characterized in that: pyrolysis oven R1, working pressure is greater than 4.0MPa; Carbon material vapourizing furnace R2, working pressure is greater than 4.0MPa, the H of gasifier gas PV2
2dividing potential drop is greater than 0.60MPa, and the CO dividing potential drop of gasifier gas PV2 is greater than 0.40MPa.
5. according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: carbon material F1 is coal charge, and partly or entirely pyrolysis oven R1 semicoke BJ enters vapourizing furnace R2 gas making.
6. according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: the steam occurred after the sewage purification that pyrolysis oven R1 coal gas PV1 sepn process produces enters vapourizing furnace R2 gas making.
7. according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: after at least a portion semicoke BJ becomes powder, the absorption of composition filter bed realizes sewage P2 preliminary cleaning containing the organism in tar sewage P2.
8. according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: vapourizing furnace R2 coal gas PV2 and or pyrolysis oven R1 coal gas PV1 manufacture synthetics.
9. according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: vapourizing furnace R2 coal gas PV2 enters pyrolysis oven R1 quenching section bottom and contacts with hot semicoke as quenching gas, and quenching gas and semicoke counter current contact absorb the cooling semicoke of heat.
10. method according to claim 9 is characterized in that: the vapourizing furnace R1 coal gas PV21 of normal temperature state enters pyrolysis oven R1 quenching section bottom and contacts with hot semicoke as quenching gas.
11. according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: vapourizing furnace R2 coal gas PV22 enters pyrolysis oven R2 pyrolysis section bottom and uses as destructive distillation thermal source gas.
12. method according to claim 11 is characterized in that: high-temperature gasification stove R2 coal gas PV22 enters pyrolysis oven R1 pyrolysis section bottom as destructive distillation thermal source gas contact coal charge.
13., according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: the carbon material vapourizing furnace R2 part that gasifies, use the gasified boiler system of two kinds of operational conditions, produce respectively normal temperature gasification gas PV21 and coal gas of high temperature PV22; Coal gas of high temperature PV22 enters pyrolysis oven R1 pyrolysis section bottom and uses as whole destructive distillation thermal source gas, and the gas of normal temperature gasification simultaneously PV21 enters pyrolysis oven R1 quenching section bottom and contacts with hot semicoke as quenching gas.
14., according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: the carbon material vapourizing furnace R2 part that gasifies, use the gasified boiler system of two kinds of operational conditions, produce respectively normal temperature gasification gas PV21 and coal gas of high temperature PV22; First via normal temperature gasification gas PV211 enters pyrolysis oven R2 quenching section bottom and contacts with hot semicoke as quenching gas, it is high-temperature flue gas that the second road normal temperature gasification gas PV212 enters combustion chambers burn, high-temperature flue gas with enter pyrolysis oven R1 pyrolysis section bottom after coal gas of high temperature PV22 Mixed adjustment temperature and contact with the charing feed coal as part or all of destructive distillation thermal source gas use.
15., according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: pyrolysis oven R1 service temperature, top is that 60～800 ℃, charing section are that 550～800 ℃, bottom coke outlet are 50～800 ℃.
16. method according to claim 15 is characterized in that: pyrolysis oven R1 service temperature, top is that 60～150 ℃, bottom coke outlet are 50～90 ℃.
17., according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: vapourizing furnace R2 burning zone service temperature, lower than 50～120 ℃ of ash fusion points; Air outlet, vapourizing furnace R2 top service temperature is 180～800 ℃; Vapourizing furnace R2 oxygenant, be selected from air, oxygen-rich air and purity oxygen; The non-oxygen gasified gas of vapourizing furnace R2, be selected from water vapor and or carbon dioxide gas.
18. method according to claim 17 is characterized in that: vapourizing furnace R2 oxygenant is purity oxygen.
19. method according to claim 8 is characterized in that: described synthetics is selected from methane, methyl alcohol, synthetic oil.
20. method according to claim 19 is characterized in that: described synthetics is synthetic oil.
21., according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: broken carbon material pressurized gasification process water steam, the steam that the water produced for described carbon material pressurized pyrolysis process and broken carbon material pressurized gasification process or synthetics building-up process occurs.
22., according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: pyrolysis oven R1 row semicoke section is used normal temperature carbonic acid gas rare gas element for isolation gas, has a rest during coke discharging and blows or blow continuously in production phase, and isolation gas enters in pyrolysis oven coal gas.
23., according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: in order to reduce the entrained foreign gas of carbon material F1 that enters pyrolysis oven, use the hopper of coalingging that possesses ventilatory, displacement gas is carbon dioxide.
24., according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal or semicoke or Jiao; The broken carbon material of described broken carbon material vapourizing furnace R2 processing is from coal or semicoke or Jiao.
25. according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal, the broken carbon material of described broken carbon material vapourizing furnace R2 processing, from semicoke, forms coal charge pressurization hydrotorting and broken semicoke pressurized gasification process combination process.
26., according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from semicoke; The broken carbon material of described broken carbon material vapourizing furnace R2 processing, from semicoke, forms semicoke pressurization activation and broken semicoke pressurized gasification process combination process, the semicoke of pyrolysis oven R1 output high-specific surface area.
27. method according to claim 26, it is characterized in that: described carbon material pyrolysis oven R1, carbon material move mode is the downflow system moving-bed, gas and the solid way of contact are adverse current, the material carbon material adds from pyrolysis oven R1 top charging opening, and the product semicoke flows out from pyrolysis oven R1 bottom; Described carbon material pyrolysis oven R1, the carbon material semicoke granularity of processing is 3.0～60.0mm, the pyrolysis section service temperature is 600～1000 ℃.
28. method according to claim 27 is characterized in that: described carbon material pyrolysis oven R1, the carbon material semicoke granularity of processing is 3.0～10.0mm.
29., according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal; Carbon material move mode is the downflow system moving-bed, and gas and the solid way of contact are adverse current, and the material carbon material adds from pyrolysis oven R1 top charging opening, and the product semicoke flows out from pyrolysis oven R1 bottom.
30. method according to claim 29 is characterized in that: described carbon material pyrolysis oven R1, the carbon material coal charge granularity of processing is 3.0～60.0mm; Pyrolysis oven R1 service temperature, top is that 60～200 ℃, charing section bottom are 550～800 ℃.
31., according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal; Carbon material move mode is the downflow system expanded bed, and gas and the solid way of contact are adverse current, and the material carbon material adds from pyrolysis oven R1 top charging opening, and the product semicoke flows out from pyrolysis oven R1 bottom.
32. method according to claim 31 is characterized in that: described carbon material pyrolysis oven R1, the carbon material F1 of processing is the coal charge that granularity is 0.001～8.0mm, the pyrolysis section service temperature is 500～800 ℃.
33. method according to claim 32 is characterized in that: described carbon material pyrolysis oven R1, the carbon material F1 of processing is the coal charge that granularity is 0.1～5.0mm, the pyrolysis section service temperature is 500～800 ℃.
34., according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal; Carbon material move mode is the upflowing fluidized-bed, and gas and the solid way of contact be and flow, and material carbon material and destructive distillation thermal source gas add from pyrolysis oven R1 bottom, and the destructive distillation product flows out from pyrolysis oven R1 top and enters gas-solid separator and be separated into semicoke and carbonization gas.
35. method according to claim 34 is characterized in that: described carbon material pyrolysis oven R1, the carbon material F1 of processing is the coal charge that granularity is 0.001～8.0mm, the pyrolysis section service temperature is 500～800 ℃.
36. method according to claim 35 is characterized in that: described carbon material pyrolysis oven R1, the carbon material F1 of processing is that granularity is 0.001～5.0mm.
37., according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: the carbon material of described carbon material pyrolysis oven R1 processing is from coal; Carbon material move mode is the upflowing ebullated bed, and the material carbon material adds from pyrolysis oven R1 bottom charging opening, and the product semicoke is collected a mouthful discharge pyrolysis oven R1 from semicoke.
38., according to the described method of claim 37, it is characterized in that: described carbon material pyrolysis oven R1, the carbon material F1 of processing is the coal charge that granularity is 0.001～8.0mm, the pyrolysis section service temperature is 500～800 ℃.
39., according to the described method of claim 38, it is characterized in that: described carbon material pyrolysis oven R1, the carbon material F1 of processing is the coal charge that granularity is 0.001～5.0mm.
40., according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal; The top temperature of carbon material in pyrolysis oven R1, lower than the temperature of the outlet coal gas of vapourizing furnace R2.
41., according to the described method of claim 40, it is characterized in that: the carbon material F1 of described carbon material pyrolysis oven R1 processing is from coal; The top temperature of carbon material in pyrolysis oven R1, lower than at least 100 ℃ of the temperature of the outlet coal gas of vapourizing furnace R2.
42. according to claim 1 or 2 or 3 or 4 described methods, the moving bed pyrolysis stove R1 of processing coal charge, structure comprises retort section and quenching section, and retort section is positioned at the top of quenching section, the semicoke of discharging is the low temperature semicoke, and its structure is: body of heater adopts water wall structure or heat-resistant lining structure; Coal charge enters furnace apparatus and adopts the material lock, and the similar lurgi gasifier coal of material lock construction is locked, and is positioned at top or the top of pyrolysis oven body of heater, with the top of pyrolysis oven body of heater or the Link Port on top, is connected; Carbon material distributor and agitator, coal charge distributor and the agitator of similar lurgi gasifier, be positioned at the top of pyrolysis oven furnace inner space; Pyrolysis thermal source gas, entering destructive distillation layer bottom by thermal source gas inlet pipe contacts with the carbon material, preferably by thermal source gas inlet pipe, entering thermal source gas sparger then enters destructive distillation layer bottom and contacts with the carbon material, thermal source gas inlet pipe is arranged in bottom or the bottom of pyrolysis oven body of heater usually, also can be arranged in the middle part of pyrolysis oven body of heater; Thermal source gas sparger is arranged in the top of the quenching section of pyrolysis oven furnace inner space usually; The effect of thermal source gas sparger is that thermal source gas is evenly distributed in co-altitude carbon material bed; Quenching gas, enter quenching layer bottom by quenching gas inlet pipe and contact with the carbon material, preferably by quenching gas inlet pipe, enters quenching gas sparger and then enter bottom the quenching layer and contact with the carbon material, and quenching gas inlet pipe is arranged in bottom or the bottom of pyrolysis oven body of heater usually; Quenching gas sparger is arranged in the bottom of the quenching section of pyrolysis oven furnace inner space usually; The effect of quenching gas sparger is that quenching gas is evenly distributed in co-altitude carbon material bed; The semicoke discharge port is positioned at bottom or the bottom of pyrolysis oven body of heater, and the semicoke discharge port of separate unit pyrolysis oven can be 1 or 2 or a plurality of, can control co-altitude carbon material, evenly drops to Action Target; The semicoke discharging device adopts burnt lock, and the similar lurgi gasifier coal of burnt lock construction is locked, and is positioned at bottom or the bottom of pyrolysis oven body of heater, with the bottom of pyrolysis oven body of heater or the Link Port of bottom, is connected.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104650933A (en) * | 2015-01-13 | 2015-05-27 | 北京神雾环境能源科技集团股份有限公司 | Garbage pyrolysis sewage treatment system and garbage pyrolysis sewage treatment method |
| CN105062526A (en) * | 2015-08-05 | 2015-11-18 | 航天长征化学工程股份有限公司 | Coal pyrolysis gasification poly-generation system and pyrolysis gasification method thereof |
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| CN105199763A (en) * | 2015-10-22 | 2015-12-30 | 航天长征化学工程股份有限公司 | Circulating gas heat carrier coal pyrolysis system and pyrolysis method thereof |
| CN111621333A (en) * | 2020-06-02 | 2020-09-04 | 新奥科技发展有限公司 | Catalytic coal gasification process |
| CN115449388A (en) * | 2022-09-07 | 2022-12-09 | 上海乐茗环保科技有限公司 | Pressure gas continuous biomass cracking carbonization reaction furnace |
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Application publication date: 20131211 |