JPS6239082Y2 - - Google Patents
Info
- Publication number
- JPS6239082Y2 JPS6239082Y2 JP1983019080U JP1908083U JPS6239082Y2 JP S6239082 Y2 JPS6239082 Y2 JP S6239082Y2 JP 1983019080 U JP1983019080 U JP 1983019080U JP 1908083 U JP1908083 U JP 1908083U JP S6239082 Y2 JPS6239082 Y2 JP S6239082Y2
- Authority
- JP
- Japan
- Prior art keywords
- coal
- drying
- hot air
- heat
- preheating
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
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- 239000003245 coal Substances 0.000 claims description 36
- 238000001035 drying Methods 0.000 claims description 31
- 239000000571 coke Substances 0.000 claims description 22
- 238000010438 heat treatment Methods 0.000 claims description 8
- 239000007789 gas Substances 0.000 description 14
- 239000000446 fuel Substances 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 239000000428 dust Substances 0.000 description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- 239000003546 flue gas Substances 0.000 description 4
- 239000002737 fuel gas Substances 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000007602 hot air drying Methods 0.000 description 2
- 238000003763 carbonization Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
Description
本考案はコークス炉に装入する石炭を乾燥予熱
する装置に関し、特に乾燥予熱に必要な燃料の消
費量を低減させるコークス炉用石炭の乾燥予熱装
置に関するものである。
従来コークス炉用石炭の乾燥予熱装置としては
第１図および第２図に示すような熱気流による乾
燥予熱装置が知られている。第１図は一塔式気流
乾燥予熱方式と言われているもので、図に示すよ
うに、原料の石炭ａはサージホツパー３から予熱
塔１に供給される。そこで熱風発生炉６からの高
温熱風ｂで増熱された熱風ｃによつて塔上部に同
伴され、その間に石炭は乾燥予熱されて、塔上部
では水分ゼロ、温度150〜250℃となり、予熱され
た石炭は捕集機４で捕集される。捕集機４を出た
熱風ｄの温度は200〜300℃となつて循環ブロワ７
に吸引される。
このうち熱風発生炉６で発生した熱風量と予熱
塔１で蒸発した水蒸気量に相当する量の熱風ｆが
余剰となつて集塵機８、煙突９を通つて系外に排
出される。残りは再び熱風ｂと混合した後、予熱
塔１に戻される。
第２図は二塔式気流乾燥予熱方式といわれてい
るもので、第１図に示した一塔式の方式に比べて
プロセスは複雑になる。乾燥塔２は石炭の予備的
な乾燥を行い、予熱塔１はその予備乾燥された石
炭を更に乾燥加熱し水分ゼロ、温度150〜250℃に
する。前述したように、捕集機４を出た熱風ｄは
200〜300℃の温度をもつので、この熱風ｄを一部
とはいえ一塔式の場合のように系外に排出するの
は熱量の大きな損失になる。そこで二塔式の場合
は熱風ｄを乾燥塔２に戻しその熱量で原料の石炭
ａの予備乾燥を行うのである。
この結果捕集機５を出る熱風ｅは約100℃の低
温になる。したがつて系外に排出される熱風ｆも
100℃の低温となるので、一塔式の場合に比較し
損失熱量は小さくなる。ただし第２図に示すよう
に一塔式の場合に比較して構造は複雑になり、設
備費は高くなる。
上述のように従来方式においては、一塔式の場
合は系外に排出される熱風による損失熱量が大き
いので熱風発生炉での燃料消費量は多くなる。ま
た二塔式の場合は系外に排出される熱風による損
失熱量は一塔式の場合に比べると少なくなり、そ
の分だけ燃料消費量は少なくてするものの、燃料
消費量の水準自体は依然として高く、その上、一
塔式の場合に比して設備費が高くなるという問題
があつた。
本考案はコークス炉に装入する石炭の乾燥予熱
にあたり、コークス炉で生じるガスの顕熱を利用
して熱風発生炉での燃料消費量を大巾に低減する
ようにしたものであり、その要旨とするところ
は、コークス炉で生じるガスの顕熱を利用して熱
媒体を加熱し循環させる手段を備え、該熱媒体に
よつて石炭を乾燥する乾燥装置と、熱風を発生さ
せ循環させる手段を備え、該熱風によつて石炭を
予熱する予熱塔および予熱された石炭を捕集する
捕集機とからなる予熱装置とを併設して、石炭を
前記乾燥装置で乾燥した後前記予熱装置で予熱す
る構成とするとともに、予熱装置から排出される
熱風を石炭乾燥用の補助熱源として前記乾燥装置
内に導入する構成としたことを特徴とするコーク
ス炉用石炭の乾燥予熱装置にある。
以下本考案を実施例にもとづき詳しく説明す
る。
第３図は本考案の実施例における装置構成を示
す図である。図において１０は第１図に示した一
塔式の気流乾燥予熱装置からサージホツパー３を
除いた構成の予熱装置であり、２０はコークス炉
３０で生じるガスの顕熱を利用して熱媒体を加熱
し循環させる手段を備え、該熱媒体によつて石炭
を間接的に乾燥させる乾燥装置である。乾燥装置
２０は間接乾燥機１１、コークス炉煙道排ガス熱
交換器１２、コークス炉上昇管発生ガス熱交換器
１３、熱媒体加熱炉１４、循環ポンプ１５、集塵
機１６およびサージホツパー１７を主要な構成と
している。
間接式乾燥機１１としては例えば円筒の内部に
多数の管を組込み、管内部に高温の熱媒体を通
し、管外部の石炭と間接的に熱交換を行つて石炭
中の水分を蒸発させる方式のいわゆる多管回転乾
燥機を用いる。
コークス炉煙道排ガス熱交換器１２はコークス
炉３０の煙道（図示外）の途中に設置し、コーク
ス炉３０の燃焼室の排ガス（図中で示す）の顕
熱を回収するものであり、コークス炉上昇管発生
ガス熱交換器１３はコークス炉上昇管に設け、コ
ークス炉３０の炭化室の発生ガス（図中で示
す）の顕熱を回収するものである。
なお、本実施例では熱交換器１２と１３の両者
を設置しているが該熱交換器の顕熱回収量が大き
い場合はいずれか一方だけでよい。熱媒体加熱炉
１４は前記熱交換器による熱媒体の加熱が不足の
場合これを補うためのもので、必要に応じて設置
して加熱操作を行うものである。
上記構成において、原料の石炭ａはサージホツ
パー１７から乾燥機１１に供給され、熱媒体ｊに
より間接的に乾燥される。乾燥機１１を出た熱媒
体は熱交換器１２，１３および必要により加熱炉
１４によつて昇温され、再び乾燥機１１に入る。
一方一塔式気流乾燥予熱装置１０から排出され
る比較的高温の熱風ｆも乾燥機１１に導入され、
乾燥用熱源として石炭を直接乾燥するのに使用さ
れるとともに、発生水蒸気の排ガスの露点を低く
して集塵機１６を通り系外に排出される。
乾燥機１１により乾燥された後の石炭ｈは予熱
塔１に供給されて更に乾燥予熱される。これによ
り熱風発生炉６に使用する燃料ガス量は第１図に
示した従来方式の場合に比して大巾に低減される
とともに、予熱塔１の規模を小さくすることが出
来る。
第３図の実施例装置により200T-dry／Ｈ、水分
10％の石炭を乾燥予熱したコークス炉に装入した
ときの消費熱量を第１図および第２図に示した従
来装置の場合と比較して第１表に示す。
また本実施例装置の場合と第１図および第２図
に示した従来装置の場合の熱の流れをそれぞれ第
４図，第５図および第６図に示す。
The present invention relates to a device for drying and preheating coal to be charged into a coke oven, and more particularly to a device for drying and preheating coal for a coke oven that reduces the amount of fuel consumed for drying and preheating. 2. Description of the Related Art As a conventional drying and preheating device for coal for coke ovens, a drying and preheating device using hot air flow as shown in FIGS. 1 and 2 is known. FIG. 1 shows what is called a one-column air flow drying preheating system, and as shown in the figure, raw material coal a is supplied from a surge hopper 3 to a preheating tower 1. There, the coal is entrained to the upper part of the tower by hot air c heated by high-temperature hot air b from the hot air generating furnace 6, and during that time, the coal is dried and preheated, and the temperature becomes 150 to 250°C with zero moisture in the upper part of the tower. The collected coal is collected by a collector 4. The temperature of the hot air d coming out of the collector 4 is 200 to 300℃, and then it is sent to the circulation blower 7.
is attracted to. Among these, a surplus of hot air f corresponding to the amount of hot air generated in the hot air generating furnace 6 and the amount of water vapor evaporated in the preheating tower 1 is discharged outside the system through the dust collector 8 and the chimney 9. The remainder is returned to the preheating tower 1 after being mixed with the hot air b again. Fig. 2 shows what is called a two-column air flow drying preheating system, and the process is more complicated than the one-column system shown in Fig. 1. The drying tower 2 performs preliminary drying of the coal, and the preheating tower 1 further dries and heats the pre-dried coal to zero moisture and a temperature of 150 to 250°C. As mentioned above, the hot air d leaving the collector 4 is
Since it has a temperature of 200 to 300°C, discharging even a portion of this hot air d out of the system as in the case of a single tower system results in a large loss of heat. Therefore, in the case of a two-column type, the hot air d is returned to the drying tower 2 and its heat is used to pre-dry the raw material coal a. As a result, the hot air e exiting the collector 5 has a low temperature of about 100°C. Therefore, the hot air f discharged outside the system also
Since the temperature is as low as 100°C, the amount of heat lost is smaller than in the case of a single tower system. However, as shown in Figure 2, the structure is more complex and the equipment cost is higher than in the case of a single tower type. As mentioned above, in the conventional system, in the case of a single tower type, the amount of heat lost due to the hot air discharged outside the system is large, so the amount of fuel consumed in the hot air generating furnace increases. In addition, in the case of a two-tower type, the amount of heat lost due to the hot air discharged outside the system is smaller than in the case of a single-tower type, and although the fuel consumption is reduced accordingly, the level of fuel consumption itself is still high. Moreover, there was a problem in that the equipment cost was higher than in the case of a single-tower type. This invention uses the sensible heat of the gas generated in the coke oven to dry and preheat the coal charged into the coke oven, thereby significantly reducing the amount of fuel consumed in the hot air generating oven. The system is equipped with a means for heating and circulating a heat medium using the sensible heat of the gas generated in the coke oven, a drying device for drying coal using the heat medium, and a means for generating and circulating hot air. and a preheating device consisting of a preheating tower that preheats the coal with the hot air and a collector that collects the preheated coal, and the coal is dried in the drying device and then preheated in the preheating device. A device for drying and preheating coal for a coke oven, characterized in that the hot air discharged from the preheating device is introduced into the drying device as an auxiliary heat source for drying the coal. The present invention will be explained in detail below based on examples. FIG. 3 is a diagram showing a device configuration in an embodiment of the present invention. In the figure, 10 is a preheating device configured by removing the surge hopper 3 from the single-column air flow drying preheating device shown in FIG. This is a drying device that is equipped with a means for circulating the coal and indirectly dries the coal using the heat medium. The drying device 20 mainly includes an indirect dryer 11, a coke oven flue gas heat exchanger 12, a coke oven riser tube generated gas heat exchanger 13, a heat medium heating furnace 14, a circulation pump 15, a dust collector 16, and a surge hopper 17. There is. The indirect type dryer 11 is, for example, a type in which a large number of tubes are installed inside a cylinder, a high temperature heat medium is passed inside the tubes, and the moisture in the coal is evaporated by indirectly exchanging heat with the coal outside the tubes. A so-called multi-tube rotary dryer is used. The coke oven flue exhaust gas heat exchanger 12 is installed in the middle of the flue (not shown) of the coke oven 30 and recovers the sensible heat of the exhaust gas (shown in the figure) in the combustion chamber of the coke oven 30. The coke oven riser tube generated gas heat exchanger 13 is provided in the coke oven riser tube, and is used to recover sensible heat of the generated gas (shown in the figure) in the carbonization chamber of the coke oven 30. In this embodiment, both the heat exchangers 12 and 13 are installed, but if the amount of sensible heat recovered by the heat exchanger is large, only one of them may be used. The heat medium heating furnace 14 is used to compensate for insufficient heating of the heat medium by the heat exchanger, and is installed as necessary to perform heating operations. In the above configuration, the raw material coal a is supplied from the surge hopper 17 to the dryer 11, and is indirectly dried by the heat medium j. The heat medium leaving the dryer 11 is heated by heat exchangers 12, 13 and, if necessary, a heating furnace 14, and then enters the dryer 11 again. On the other hand, relatively high-temperature hot air f discharged from the single-tower flash drying preheating device 10 is also introduced into the dryer 11,
It is used as a drying heat source to directly dry coal, and also lowers the dew point of the generated water vapor exhaust gas, which passes through the dust collector 16 and is discharged to the outside of the system. The coal h after being dried by the dryer 11 is supplied to the preheating tower 1 where it is further dried and preheated. As a result, the amount of fuel gas used in the hot air generating furnace 6 can be greatly reduced compared to the conventional method shown in FIG. 1, and the scale of the preheating tower 1 can be reduced. 200 T-dry /H, moisture
Table 1 shows the amount of heat consumed when 10% of coal is charged into a dry and preheated coke oven in comparison with the conventional apparatus shown in FIGS. 1 and 2. 4, 5, and 6 show the heat flow in the case of the present embodiment apparatus and the conventional apparatus shown in FIGS. 1 and 2, respectively.
【表】
第１表および第４図〜第６図から明らかなよう
に、本考案装置によればコークス炉で生じるガス
の顕熱を石炭乾燥に活用することにより熱気流乾
燥予熱装置における熱風発生炉の燃料消費量を大
巾に低減することができる。[Table] As is clear from Table 1 and Figures 4 to 6, according to the device of the present invention, hot air is generated in the hot air drying preheating device by utilizing the sensible heat of the gas generated in the coke oven for drying the coal. The fuel consumption of the furnace can be significantly reduced.
第１図および第２図は従来の熱気流乾燥予熱装
置の構成例を示す図、第３図は本考案の実施例装
置の構成を示す図、第４図は本考案実施例装置に
おける熱の流れを示す図、第５図および第６図は
第１図および第２図の従来装置における熱の流れ
を示す図である。
１……予熱塔、２……乾燥塔、３……サージホ
ツパー、４，５……捕集機、６……熱風発生炉、
７……ブロワ、８……集塵機、９……煙突、１０
……熱気流乾燥予熱装置、１１……間接乾燥機、
１２……コークス炉煙道排ガス熱交換器、１３…
…コークス炉上昇管発生ガス熱交換器、１４……
熱媒体加熱炉、１５……ポンプ、１６……集塵
機、１７……サージホツパー、２０……乾燥装
置、３０……コークス炉。
第４図において、
Ａ……乾燥機、Ｂ……予熱塔、ａ……煙道排ガ
ス入熱、ｂ……上昇管顕熱回収分、ｃ……蒸気，
排ガス顕熱、ｄ……煙道排ガス出熱、ｅ……石
炭，水，蒸気、ｆ……燃料ガス、ｇ……石炭顕
熱、ｈ……蒸発熱、ｉ……放散熱、ｊ……予熱塔
排出ガス。
第５図において、
Ｄ……予熱塔、ｋ……燃料ガス、ｌ……石炭顕
熱、ｍ……蒸発熱、ｎ……水蒸気燃焼排ガス顕
熱、ｐ……放散熱。
第６図において、
Ｅ……乾燥予熱塔、ｑ……燃料ガス、ｒ……石
炭顕熱、ｓ……蒸発熱、ｔ……放散熱、ｕ……水
蒸気燃焼排ガス顕熱。
なお第４図，第５図，第６図中の数字の単位は
106kcal／Ｈである。
1 and 2 are diagrams showing a configuration example of a conventional hot air flow drying preheating device, FIG. 3 is a diagram showing a configuration of an embodiment of the device of the present invention, and FIG. Flow diagrams, FIGS. 5 and 6, are diagrams showing the flow of heat in the conventional apparatus of FIGS. 1 and 2. 1... Preheating tower, 2... Drying tower, 3... Surge hopper, 4, 5... Collector, 6... Hot air generator,
7... Blower, 8... Dust collector, 9... Chimney, 10
...Hot air drying preheating device, 11...Indirect dryer,
12...Coke oven flue gas heat exchanger, 13...
...Coke oven riser tube generated gas heat exchanger, 14...
Heat medium heating furnace, 15... pump, 16... dust collector, 17... surge hopper, 20... drying device, 30... coke oven. In Figure 4, A...dryer, B...preheating tower, a...flue gas heat input, b...sensible heat recovery from riser tube, c...steam,
Sensible heat of exhaust gas, d...Heat output from flue gas, e...Coal, water, steam, f...Fuel gas, g...Sensible heat of coal, h...Heat of evaporation, i...Radiation heat, j... Preheating tower exhaust gas. In Fig. 5, D... preheating tower, k... fuel gas, l... sensible heat of coal, m... heat of evaporation, n... sensible heat of steam combustion exhaust gas, p... dissipated heat. In Fig. 6, E: dry preheating tower, q: fuel gas, r: sensible heat of coal, s: heat of evaporation, t: dissipated heat, u: sensible heat of steam combustion exhaust gas. The units of numbers in Figures 4, 5, and 6 are
10 6 kcal/H.
Claims (1)
体を加熱し循環させる手段を備え、該熱媒体によ
つて石炭を乾燥する乾燥装置と、熱風を発生させ
循環させる手段を備え、該熱風によつて石炭を予
熱する予熱塔および予熱された石炭を捕集する捕
集機とからなる予熱装置とを併設して、石炭を前
記乾燥装置で乾燥した後前記予熱装置で予熱する
構成とするとともに、予熱装置から排出される熱
風を石炭乾燥用の補助熱源として前記乾燥装置内
に導入する構成としたことを特徴とするコークス
炉用石炭の乾燥予熱装置。 It is equipped with a means for heating and circulating a heat medium using the sensible heat of gas generated in a coke oven, a drying device for drying coal using the heat medium, and a means for generating and circulating hot air, and a means for generating and circulating hot air. Therefore, a preheating device consisting of a preheating tower that preheats the coal and a collector that collects the preheated coal is installed, and the coal is dried in the drying device and then preheated in the preheating device. A coal drying and preheating device for a coke oven, characterized in that hot air discharged from the preheating device is introduced into the drying device as an auxiliary heat source for drying the coal.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1908083U JPS59125953U (en) | 1983-02-14 | 1983-02-14 | Coal drying and preheating equipment for coke ovens |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1908083U JPS59125953U (en) | 1983-02-14 | 1983-02-14 | Coal drying and preheating equipment for coke ovens |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS59125953U JPS59125953U (en) | 1984-08-24 |
| JPS6239082Y2 true JPS6239082Y2 (en) | 1987-10-05 |
Family
ID=30150235
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1908083U Granted JPS59125953U (en) | 1983-02-14 | 1983-02-14 | Coal drying and preheating equipment for coke ovens |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS59125953U (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5490301A (en) * | 1977-12-28 | 1979-07-18 | Nippon Steel Corp | Coal preheating combined with coke dry cooling |
| JPS57100184A (en) * | 1980-12-13 | 1982-06-22 | Nippon Steel Corp | Drying treating method of raw material coal for coke oven |
-
1983
- 1983-02-14 JP JP1908083U patent/JPS59125953U/en active Granted
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5490301A (en) * | 1977-12-28 | 1979-07-18 | Nippon Steel Corp | Coal preheating combined with coke dry cooling |
| JPS57100184A (en) * | 1980-12-13 | 1982-06-22 | Nippon Steel Corp | Drying treating method of raw material coal for coke oven |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS59125953U (en) | 1984-08-24 |
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