CN102533295A - Coal dry distillation method for mixture of main coal material and auxiliary solid material - Google Patents
Coal dry distillation method for mixture of main coal material and auxiliary solid material Download PDFInfo
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- CN102533295A CN102533295A CN2012100254761A CN201210025476A CN102533295A CN 102533295 A CN102533295 A CN 102533295A CN 2012100254761 A CN2012100254761 A CN 2012100254761A CN 201210025476 A CN201210025476 A CN 201210025476A CN 102533295 A CN102533295 A CN 102533295A
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Abstract
The invention discloses a coal dry distillation method for a mixture of a main coal material and an auxiliary solid material. The dry distillation method is used for reducing the apparent gasification rate (namely the apparent gasification intensity) of the solid materials and enlarging an area of an airflow channel. Compared with a separate coal processing method, the dry distillation method has the advantage that: coal with small granularity can be processed. The auxiliary solid material can be coke with proper granularity, which comes from the outside of the pulverized coal F dry distillation process or is generated by the pulverized coal F dry distillation process.
Description
Technical field
The present invention relates to a kind of dry distillation of coal method that is raw material with major ingredient coal and auxiliary solid material mixture; Say that especially the present invention relates to a kind of is the internally heated coal carbonization method of raw material with fine coal and coke breeze mixture; More particularly; The present invention relates to a kind of internally heated coal carbonization method that is raw material with fine coal and self-produced coke breeze mixture; Be used for reduction and go into the apparent vaporization rate of stove coal charge (being apparent gasification intensity); Enlarged the gas channel area simultaneously, compared, can realize tinyization of raw material powder coal particle size with independent processing coal charge.
Background technology
As everyone knows; Anshan Thermal Energy Inst. of China Steel Group begins " is that raw material is at the special-purpose blue charcoal of vertical retort refining iron alloy with non-caking coal or weakly caking coal lump coal " technology (hereinafter to be referred as middle steel internally heated coal carbonization gas making technology BT) of constantly research and development the early 1980s; Adopt and be fit to coal source (such as Chinese Datong District, the geographic coal in refreshing mansion); The blue charcoal of refining and by-product raw gas and middle coalite tar in vertical retort; Be the mature industryization technology that a kind of blue charcoal good quality of product, coal tar productive rate are high, lower, the supporting green technology of construction costs is perfect, obtained already widely applying.
The thermal equilibrium of the heat transfer process that internally heated coal carbonization furnace is comprised; The mass ratio that relates to solid amount of vaporization and gas stream; The solid voidage is exactly gas-phase space in essence; Represent gas phase operation pressure (absolute pressure) with PV, represent bed voidage with ε, then the gaseous stream quality is expressed as with the ratio KW of solid amount of vaporization quality:
KW=(PV * gas-phase space volume * gas phase average density)/(coal charge entity volume * solid mean density * solid vaporization rate)
For the particular coal retort process, because gas phase average density, solid mean density, solid vaporization rate are constant relatively, following formula is changed to the volume ratio KV of gaseous phase materials and solid amount of vaporization:
KV=(PV * gas-phase space volume)/(coal charge entity volume * solid vaporization rate)
=(PV * ε/(1-ε))/solid vaporization rate
=(KW * solid mean density)/gas phase average density
The suitable operational condition of any specific internally heated coal carbonization process all must satisfy the thermal equilibrium requirement; Kinetics requirement based on the heat supply cascade process; During gas phase heating coal charge: gas phase (heat supply side) ability of conducting heat must be more than or equal to solid phase (side of the being heated) ability of being heated; During gas phase cooling charcoal material: gas phase is conducted heat (endothermic side) ability must be more than or equal to solid phase heat release (side of being cooled) ability; Therefore there is corresponding minimum KW; That is to say to have corresponding minimum KV, have specific minimum PV, must keep specific minimum bed voidage ε for specific " PV and solid vaporization rate " in other words for specific " bed voidage ε and solid vaporization rate ".
Because it is that PV is about 0.12～0.18MPa (absolute pressure) that the PV of existing internally heated coal carbonization furnace is normal pressure; For coal charge and the definite destructive distillation operating process of destructive gasifying rate thereof; There is a lower value in the bed voidage ε that adapts with it, when bed voidage ε reaches or be lower than this lower value, only says from the thermal equilibrium angle; Internally heated coal carbonization furnace can't works better, a basic reason of Here it is existing internally heated coal carbonization furnace restriction coal charge granularity lower limit.
Can find out that from KV=((PV * ε/(1-ε))/solid vaporization rate) improving one of fine coal destructive distillation manipulating approach is to increase PV, the inventor has related application in addition.
Can find out that from KV=((PV * ε/(1-ε))/solid vaporization rate) improving one of fine coal destructive distillation manipulating approach is to increase bed voidage ε, the inventor has related application in addition.
Can find out that from KV=((PV * ε/(1-ε))/solid vaporization rate) improving one of fine coal destructive distillation manipulating approach is to reduce the solid vaporization rate, application of the present invention is exactly that this is proposed a solution.
Above-mentioned analysis is pointed out; Reduce the solid vaporization rate and can reduce the granularity that to process fine coal; Because the destructive distillation task of target coal charge is that the solid vaporization rate can not reduce; Therefore can only reduce destructive distillation apparent material vaporization rate; That is to say and can only in coal charge, sneak into density, the approaching low vaporization rate solid blend composition C of particle diameter height, and burnt the separating and must accomplish easily or need not separate of destructive distillation product of solid phase prod CGP and target coal charge after the gasification of this solid blend composition C, gas products CVP must accomplish or need not separate with separating of coal gas easily after the gasification of this solid blend composition C.And the source that conveniently is easy to get of the above-mentioned low vaporization rate solid blend composition C fine coal destructive distillation solid product coke that granularity is suitable just, the perhaps self-produced solid product coke of said just fine coal retort process.
The main effect of technical scheme of the present invention is:
1. for existing non-pressure process internally heated coal carbonization technology,, mix suitable low gasification charcoal material of granularity or burnt material to the small grain size coal charge; Mix the back as the destructive distillation raw material; Reduce the apparent vaporization rate of retort process, enlarged gas passage area, have the function that realizes tinyization of coal charge granularity;
2. for novel pressurization internally heated coal carbonization technology, realize the coal charge granular;
3. for external-heat dry distillation of coal technology, help tinyization of coal charge to a certain extent.
Because the internal heat type retort process bed voidage ε of granularity, volume particle size coal charge is superfluous in the routine, for middle granularity, volume particle size coal charge, the present invention is unsuitable.
The method of the invention is not appeared in the newspapers.
First purpose of the present invention is to propose a kind of dry distillation of coal method that is raw material with major ingredient coal and auxiliary solid material mixture.
It is the dry distillation of coal method of raw material with fine coal and coke breeze mixture that second purpose of the present invention is to propose a kind of.
The 3rd purpose of the present invention is to propose a kind of dry distillation of coal method that is raw material with fine coal and self-produced coke breeze mixture; Be used to reduce the apparent vaporization rate of solid material (being apparent gasification intensity); Enlarged the gas channel area simultaneously; Compare with independent processing coal charge, can realize tinyization of raw material powder coal particle size.
Summary of the invention
A kind of dry distillation of coal method that is raw material with major ingredient coal and auxiliary solid material mixture of the present invention is characterized in that: will mix back gained solid mixture HL as dry distillation of coal process raw material with major ingredient coal F granularity, approaching low vaporization rate solid blend composition C and the major ingredient coal F of density altitude.
The present invention is particularly suitable for the internally heated coal carbonization process; Usually will mix back gained solid mixture HL as solid blend composition C and major ingredient coal F with the approaching coke of major ingredient coal F granularity height and be used as dry distillation of coal process raw material, among the raw material HL solid blend composition C weight content be generally 0.1～0.9, be generally 0.2～0.8, preferable be 0.3～0.7.
The present invention is particularly suitable for the internally heated coal carbonization process, can self-produced charcoal product ZCT be mixed the back as dry distillation of coal process raw material HL as solid blend composition C and major ingredient coal F, and solid blend composition C weight content is 0.1～0.9 among the raw material HL; Said internally heated coal carbonization process flow is: comprise charring furnace and coking chamber heat-carrying component internal circulation system, charring furnace comprises the coking chamber of coal and the fuel gas combustion chamber that possibly exist; In coking chamber, according to the advance route of coal charge, being divided into first section is that coal preheating section (or claim gas cooling section), second section are that coal carbonization section, the 3rd section are charcoal cooling section (or claiming gas preheating section); In the 3rd section zone, the first via gas and the two sections process material contact heat-exchangings that comprise coking chamber heat-carrying component reclaim and become three sections process gas after its heats heat up, and three sections process material leave three sections zones; In second section zone; The gas fume of combustion chamber of three sections process gas and existence; Carry out gas-solid with one section process material and directly contact the charing effect that takes place, two sections process material leave second section zone and get into the 3rd section zone, and two sections process gas leave second section zone and get into first section zone; In first section zone, after transmitting the heat cooling and sneak into one section generation gas with the outside certainly coal charge Contact Heating coal charge that adds, two sections process gas become one section product gas (raw gas), and become one section process material after coal charge heats up and get into second section zone; Raw gas is discharged charring furnace; Charcoal product ZCT discharges charring furnace; In raw gas refrigerated separation part, the raw gas that charring furnace is discharged in cooling and separation obtains from ring coal gas, coal tar, contains tar sewage; At least a portion is returned coking chamber as coking chamber heat-carrying component based on the gas stream of raw gas, constitutes destructive distillation part coking chamber heat-carrying component internal recycle.
The present invention is particularly suitable for the internally heated coal carbonization process, in the charring furnace gas phase operation pressure P V usually greater than 0.20MPa (absolute pressure), be generally 0.40～3.0MPa (absolute pressure).
The present invention is particularly suitable for the internally heated coal carbonization process, and coking chamber coal carbonization section service temperature is 500～900 ℃ or is 550～800 ℃ or is 600～750 ℃ or is 600～700 ℃.
When the present invention is applied to blue charcoal and produces; Operational condition is generally: in coking chamber; Said coal charge is non-caking coal or weakly caking coal; The charcoal product is semicoke (being blue charcoal), and coal carbonization section service temperature is 550～850 ℃, and the long-pending flow rate of circulation heat-carrying gas is 150～450 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
When the present invention was applied to blue charcoal and produces, operational condition is generally: in coking chamber, coal carbonization section service temperature was 550～800 ℃, and the long-pending flow rate of circulation heat-carrying gas is 200～400 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
When the present invention was applied to blue charcoal and produces, operational condition preferably is: in coking chamber, coal carbonization section service temperature was 600～700 ℃, and the long-pending flow rate of circulation heat-carrying gas is 250～350 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
Internally heated retort oven gas-operated pressure of the present invention can be higher than normal pressure or far above normal pressure; At this moment; The present invention uses the reinforced material of coal charge lock system, withstand voltage gas retort, pressure combustion chamber, charcoal material to go out furnace charge lock system, dry cooling system usually, and facilities such as circulation heat-carrying gas sparger, gas fume of combustion chamber sparger also possibly arranged in coking chamber inside.
The used coal charge of coking chamber of the present invention is non-caking coal or weakly caking coal, and granularity is: 25～100mm or 10～40mm or 3～15mm or 1～5mm or 0.5～3mm.
The present invention is particularly suitable for the internally heated coal carbonization process, and solid blend composition C median size Φ C and the ratio Φ C/ Φ F of major ingredient coal F median size Φ F be generally 0.3～4.0, be generally 0.5～2.0, the preferably is 0.7～1.5.
The present invention is particularly suitable for the internally heated coal carbonization process, and the requirement of solid material particle diameter is generally:
Solid blend composition C median size Φ C and the ratio Φ C/ Φ F of major ingredient coal F median size Φ F are 0.3～4.0;
The ascending Φ C1～Φ C2 that is distributed as of solid blend composition C particle diameter, Φ C1/ Φ C2 >=0.15;
The ascending Φ F1～Φ F2 that is distributed as of major ingredient coal F particle diameter, Φ F1/ Φ F >=0.15.
The present invention is particularly suitable for the internally heated coal carbonization process, and the requirement of solid material particle diameter is generally:
Solid blend composition C median size Φ C and the ratio Φ C/ Φ F of major ingredient coal F median size Φ F are 0.5～2.0;
The ascending Φ C1～Φ C2 that is distributed as of solid blend composition C particle diameter, Φ C1/ Φ C2 >=0.3;
The ascending Φ F1～Φ F2 that is distributed as of major ingredient coal F particle diameter, Φ F1/ Φ F2 >=0.3.
The present invention is particularly suitable for the internally heated coal carbonization process, and the requirement of solid material particle diameter is preferably:
Solid blend composition C median size Φ C and the ratio Φ C/ Φ F of major ingredient coal F median size Φ F are 0.7～1.5;
The ascending Φ C1～Φ C2 that is distributed as of solid blend composition C particle diameter, Φ C1/ Φ C2 >=0.45;
The ascending Φ F1～Φ F2 that is distributed as of major ingredient coal F particle diameter, Φ F1/ Φ F2 >=0.45.
Range of application of the present invention comprises: external-heat dry distillation of coal process, dry distillation of coal process are for using coal charge angle of rake external-heat dry distillation of coal process or internally heated coal carbonization process, the internally heated coal carbonization process of gas-solid counter current contact, gas-solid cocurrent flow type dry distillation of coal process.
Embodiment
Below describe the present invention in detail.
Pressure of the present invention refers to absolute pressure.
Gas component concentrations of the present invention when not specializing, is volumetric concentration.
This paper is the process modification of example explanation the present invention to the blue charcoal device of internal heat type with the blue charcoal device technique of large-scale upright furnace (600,000 t/a upright furnace) of Anshan Research Inst. of Heat Energy, China Iron & Steel Group and Huang gang, Hubei metallurgical furnace Ltd of Huaxing, yet this can not limit Application Areas of the present invention.
The present invention can be applied to the dry distillation of coal gas making process of all uses, comprise the gas-solid counter current contact internally heated coal carbonization gas making process, external-heat dry distillation of coal gas making process, use the angle of rake dry distillation of coal gas making of coal charge process, gas-solid cocurrent flow type dry distillation of coal gas making process etc.
The technical process of this section internally heated coal carbonization gas making part that is used to describe the gas-solid counter current contact of common process (or be referred to as " carbonization process and charring furnace perolene cyclic part ").The coal gas of upright furnace heating usefulness is through the further cooling of gas purification workshop section and the coal gas after purifying.The air of upright furnace heating usefulness is supplied with by air-blaster pressurization back; Coal gas and air mix through burner, in horizontal quirk internal combustion, and the high-temp waste gas that burning produces; Get into coking chamber through equally distributed air inlet port on the coking chamber side wall, utilize the heat of high-temp waste gas that coal charge is carried out charing.Burner is established two-layer up and down, and heating is main with lower floor, and safety effect is played on the upper strata.
At first pack in the coal groove of furnace roof topmost by being equipped with qualified shove charge coal that coal workshop section ships, pack in the coking chamber through putting coal cock and auxiliary coal bin again.Continuously to the coking chamber coal.The lump coal that adds coking chamber moves from top to bottom, sends into the high-temperature gas counter current contact of coking chamber with the combustion chamber.The top of coking chamber is preheating section, and lump coal is heated to about 350～550 ℃ in this section; Lump coal continues to move down the retort section that gets into the coking chamber middle part, and lump coal is heated to pyrolysis temperature as 550～900 ℃ through this section, and is blue charcoal by charing; When blue charcoal passes through the cooling section of coking chamber bottom; Being passed into this section perolene circulating gas is cooled to 180～250 ℃ and becomes warm charcoal; The temperature charcoal gets into and to put out charcoal section (quenching section) and be cooled to about 80 ℃ by coke quenching water, after putting burnt machine and discharge continuously with scraper plate, falls on the dryer through chute.The gas mixture (raw gas) of the coal gas that produces when the high-temp waste gas of the coal gas that coal charge produces in carbonization process, combustion chamber entering coking chamber and cooling coke; Get into pneumatic trough through upcast, bridge tube; Gas mixture about 150～200 ℃ (raw gas) after the cyclic ammonia water sprinkling is cooled to 80～90 ℃, gets into washing tower along inhaling gas pipe through gas-liquid separator in bridge tube and pneumatic trough; Ammoniacal liquor is by washing tower top spray, and the ammoniacal liquor that the bottom has tar gets into heat ring tank; Coal gas is got into by direct-cooled washing tower bottom, and top is discharged and got into the indirect cooler that uses recirculated water usually; Coal gas is cooled to 40～45 ℃ by 80 ℃.Coal gas gets into the Root's blower pressurization behind straight a, water cooler, behind electrical tar precipitator, use as purifying coal gas.In common process, the part raw gas is directly sent the upright furnace combustion chamber back to and is acted as a fuel, and a large amount of raw gass are directly sent upright furnace back to and used as circulation heat-carrying gas.From the tar ammonia that gas-liquid separator and direct-cooled washing tower come out, flow into heat ring tank standing separation tar certainly, tar dewaters with being pumped to the tar storage tank, and thermal cycling ammoniacal liquor is with being pumped to the furnace roof effuser and direct-cooled washing tower recycles.From the tar ammonia that indirect cooler comes out, flow into cold ring tank standing separation tar certainly, tar is with being pumped to the dehydration of tar storage tank, and cold cyclic ammonia water recycles with being pumped to inter cooler.Tar (moisture＜4%) after the dehydration of tar storage tank is delivered to tar job shop or entrucking outward transport.
Below describe characteristic of the present invention in detail.
A kind of dry distillation of coal method that is raw material with major ingredient coal and auxiliary solid material mixture of the present invention is characterized in that: will mix back gained solid mixture HL as dry distillation of coal process raw material with major ingredient coal F granularity, approaching low vaporization rate solid blend composition C and the major ingredient coal F of density altitude.
The present invention is particularly suitable for the internally heated coal carbonization process; Usually will mix back gained solid mixture HL as solid blend composition C and major ingredient coal F with the approaching coke of major ingredient coal F granularity height and be used as dry distillation of coal process raw material, among the raw material HL solid blend composition C weight content be generally 0.1～0.9, be generally 0.2～0.8, preferable be 0.3～0.7.
The present invention is particularly suitable for the internally heated coal carbonization process, can self-produced charcoal product ZCT be mixed the back as dry distillation of coal process raw material HL as solid blend composition C and major ingredient coal F, and solid blend composition C weight content is 0.1～0.9 among the raw material HL; Said internally heated coal carbonization process flow is: comprise charring furnace and coking chamber heat-carrying component internal circulation system, charring furnace comprises the coking chamber of coal and the fuel gas combustion chamber that possibly exist; In coking chamber, according to the advance route of coal charge, being divided into first section is that coal preheating section (or claim gas cooling section), second section are that coal carbonization section, the 3rd section are charcoal cooling section (or claiming gas preheating section); In the 3rd section zone, the first via gas and the two sections process material contact heat-exchangings that comprise coking chamber heat-carrying component reclaim and become three sections process gas after its heats heat up, and three sections process material leave three sections zones; In second section zone; The gas fume of combustion chamber of three sections process gas and existence; Carry out gas-solid with one section process material and directly contact the charing effect that takes place, two sections process material leave second section zone and get into the 3rd section zone, and two sections process gas leave second section zone and get into first section zone; In first section zone, after transmitting the heat cooling and sneak into one section generation gas with the outside certainly coal charge Contact Heating coal charge that adds, two sections process gas become one section product gas (raw gas), and become one section process material after coal charge heats up and get into second section zone; Raw gas is discharged charring furnace; Charcoal product ZCT discharges charring furnace; In raw gas refrigerated separation part, the raw gas that charring furnace is discharged in cooling and separation obtains from ring coal gas, coal tar, contains tar sewage; At least a portion is returned coking chamber as coking chamber heat-carrying component based on the gas stream of raw gas, constitutes destructive distillation part coking chamber heat-carrying component internal recycle.
The present invention is particularly suitable for the internally heated coal carbonization process, in the charring furnace gas phase operation pressure P V usually greater than 0.20MPa (absolute pressure), be generally 0.40～3.0MPa (absolute pressure).
The present invention is particularly suitable for the internally heated coal carbonization process, and coking chamber coal carbonization section service temperature is 500～900 ℃ or is 550～800 ℃ or is 600～750 ℃ or is 600～700 ℃.
When the present invention is applied to blue charcoal and produces; Operational condition is generally: in coking chamber; Said coal charge is non-caking coal or weakly caking coal; The charcoal product is semicoke (being blue charcoal), and coal carbonization section service temperature is 550～850 ℃, and the long-pending flow rate of circulation heat-carrying gas is 150～450 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
When the present invention was applied to blue charcoal and produces, operational condition is generally: in coking chamber, coal carbonization section service temperature was 550～800 ℃, and the long-pending flow rate of circulation heat-carrying gas is 200～400 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
When the present invention was applied to blue charcoal and produces, operational condition preferably is: in coking chamber, coal carbonization section service temperature was 600～700 ℃, and the long-pending flow rate of circulation heat-carrying gas is 250～350 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
Internally heated retort oven gas-operated pressure of the present invention can be higher than normal pressure or far above normal pressure; At this moment; The present invention uses the reinforced material of coal charge lock system, withstand voltage gas retort, pressure combustion chamber, charcoal material to go out furnace charge lock system, dry cooling system usually, and facilities such as circulation heat-carrying gas sparger, gas fume of combustion chamber sparger also possibly arranged in coking chamber inside.
The used coal charge of coking chamber of the present invention is non-caking coal or weakly caking coal, and granularity is: 25～100mm or 10～40mm or 3～15mm or 1～5mm or 0.5～3mm.
The present invention is particularly suitable for the internally heated coal carbonization process, and solid blend composition C median size Φ C and the ratio Φ C/ Φ F of major ingredient coal F median size Φ F be generally 0.3～4.0, be generally 0.5～2.0, the preferably is 0.7～1.5.
The present invention is particularly suitable for the internally heated coal carbonization process, and the requirement of solid material particle diameter is generally:
Solid blend composition C median size Φ C and the ratio Φ C/ Φ F of major ingredient coal F median size Φ F are 0.3～4.0;
The ascending Φ C1～Φ C2 that is distributed as of solid blend composition C particle diameter, Φ C1/ Φ C2 >=0.15;
The ascending Φ F1～Φ F2 that is distributed as of major ingredient coal F particle diameter, Φ F1/ Φ F >=0.15.
The present invention is particularly suitable for the internally heated coal carbonization process, and the requirement of solid material particle diameter is generally:
Solid blend composition C median size Φ C and the ratio Φ C/ Φ F of major ingredient coal F median size Φ F are 0.5～2.0;
The ascending Φ C1～Φ C2 that is distributed as of solid blend composition C particle diameter, Φ C1/ Φ C2 >=0.3;
The ascending Φ F1～Φ F2 that is distributed as of major ingredient coal F particle diameter, Φ F1/ Φ F2 >=0.3.
The present invention is particularly suitable for the internally heated coal carbonization process, and the requirement of solid material particle diameter is preferably:
Solid blend composition C median size Φ C and the ratio Φ C/ Φ F of major ingredient coal F median size Φ F are 0.7～1.5;
The ascending Φ C1～Φ C2 that is distributed as of solid blend composition C particle diameter, Φ C1/ Φ C2 >=0.45;
The ascending Φ F1～Φ F2 that is distributed as of major ingredient coal F particle diameter, Φ F1/ Φ F2 >=0.45.
Range of application of the present invention comprises: external-heat dry distillation of coal process, dry distillation of coal process are for using coal charge angle of rake external-heat dry distillation of coal process or internally heated coal carbonization process, the internally heated coal carbonization process of gas-solid counter current contact, gas-solid cocurrent flow type dry distillation of coal process.
Roll-over V0 is provided with feed valve 01, discharge valve 02, breather valve 0K1, breather valve 0K2, breather valve 0K3 usually in the coal charge that the reinforced material of coal charge of the present invention lock system uses.Roll-over V0 coal expects that reaching when height expection stops to feed in raw material in the coal charge; Be normal gas-phase space more than the coal charge surface, be the solid phase space below the coal charge surface; The interface of breather valve 0K1, breather valve 0K2 is usually located at normal gas-phase space zone; The interface of feed valve 01 is usually located at normal gas-phase space top, and the interface of discharge valve 02 is usually located at bottom, solid phase space, is convenient to utilize gravity flowage.
The algorithm of roll-over V0 in the coal charge that the reinforced material of coal charge of the present invention lock system uses is below described:
1. the coal gas displacement step before the charging: accomplish that roll-over V0 contains inflammable gas (raw gas) in the coal charge of discharging step, steps of exhausting can be set create conditions for the air of displacement coal charge absorption.All be under the closing condition at discharge valve 02, feed valve 01, open breather valve 0K2 roll-over V0 in coal charge and feed indifferent gas (like CO
2Gas), punching press is closed breather valve 0K2 after accomplishing; Opening breather valve 0K1 then makes in the coal charge among the roll-over V0 gas get into the safety dumping point to accomplish the bleed step such as torch or gas holder, close breather valve 0K1 then; Above-mentioned steps can repeat repeatedly; Open feed valve 01 then and coal charge is discharged into or waits for reinforced, close charging valve 01 after addition step finishes, wait for the subsequent action instruction.
2. the air displacement step after the charging: accomplish that roll-over V0 contains the air compsn that coal charge is brought in the coal charge of addition step, the quantity that gas displacement step reduces the nitrogen of bringing gas retort into, argon gas, oxygen etc. can be set.All be under the closing condition at discharge valve 02, feed valve 01, open gas ventilation valve 0K2 roll-over V0 in coal charge and feed displacement gas (like CO
2Gas), punching press is closed breather valve 0K2 after accomplishing; Open breather valve 0K3 then, gaseous emission to securing point is accomplished displacement bleed step such as characteristics airborne release mouth, displacement step can be carried out repeatedly, reach requirement after, close gas ventilation valve 0K3, wait for the subsequent action instruction.
3. to coking chamber discharging step: roll-over V0 in the coal charge; Regularly close feed valve 01; Opening breather valve 0K2 makes displacement gas gas get into that roll-over V0 accomplishes the step of boosting in the coal charge; Open discharge valve 02 then coal charge is discharged into gas retort coking chamber L101 top, the discharging step is closed discharge valve 02 after finishing, is closed breather valve 0K2, waits for the subsequent action instruction.
In the course of normal operation, in any moment, valve 01 can not be in opening state simultaneously with valve 02.
Roll-over V0 operation index comprises material level, pressure, temperature etc. in the coal charge.
The charcoal material goes out furnace charge lock system, dry cooling system, and the publication number that sees also inventor's proposition is a kind of coal system coke installation dry coke quenching method of 201110086594.9.
When the present invention was applied to the fine coal destructive distillation, facilities such as circulation heat-carrying gas sparger, gas fume of combustion chamber sparger also possibly arranged in coking chamber inside.The structure formation of the two can be identical or different.
The circulation heat-carrying gas sparger of coking chamber internal layout; Be positioned at solid bed of material bottom; Can be arranged in charring furnace on vertical 1,2 of solid materials direct of travels or a plurality of gas distributions cross section, each arranges the parallel pipe that many parallel pipes or ring pipe or many subsidiary vertical gas distributionbranch pipes can be set on gas distribution cross section or the ring pipes of many subsidiary vertical gas distributionbranch pipes.Lay out pore on the above-mentioned gas distribution pipe, production well can be an any direction, but the recommendation outgassing direction of gas distribution pipe production well is vertical with the solid materials direct of travel or forward, the outgassing direction of not recommending is reverse with the solid materials direct of travel.
The circulation heat-carrying gas sparger of coking chamber internal layout; Can be arranged on 1,2 or a plurality of gas distributions cross section; Each arranges that the gas distribution pipe that is provided with on the gas distribution cross section constitutes 1,2 or a plurality of independent gas supplies unit usually, and each independent gas supply unit is provided with 1,2 or a plurality of circulation heat-carrying gas inlet mouth.
The present invention relates to the mixing process of fine coal material and coke breeze material, the powder mixier of use or mixing machine can be the equipment or the systems of any use.
Major advantage of the present invention is to have reduced the apparent vaporization rate of coal charge.
Claims (30)
1. the dry distillation of coal method that is raw material with major ingredient coal and auxiliary solid material mixture is characterized in that: will mix back gained solid mixture HL as dry distillation of coal process raw material with major ingredient coal F granularity, approaching low vaporization rate solid blend composition C and the major ingredient coal F of density altitude.
2. method according to claim 1 is characterized in that:
To mix back gained solid mixture HL as dry distillation of coal process raw material as solid blend composition C and major ingredient coal F with the approaching coke of major ingredient coal F granularity height, solid blend composition C weight content is 0.1～0.9 among the raw material HL; Dry distillation of coal process is the internally heated coal carbonization process.
3. method according to claim 2 is characterized in that:
Dry distillation of coal process is the internally heated coal carbonization process, comprises charring furnace and coking chamber heat-carrying component internal circulation system, and charring furnace comprises the coking chamber of coal and the fuel gas combustion chamber that possibly exist; In coking chamber, according to the advance route of coal charge, being divided into first section is that coal preheating section (or claim gas cooling section), second section are that coal carbonization section, the 3rd section are charcoal cooling section (or claiming gas preheating section); In the 3rd section zone, the first via gas and the two sections process material contact heat-exchangings that comprise coking chamber heat-carrying component reclaim and become three sections process gas after its heats heat up, and three sections process material leave three sections zones; In second section zone; The gas fume of combustion chamber of three sections process gas and existence; Carry out gas-solid with one section process material and directly contact the charing effect that takes place, two sections process material leave second section zone and get into the 3rd section zone, and two sections process gas leave second section zone and get into first section zone; In first section zone, after transmitting the heat cooling and sneak into one section generation gas with the outside certainly coal charge Contact Heating coal charge that adds, two sections process gas become one section product gas (raw gas), and become one section process material after coal charge heats up and get into second section zone; Raw gas is discharged charring furnace; Charcoal product ZCT discharges charring furnace; In raw gas refrigerated separation part, the raw gas that charring furnace is discharged in cooling and separation obtains from ring coal gas, coal tar, contains tar sewage; At least a portion is returned coking chamber as coking chamber heat-carrying component based on the gas stream of raw gas, constitutes destructive distillation part coking chamber heat-carrying component internal recycle;
Self-produced charcoal product ZCT is mixed the back as dry distillation of coal process raw material HL as solid blend composition C and major ingredient coal F.
4. method according to claim 2 is characterized in that:
Solid blend composition C weight content is 0.2～0.8 among the raw material HL.
5. method according to claim 2 is characterized in that:
Solid blend composition C weight content is 0.3～0.7 among the raw material HL.
6. according to claim 2 or 3 or 4 or 5 described methods, it is characterized in that:
Gas phase operation pressure P V is greater than 0.20MPa (absolute pressure) in the charring furnace.
7. according to claim 2 or 3 or 4 or 5 described methods, it is characterized in that:
Gas phase operation pressure P V is 0.40～3.0MPa (absolute pressure) in the charring furnace.
8. according to claim 2 or 3 or 4 or 5 described methods, it is characterized in that:
Coking chamber coal carbonization section service temperature is 500～900 ℃.
9. method according to claim 8 is characterized in that:
Coking chamber coal carbonization section service temperature is 550～800 ℃.
10. method according to claim 8 is characterized in that:
Coking chamber coal carbonization section service temperature is 600～750 ℃.
11. method according to claim 8 is characterized in that:
Coking chamber coal carbonization section service temperature is 600～700 ℃.
12., it is characterized in that according to claim 2 or 3 or 4 or 5 described methods:
In coking chamber, said coal charge is non-caking coal or weakly caking coal, and the charcoal product is semicoke (being blue charcoal), and coal carbonization section service temperature is 550～850 ℃, and the long-pending flow rate of circulation heat-carrying gas is 150～450 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
13. method according to claim 12 is characterized in that:
In coking chamber, coal carbonization section service temperature is 550～800 ℃, and the long-pending flow rate of circulation heat-carrying gas is 200～400 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
14. method according to claim 13 is characterized in that:
In coking chamber, coal carbonization section service temperature is 600～700 ℃, and the long-pending flow rate of circulation heat-carrying gas is 250～350 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
15., it is characterized in that according to claim 2 or 3 or 4 or 5 described methods:
Use the reinforced material of coal charge lock system, withstand voltage gas retort, pressure combustion chamber, charcoal material to go out furnace charge lock system, dry cooling system.
16., it is characterized in that according to claim 2 or 3 or 4 or 5 described methods:
In coking chamber, said coal charge is non-caking coal or weakly caking coal, and granularity is 25～100mm.
17. method according to claim 16 is characterized in that:
In coking chamber, said coal charge granularity is 10～40mm.
18. method according to claim 16 is characterized in that:
In coking chamber, said coal charge granularity is 3～15mm.
19. method according to claim 16 is characterized in that:
In coking chamber, said coal charge granularity is 1～5mm.
20. method according to claim 16 is characterized in that:
In coking chamber, said coal charge granularity is 0.5～3mm.
21. according to claim 1 or 2 or 3 or 4 or 5 described methods, it is characterized in that: solid blend composition C median size Φ C and the ratio Φ C/ Φ F of major ingredient coal F median size Φ F are 0.3～4.0.
22. according to claim 1 or 2 or 3 or 4 or 5 described methods, it is characterized in that: solid blend composition C median size Φ C and the ratio Φ C/ Φ F of major ingredient coal F median size Φ F are 0.5～2.0.
23. according to claim 1 or 2 or 3 or 4 or 5 described methods, it is characterized in that: solid blend composition C median size Φ C and the ratio Φ C/ Φ F of major ingredient coal F median size Φ F are 0.7～1.5.
24., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 described methods:
Solid blend composition C median size Φ C and the ratio Φ C/ Φ F of major ingredient coal F median size Φ F are 0.3～4.0;
The ascending Φ C1～Φ C2 that is distributed as of solid blend composition C particle diameter, Φ C1/ Φ C2 >=0.15;
The ascending Φ F1～Φ F2 that is distributed as of major ingredient coal F particle diameter, Φ F1/ Φ F >=0.15.
25., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 described methods:
Solid blend composition C median size Φ C and the ratio Φ C/ Φ F of major ingredient coal F median size Φ F are 0.5～2.0;
The ascending Φ C1～Φ C2 that is distributed as of solid blend composition C particle diameter, Φ C1/ Φ C2 >=0.3;
The ascending Φ F1～Φ F2 that is distributed as of major ingredient coal F particle diameter, Φ F1/ Φ F2 >=0.3.
26., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 described methods:
Solid blend composition C median size Φ C and the ratio Φ C/ Φ F of major ingredient coal F median size Φ F are 0.7～1.5;
The ascending Φ C1～Φ C2 that is distributed as of solid blend composition C particle diameter, Φ C1/ Φ C2 >=0.45;
The ascending Φ F1～Φ F2 that is distributed as of major ingredient coal F particle diameter, Φ F1/ Φ F2 >=0.45.
27. method according to claim 1 is characterized in that:
Dry distillation of coal process is an external-heat dry distillation of coal process.
28. method according to claim 1 is characterized in that:
Dry distillation of coal process is for using coal charge angle of rake external-heat dry distillation of coal process or internally heated coal carbonization process.
29. method according to claim 1 is characterized in that:
Dry distillation of coal process is the internally heated coal carbonization process of gas-solid counter current contact.
30. method according to claim 1 is characterized in that:
Dry distillation of coal process is a gas-solid cocurrent flow type dry distillation of coal process.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104807030A (en) * | 2015-04-14 | 2015-07-29 | 西安热工研究院有限公司 | Method for reducing fine particles of coal burning boiler |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104807030A (en) * | 2015-04-14 | 2015-07-29 | 西安热工研究院有限公司 | Method for reducing fine particles of coal burning boiler |
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