CN1834204A - Technique for preparing furnace coal combined coking with coals - Google Patents
Technique for preparing furnace coal combined coking with coals Download PDFInfo
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- CN1834204A CN1834204A CN 200610031537 CN200610031537A CN1834204A CN 1834204 A CN1834204 A CN 1834204A CN 200610031537 CN200610031537 CN 200610031537 CN 200610031537 A CN200610031537 A CN 200610031537A CN 1834204 A CN1834204 A CN 1834204A
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Abstract
This invention discloses a method for manufacturing furnace coal from coking mixed coal. The method directs the mixed coal into a pneumatic separation drier of semi-boiling fluidized bed for grading of grain fineness and drying. The mixed coal is divided into two grades of furnace coal: one with grain fineness of lower than 3 mm and the other with grain fineness of higher than 3 mm, and the content of water in the mixed water is reduced to 6.5-7.5%. The furnace coal with grain fineness of lower than 3 mm is directed to the overhead of the column for coking; the furnace coal with grain fineness of higher than 3 mm is directed into a pulveriser chamber for pulverization, and the pulverized coal is directed into the pneumatic separation drier again for grading of grain fineness and drying, or directed into the overhead of the column for coking. This invention has such advantages of even distribution of furnace coal grain fineness, reducing water content in furnace coal and improving coking capacity.
Description
Technical field
The present invention is mainly concerned with the pretreated technical field of coke-oven plant's coking coal, particularly a kind of technology that adopts wind driven separation dryer of semi-fluidizing fluid-bed as the preparing furnace coal combined coking with coals of preparation equipment.
Background technology
In coking is produced, the existing production technique that is equipped with between coal car is: will contain that moisture is about 10%, after the accounting for 60% coking coal and transport the coke-oven plant of coal charge granularity＜3mm, unload and be transported to coal yard by unloading unit and store respectively, carry out the ature of coal homogenizing by coal through endless belt conveyor.The coking coal that is stored in coal yard is delivered to the blending ratio that coal blending workshop section determines according to the coal blending experiment and is prepared into mixed coal by getting material equipment, endless belt conveyor, mixed coal is delivered to break section through endless belt conveyor and is carried out pulverization process and be prepared into the shove charge coal, and the coal charge of granularity≤3mm will reach about 80% in the shove charge this moment coal.The shove charge coal is delivered to the coal cat head through endless belt conveyor again and is used for coking by coke oven production.
In institution of higher education's didactic works " coking " that Yao Shaozhang, Zheng Ming owner compile (metallurgical industry press 2005 September the 3rd edition) P101 page or leaf the granularity of coking coal is described in detail: " in the granularity control of coking coal the granularity of shove charge coal has been carried out detailed argumentation; the grain refined of shove charge coal and homogenizing are promptly as a whole; most of granularity of shove charge coal should be less than 3mm; mix between each component guaranteeing; the coal particle of different components is interacted; mutual filling gap in process of coking; mutually combine, to guarantee to obtain the coke of even structure." above-mentioned teaching material P103 page table 3-10 (following table 1) is certain mixed coal grade character:
Table 1
| Grade/mm | Size composition/% | Technical analysis/% | Roga index/% | Caking index/% | ||
| Ad | Mt | Vdaf | ||||
| ＞5 | 12.0 | 9.11 | 1.43 | 34.04 | 63 | 56.5 |
| 5～3 | 14.5 | 8.77 | 1.23 | 33.89 | 66 | 60 |
| 3～2 | 12.6 | 8.84 | 1.98 | 33.26 | 68 | 62 |
| 2～1 | 8.4 | - | - | - | 70 | 65 |
| 1～0.5 | 14.6 | 8.82 | 1.41 | 31.92 | 71 | 66 |
| ＜0.5 | 38.1 | 12.04 | 2.13 | 33.06 | 66 | 59 |
By above-mentioned data show coarse fraction (＞5mm) and fine fraction (＜0.5mm) Roga index and the caking index of coal are all lower, caking coal should be given full play to the cohesive action of its active particle in the mixed coal process of coking, the weakly caking coal be should bear lax contraction as inactive particle, therefore meticulous pulverizing not only reduces the active particle effect of cohering coal, and the specific surface of increase inactive particle, both all make the agglutinating value(of coal) of coal charge reduce, so must control the lower limit of coal charge granularity.
And existing conventional is equipped with the coal production technique and can not forms according to coal and petrofacies and carry out corresponding pulverization process to coal charge, the ratio of coal charge granularity＜0.5mm grade increases in the shove charge coal charge of feasible existing prepared, like this, not only affect coke quality, also will cause the waste of the energy and increase environmental pollution.
In addition, above-mentioned routine is equipped with the coal production technique also there are the following problems:
1, the moisture of going into factory's feed coal generally is about 10%, and the moisture of storage in open system coal charge changes along with changes of seasons, the moisture of artificial uncontrollable shove charge coal; Adopt existing coal preparation technology, the moisture in China's coking enterprise shove charge coal is generally higher, and fluctuation range is big.Add up the annual of national large-scale coal chemical enterprise shove charge moisture content of coal according to coking industry association and be about 11%, particularly southern coke-oven plants meet shove charge in rainy season moisture content of coal to surpass 15% sometimes.The shove charge moisture content of coal is higher and unstable, has a strong impact on coke output, quality and coke oven life-span and operation.Usually the every increase by 1% of shove charge moisture content of coal, coking time will prolong 10～15 minutes, and the fluctuation of shove charge moisture content of coal furnace temperature is regulated, control difficulty, thereby it is low or too high to cause the charge of coke temperature to cross greatly in production operation.According to the actual production service data, when the every reduction by 1% of shove charge moisture content of coal, the coking thermal losses just can reduce by 60～75kJ/kg.If the shove charge moisture content of coal is removed 3～4 percentage points before shove charge, can save a large amount of energy every year with regard to national coke ultimate production, also reduce a large amount of CO simultaneously
2And other exhaust gas discharging, so its economic benefit and social benefit are considerable.
2, because go into coal charge granularity＜3mm in factory's feed coal account for 60%, to all carry out pulverization process after the various coking coals cooperations, just exist that the pulverizer processing power is big, electrical consumption power is big, high-quality caking coal can meticulous pulverizing and bottle coal lean coal etc. also can not reach fineness requirement simultaneously.
At present, that domestic coal chemical enterprise generally adopts is the coking shove charge coal preparation technology of above-mentioned routine, because The application of new technique such as the blast furnace of steel industry maximization at present and oxygen-enriched coal spray strengthening smelting, the requirement of STRENGTH ON COKE quality is more and more higher, and therefore how improving coke quality, enlarging the coking coal source, reduce production costs is that a difficult problem that needs to be resolved hurrily is produced in coke-oven plant's coking.
Summary of the invention
The technical problem to be solved in the present invention just is: at the technical problem of prior art existence, the invention provides a kind of employing wind driven separation dryer of semi-fluidizing fluid-bed and mixed coal is carried out pneumatic classification and appropriate drying treatment as preparation equipment, make shove charge coal grade be evenly distributed, also can obviously reduce and control into the stove moisture content of coal, thereby the throughput of raising pit kiln also improves coke quality and output, reduces cost, the technology of the preparing furnace coal combined coking with coals of environmental protection and energy saving.
In order to solve the problems of the technologies described above, the solution that the present invention proposes is: a kind of technology of preparing furnace coal combined coking with coals, it is characterized in that: mixed coal is delivered to carried out size classification and appropriate drying treatment in the wind driven separation dryer of semi-fluidizing fluid-bed, by wind driven separation dryer of semi-fluidizing fluid-bed mixed coal is divided into≤3mm and＞two grain size categories of 3mm, simultaneously the moisture of mixed coal is reduced to 6.5%～7.5%, wherein: granularity is discharged from wind driven separation dryer of semi-fluidizing fluid-bed for the shove charge coal of≤3mm level and is delivered to the coal cat head and use for coking by coke oven production; The coal charge of granularity＞3mm level is discharged the pulverizing unit room of delivering to auxiliary construction and is carried out pulverization process from wind driven separation dryer of semi-fluidizing fluid-bed, the coal charge after the pulverization process is recycled to and carries out size classification and appropriate drying treatment in the wind driven separation dryer of semi-fluidizing fluid-bed or directly use for coking by coke oven production with the≤3mm level shove charge coal cat head of delivering coal.
The thermal source that described wind driven separation dryer of semi-fluidizing fluid-bed adopts is that temperature is 180 ℃～200 ℃ a hot waste gas, and the waste gas of discharging from wind driven separation dryer of semi-fluidizing fluid-bed discharges after sack cleaner purifies.
Compared with prior art, advantage of the present invention just is:
1, the technology of preparing furnace coal combined coking with coals of the present invention the shove charge moisture content of coal can be reduced to from about 10% about 6.5%～7.5%, thereby reduced the about 45～54Mcal/t coal of coking thermal losses, improved coke oven throughput and improved coke quality;
2, the technology of preparing furnace coal combined coking with coals of the present invention is to adopt hot blast that coal charge is carried out pneumatic fractionated, carry out the also automatic control≤3mm level shove charge moisture content of coal of appropriate drying treatment simultaneously and remain on 6.5%～7.5%, therefore the present invention prepares the shove charge moisture content of coal and not influenced by seasonal climate, can keep constant, guarantee that the coke oven production operation is stable, prolong coke oven work-ing life.
3, the technology of preparing furnace coal combined coking with coals of the present invention, in technical process of the present invention, adopt wind driven separation dryer of semi-fluidizing fluid-bed that mixed coal is carried out pneumatic separation classification, mixed coal is fluidisation and semi-fluid state in equipment, discharge no longer through pulverization process particulate, light-weight shove charge coal slave unit bottom, avoid meticulous pulverizing, reduced the content of 0～0.5mm grade coal charge;
4, the shove charge coal grade of the technology of preparing furnace coal combined coking with coals of the present invention is evenly distributed rationally also to have reduced simultaneously and goes into stove moisture, thereby improved the bulk density of shove charge coal, at the proportioning polygamy weakly caking coal that guarantees to reduce under the constant condition of coke quality high-quality caking coal, can enlarge the coking coal source, reduce production costs;
5, the technology of preparing furnace coal combined coking with coals of the present invention can be optimized the minimizing of the technological process between coal car occupation of land and investment fully;
6, the technology of preparing furnace coal combined coking with coals of the present invention coal charge moisture before shove charge reduces to 6%～7% from about 10%, owing to go into the reduction of stove moisture content of coal, being vaporized the water vapour of taking away with raw gas in retort process reduces, so gas cleaning system ammoniacal liquor and various wastewater flow rate reduce, reduced sewage load and quantity discharged, reduced pollution environment.
Description of drawings
Fig. 1 is a process flow diagram of the present invention;
Fig. 2 is the longitudinal section synoptic diagram of structure of the present invention;
Fig. 3 is the schematic cross section of structure of the present invention;
Fig. 4 is a semi-fluidizing fluid-bed longitudinal section synoptic diagram among the present invention;
Fig. 5 is a semi-fluidizing fluid-bed schematic cross section among the present invention;
Fig. 6 is the longitudinal section synoptic diagram of fluid-bed depth setting device among the present invention;
Fig. 7 is the schematic cross section of fluid-bed depth setting device among the present invention;
Fig. 8 is the longitudinal section synoptic diagram of coarse particles material chain scraper discharge mechanism among the present invention;
Fig. 9 is the schematic cross section of coarse particles material chain scraper discharge mechanism among the present invention;
Figure 10 be among the present invention feed bin and the revolution scraper feeder the longitudinal section synoptic diagram;
Figure 11 be among the present invention feed bin and the revolution scraper feeder schematic cross section;
Figure 12 is the longitudinal section synoptic diagram of fine particle material bunker for collecting and revolution scraper-type discharge machine among the present invention;
Figure 13 is the schematic cross section of fine particle material bunker for collecting and revolution scraper-type discharge machine among the present invention;
Figure 14 is the longitudinal section synoptic diagram of mid frame of the present invention and outer outlet body;
Figure 15 is the schematic cross section of mid frame of the present invention and outer outlet body;
Figure 16 is an electric automatization control principle block diagram among the present invention;
Figure 17 is the synoptic diagram of coal charge bulk density and water relation.
Marginal data
1, semi-fluidizing fluid-bed 2, fluid-bed depth setting device
3, coarse particles material chain scraper discharge device 4, revolution scraper feeder
5, feed bin 6, fine particle material are collected discharger
7, frame 8, outer outlet body
9, electric automatization Controlling System 10, bed body
11, air distribution plate 12, segmentation air compartment
13, leak material collection bucket 14, hot-air inlet pipe flange base
15, revolution scraper-type discharge device 20, bearing
21, the first electronic deceleration mechanism 22, first fork
23, connecting rod 24, second fork
25, rotating shaft 26, runner
27, chain tension eccentric weight 28, chain
29, adjustable plate 30, drive unit
31, shaft coupling 32, main drive shaft
33, first sprocket wheel 34, driven shaft
35, second sprocket wheel 36, chain stretching device
37, commutation guide wheel 38, chain scraper
380, chain holder rail 39, the soft board curtain keeps out the wind
320, bearing 370, limit bearing
371, the electronic deceleration of middle part bearing 41, second mechanism
42, shaft coupling 43, bearing
44, rotating shaft 45, scraper-type rotary drum
46, slide flitch 47, oscillatory gearing mechanism
48, guide cover 60, bunker for collecting
61, revolution scraper-type discharge machine 80, pick up and repair door
81, fire extinguishing inert gas import flange base 82, suction opening flange base
83, spy on door 84, the explosion-proof base of drawing
85, manhole door 91, touch-screen
92, programmable logic controller
Embodiment
Below with reference to the drawings and specific embodiments the present invention is described in further details.
In conjunction with the practice of coking theory and coal preparation technology, the applicant finds that the shove charge moisture content of coal has considerable influence to the coking process, and moisture increases and will coking time be prolonged, usually the every increase by 1% of moisture, coking time prolongs 20min, not only influences output, also influences coking speed.The shove charge moisture content of coal also influences bulk density, and as seen from Figure 17, coal charge moisture is lower than at 6%～7% o'clock, reduces with moisture, and bulk density increases.Moisture is greater than 7%, and bulk density also increases, and this is because the lubrication of moisture promotes due to the relative displacement of coal grain, but moisture increases and coking time is prolonged and the coking thermal losses increases, so the shove charge moisture content of coal should not be too high.In addition, granularity to the shove charge coal in the granularity control of coking coal has very high requirement, most of granularity of shove charge coal should be less than 3mm, mix between each component guaranteeing, the coal particle of different components is interacted in process of coking, the filling gap mutually combines, to guarantee to obtain the coke of even structure mutually.But the ratio of coal charge granularity＜0.5mm grade can not too increase, otherwise not only affects coke quality, also will cause the waste of the energy and increase environmental pollution.
Function according to above theory and actual coal preparation technology needs and concrete equipment, the technology of a kind of preparing furnace coal combined coking with coals of the present invention is: mixed coal is delivered to carried out size classification and appropriate drying treatment in the wind driven separation dryer of semi-fluidizing fluid-bed, by wind driven separation dryer of semi-fluidizing fluid-bed mixed coal is divided into≤3mm and＞two grain size categories of 3mm, simultaneously the moisture of mixed coal is reduced to 6.5%～7.5%, wherein: granularity is discharged from wind driven separation dryer of semi-fluidizing fluid-bed for the shove charge coal of≤3mm level and is delivered to the coal cat head and use for coking by coke oven production; The coal charge of granularity＞3mm level is discharged the pulverizing unit room of delivering to auxiliary construction and is carried out pulverization process from wind driven separation dryer of semi-fluidizing fluid-bed, the coal charge after the pulverization process is recycled to and carries out size classification and appropriate drying treatment in the wind driven separation dryer of semi-fluidizing fluid-bed or directly use for coking by coke oven production with the≤3mm level shove charge coal cat head of delivering coal.The thermal source that wind driven separation dryer of semi-fluidizing fluid-bed adopts is that temperature is 180 ℃～200 ℃ a hot waste gas, and the waste gas of discharging from wind driven separation dryer of semi-fluidizing fluid-bed discharges (referring to as shown in Figure 1) after sack cleaner purifies.Wherein, finish coking workshop section in the coal tower, mixed coal is finished by coal blending workshop section, and wind driven separation dryer of semi-fluidizing fluid-bed is finished size classification and dry workshop section, pulverizes unit room and finishes break section, and fly-ash separator is finished dedusting workshop section.The shove charge moisture content of coal is meant the moisture that ejects the shove charge coal from wind driven separation dryer of semi-fluidizing fluid-bed 6.5%～7.5%.The coal charge of discharging from drying machine according to production practice and pertinent data introduction has certain temperature (being generally 70 ℃～80 ℃) and will evaporate 0.5% moisture in transit, so its moisture as charged of shove charge coal that adopts the present invention to prepare is 6%～7%.Reduced the about 45～54Mcal/t coal of coking thermal losses after the shove charge moisture content of coal reduced to about 6.5%～7.5% from about 10%, improve coke oven throughput and improved coke quality, and owing to go into the reduction of stove moisture content of coal, being vaporized the water vapour of taking away with raw gas in retort process reduces, so gas cleaning system ammoniacal liquor and various wastewater flow rate reduce, reduced sewage load and quantity discharged, reduced pollution environment.Technology of the present invention is to adopt hot blast that coal charge is carried out pneumatic fractionated, carry out the also automatic control≤3mm level shove charge moisture content of coal of appropriate drying treatment simultaneously and remain on 6.5%～7.5%, as seen the present invention prepares the shove charge moisture content of coal and not influenced by seasonal climate, can keep constant, guarantee that the coke oven production operation is stable, prolong coke oven work-ing life.In addition, in technical process of the present invention, adopt wind driven separation dryer of semi-fluidizing fluid-bed that mixed coal is carried out pneumatic separation classification, mixed coal is fluidisation and semi-fluid state in equipment, discharge no longer through pulverization process particulate, light-weight shove charge coal slave unit bottom, avoid meticulous pulverizing, reduced the content of 0～0.5mm grade coal charge; Because shove charge coal grade is evenly distributed rationally also to have reduced simultaneously and goes into stove moisture, thereby improved the bulk density of shove charge coal, proportioning polygamy weakly caking coal guaranteeing can reduce under the constant condition of coke quality high-quality caking coal can enlarge the coking coal source, reduces production costs.
Embodiment 1: through the Automatic coal blending device, the blending ratio of determining by coal blending test fits in mixed coal to each single kind coking coal in coal blending workshop section.Mixed coal is delivered to wind driven separation dryer of semi-fluidizing fluid-bed through endless belt conveyor and is carried out size classification and appropriate drying treatment, mixed coal is subjected to the effect of 180 ℃ of hot waste gass and carries out pneumatic classification and appropriate drying treatment in wind driven separation dryer of semi-fluidizing fluid-bed, mixed coal is divided into≤3mm and＞the 3mm secondary; Simultaneously the moisture of mixed coal is reduced to 7.2%～7.5%.Wherein :≤3mm level shove charge coal is discharged from the bottom of wind driven separation dryer of semi-fluidizing fluid-bed, delivers to the coal cat head through endless belt conveyor and uses for coking by coke oven production; The coal charge of＞3mm level is discharged from the front portion of wind driven separation dryer of semi-fluidizing fluid-bed, the pulverizing unit room of delivering to auxiliary construction through endless belt conveyor carries out pulverization process, and the coal charge after the pulverization process is recycled to wind driven separation dryer of semi-fluidizing fluid-bed again to carry out size classification and appropriate drying treatment or use for coking by coke oven production with the≤3mm level coal charge cat head of delivering coal.The waste gas of discharging from wind driven separation dryer of semi-fluidizing fluid-bed after sack cleaner purifies by smoke stack emission.
Embodiment 2: through the Automatic coal blending device, the blending ratio of determining by coal blending test fits in mixed coal to each single kind coking coal in coal blending workshop section.Mixed coal is delivered to wind driven separation dryer of semi-fluidizing fluid-bed through endless belt conveyor and is carried out size classification and appropriate drying treatment, mixed coal is subjected to the effect of 190 ℃ of hot waste gass and carries out pneumatic classification and appropriate drying treatment in wind driven separation dryer of semi-fluidizing fluid-bed, mixed coal is divided into≤3mm and＞the 3mm secondary; Simultaneously the moisture of mixed coal is reduced to 6.8%～7.2%.Wherein :≤3mm level shove charge coal is discharged from the bottom of wind driven separation dryer of semi-fluidizing fluid-bed, delivers to the coal cat head through endless belt conveyor and uses for coking by coke oven production; The coal charge of＞3mm level is discharged from the front portion of wind driven separation dryer of semi-fluidizing fluid-bed, the pulverizing unit room of delivering to auxiliary construction through endless belt conveyor carries out pulverization process, and the coal charge after the pulverization process is recycled to wind driven separation dryer of semi-fluidizing fluid-bed again to carry out size classification and appropriate drying treatment or use for coking by coke oven production with the≤3mm level coal charge cat head of delivering coal.The waste gas of discharging from wind driven separation dryer of semi-fluidizing fluid-bed after sack cleaner purifies by smoke stack emission.
Embodiment 3: through the Automatic coal blending device, the blending ratio of determining by coal blending test fits in mixed coal to each single kind coking coal in coal blending workshop section.Mixed coal is delivered to wind driven separation dryer of semi-fluidizing fluid-bed through endless belt conveyor and is carried out size classification and appropriate drying treatment, mixed coal is subjected to the effect of 200 ℃ of hot waste gass and carries out pneumatic classification and appropriate drying treatment in wind driven separation dryer of semi-fluidizing fluid-bed, mixed coal is divided into≤3mm and＞the 3mm secondary; Simultaneously the moisture of mixed coal is reduced to 6.5%～6.8%.Wherein :≤3mm level shove charge coal is discharged from the bottom of wind driven separation dryer of semi-fluidizing fluid-bed, delivers to the coal cat head through endless belt conveyor and uses for coking by coke oven production; The coal charge of＞3mm level is discharged from the front portion of wind driven separation dryer of semi-fluidizing fluid-bed, the pulverizing unit room of delivering to auxiliary construction through endless belt conveyor carries out pulverization process, and the coal charge after the pulverization process is recycled to wind driven separation dryer of semi-fluidizing fluid-bed again to carry out size classification and appropriate drying treatment or use for coking by coke oven production with the≤3mm level coal charge cat head of delivering coal.The waste gas of discharging from wind driven separation dryer of semi-fluidizing fluid-bed after sack cleaner purifies by smoke stack emission.
As shown in Figures 2 and 3, wind driven separation dryer of semi-fluidizing fluid-bed among the present invention, it comprises semi-fluidizing fluid-bed 1, fluid-bed depth setting device 2, coarse particles material chain scraper discharge device 3, revolution scraper feeder 4, feed bin 5, the fine particle material is collected discharger 6, frame 7, outer outlet body 8 and automatic control system 9, outer outlet body 8 links to each other with frame 7, semi-fluidizing fluid-bed 1 is fixed on the frame 7 and a bed body 10 of semi-fluidizing fluid-bed 1 is positioned at outer outlet body 8, revolution scraper feeder 4 is positioned at the top of a body 10, coarse particles material chain scraper discharge device 3 is between bed body 10 and revolution scraper feeder 4 and be close to a body 10, feed bin 5 is positioned at the top of revolution scraper feeder 4 and is communicated with revolution scraper feeder 4, and the fine particle material is collected discharger 6 and is positioned at semi-fluidizing fluid-bed 1 both sides.
As shown in Figure 4 and Figure 5, in the present embodiment, of the present invention semi-fluidizing fluid-bed 1 comprises a body 10, air distribution plate 11, segmentation air compartment 12, leaks material collection bucket 13, hot-air inlet pipe flange base 14 and turns round scraper-type discharge device 15, bed body 10 is fixed on frame 7 and is positioned at outer outlet body 8, and air distribution plate 11 is located on the body 10; Segmentation air compartment 12 is fixed on the lower end of frame 7, and links to each other with the bottom of bed body 10; Hot-air inlet pipe flange base 14 is located on the side of segmentation air compartment 12 housings, and described leakage material collection bucket 13 links to each other with the lower end of segmentation air compartment 12, and revolution scraper-type discharge device 15 is positioned at the lower end of leaking material collection bucket 13.
As shown in Figure 6 and Figure 7, in the present embodiment, fluid-bed depth setting device 2 of the present invention comprises the first electronic deceleration mechanism 21, transmission rig, rotating shaft 25, chain stretching device, chain 28 and adjustable plate 29, the side that the first electronic deceleration mechanism 21 is fixed on the outer outlet body 8, the output shaft of the first electronic deceleration mechanism 21 links to each other with rotating shaft 25 by transmission rig, rotating shaft 25 is fixed on the housing of outer outlet body 8 by bearing 20, be equiped with runner 26 on the two ends of rotating shaft 25, chain 28 is set around on the runner 26 and with the adjustable plate 29 of being located at semi-fluidizing fluid-bed 1 both sides and links to each other.This transmission rig comprises that first fork 22, connecting rod 23 and second fork, 24, the first forks, 22 1 ends link to each other with the output shaft of the first electronic deceleration mechanism 21, and the other end links to each other with second fork 24 by connecting rod 23, and second fork 24 links to each other with rotating shaft 25.Wherein, the output shaft of the first electronic deceleration mechanism 21 is affixed with the key and first fork 22, first fork, 22 usefulness bearing pins slide in connecting rod 23 middle part slotted holes and drive beat, connecting rod 23 1 ends are hinged with the bearing pin and second fork 24, connecting rod 23 usefulness keys and rotating shaft 25 are affixed, chain tension adopts chain tension eccentric weight 27, this chain tension eccentric weight 27 and runner 26 all are affixed with key and rotating shaft 25, chain 28 upper ends are hinged with bearing pin and runner 26, and chain 28 lower ends are hinged with bearing pin and adjustable plate 29 earholes.Drive adjustable plates 29 liftings by the first electronic deceleration mechanism 21, can regulate the height of fluidized bed on the body 10.
As Fig. 8 and shown in Figure 9, in the present embodiment, the particle that coarse particles material chain scraper discharge device 3 of the present invention is used to separate greater than 3mm, this coarse particles material chain scraper discharge device 3 be positioned at outer outlet body 8 and be arranged at semi-fluidizing fluid-bed 1 the bed body 10 on, it comprises drive unit 30, shaft coupling 31 main drive shafts 32, first sprocket wheel 33, driven shaft 34, second sprocket wheel 35, chain stretching device 36, commutation guide wheel 37, chain scraper 38, the chain holder rail 380 and the soft board curtain 39 that keeps out the wind, drive unit 30 is fixed on the ground, an outside of frame 7 of wind driven separation dryer of semi-fluidizing fluid-bed firing floor, the output shaft of drive unit 30 links to each other with main drive shaft 32 by shaft coupling 31, is fixed with first sprocket wheel 33 with key on the main drive shaft 32; Be equiped with second sprocket wheel 35 on the driven shaft 34, and be provided with second chain stretching device 36 in the two ends of driven shaft 34, driven shaft 34, second sprocket wheel 35 and chain stretching device 36 are complete integrated devices, can guarantee that like this chain scraper 38 constantly rotatablely moves, can reach the purpose of tension chain scraper plate 38 again, guarantee the relativeness between chain scraper 38 and the bed body 10, the phenomenon of jam can not occur; Chain scraper 38 is set around on first sprocket wheel 33 and second sprocket wheel 35, and chain scraper 38 pilled-in selvedges (lower edge) scraper plate be close on semi-fluidizing fluid-bed 1 the air distribution plate 11, the macrobead band that can not seethe with excitement that moves by chain scraper 38 is discharged from bed, guarantee not dead bed, reach the isolating purpose of thickness gradation.Chain holder rail 380 bottoms are fixed by bolts on the body 10, and chain holder rail 380 tops are fixed on the support of a body 10, and chain scraper 38 is roll-sliding on chain holder rail 380; The soft board curtain 39 that keeps out the wind is installed on the support of a body 10 and is positioned at the side of first sprocket wheel 33, plays the effect that prevents that air-flow from leaking and spreading; Commutation guide wheel 37 is installed on the support of a body 10 and between first sprocket wheel 33 and second sprocket wheel 35, the limit bearing 370 of commutation guide wheel 37 is fixed on the housing of outer outlet body 8, the middle part bearing 371 of commutation guide wheel 37 is fixed on the support of a body 10, and commutation guide wheel 37 plays and changes the effect that chain scraper 38 moves commutation.
As shown in Figure 10 and Figure 11, in the present embodiment, feed bin 5 of the present invention is positioned at the top of revolution scraper feeder 4 and is communicated with in revolution scraper feeder 4, a last workshop section can be sent here by revolution scraper feeder 4 and to contain being given in the wind driven separation dryer of semi-fluidizing fluid-bed of the bigger material equal and quantitative of moisture, feed bin 5 can also play the effect of sealing simultaneously.Revolution scraper feeder 4 of the present invention comprises the second electronic deceleration mechanism 41, rotating shaft 44, scraper-type rotary drum 45, guide cover 48, slide flitch 46 and oscillatory gearing mechanism 47, revolution scraper feeder 44 bodies place semi-fluidizing fluid-bed feed end top and link to each other with feed bin 5 by guide cover 48, rotating shaft 44, scraper-type rotary drum 45 is installed in the guide cover 48, rotating shaft 44 is fixed on the guide cover 48 by bearing 43, the output shaft of the second electronic deceleration mechanism 41 links to each other with rotating shaft 44 by shaft coupling 42, scraper-type rotary drum 45 usefulness keys are fixed in the rotating shaft 44, and the second electronic deceleration mechanism 41 drives scraper-type rotary drums 45 wet stocks in the feed bin 5 are discharged from guide cover 48 equal and quantitatives.Slip flitch 46 by being hingedly fixed on the outer outlet body 8, the flitch 46 that slips nestles up the output shaft of oscillatory gearing mechanism 47, this oscillatory gearing mechanism 47 is fixed on the outside of outer outlet body 8, the flexible swing angle of rotation that can change slide flitch 46 of the output shaft of oscillatory gearing mechanism 47 reaches the purpose that makes wet stock drop on the appropriate location of air distribution plate 11.The wet stock of discharging from guide cover 48 equal and quantitatives drops on semi-fluidizing fluid-bed 1 the air distribution plate 11 through slipping flitch 46, and the chain scraper 38 through coarse particles material chain scraper discharge device 3 drives on the air distribution plate 11 that is covered with semi-fluidizing fluid-bed 1 again.
As Figure 12 and shown in Figure 13, in the present embodiment, fine particle material of the present invention is collected discharger 6 and is used to separate the particle that is less than or equal to 3mm.This fine particle material is collected discharger 6 and is comprised bunker for collecting 60 and revolution scraper-type discharge machine 61, and bunker for collecting 60 is arranged in semi-fluidizing fluid-bed 1 both sides, and the upper end is the import of fine particle material, and the lower end links to each other with revolution scraper-type discharge machine 61.
As Figure 14 and shown in Figure 15, in the present embodiment, frame 7 of the present invention is fixed on the firing floor basis, guarantees that this equipment operates steadily, reliably.Outer outlet body 8 adopts the thermal-insulating sealing outer outlet bodies and links to each other with frame 7, and thermal-insulating sealing outer outlet body 8 is provided with suction opening flange base 82, explosion-proofly draw base 84, fire extinguishing inert gas import flange base 81, spy on door 83, pick up and repair 80 and manhole door 85.Suction opening flange base 82 is outlet ports, the explosion-proof base 84 of drawing is detonation gas discharge outlets, fire extinguishing inert gas import flange base 81 is imports of fire extinguishing rare gas element, spy on the porthole that door is an operation condition in the operation personnel monitoring equipment, pick up and repair door 80 and are loading ports of chain scraper 38 and pick up picking up of the personnel of repairing and repair mouth that manhole door 85 is inlets of personnel's access arrangement inside.
As shown in figure 16, in the present embodiment, electric control system 9 of the present invention comprises touch-screen 91 (TP) and programmable logic controller 92 (PLC), and touch-screen 91 (TP) links to each other with programmable logic controller 92 (PLC) by network.The importation of programmable logic controller 92 (PLC) receives from each position transducer, imports near the signal of switch, interlock each point logistics capacity, wind-warm syndrome, blast, air draft oxygen level, air draft dust concentration and guard signal and manual control part, and through after the sequential operation processing, control each topworks and regulate, thereby realize the automatic adjusting of complete machine is controlled by each reference mark.Touch-screen 91 (TP) and programmable logic controller 92 (PLC) communication fetch equipment status information also show, also can issue control command and controlled variable to programmable logic controller 92 (PLC) by touch-screen 91 (TP) simultaneously.This equipment can be equipped with coal DCS system interface, the equipment operation condition is passed to control center and receives the control of control center.
Principle of work: mass transport conveyor wind driven separation dryer of semi-fluidizing fluid-bed in the time of feed bin 5 feedings starts, after feed bin 5 material levels arrive high material, start vacuum fan earlier and be provided with suction opening flange base 82 exhausting from outer outlet body 8, restart calorifier to 12 air-supplies of segmentation air compartment, restart coarse particles material chain scraper discharge device 3, turning round scraper feeder 4 then starts to semi-fluidizing fluid-bed 1 feed, wet stock drops on semi-fluidizing fluid-bed 1 the air distribution plate 11 through slipping flitch 46, and wet stock drives on the air distribution plate 11 that is covered with semi-fluidizing fluid-bed 1 through the chain scraper 38 of coarse particles material chain scraper discharge device 3.Enter segmentation air compartment 12 hot blasts pass air distribution plate 11 make wet stock under the effect of wind-force on semi-fluidizing fluid-bed 1 the boiling, semi-fluidizing fluid-bed 1 feed end leading portion wet stock boiling mainly is the drying process of mainly carrying out heat exchange under the effect of hot blast, reaches the purpose that appropriate drying is removed the moisture of wet stock (being damping).Because chain scraper 38 drives the exsiccant material and arrives semi-fluidizing fluid-bed 1 back segment, the dried material boiling mainly is to carry out thickness particulate fractionation processes under the effect of hot blast, reaches the isolating purpose of material thickness gradation.The coarse particles material is discharged to the elephant trunk outside the machine under chain scraper 38 drives, fall to carry on the conveyor and go to carry out fragmentation, material after the fragmentation is transported to that belt feeder is enterprising goes in the feed bin 5 again, recirculation enters the wind driven separation dryer of semi-fluidizing fluid-bed fractional separation of seething with excitement, and reaches the purpose of selection by winnowing fragmentation.Fine granular materials enters in the fine particle material bunker for collecting 60 of fine particle material collection discharger 6 from the overflow port of semi-fluidizing fluid-bed 1 both sides, be discharged on the fines conveyor through revolution scraper-type discharge machine 61, the leakage material that semi-fluidizing fluid-bed 1 leakage material collection bucket 13 is collected is discharged on the fines conveyor by revolution scraper-type discharge device 15, is delivered to coal tower fully together.Semi-fluidizing fluid-bed 1 fluid-bed depth is regulated by fluid-bed depth setting device 2, and it is determine to regulate the height of fluidized bed afterwards by picking up the sizing of testing fine granular materials.Semi-fluidizing fluid-bed 1 waste gas is provided with suction opening flange base 82 through vacuum fan from outer outlet body 8 and extracts out, drains into the fly-ash separator dedusting, arranges to atmosphere from chimney then, delivers on the fines belt conveyer behind the dust humidification that fly-ash separator is collected.Also be provided with on the outer outlet body 8 and explosion-proofly draw base 84, fire extinguishing inert gas import flange base 81, spy on door 83, pick up and repair door 80, manhole 85 etc., in case detect the dust concentration, oxygen level of waste gas, when temperature is too high, automatically open the rare gas element supply valve, rare gas element enters in the outer outlet body 8 from fire extinguishing inert gas import flange base 81, suppress burning, reach the fire extinguishing effect, even detonation, detonation gas is gone out explosive door and is discharged from the explosion-proof base 84 of drawing, through row of conduits to outdoor safe place, can damage equipment and the personnel safety that jeopardizes the operations staff.Electric control system 9 comprises touch-screen 91 (TP) and programmable logic controller 92 (PLC), and touch-screen 91 (TP) links to each other with programmable logic controller 92 (PLC) by network.The importation of programmable logic controller 92 (PLC) receives from each position transducer, imports near the signal of switch, interlock each point logistics capacity, wind-warm syndrome, blast, air draft oxygen level, air draft dust concentration and guard signal and manual control part, and through after the sequential operation processing, control each topworks and regulate, thereby realize the automatic adjusting of complete machine is controlled by each reference mark.Touch-screen 91 (TP) and programmable logic controller 92 (PLC) communication fetch equipment status information also show, also can issue control command and controlled variable to programmable logic controller 92 (PLC) by touch-screen 91 (TP) simultaneously.This equipment can be equipped with coal DCS system interface, the equipment operation condition is passed to control center and receives the control of control center.
Claims (2)
1, a kind of technology of preparing furnace coal combined coking with coals, it is characterized in that: mixed coal is delivered to carried out size classification and appropriate drying treatment in the wind driven separation dryer of semi-fluidizing fluid-bed, by wind driven separation dryer of semi-fluidizing fluid-bed mixed coal is divided into≤3mm and＞two grain size categories of 3mm, simultaneously the moisture of mixed coal is reduced to 6.5%～7.5%, wherein: granularity is discharged from wind driven separation dryer of semi-fluidizing fluid-bed for the shove charge coal of≤3mm level and is delivered to the coal cat head and use for coking by coke oven production; The coal charge of granularity＞3mm level is discharged the pulverizing unit room of delivering to auxiliary construction and is carried out pulverization process from wind driven separation dryer of semi-fluidizing fluid-bed, the coal charge after the pulverization process is recycled to and carries out size classification and appropriate drying treatment in the wind driven separation dryer of semi-fluidizing fluid-bed or directly use for coking by coke oven production with the≤3mm level shove charge coal cat head of delivering coal.
2, the technology of preparing furnace coal combined coking with coals according to claim 1, it is characterized in that: the thermal source that described wind driven separation dryer of semi-fluidizing fluid-bed adopts is that temperature is 180 ℃～200 ℃ a hot waste gas, and the waste gas of discharging from wind driven separation dryer of semi-fluidizing fluid-bed discharges after sack cleaner purifies.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101838540A (en) * | 2010-04-27 | 2010-09-22 | 莱芜钢铁集团有限公司 | Vibrational fluidized bed device for controlling humidity and grading coking coal and fluidizing process thereof |
| CN101906310A (en) * | 2010-09-09 | 2010-12-08 | 武汉钢铁(集团)公司 | Method for drying coking coal materials |
| CN101967387A (en) * | 2010-07-10 | 2011-02-09 | 新兴铸管股份有限公司 | Application of medium caking coal to stamp-charging coke |
| CN102021006A (en) * | 2009-09-22 | 2011-04-20 | 山东省冶金设计院有限责任公司 | Process for removing water content from coking coal |
| CN102676193A (en) * | 2012-05-11 | 2012-09-19 | 无锡亿恩科技股份有限公司 | Humidifying process for high-moisture charged coking coal |
| CN101643657B (en) * | 2009-09-02 | 2013-03-06 | 袁长胜 | Coking coal pretreatment method and special device thereof |
| CN104140832A (en) * | 2013-05-10 | 2014-11-12 | 山东钢铁集团日照有限公司 | Technology for improving quality stability of coking charge coal |
| CN104327870A (en) * | 2014-10-14 | 2015-02-04 | 辽宁中弘信冶金技术有限公司 | Coking coal production method and coking coal |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1127286A (en) * | 1995-01-17 | 1996-07-24 | 湖南省资兴矿务局煤电焦化总厂 | Coal adding method for coking |
| CN2494964Y (en) * | 2001-08-11 | 2002-06-12 | 哈尔滨工业大学达通热能工程有限公司 | Full-automatic high-moisture raw coal fluidized bed dryer |
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| CN101643657B (en) * | 2009-09-02 | 2013-03-06 | 袁长胜 | Coking coal pretreatment method and special device thereof |
| CN102021006A (en) * | 2009-09-22 | 2011-04-20 | 山东省冶金设计院有限责任公司 | Process for removing water content from coking coal |
| CN102021006B (en) * | 2009-09-22 | 2014-01-08 | 山东省冶金设计院股份有限公司 | Process for removing water content from coking coal |
| CN101838540A (en) * | 2010-04-27 | 2010-09-22 | 莱芜钢铁集团有限公司 | Vibrational fluidized bed device for controlling humidity and grading coking coal and fluidizing process thereof |
| CN101967387A (en) * | 2010-07-10 | 2011-02-09 | 新兴铸管股份有限公司 | Application of medium caking coal to stamp-charging coke |
| CN101906310A (en) * | 2010-09-09 | 2010-12-08 | 武汉钢铁(集团)公司 | Method for drying coking coal materials |
| CN101906310B (en) * | 2010-09-09 | 2013-01-02 | 武汉钢铁(集团)公司 | Method for drying coking coal materials |
| CN102676193A (en) * | 2012-05-11 | 2012-09-19 | 无锡亿恩科技股份有限公司 | Humidifying process for high-moisture charged coking coal |
| CN104140832A (en) * | 2013-05-10 | 2014-11-12 | 山东钢铁集团日照有限公司 | Technology for improving quality stability of coking charge coal |
| CN104327870A (en) * | 2014-10-14 | 2015-02-04 | 辽宁中弘信冶金技术有限公司 | Coking coal production method and coking coal |
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Effective date of registration: 20180725 Address after: 116085 128 high energy street, Qixian Ling high tech Industrial Park, Dalian, Liaoning Patentee after: ACRE Coking And Refractory (Dalian) Engineering Consulting Corp., MCC Address before: No. 27, Shengnan Road, Dong Dong District, Anshan, Liaoning Province Patentee before: ACRE Coking and Refractory Engineering Consulting Corporation, MCC |
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