CN101395249A - Process for production of coke and process for production of pig iron - Google Patents
Process for production of coke and process for production of pig iron Download PDFInfo
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- CN101395249A CN101395249A CNA2007800077232A CN200780007723A CN101395249A CN 101395249 A CN101395249 A CN 101395249A CN A2007800077232 A CNA2007800077232 A CN A2007800077232A CN 200780007723 A CN200780007723 A CN 200780007723A CN 101395249 A CN101395249 A CN 101395249A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B5/00—Making pig-iron in the blast furnace
- C21B5/007—Conditions of the cokes or characterised by the cokes used
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Abstract
The invention provides a process for the production of coke which brings about an improvement in the strength of coke or which permits simplification of the humidity control step substantially without lowering the strength of coke; and a process for the production of pig iron by using the coke obtained by the process, more specifically, a process for the production of coke by loading coal into the carbonization chamber of a coke oven and carbonizing the coal which is characterized in that the coal to be loaded into the carbonization chamber is a mixture of 100 parts by mass of coal for coke making with at most one part by mass of substantially ash-free coal; and a process for the production of pig iron which is characterized by using a coke obtained by the above process for the production of coke.
Description
Technical field
The present invention relates to the manufacturing technology of coke and utilize the manufacturing technology of the pig iron of this technology, in more detail, relate to the manufacturing technology of the coke of intensity raising, or the intensity of the coke that obtains is reduced, can simplify the moisture control operation coke manufacturing technology and utilize the manufacturing technology of its pig iron.
Background technology
In the manufacturing of coke, in order to improve the intensity of the coke that obtains, the known tamped density that the coal charge that improves the carbonization chamber of packing into is arranged.In order to improve the tamped density of coal charge, and the humidity of regulating feed coal reduces moisture content, perhaps when packing coal charge in the carbonization chamber, carries out the operation that compresses of machinery.But at the manufacturing scene of coke, feed coal is carried with travelling belt usually, the moisture content of feed coal is reduced to is less than about at 7% o'clock, and the powder of coal becomes and disperses easily, is not preferred on environment therefore.On the other hand, carry out the operation that compresses of machinery when packing coal charge in the carbonization chamber, it is complicated that its operation also becomes.
For example, open in the flat 9-31469 communique the spy, a kind of coke oven loading coal treatment process is before disclosed, its purpose is really and to stablize the intensity that improves coke, it is characterized in that, moisture-free coal is separated into meal smalls and fine powder smalls, after interpolation heavy oil 5～40% and water generate water slurry in the fine powder smalls, by wet type granulation granulation is the prilled coal that has above the particle diameter of separation point, then implements processed and mixes with the meal smalls.In addition, open in the 2003-226879 communique, disclose a kind of method, when making metallurgical coke,, pack into the coke oven of the strong caking coal of optimal size-grade distribution state adjustment, caking coal, non-little caking coal etc. and to use coal in order to obtain high bulk density the spy.
Also in No. 3566834 communique of patent, a kind of manufacture method of coke is disclosed, its purpose is to propose a kind of inexpensive method that is used to reduce the manufacturing cost of blast furnace coke and makes high-intensity coke, in this feed coal, add to contain and have more than the 80wt% than the tar last running of the composition of the above boiling point of low 50 ℃ of the softening beginning temperature of feed coal and the high strength coke is made in destructive distillation.In addition, open the manufacture method that discloses a kind of coke in the flat 3-7796 communique the spy, it is characterized in that, the manufacture method of the coke that all improves as intensity and productivity, pulverize coal blending, destructive distillation mixing coal charge in coke oven and make coke, wherein, refinement coal blending granularity cooperates interfacial agent and makes coke in coal blending.
Summary of the invention
As mentioned above, improve method, the micro mist of coal is dispersed, therefore have to be difficult to that moisture content is reduced and to be less than about 7% restriction to the tamped density of carbonization chamber because reduce the moisture content of employed feed coal.On the other hand, when packing coal charge in the carbonization chamber, if carry out the operation that compresses of machinery, it is complicated that operation also just becomes.
In view of the foregoing, the object of the present invention is to provide the coke manufacture method that improves the coke strenth that obtains, or do not make the intensity of the coke that obtains reduce method that can simplify the moisture control operation and the manufacture method of utilizing the pig iron that obtains by this method in fact.
The so-called coke manufacture method of the present invention that can solve above-mentioned problem, be coal to be packed into carry out the manufacture method of pyrogenous coke in the carbonizing chamber of coke oven, wherein, as coal charge, use is added the coal that does not contain ash content below 1 mass parts in fact with respect to feed coal 100 mass parts.Promptly, purport of the present invention is, if using with respect to feed coal 100 mass parts as coal charge, discovery adds the coal that does not contain ash below 1 mass parts in fact, the intensity of the coke that then obtains improves this point, also have the intensity of utilizing the coke that obtains to improve, simplify and bring on manufacturing process's this point of influence to coke strenth.For example, above-mentioned coal charge and the intensity of regulating the coke that the coal do not contain ash content in fact obtains for the humidity of not having the feed coal that adds and to its destructive distillation are roughly the same degree, therefore, can simplify and regulate the humidity operation and make coke.
As the coal that does not contain ash content in fact, preferred to use from carbon containing ratio (d.a.f.) be more than 60% but be lower than the solvable composition that obtains with organic solvent extraction 95% the coal.In addition, be preferably as above-mentioned organic solvent that can to enumerate with 2 cyclic aromatic series compounds be the organic solvent of main component.In the present invention, contain the coke that obtains with the manufacture method of using according to above-mentioned coke manufacture method as the pig iron of feature.
Also have, " coal " generally is classified as hard coal, heavy caking coal, caking coal, weakly caking coal, noncaking coal, brown coal, mud coal etc., and its definition is not necessarily clear and definite.The part of caking coal also has the situation that is called the coal of adhering.Therefore, in the present invention, with carbon containing ratio (d.a.f.) classification, carbon containing ratio (d.a.f.) is a hard coal above 91% coal with hard coal, heavy caking coal, caking coal, weakly caking coal, noncaking coal etc.; Carbon containing ratio (d.a.f.) is being a heavy caking coal more than 85% but at the coal below 91%; Carbon containing ratio (d.a.f.) is more than 83% but to be lower than 85% coal be caking coal; Carbon containing ratio (d.a.f.) is more than 80% but to be lower than 83% coal be weak caking coal; Carbon containing ratio (d.a.f.) is more than 78% but to be lower than 80% coal be noncaking coal; Carbon containing ratio (d.a.f.) is more than 70% but to be lower than 78% coal be brown coal; Being lower than 70% coal with carbon containing ratio (d.a.f.) is mud coal.At this, carbon containing ratio (d.a.f=dry ash free) is the containing ratio (quality %) except that the carbon of the moisture of coal and the organic substance the ash content (C, H, O, S, N), can be that standard is measured with JIS M8819.Below, sometimes with carbon containing ratio (d.a.f.) more than 85% but abbreviate " heavy caking coal " as at the coal below 91%, with carbon containing ratio (d.a.f.) more than 60% but abbreviate " noncaking coal " as at the coal below 85%.
According to coke manufacture method of the present invention, can obtain the coke that intensity improves.In addition, in the undiminished in fact scope of the intensity of the coke that obtains, can simplify the damping operation.
The coke that manufacture method by coke of the present invention obtains can be used in the manufacturing of the pig iron of blast furnace well.
Description of drawings
Fig. 1 is the device of the manufacturing ashless coal that uses in the present invention and the explanatory view of exemplary process.
Embodiment
The manufacture method of coke of the present invention is packed coal into and is carried out destructive distillation in the carbonizing chamber of coke oven, as coal charge, wherein, as coal charge, uses with respect to feed coal 100 mass parts, adds the following coal that does not contain ash content in fact of 1 mass parts.
(1) about ashless coal
At first, the coal that does not contain ash content in fact that uses in the present invention (below, the situation that is called " ashless coal " is arranged) is illustrated.Above-mentioned ashless coal can be the coal that does not contain ash in fact, also can contain micro-ash content.The containing ratio of ash content at this moment is preferably below the 5000ppm, more preferably below the 2000ppm.Also have, ash content is to the coal heating and the residual inorganics during ashing for example, is made of silicic acid, aluminum oxide, ferric oxide, lime, magnesium oxide, basic metal etc. at 815 ℃.
In the present invention, as above-mentioned ashless coal, preferred to use from carbon containing ratio (d.a.f.) be more than 60% but the solvable composition that obtains with organic solvent extraction be lower than 95% coal of (more preferably more than 60% but be lower than 85%).The mode that non-adhesive carbon etc. is effectively utilized as original raw material is because be the mode of not using exhausted may the raw material unit price high strong cohesive property carbon, so be preferred mode.In preferred mode, as to use carbon containing ratio (d.a.f.) with the coal of organic solvent extraction be 70% or more but be lower than 83% weak caking coal, noncaking coal, reach brown coal, or these mixture.
Specifically, above-mentioned ashless coal is following to be obtained: carbon containing ratio (d.a.f.) is more than 60% but is lower than 95% (more preferably more than 60%, but be lower than 85%) coal and organic solvent mix and be modulated into slurry, heat above-mentioned slurry maturation and from above-mentioned organic solvent, extract solvable composition, with the pulp separation that obtains is the clarification partially liq and the spissated concentrated solution of solid phase composition on top, filter the clarified liq evaporation of above-mentioned top and remove organic solvent, obtain ashless coal thus.Fig. 1 is an explanatory view of making anthracitic device and exemplary process.In box container 1, be more than 60% with carbon containing ratio (d.a.f.) but be lower than 95% coal and organic solvent and mix, generate slurry.The slurry that obtains is extracted the extraction tank 4 of processing by pump 2 supplies.At this moment, slurry is warmed to the temperature of regulation by preheater 3.After in extraction tank 4, stirring slurries solvable composition extracted in organic solvent, with the slurry supply gravity settling tank 5 that obtains with stirrer 10.In gravity settling tank 5, carry out gravity settling and make solid phase composition sedimentation (arrow 11), make pulp separation become the clarification partially liq and the spissated liquid of solid phase composition on top.The clarifying liquid in the top that obtains is supplied to filter unit 8, and in gravity settling tank 5, settled solid phase composition concentrated solution is recovered in the solid phase composition concentrated solution collector 6.The filter member 7 that the clarifying liquid in top is filtered device unit 8 filters, and the filtrate that obtains is recycled in the clarifying liquid accommodating device 9 in top that reclaims the clarifying liquid in top.Then, remove organic solvent by evaporation from the clarified liq of above-mentioned top and can access ashless coal.As the method that organic solvent is removed in evaporation from the clarified liq of top, for example can use general drying meanss such as spray-drying process, distillation method, boulton process.
Coal concentration is that 10～35 quality % are fit in the above-mentioned slurry, and the condition as the above-mentioned slurry of thermal ripening makes solvable composition extract in organic solvent for example kept above-mentioned slurry 5～120 minutes at 300 ℃～420 ℃, and the solvable composition in the coal can be dissolved.This is because than 300 ℃ of low temperature, and is insufficient for the intermolecular bonded reduction that constitutes coal, the ratio reduction of the solvable composition that can extract from coal.On the other hand, than 420 ℃ of high temperature, the thermal response of coal comes to life, and the combination again of the thermolysis base that generates takes place, and therefore the ratio of the solvable composition that is extracted reduces.On the other hand, 300～420 ℃ temperature, the intermolecular combination that constitutes coal is slowed down, and gentle thermolysis takes place, and the ratio of the solvable composition that extracts from coal uprises.At this moment, the thermolysis of the gentleness by coal, main mean boiling point (Tb50:50% distillation temperature) is that the abundant composition of 200～300 ℃ aromatic series generates, and can effectively utilize as the part of organic solvent.
Resulting slurry is that the temperature of the clarification partially liq on top and solid phase composition concentrated solution is preferably more than 300 ℃ but below 420 ℃ by gravity settling separation.When being lower than 300 ℃, a part that is dissolved in the composition in the liquid composition is separated out, and the situation of the yield rate reduction of ashless coal is arranged.
As above-mentioned organic solvent, preferably high solvent to the solvability of coal, preferably 2 cyclic aromatic series compounds with the structural unit that is similar to coal are the organic solvent of main component.In addition, as above-mentioned organic solvent, its boiling point is 180 ℃～330 ℃ and is fit to.When boiling point is lower than 180 ℃, the situation of the Recovery of Organic Solvent rate reduction that evaporation is removed from the clarified liq of top is arranged.On the other hand, when boiling point surpasses 330 ℃, coal and organic solvent separation difficulty, the situation that the Recovery of Organic Solvent rate reduces.As the object lesson of above-mentioned 2 cyclic aromatic series compounds, can enumerate the naphthalene class of the aliphatic lateral chain of for example have naphthalene (boiling point: 218 ℃), methylnaphthalene (boiling point: 241～242 ℃), methylnaphthalene isomer (boiling point: 261～272 ℃), front three naphthalene (ト リ メ チ Le Na Off レ Application) etc.; Biphenyl; The substituent biphenyl class of aliphatic lateral chain or aromatic series, or these mixture etc.
The carbon containing ratio (d.a.f.) that uses as being used to make the original raw material of ashless coal is more than 60% but is lower than 95% coal (noncaking coal), and for example preferred the use has following characteristic.The volatile component of above-mentioned noncaking coal etc. is preferably more than 30%, more preferably more than 32%, is preferably below 40%, more preferably below 36%.The average reflectance of above-mentioned noncaking coal is preferably more than 0.6, more preferably more than 0.8, is preferably below 1.0, more preferably below 0.9.The overall inertia of above-mentioned noncaking coal is preferably more than 5%, more preferably more than 15%, is preferably below 35%, more preferably below 20%.The high fluidity (logMFD) of the slurries of above-mentioned noncaking coal etc. is preferably more than 3.0 (logddpm), more preferably more than 3.3 (logddpm), is preferably below 4.5 (logddpm), more preferably below 3.6 (logddpm).Volatile component is measured according to the method stipulated among the JIS M8812, and average reflectance is measured according to the method for stipulating among the JIS M8816, and the high fluidity (logMFD) of slurries can be measured by the slurries plastometer method of stipulating among the JIS M8801.In addition, overall inertia (TI) uses the coal of JIS M8816 to maintain in the analytical value of structural constituent (maceral), and semifusinite (can obtain according to following formula by the ratio of semi-fusinite) and micro organization become the to hive off ratio of (maceral/colony).
[several 1]
The overall positive inert component/100+MM of inertia (TI)=(100-MM) × Fill
The positive inert component of Fill=inert component %-semifusinite % * 1/3
In the formula, the meaning of MM (ミ ネ ラ Le マ -) is a mineral substance, and the meaning of A is that the meaning of ash content (measuring with anhydrous JIS M8812), S is whole sulphur compositions (measuring with anhydrous JIS M8813).
(2) about feed coal
Then, the feed coal that uses in the present invention is illustrated.In the present invention,, use, add below 1 mass parts with respect to feed coal 100 mass parts as coal charge, more preferably below 0.7 mass parts, the following above-mentioned ashless coal of 0.5 mass parts more preferably.Lower limit as the content of ashless coal is not done special the qualification, but is preferably more than 0.2 mass parts.
Because ashless coal contains more than 0.2 mass parts, the intensity that confirms resulting coke has great raising in fact.When particularly the content of ashless coal was 0.5 mass parts, the intensity of the coke that obtains had maximum value.On the other hand, the content of ashless coal surpasses 0.5 mass parts but when 1 mass parts is following, compares the excellent strength of coke when not adding ashless coal, but along with the content of ashless coal increases, and the intensity of the intensity of resulting coke when not adding ashless coal is approaching.And, when surpassing 1 mass parts, to compare when not adding ashless coal, the intensity of coke reduces on the contrary.
As the above-mentioned raw materials coal, for example can use the coal of for example single kind and kind or cooperate the coal of a plurality of kinds and kind, the preferred mixed coal that cooperates a plurality of kinds and kind that uses.In addition, according to the kind and the kind of coal, therefore the granularity difference to the coal of pulverizer carrying coal yard, is preferably pulverized with the particle diameter of regulation.
As above-mentioned mixed coal, preference such as carbon containing ratio (d.a.f.) are more than 85% but are lower than 91% coal and carbon containing ratio (d.a.f.) is more than 60% but is lower than the mixed coal of 85% coal.Be more than 60% as above-mentioned carbon containing ratio (d.a.f.) but be lower than 85% coal and for example can enumerate as preferred that carbon containing ratio (d.a.f.) is more than 78% but is lower than 83% weak caking coal, noncaking coal or these mixture.As carbon containing ratio (d.a.f.) is more than 85% but at the coal below 91% and carbon containing ratio (d.a.f.) to be more than 60% but to be lower than the combination of 85% coal, the mode that can enumerate the mode that for example is made of heavy caking coal and weak caking coal, be made of heavy caking coal and noncaking coal, the mode that is made of heavy caking coal and weak caking coal and noncaking coal.
Above-mentioned carbon containing ratio (d.a.f.) in the mixed coal is more than 85% but cooperates in order to improve resulting coke strenth at the coal below 91% (heavy caking coal), its use level is with mixed coal integral body during as 100 mass parts, be preferably more than 10 mass parts, more preferably more than 40 mass parts.When the use level of heavy caking coal is lower than 10 mass parts,,, the situation of the intensity of the coke that can not get wishing is arranged also even therefore add the following ashless coal of 1 mass parts with respect to mixed coal 100 mass parts because the cohesiveness composition is very few.On the other hand, there is no particular limitation for the upper limit of the use level of heavy caking coal, is preferably 100 mass parts, more preferably 90 mass parts, more preferably 60 mass parts.This is because if the use level of heavy caking coal becomes too much, the raw materials cost when then coke is made rises.On the other hand, carbon containing ratio (d.a.f.) is more than 60% but is lower than 85% coal (noncaking coal etc.) and is preferably total use level with heavy caking coal and becomes 100 mass parts and be engaged like this.
In the present invention, cooperate heavy caking coal and noncaking coal and the mixed coal that obtains, preferably have following characteristic.The volatile component of above-mentioned mixed coal is preferably more than 15%, more preferably more than 26%, is preferably below 35%, more preferably below 29%.The average reflectance of above-mentioned mixed coal is preferably more than 0.65, more preferably more than 1.00, is preferably below 1.60, more preferably below 1.10.The overall inertia of above-mentioned mixed coal is preferably more than 15%, more preferably more than 20%, is preferably below 35%, more preferably below 23%.The high fluidity (logMFD) of the slurries of above-mentioned mixed coal is preferably more than 0.7 (logddpm), more preferably more than 2.0 (logddpm), is preferably below 3.5 (logddpm), more preferably below 2.3 (logddpm).The granularity of above-mentioned mixed coal constitutes, and what 3mm was following preferably is more than 50%, more preferably more than 75%, is preferably below 90%, more preferably below 85%.Above-mentioned each characteristic numerical range widely is the scope that is fit to that the raw material as blast furnace coke can use, and is formed in the narrower numerical range by making above-mentioned each characteristic, can access the coke of the no problem degree of intensity in fact.
(3) manufacturing process of relevant coke
The manufacture method of coke of the present invention is, adds above-mentioned ashless coal below 1 mass parts as coal charge with respect to 100 mass parts, will carry out destructive distillation in its carbonizing chamber of coke oven of packing into.
Generally, in the manufacturing of coke, regulate feed coal humidity as coal charge and use the coal charge of having regulated amount of moisture.If the moisture content of coal charge is too much, then the heat of the surplus of necessity is not only bad economically during destructive distillation, also becomes the reason of mass deviation.According to the present invention, by in feed coal, adding ashless coal, just improved the intensity of resulting coke, therefore can change in such a way the intensity of the coke that obtains is brought the moisture control operation of influence.
As coal charge, use the above-mentioned coal charge that is conditioned humidity.That is,, the feed coal that does not add ashless coal is carried out regulating the coal charge of humidity and the intensity of the coke that obtains is compared with degree with using, can access the coke that intensity improves if use the above-mentioned coal charge that is conditioned humidity as coal charge.
For example, even the feed coal of moisture content damping to 7%～9%, also improve by the intensity of adding the coke that the above-mentioned raw materials coal obtains, can access with the destructive distillation moisture content is the coke of the roughly the same intensity of coke that obtains of about 5%～7% feed coal (no coal blending does not have interpolation).As mentioned above, when using amount of moisture for about 5%～7% material carbon, can produce the problem of dispersing of the micro mist of coal, according to the present invention, by using amount of moisture is about 7%～9% feed coal, can access the coke that obtains for about 5%～7% feed coal with the destructive distillation moisture content coke of equality strength in fact.
Even moisture content is than higher 7%～9% feed coal, by adding above-mentioned ashless coal, can access the roughly identical coke of intensity of the coke that obtains for about 5%～7% feed coal with the destructive distillation moisture content, therefore needn't specially adjust the moisture content (7～9%) of feed coal.In addition, also can alleviate the degree of adjusting humidity.The damping operation is because remove moisture by heat energy, so omitted the damping operation in fact, this is extremely beneficial economically manufacture method.
In the present invention, add the following ashless coal of 1 mass parts, in carbonizing chamber of coke oven, pack into coal charge and destructive distillation with respect to feed coal 100 mass parts.Tamped density when packing above-mentioned coal in the carbonization chamber is not specially limited, and for example is preferably 600kg/m
3More than, 650kg/m more preferably
3More than, be preferably 1000kg/m
3Below, 850kg/m more preferably
3Below.This is because tamped density is for being lower than 600kg/m
3The time, because the weight of coal self, the space of powder layer is filled, and is difficult to be lower than this value in fact, tamped density surpasses 1000kg/m
3The time, be difficult in this in fact and fill up more than the value and compress the bisque space.
Moreover, the tamped density of coal charge do not carry out machinery to compress when operation also relevant with above-mentioned moisture content, generally, use the low coal charge of moisture content more, can improve tamped density more to the carbonization chamber, the tamped density of the carbonizing chamber of coke oven when for example, using the coal of moisture content about 7% is about 720kg/m usually
3
The condition of the above-mentioned coal charge of destructive distillation is not limited especially, can adopt the common destructive distillation condition in the manufacturing of the coke that uses coke oven, for example be preferably more than 950 ℃, more preferably more than 1000 ℃, below 1200 ℃, the temperature below 1050 ℃ more preferably, destructive distillation is more than 8 hours, more preferably more than 10 hours, be preferably below 24 hours, more preferably below 20 hours.
(4) manufacture method of the pig iron
In the present invention, comprise the manufacture method of the pig iron, it is characterized in that, use manufacture method to obtain coke by coke of the present invention.By coke excellence on intensity that manufacture method of the present invention obtains, therefore can be used in the manufacturing of the pig iron well.That is, if use the coke that obtains by manufacture method of the present invention, gas ventilation raising when in blast furnace, making the pig iron.In addition, to omit the damping operation or, to obtain the cheap coke of price comparison to reduce the mode of damping degree.Also have, the manufacture method of the pig iron in the blast furnace can adopt known method, can enumerate for example to make iron ore and coke separately with the stratiform interaction cascading in blast furnace, is blown into hot blast from bottom house, is blown into the method for dust coal as required.
Embodiment
Below, describing the present invention in detail by embodiment, the present invention also can't help following embodiment and limits, and change, embodiment all are included in whole scopes of the present invention in the scope that does not break away from purport of the present invention.
Shown in table 1 and table 2, in mixed coal, add ashless coal and modulate coal charge.As ashless coal, use from Australia and produce the solvable composition (ash content 600ppm) that extracts with the 1-methylnaphthalene the caking coal (carbon containing ratio (d.a.f.) is 84%).Also having ashless coal is to modulate by following method with the device of Fig. 1.In box container 1, mix Australia and produce caking coal (carbon containing ratio (d.a.f.) is 84%) and 1-methylnaphthalene (Australia's product caking coal: furnishing slurry 1-methylnaphthalene=20 quality %:80 quality %).With preheater 3 slurry that obtains is warmed to 370 ℃, produces from Australia at extraction tank 4 and extract solvable composition the caking coal.With the flow is that 15kg/h supplies with the slurry that extracts after handling in gravity settling tank 5, carry out gravity settling, be separated into top clear liquor and solid phase composition concentrated solution, flow with 3kg/h supplies with the clarifying liquid in top to filter unit 8, discharges solid phase composition concentrated solution from the bottom of gravity settling tank 5 to solid phase composition concentrated solution collector 6 with the flow of 12kg/h.The clarifying liquid in top is recovered in the clarifying liquid accommodating device 9 in top after being filtered 8 filtrations of device unit, removes organic solvent by spray method evaporation from reclaim liquid, obtains ashless coal (ash content 600ppm).
In the can container of the size of wide 378mm * long 121mm height * 114mm, fill above-mentioned coal charge with desirable tamped density.4 these can container are put into the retort bottle of steel side by side, above-mentioned retort bottle is put into and can be carried out destructive distillation to coal charge at cross direction to the sandwich heating formula electric furnace that this can container heats.1000 ℃ of destructive distillation of carrying out 10 hours, subsequently, from electric furnace, take out retort bottle, carry out about 16 hours naturally cooling.
From the refrigerative retort bottle, take out 4 can container, cut out and be equivalent to half the coke of 189mm part of cross direction.Carrying out when sandwich heating, be called the charcoal core in the position of cross direction central authorities, the coke from hot face is fired to the charcoal core begins to be called head, body, tail from the position near hot face, since the heat-up rate difference the during heating of head, body, tail and on intensity generation poor, this is known.For this reason, be equivalent to half the coke of 189mm part of cross direction, be cut into and be roughly rectangular parallelepiped (on one side: about 20mm ± 1mm) obtains regular coke from each position that the 60mm that is equivalent to head, body, portion is cut apart.With the coke of clean this rule grain of distilled water, remove the micro mist of the coke that (during cutting) adheres to when granulating, with 150 ℃ ± 2 ℃ drying machine drying.
With the strength detection sample that obtains, measure I type intensity.As the device that uses in the strength trial of I type, the container cylindraceous (the bottom surface diameter 132mm of long 720mm, tube) that uses the SUS material to make, in this container, put into above-mentioned sample 200g,, apply the impact of the generation that rotatablely moves that adds up to 600 times with 1 minute 20 times speed of rotation rotations 30 minutes.The position of the 360mm that rotates to be at the middle part of the length 720mm that is equivalent to cylinder of this cylinder is provided with turning axle, is that the center makes the cylinder rotation with this turning axle, and drawing diameter with the bottom surface of cylinder is that the mode of the circle of 720mm is carried out.After the impact that 600 times the rotation that applies regulation brings, from this container cylindraceous, take out sample, the quality on the sieve distinguishing assay sieve of the screen cloth of usefulness 9.5mm.At this moment, adhere on the sieve also as the quality determination on the sieve.I type intensity index is calculated as follows, demonstrates the result who calculates in table 1 and table 2.
I type intensity index I
600 9.5=100 * 9.5mm sieve (unit: g)/200g that improves quality
Also have, the spin intensity of general coke is divided into the STRENGTH ON COKE piece and estimates as the volumetric fracture of rock of big block splitting and the surface breakdown that surface abrasion causes is estimated, the I type intensity index I that uses among the present invention
600 9.5Be interpreted as being used to estimate surperficial destructive index.
[table 1]
Cooperate: mass parts, mixed coal: be charcoal containing ratio (d.a.f) in the bracket
As can be known from the results of Table 1, o.1 when No.7 compares, find that the intensity of resulting coke improves by adding the following ashless coal of 1 mass parts with respect to mixed coal 100 mass parts from char N.When particularly adding 0.5 mass parts ashless coal with respect to mixed coal 100 mass parts, the intensity of resulting coke becomes maximum.In addition, from char N o.6 to the result of No.7 as can be known, when the addition of ashless coal surpassed 1 mass parts with respect to mixed coal 100 mass parts, the intensity of coke reduced on the contrary.
[table 2]
Cooperate: mass parts, mixed coal: be charcoal containing ratio (d.a.f) in the bracket
As can be known from the results of Table 2, use to add the coal charge of the ashless coal of 0.5 mass parts, with the coal charge tamped density be adjusted into 720,740kg/m
3Raw material and the intensity of the coke that obtains (char N o.8,9) respectively with the coal charge that uses the situation of not adding ashless coal, with the coal charge tamped density be adjusted into 745,760kg/m
3And the intensity of the coke that obtains (char N o.10,11) equates.In addition, situation of not adding ashless coal and the situation of adding 0.5 mass parts ashless coal are compared, find to use the coal charge that adds 0.5 mass parts ashless coal and the coke strenth height that obtains.
From these results, if use the coal charge that is adjusted humidity, compare with the intensity of using the coke that obtains with the feed coal that does not add ashless coal of degree adjustment humidity as coal charge, confirm and can obtain the coke that intensity improves.In addition, if make to have with using ashless coal is carried out coke strenth that common moisture control obtains roughly with the coke of the intensity of degree for the feed coal that not have interpolation, then, can use the coal charge that does not carry out moisture control in fact or alleviate the moisture control degree as coal charge.
Industrial practicality
The present invention can be applicable to the manufacturing of coke and the manufacturing of the pig iron well.
Claims (5)
1, a kind of manufacture method of coke is packed coal into and is carried out destructive distillation in the carbonizing chamber of coke oven, it is characterized in that,
Use is added with respect to feed coal 100 mass parts and is not contained the coal of ash content in fact as coal charge below 1 mass parts.
2, the manufacture method of coke according to claim 1 is characterized in that, uses the coal charge that does not carry out moisture control or the reduction of moisture control degree in fact as above-mentioned coal charge.
3, the manufacture method of coke according to claim 1 and 2, it is characterized in that, as the above-mentioned coal that does not contain ash content in fact, to use from carbon containing ratio (d.a.f.) be more than 60% but be lower than the solvable composition that obtains with organic solvent extraction 95% the coal.
4, the manufacture method of coke according to claim 3 is characterized in that, above-mentioned organic solvent is for being the organic solvent of principal constituent with 2 cyclic aromatic series compounds.
5, a kind of manufacture method of the pig iron is characterized in that, the coke that uses the manufacture method by each described coke in the claim 1～4 to obtain.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201410443055.XA CN104277856B (en) | 2006-03-15 | 2007-03-12 | The manufacturing method of coke and the manufacturing method of the pig iron |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2006071704A JP4950527B2 (en) | 2006-03-15 | 2006-03-15 | Coke manufacturing method and pig iron manufacturing method |
| JP071704/2006 | 2006-03-15 |
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| CN201410443055.XA Division CN104277856B (en) | 2006-03-15 | 2007-03-12 | The manufacturing method of coke and the manufacturing method of the pig iron |
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| CN101395249A true CN101395249A (en) | 2009-03-25 |
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| CN201410443055.XA Expired - Fee Related CN104277856B (en) | 2006-03-15 | 2007-03-12 | The manufacturing method of coke and the manufacturing method of the pig iron |
| CNA2007800077232A Pending CN101395249A (en) | 2006-03-15 | 2007-03-12 | Process for production of coke and process for production of pig iron |
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| CN201410443055.XA Expired - Fee Related CN104277856B (en) | 2006-03-15 | 2007-03-12 | The manufacturing method of coke and the manufacturing method of the pig iron |
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| Country | Link |
|---|---|
| JP (1) | JP4950527B2 (en) |
| KR (1) | KR101023302B1 (en) |
| CN (2) | CN104277856B (en) |
| WO (1) | WO2007105682A1 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103517965A (en) * | 2011-05-11 | 2014-01-15 | 驰瑞莱股份公司 | Closed coke slurry system and method for gaining sellable petroleum coke pieces out of solidified petroleum coke in a coke drum unit |
| CN104395431A (en) * | 2012-06-29 | 2015-03-04 | 株式会社神户制钢所 | Coke composed mainly of by-product coal |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5328180B2 (en) * | 2008-03-10 | 2013-10-30 | 株式会社神戸製鋼所 | Production method of ashless coal |
| JP5247193B2 (en) * | 2008-03-17 | 2013-07-24 | 株式会社神戸製鋼所 | Coke manufacturing method and pig iron manufacturing method |
| JP2014015502A (en) * | 2012-07-06 | 2014-01-30 | Kobe Steel Ltd | Coke and method of producing the same |
Family Cites Families (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5448802A (en) | 1977-09-26 | 1979-04-17 | Kawasaki Steel Co | Manufacture of coke for iron manufacture |
| JPS5575485A (en) * | 1978-12-05 | 1980-06-06 | Mitsui Cokes Kogyo Kk | Coke production and coke composition |
| JP3279630B2 (en) * | 1992-04-14 | 2002-04-30 | 新日本製鐵株式会社 | Coal carbonization method |
| JPH06116565A (en) * | 1992-10-09 | 1994-04-26 | Nippon Steel Corp | Method for controlling coke quality of moisture conditioned coal |
| CN1192477A (en) * | 1997-12-26 | 1998-09-09 | 杨本 | Method for prodn. of pig iron by utilizing iron-contg. dust as raw material |
| JP2003055667A (en) | 2001-08-17 | 2003-02-26 | Sumitomo Metal Ind Ltd | Production method for blast furnace coke |
| JP4295544B2 (en) * | 2003-04-09 | 2009-07-15 | 株式会社神戸製鋼所 | Method for producing reformed coal for metallurgy, and method for producing slag containing reduced metal and non-ferrous metal oxide using reformed coal for metallurgy |
| CN1211456C (en) * | 2003-08-12 | 2005-07-20 | 山西同嘉钢铁有限公司 | Furnace core and its production method |
| JP4045229B2 (en) * | 2003-10-15 | 2008-02-13 | 株式会社神戸製鋼所 | Production method of ashless coal |
| JP4109686B2 (en) * | 2005-07-19 | 2008-07-02 | 株式会社神戸製鋼所 | Coke manufacturing method and pig iron manufacturing method |
-
2006
- 2006-03-15 JP JP2006071704A patent/JP4950527B2/en not_active Expired - Fee Related
-
2007
- 2007-03-12 CN CN201410443055.XA patent/CN104277856B/en not_active Expired - Fee Related
- 2007-03-12 CN CNA2007800077232A patent/CN101395249A/en active Pending
- 2007-03-12 KR KR1020087022302A patent/KR101023302B1/en active IP Right Grant
- 2007-03-12 WO PCT/JP2007/054822 patent/WO2007105682A1/en active Application Filing
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103517965A (en) * | 2011-05-11 | 2014-01-15 | 驰瑞莱股份公司 | Closed coke slurry system and method for gaining sellable petroleum coke pieces out of solidified petroleum coke in a coke drum unit |
| CN104395431A (en) * | 2012-06-29 | 2015-03-04 | 株式会社神户制钢所 | Coke composed mainly of by-product coal |
| CN104395431B (en) * | 2012-06-29 | 2017-03-08 | 株式会社神户制钢所 | Coke with extract residue as main material |
Also Published As
| Publication number | Publication date |
|---|---|
| JP4950527B2 (en) | 2012-06-13 |
| KR20080094724A (en) | 2008-10-23 |
| CN104277856B (en) | 2018-10-16 |
| WO2007105682A1 (en) | 2007-09-20 |
| KR101023302B1 (en) | 2011-03-18 |
| JP2007246674A (en) | 2007-09-27 |
| CN104277856A (en) | 2015-01-14 |
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