JPS6345435B2 - - Google Patents
Info
- Publication number
- JPS6345435B2 JPS6345435B2 JP53065897A JP6589778A JPS6345435B2 JP S6345435 B2 JPS6345435 B2 JP S6345435B2 JP 53065897 A JP53065897 A JP 53065897A JP 6589778 A JP6589778 A JP 6589778A JP S6345435 B2 JPS6345435 B2 JP S6345435B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- coke
- coal
- heat transfer
- preheating device
- 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
Links
- 239000007789 gas Substances 0.000 claims description 80
- 239000000571 coke Substances 0.000 claims description 60
- 239000003245 coal Substances 0.000 claims description 44
- 238000000034 method Methods 0.000 claims description 28
- 238000001816 cooling Methods 0.000 claims description 20
- 239000003546 flue gas Substances 0.000 claims description 16
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 15
- 238000004939 coking Methods 0.000 claims description 10
- 238000002485 combustion reaction Methods 0.000 claims description 10
- 239000000428 dust Substances 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 6
- 230000005494 condensation Effects 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 5
- 229910000831 Steel Inorganic materials 0.000 claims description 3
- 238000005338 heat storage Methods 0.000 claims description 3
- 238000000746 purification Methods 0.000 claims description 3
- 239000010959 steel Substances 0.000 claims description 3
- 238000009736 wetting Methods 0.000 claims 1
- 238000001035 drying Methods 0.000 description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 6
- 239000002737 fuel gas Substances 0.000 description 5
- 239000011261 inert gas Substances 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000000112 cooling gas Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000007747 plating Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
Classifications
-
- 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
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
-
- 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
- C10B39/00—Cooling or quenching coke
- C10B39/02—Dry cooling outside the oven
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Coke Industry (AREA)
- Drying Of Solid Materials (AREA)
- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
Description
【発明の詳細な説明】
本発明は、熱伝達ガスがコークス冷却装置およ
び石炭予熱装置を順々に通つて案内される、コー
クス化装置におけるコークス冷却および石炭予熱
のさいのコークスの顕熱の利用方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to the utilization of sensible heat of coke during coke cooling and coal preheating in a coking unit in which the heat transfer gas is guided through a coke cooler and a coal preheating unit in sequence. Regarding the method.
ドイツ連邦共和国特許出願公開第2415758号明
細書から、コークス乾燥消火装置と組合されかつ
赤熱するコークスから混合ガスへ伝達される熱量
を利用して連続的な石炭の乾燥および予熱を行な
いしかも消火ガス用循環回路と乾燥および予熱装
置を含む乾燥ガス通路とを有する装置が公知であ
り、この装置においては乾燥ガス通路と消火ガス
用循環回路とが単一のガス循環回路にまとめられ
ており、乾燥のさい遊離する水蒸気を凝縮させる
装置をガス循環回路が有し、ガス循環回路が後燃
焼室を通つて案内されている。この装置は、燃焼
室の燃焼ずみガスを、閉循環回路内を循環する熱
伝達ガスとして使用し、この熱伝達ガスは継続的
に発生せしめられねばならず、しかも循環回路に
は、除塵装置、送風機、噴射凝縮器、熱交換器お
よび消火バンカから出る含有水性ガスを燃焼する
後燃焼室のような必要かつきわめて広範囲な装置
部分を追加しなければならない。したがつてこの
装置は製造面ならびに運転面から見てきわめて高
価である。 German Patent Application No. 2415758 discloses a method for continuously drying and preheating coal, which is combined with a coke drying extinguishing device and utilizes the amount of heat transferred from red-hot coke to a mixed gas, and which is used for extinguishing gas. Devices are known which have a circulation circuit and a drying gas passage containing a drying and preheating device, in which the drying gas passage and the extinguishing gas circulation circuit are combined into a single gas circulation circuit, and the drying gas passage includes a drying and preheating device. The gas circulation circuit has a device for condensing the water vapor liberated during the combustion process, and is guided through the afterburning chamber. This device uses the combusted gases of the combustion chamber as a heat transfer gas that circulates in a closed circulation circuit, which must be continuously generated, and the circulation circuit includes a dust removal device, Necessary and very extensive equipment parts must be added, such as blowers, injection condensers, heat exchangers, and post-combustion chambers for burning the contained water gas leaving the fire bunker. This device is therefore very expensive both from a manufacturing and operational point of view.
ドイツ連邦共和国特許出願公開第2434837号明
細書から、ガス発生処理過程たとえば装入材料と
くにコークス工場運転用粉炭の乾燥あるいは予熱
のための石炭気化装置あるいは石炭コークス化装
置におけるエネルギー回収の方法が公知であり、
この方法においては装入材料の乾燥および予熱が
廃熱によつて行なわれ、処理の固体の残渣の冷却
のさいたとえばコークス工場におけるコークスの
乾式冷却のさいに、除塵装置を備えた一次ガスの
閉循環回路においてこの廃熱が得られ、そのさい
熱伝達媒体および乾燥媒体としては、たとえば窒
素、コークス炉からの煙道ガス、あるいは炉頂ガ
ス燃焼から生ずる煙道ガスのような不活性ガス
が、除塵装置をもつ二次ガスの循環回路において
使用される。別々の2つの循環回路が必要である
ことにより、この方法を実施するために、同様に
費用のかかる装備部分たとえば熱交換器、除塵装
置および送風機が必要となる。 From German Patent Application No. 24 34 837 a method is known for energy recovery in gas generation processes, for example in coal vaporizers or coal coking plants for drying or preheating the charging material, in particular pulverized coal for coking plant operations. can be,
In this process, the drying and preheating of the charge material is carried out using waste heat, and during the cooling of solid residues of the process, for example during the dry cooling of coke in a coke plant, the primary gas is shut down with a dedusting device. This waste heat is obtained in a circulation circuit, in which case an inert gas such as nitrogen, flue gas from a coke oven or flue gas resulting from top gas combustion is used as heat transfer medium and drying medium. Used in secondary gas circulation circuits with dust removal equipment. Due to the necessity of two separate circulation circuits, likewise expensive equipment parts such as heat exchangers, dust removers and blowers are required to carry out the method.
英国特許第1334373号明細書から、不活性ガス
を循環回路中で高温のコークスおよび石炭に通し
て導くことにより、コークス化処理における高温
のコークスの顕熱を石炭の乾燥および(あるい
は)予熱に使用することは公知であり、そのさい
この不活性ガスは、コークス化のためにも使用さ
れる燃料ガスの燃焼生成物の一部であることも可
能である。この場合同様にコークス冷却装置に送
られる熱伝達ガスならびに循環回路においてコー
クス冷却装置と予熱装置との間にある熱伝達ガス
が不活性化のために予備処理される。 From GB 1334373, the sensible heat of the hot coke in the coking process is used for drying and/or preheating the coal by directing an inert gas through the hot coke and coal in a circulating circuit. It is known to do so, and the inert gas can also be part of the combustion products of the fuel gas, which is also used for coking. In this case, the heat transfer gas that is sent to the coke cooler as well as the heat transfer gas that is present in the circuit between the coke cooler and the preheater is pretreated for inertization.
本発明の課題は、最初に述べた種類の方法にお
いて、前述した公知技術の欠点を除去しかつコー
クスの顕熱の経済的利用を可能にすることであ
る。 The object of the invention is to eliminate the drawbacks of the known technology mentioned above and to make possible an economical use of the sensible heat of the coke in a process of the type mentioned at the outset.
この課題を解決するため本発明によれば、コー
クス炉団が乾式コークス冷却装置と石炭予熱装置
とに結合され、この乾式コークス冷却装置と石炭
予熱装置とが、熱伝達ガスとして前処理されずし
かも乾式のコークス冷却中に反応して貧ガスにな
る煙道ガスおよび赤熱したコークスに対して不活
性な製鋼所の炉頂ガスを介して互いに結合され
る。 In order to solve this problem, according to the invention, a coke oven bank is coupled to a dry coke cooler and a coal preheater, which dry coke cooler and coal preheater are not pretreated as a heat transfer gas and are They are coupled together via the flue gas, which reacts to become gas-poor during dry coke cooling, and the steelwork top gas, which is inert to the red-hot coke.
こうして本発明によれば、いずれにせよ製鋼所
において多量に生ずる炉頂ガスもコークスの乾式
冷却および石炭予熱に利用することにより、コー
クス化装置全体の熱効率をさらに高めることがで
きる。 Thus, according to the present invention, the thermal efficiency of the entire coking apparatus can be further improved by utilizing the furnace top gas, which is produced in large quantities in steel plants, for dry cooling of coke and preheating of coal.
そのさいコークス炉団の蓄熱装置あるいは復熱
装置からの煙道ガスおよび製鋼所の炉頂ガスが直
接乾式コークス冷却装置に送られ、この乾式コー
クス冷却装置において発生する貧ガスおよびほと
んど変化しない炉頂ガスが石炭予熱装置に送られ
ることも有利となる可能性がある。 At that time, the flue gas from the regenerator or recuperator of the coke oven bank and the top gas of the steelworks are sent directly to the dry coke cooler, where the poor gases generated and the top gas that hardly changes are passed directly to the dry coke cooler. It may also be advantageous for the gas to be sent to a coal preheater.
本発明による方法においては、コークス炉団か
ら来て熱伝達ガスとして使用できる煙道ガスの浄
化が省略され、かつコークスの冷却のさいに貧ガ
スが発生せしめられる。コークス炉の蓄熱装置あ
るいは復熱装置から出て行く煙道ガスは、かなり
の水蒸気含有量とその残部の酸素含有量とを有し
ているから、コークスの乾式冷却の場合の600℃
を超える温度範囲においては、発熱による部分酸
化のほかに水性ガスの吸熱反応が起こる。しかし
水性ガス反応の過剰のために反応全体としては著
しく吸熱的である。200℃ないし250℃で発生する
高温の煙道ガスのほかに、この反応の吸熱性もコ
ークスの冷却に大いに役立つ。したがつて水蒸気
と酸素とは、煙道ガスからは除去されない。 In the process according to the invention, purification of the flue gas coming from the coke oven bed and which can be used as heat transfer gas is omitted, and lean gases are generated during cooling of the coke. Since the flue gas leaving the coke oven heat storage or recuperator has a significant water vapor content and a balance oxygen content, the
In the temperature range exceeding 100 ml, an endothermic reaction of the water gas occurs in addition to exothermic partial oxidation. However, due to the excess of water gas reaction, the overall reaction is highly endothermic. In addition to the hot flue gases generated at 200°C to 250°C, the endothermic nature of the reaction also greatly aids in cooling the coke. Water vapor and oxygen are therefore not removed from the flue gas.
本発明による方法においては、熱伝達ガスが、
コークス冷却装置および石炭予熱装置においてそ
れぞれコークスあるいは石炭に直接接触せしめら
れる。前記の反応によつて乾式コークス冷却装置
においては煙道ガスが貧ガスとなり、この貧ガス
は、乾式コークス冷却装置において直接加熱され
た後石炭予熱装置へ送られ、かつそこでコークス
用石炭に直接接触してこれを乾燥せしめ、かつ
100℃以上まで予熱する。炉頂ガスは、乾式コー
クス冷却装置の中では、炉頂ガスの組成に基因し
て不活性ガスの状態であり、かつ冷却処理におい
ても反応は生じない。通常各製鋼所において使用
できる炉頂ガスは、本装置を介して冷却ガスとし
て乾式コークス冷却装置に送られ、そこで加熱さ
れ、引きつづき石炭予熱装置へ送られる。ここで
この炉頂ガスはコークス用石炭と直接接触し石炭
から抽出される水を同時に吸収するさいに再び熱
を放出する。 In the method according to the invention, the heat transfer gas is
It is brought into direct contact with coke or coal in a coke cooling device and a coal preheating device, respectively. In the dry coke chiller, the above-mentioned reactions result in the flue gas becoming lean, which is heated directly in the dry coke chiller and then sent to the coal preheater where it is brought into direct contact with the coking coal. and let it dry, and
Preheat to over 100℃. In the dry coke cooling device, the furnace top gas is in an inert gas state due to the composition of the furnace top gas, and no reaction occurs during the cooling process. The top gas, which is normally available in each steel mill, is sent via this device as cooling gas to a dry coke cooler, where it is heated and then sent to a coal preheating device. Here, this furnace top gas is in direct contact with the coking coal and gives off heat again as it simultaneously absorbs the water extracted from the coal.
別の用途に送ろうとするのでなければ、乾式コ
ークス冷却装置において発生せしめられた貧ガス
は、その少なくとも一部が燃焼室に送られ、この
燃焼室の中でこの貧ガスを燃焼せしめて石炭予熱
装置用の不活性の熱伝達ガスにすることができ
る。乾式コークス冷却装置において発生せしめら
れた貧ガスが燃焼せしめられかつ煙道ガスとして
石炭予熱装置を通して送られる場合には、含有水
分の凝縮が過剰になる。 Unless it is intended to be sent to another use, at least a portion of the lean gas generated in the dry coke cooler is sent to the combustion chamber, where it is combusted to preheat the coal. It can be an inert heat transfer gas for equipment. If the lean gas produced in the dry coke chiller is combusted and passed through the coal preheater as flue gas, there will be excessive condensation of the moisture content.
石炭予熱装置を通過した後、含有水分を凝縮段
階において熱伝達ガスから除去せしめ、かつ(あ
るいは)塵埃を微細塵埃浄化段階において熱伝達
ガスから除去せしめることができる。 After passing through the coal preheater, the moisture content can be removed from the heat transfer gas in a condensation stage and/or dust can be removed from the heat transfer gas in a fine dust cleaning stage.
凝縮のさいに生ずる凝縮物を湿式後消火に用い
ることができる。 The condensate formed during condensation can be used for wet post-extinguishing.
石炭予熱装置から出て場合により乾燥かつ浄化
された貧ガスおよび炉頂ガスが、コークス炉団に
おける下だきガスとして、下だきガスの代わりの
増熱ガスとして、および(あるいは)他の増熱あ
るいは下だきのために使用されるのに適してい
る。 The optionally dried and purified lean gas and top gas leaving the coal preheater can be used as bottom gas in the coke oven bank, as heating gas instead of bottom gas, and/or for other heating or heating purposes. Suitable to be used for undercoating.
石炭予熱装置から出る炉頂ガスを再び炉頂ガス
導管へ戻すことができる。このように炉頂ガスを
熱伝達ガスとして使用する場合には、熱交換器に
よる冷却、浄化あるいは乾燥は不要である。 The top gas leaving the coal preheating device can be returned to the top gas conduit. When the furnace top gas is used as a heat transfer gas in this manner, cooling, purification, or drying by a heat exchanger is not necessary.
熱伝達ガスとして貧ガスおよび炉頂ガスが用い
られる場合には、貧ガスあるいは燃料ガスが圧力
をかけて案内されるようにし、したがつて本装置
への酸素の侵入が確実に防止される。 If lean gases and furnace top gases are used as heat transfer gases, it is ensured that the lean gases or fuel gases are introduced under pressure, thus ensuring that no oxygen enters the device.
図面に示された実施例について本発明を以下に
説明する。 The invention will be explained below with reference to the embodiments shown in the drawings.
本発明による方法の特別な利点は、コークス炉
団の煙道ガス1から生じまた炉頂ガス2として使
用される冷却ガスが、赤熱するコークスの上方な
らびに石炭予熱装置3を通して、しかも閉循環回
路でなくて開循環回路として導かれることから明
らかである。連続的に発生せしめられる煙道ガス
1と炉頂ガス2もつねに使用できかつこの煙道ガ
ス1および炉頂ガス2は種々の処理段階を通つて
一度だけしか導かれないから、これらのガスに対
し何らかの代わりになるものを調達する必要はな
いが、必然的に漏れを生ずる閉循環回路によつて
動作する公知の装置においてはこの代わりのもの
が必要である。 A particular advantage of the process according to the invention is that the cooling gas originating from the flue gas 1 of the coke oven bank and used as top gas 2 is passed above the red-hot coke as well as through the coal preheating device 3 and in a closed circuit. This is clear from the fact that the circuit is led as an open circuit. Since the continuously generated flue gas 1 and furnace top gas 2 can also be used at all times and are led through the various treatment stages only once, these gases It is not necessary to procure any alternative, but such an alternative is necessary in known devices which operate with closed circuits that inevitably leak.
本発明による解決策の別の特別な利点は、コー
クス炉団の煙道ガス1から発生せしめられる貧ガ
スと、含水量の少ない炉頂ガス2とが石炭予熱装
置3において水分を含む石炭にぶつかることであ
る。 Another particular advantage of the solution according to the invention is that the lean gas generated from the flue gas 1 of the coke oven bank and the top gas 2 with a low moisture content impinge on the moist coal in the coal preheating device 3. That's true.
本発明にしたがつて発生せしめられしかも石炭
予熱装置3の燃焼室4へ500℃ないし800℃の温度
ではいる貧ガスの燃焼のさいにも、コークス炉ガ
ス、天然ガス等のような燃料ガスよりも含水量の
はるかに少ない不活性の熱伝達ガスが発生する。
したがつて水分を含む石炭と熱伝達ガスとの間の
濃度勾配は、本発明による方法のすべての変形例
において非常に大きく、しかも公知の空気式石炭
乾燥方法に比べてつねにはるかに大きい。この大
きい濃度勾配は本来の乾燥処理にとつて非常に有
利である。 Even during the combustion of the lean gas produced according to the invention and entering the combustion chamber 4 of the coal preheating device 3 at a temperature of 500°C to 800°C, the fuel gas such as coke oven gas, natural gas, etc. An inert heat transfer gas with a much lower water content is also generated.
The concentration gradient between the moist coal and the heat transfer gas is therefore very large in all variants of the process according to the invention, and always much larger than in the known pneumatic coal drying process. This large concentration gradient is very advantageous for the actual drying process.
したがつて本発明による方法においては、コー
クス化処理の固体残渣の廃熱が、石炭予熱3を介
して間接的にきわめて経済的に再利用される。遊
離した熱伝達ガスは、装置を離れた後各種の下だ
きの目的等に使用可能である。すべての処理段階
に対して共通な熱伝達ガスを利用することによつ
て、乾式コークス冷却後の微細塵埃分離をなしで
すますことができる。したがつて必要な若干の装
備部材は、本発明による装置に対しては公知の装
置と比較して減少せしめられている。 In the process according to the invention, the waste heat of the solid residue of the coking process is therefore recycled indirectly via the coal preheating 3 in a very economical manner. The liberated heat transfer gas can be used for various plating purposes etc. after leaving the device. By utilizing a common heat transfer gas for all process steps, fine dust separation after dry coke cooling can be dispensed with. The number of necessary equipment parts is therefore reduced for the device according to the invention compared to known devices.
図面に示されたすべての特徴は、それ自体であ
るいは任意の有効な組合わせにおいて本発明の対
象を形成する。 All the features shown in the drawings form the subject matter of the invention in themselves or in any advantageous combination.
図面は本発明によるコークスの顕熱の利用方法
を構成図として示したものである。
1…煙道ガス、2…燃料ガス(炉頂ガス)、3
…石炭予熱装置、4…燃焼室、5…乾式コークス
冷却装置、6…凝縮段階、7…凝縮物、8…湿式
後消火装置、9…貧ガス、10…燃料ガス(炉頂
ガス)、11…コークス炉、12…蓄熱装置、1
3…復熱装置。
The drawing shows a method of utilizing sensible heat of coke according to the present invention as a configuration diagram. 1... Flue gas, 2... Fuel gas (furnace top gas), 3
Coal preheating device, 4 Combustion chamber, 5 Dry coke cooling device, 6 Condensation stage, 7 Condensate, 8 Wet post-extinguishing device, 9 Poor gas, 10 Fuel gas (top gas), 11 ... Coke oven, 12 ... Heat storage device, 1
3...Recuperator.
Claims (1)
熱装置を順々に通つて案内されて、コークス冷却
および石炭予熱を行なう方法において、コークス
炉団11が乾式コークス冷却装置5と石炭予熱装
置3とに結合され、この乾式コークス冷却装置5
と石炭予熱装置3とが、熱伝達ガスとして前処理
されずしかも乾式のコークス冷却中に反応して貧
ガスになる煙道ガス1および赤熱したコークスに
対して不活性な製鋼所の炉頂ガス2を介して互い
に結合されることを特徴とする、コークス化装置
におけるコークス冷却および石炭予熱のさいのコ
ークスの顕熱の利用方法。 2 コークス炉団11の蓄熱装置12あるいは復
熱装置13からの煙道ガス1および製鋼所の炉頂
ガス2が直接乾式コークス冷却装置5に送られ、
この乾式コークス冷却装置において発生する貧ガ
スおよびほとんど変化しない炉頂ガスが石炭予熱
装置3に送られることを特徴とする、特許請求の
範囲第1項に記載の方法。 3 熱伝達ガスが、コークス冷却装置5および石
炭予熱装置3においてそれぞれコークスおよび石
炭に直接接触せしめられることを特徴とする、特
許請求の範囲第1項または第2項に記載の方法。 4 コークス冷却装置5から来る貧ガスの少なく
とも一部が燃焼室4に送られ、この燃焼室の中で
この貧ガスが燃焼せしめられて石炭予熱装置3用
の不活性の熱伝達ガスになることを特徴とする、
特許請求の範囲第1項または第2項に記載の方
法。 5 熱伝達ガスが、石炭予熱装置3を通過した
後、含有水分を凝縮段階6において除去せしめら
れ、また微細塵埃浄化段階において塵埃を除去せ
しめられることを特徴とする、特許請求の範囲第
1項ないし第4項のうち1つに記載の方法。 6 凝縮のさいに生ずる凝縮物7が湿式後消火8
に用いられることを特徴とする、特許請求の範囲
第5項に記載の方法。 7 石炭予熱装置3から出る貧ガス9および炉頂
ガス10が、コークス炉団における下だきガスと
して、下だきガスの代わりの増熱ガスとして、ま
たは他の増熱あるいは下だきのために使用される
ことを特徴とする、特許請求の範囲第1項ないし
第5項のうち1つに記載の方法。 8 石炭予熱装置3から出る炉頂ガス10が再び
炉頂ガス導管へ戻されることを特徴とする、特許
請求の範囲第1項または第2項に記載の方法。 9 熱伝達ガスが圧力をかけて案内されることを
特徴とする、特許請求の範囲第1項ないし第5項
のうち1つに記載の方法。[Claims] 1. A method in which a heat transfer gas is guided through a coke cooler and a coal preheater in order to perform coke cooling and coal preheating, in which a coke oven bank 11 is connected to a dry coke cooler 5 and a coal preheater. This dry coke cooling device 5 is coupled to the preheating device 3.
and a coal preheating device 3, a flue gas 1 which is not pretreated as a heat transfer gas and reacts to become a poor gas during dry coke cooling, and a steel mill top gas which is inert to red-hot coke. A method of utilizing sensible heat of coke during coke cooling and coal preheating in a coking apparatus, characterized in that the coke is coupled to each other via two. 2 Flue gas 1 from the heat storage device 12 or recuperator 13 of the coke oven bank 11 and furnace top gas 2 of the steelworks are directly sent to the dry coke cooling device 5,
2. A method according to claim 1, characterized in that the lean gases and the almost unchanged furnace top gas generated in this dry coke cooling device are sent to the coal preheating device (3). 3. Process according to claim 1 or 2, characterized in that the heat transfer gas is brought into direct contact with the coke and the coal in the coke cooling device 5 and the coal preheating device 3, respectively. 4. At least a portion of the lean gas coming from the coke cooler 5 is sent to the combustion chamber 4, in which it is combusted to become an inert heat transfer gas for the coal preheater 3. characterized by
A method according to claim 1 or 2. 5. After the heat transfer gas has passed through the coal preheating device 3, the moisture content is removed in a condensation stage 6, and the dust is removed in a fine dust purification stage. The method according to any one of paragraphs 1 to 4. 6 The condensate 7 produced during condensation is extinguished after wetting 8
The method according to claim 5, characterized in that it is used for. 7. The lean gas 9 and top gas 10 coming out of the coal preheating device 3 are used as undercooking gas in a coke oven bank, as heating gas instead of undercooking gas, or for other heating or undercooking purposes. 6. Method according to one of the claims 1 to 5, characterized in that: 8. The method according to claim 1 or 2, characterized in that the furnace top gas 10 exiting the coal preheating device 3 is returned to the furnace top gas conduit. 9. Method according to one of claims 1 to 5, characterized in that the heat transfer gas is guided under pressure.
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE2733365A DE2733365C3 (en) | 1977-07-23 | 1977-07-23 | Process for using the sensible heat of coke in a coking plant |
Publications (2)
Publication Number | Publication Date |
---|---|
JPS5423601A JPS5423601A (en) | 1979-02-22 |
JPS6345435B2 true JPS6345435B2 (en) | 1988-09-09 |
Family
ID=6014701
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP6589778A Granted JPS5423601A (en) | 1977-07-23 | 1978-06-02 | Utilization of sensible heat of coke in coking apparatus |
Country Status (13)
Country | Link |
---|---|
JP (1) | JPS5423601A (en) |
AU (1) | AU532280B2 (en) |
BR (1) | BR7804040A (en) |
CA (1) | CA1135211A (en) |
DD (1) | DD137598A5 (en) |
DE (1) | DE2733365C3 (en) |
ES (1) | ES471357A1 (en) |
FR (1) | FR2398103A1 (en) |
GB (1) | GB2002412B (en) |
IT (1) | IT1105634B (en) |
PL (1) | PL112401B1 (en) |
SE (1) | SE433616B (en) |
ZA (1) | ZA784171B (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH0274636U (en) * | 1988-11-28 | 1990-06-07 |
Families Citing this family (16)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5923591B2 (en) * | 1978-05-26 | 1984-06-02 | 日本鋼管株式会社 | Coke oven gas heat recovery method |
US4288295A (en) * | 1979-06-12 | 1981-09-08 | Interlake, Inc. | Coke oven with apparatus for partially drying and preheating coal |
DE3000808C2 (en) * | 1980-01-11 | 1987-08-20 | Didier Engineering Gmbh, 4300 Essen | Process for using the sensible heat of coke in a coking plant and system for carrying out such a process |
DE3047240C2 (en) * | 1980-12-16 | 1983-03-10 | Didier Engineering Gmbh, 4300 Essen | Method for increasing the calorific value of a furnace gas in a coking plant |
JPS59108067A (en) * | 1982-12-10 | 1984-06-22 | Pilot Ink Co Ltd | Ink for screen printing |
DE3329163C2 (en) * | 1983-08-12 | 1985-08-01 | Didier Engineering Gmbh, 4300 Essen | Process for using the sensible heat of coke in a coking plant |
NZ210093A (en) * | 1983-11-18 | 1988-11-29 | Lubrizol Genetics Inc | Genetic modification of plant cells by octopine t-dna promoters and/or polyadenylation sites; dna vectors, bacterial strains and plant tissue |
DE3404684C2 (en) * | 1984-02-10 | 1986-01-23 | Didier Engineering Gmbh, 4300 Essen | Process for utilizing the sensible heat generated when coke is dry-cooled by means of a gas |
JP2540054B2 (en) * | 1987-10-29 | 1996-10-02 | 株式会社リコー | Ink for stencil printing |
US5054391A (en) | 1989-05-12 | 1991-10-08 | Riso Kagaku Corporation | Thermal stencil sheet assembly with stencil sheet temporarily detachable from frame |
JPH10114135A (en) * | 1996-10-12 | 1998-05-06 | Riso Kagaku Corp | Pressure reducing stencil printer and printing method |
JPH10129098A (en) * | 1996-10-30 | 1998-05-19 | Riso Kagaku Corp | Method and apparatus for pressure-reduction type stencil printing |
CN1186407C (en) | 1999-12-28 | 2005-01-26 | 理想科学工业株式会社 | Ink for stencilling |
DE102011115699A1 (en) * | 2011-10-12 | 2013-04-18 | Thyssenkrupp Uhde Gmbh | Process for the dry cooling of coke with carbon dioxide with subsequent use of the carbon monoxide produced |
RU2596759C1 (en) * | 2015-08-03 | 2016-09-10 | Открытое акционерное общество "Научно-производственное объединение по исследованию и проектированию энергетического оборудования им. И.И. Ползунова" (ОАО "НПО ЦКТИ") | Energy process plant for coke cooling and thermal treatment of coal charge |
RU2596760C1 (en) * | 2015-08-03 | 2016-09-10 | Открытое акционерное общество "Научно-производственное объединение по исследованию и проектированию энергетического оборудования им. И.И. Ползунова" (ОАО "НПО ЦКТИ") | Energy process plant for coke cooling and thermal treatment of coal charge |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS50113501A (en) * | 1974-01-23 | 1975-09-05 | ||
JPS5145103A (en) * | 1974-10-16 | 1976-04-17 | Osaka Gas Co Ltd | Kookusuronenshohaigasuno shorihoho |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US1854407A (en) * | 1927-11-03 | 1932-04-19 | U G I Contracting Company | Means for preheating coal and cooling coke |
GB1334373A (en) * | 1970-11-10 | 1973-10-17 | British Steel Corp | Carbonising coal |
-
1977
- 1977-07-23 DE DE2733365A patent/DE2733365C3/en not_active Expired
-
1978
- 1978-06-02 JP JP6589778A patent/JPS5423601A/en active Granted
- 1978-06-26 BR BR7804040A patent/BR7804040A/en unknown
- 1978-06-29 PL PL1978208015A patent/PL112401B1/en unknown
- 1978-07-03 ES ES471357A patent/ES471357A1/en not_active Expired
- 1978-07-10 IT IT50229/78A patent/IT1105634B/en active
- 1978-07-20 AU AU38216/78A patent/AU532280B2/en not_active Expired
- 1978-07-21 SE SE7808045A patent/SE433616B/en not_active IP Right Cessation
- 1978-07-21 CA CA000307838A patent/CA1135211A/en not_active Expired
- 1978-07-21 GB GB7830695A patent/GB2002412B/en not_active Expired
- 1978-07-21 FR FR7821784A patent/FR2398103A1/en active Granted
- 1978-07-21 DD DD78206859A patent/DD137598A5/en unknown
- 1978-07-21 ZA ZA00784171A patent/ZA784171B/en unknown
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS50113501A (en) * | 1974-01-23 | 1975-09-05 | ||
JPS5145103A (en) * | 1974-10-16 | 1976-04-17 | Osaka Gas Co Ltd | Kookusuronenshohaigasuno shorihoho |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH0274636U (en) * | 1988-11-28 | 1990-06-07 |
Also Published As
Publication number | Publication date |
---|---|
DE2733365B2 (en) | 1979-10-04 |
JPS5423601A (en) | 1979-02-22 |
DE2733365A1 (en) | 1979-02-01 |
SE7808045L (en) | 1979-01-24 |
ES471357A1 (en) | 1979-01-16 |
DD137598A5 (en) | 1979-09-12 |
FR2398103A1 (en) | 1979-02-16 |
GB2002412B (en) | 1982-03-17 |
AU532280B2 (en) | 1983-09-22 |
PL208015A1 (en) | 1979-03-26 |
IT1105634B (en) | 1985-11-04 |
IT7850229A0 (en) | 1978-07-10 |
GB2002412A (en) | 1979-02-21 |
DE2733365C3 (en) | 1980-06-19 |
AU3821678A (en) | 1980-01-24 |
FR2398103B1 (en) | 1981-03-27 |
CA1135211A (en) | 1982-11-09 |
SE433616B (en) | 1984-06-04 |
ZA784171B (en) | 1979-07-25 |
BR7804040A (en) | 1979-04-03 |
PL112401B1 (en) | 1980-10-31 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
JPS6345435B2 (en) | ||
CA1103193A (en) | Process and apparatus for the recovery of waste heat from a coke oven operation | |
US4284476A (en) | Process and apparatus for utilization of the sensible heat of hot coke for drying and preheating coking coal | |
US4308102A (en) | Process and apparatus for drying and preheating coking coal by means of flue gas | |
JPS588720B2 (en) | Coal drying and preheating method using coke sensible heat during dry coke cooling | |
JP2007039608A (en) | Method and device for utilizing circulating coolant gas of coke dry quenching apparatus | |
US4255926A (en) | Installation for recovering energy from solid fossil fuels, more particularly bituminous coal high in inerts | |
CA1245595A (en) | Method for dry cooling coke using the sensible heat formed during dry cooling | |
JP4074521B2 (en) | Combustible gas recovery method during biomass processing in CDQ | |
KR810001672B1 (en) | Process for utilization of the sensible heat of in a coking plant | |
JPS5839462B2 (en) | Method for recovering coke oven waste heat | |
JPS5819384A (en) | Heating of coke oven | |
JPS593506B2 (en) | Preliminary drying of coal to be combined with a coke plant ↓ - or operating method of heating equipment | |
JPS6019099A (en) | Treatment of excessive sludge by dry coke extinguishing equipment | |
SU1043159A1 (en) | Method and apparatus for dry quenching of coke and for producing gases containing hydrogen and carbon oxide | |
KR810001673B1 (en) | Process for drying and preparating coking coal by means of flue gas | |
JPS57117591A (en) | Heat recovery from coke oven by-product gas | |
JPS6239082Y2 (en) | ||
JPS62124186A (en) | Dry quenching device for coke | |
KR820000571B1 (en) | Process for the recovery of coke oven waste heat | |
IE46682B1 (en) | Process for operating a plant for the wet carbonizing of peat | |
JPS604992Y2 (en) | Coal drying preheating equipment | |
JPS61195189A (en) | Heat-decomposition treatment of coal | |
DE3368675D1 (en) | Process for preheating cold moist coal | |
SU37686A1 (en) | The method of heating the gas spool for retort internal heating |