JPH09110485A - Cement production equipment - Google Patents
Cement production equipmentInfo
- Publication number
- JPH09110485A JPH09110485A JP26146195A JP26146195A JPH09110485A JP H09110485 A JPH09110485 A JP H09110485A JP 26146195 A JP26146195 A JP 26146195A JP 26146195 A JP26146195 A JP 26146195A JP H09110485 A JPH09110485 A JP H09110485A
- Authority
- JP
- Japan
- Prior art keywords
- cement
- absorption
- carbon dioxide
- regeneration tower
- preheater
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
- C04B7/432—Preheating without addition of fuel
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/364—Avoiding environmental pollution during cement-manufacturing
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Ceramic Engineering (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Structural Engineering (AREA)
- Ecology (AREA)
- Environmental & Geological Engineering (AREA)
- Environmental Sciences (AREA)
- Public Health (AREA)
- Biodiversity & Conservation Biology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Health & Medical Sciences (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、セメント製造設備
に関するものである。TECHNICAL FIELD The present invention relates to a cement manufacturing facility.
【０００２】[0002]
【従来の技術】従来から実施されているセメント製造設
備の一例を図３によって説明すると、排風機１で吸引さ
れる多段のサイクロン２からなるプレヒータ３により、
粉末のセメント原料４を上昇してくる高温ガスと熱交換
して予熱し、予熱したセメント原料４を前記プレヒータ
３下部に備えた仮焼炉５により仮焼し、更にロータリー
キルン６からなるセメント焼成炉１６に供給して１３５
０℃〜１４５０℃前後で焼成してセメントクリンカ７と
し、得られたセメントクリンカ７はグレート式クーラ８
からなる冷却装置１７に投入して１００℃前後に冷却す
るようにしている。2. Description of the Related Art An example of conventional cement manufacturing equipment will be described with reference to FIG. 3, in which a preheater 3 consisting of a multistage cyclone 2 sucked by an exhaust fan 1 is used.
The cement raw material 4 in powder form is preheated by exchanging heat with the rising high temperature gas, the preheated cement raw material 4 is calcined by a calcining furnace 5 provided under the preheater 3, and further a cement firing furnace comprising a rotary kiln 6. Supply to 16 and 135
Cement clinker 7 is obtained by firing at around 0 ° C to 1450 ° C, and the obtained cement clinker 7 is a great type cooler 8
It is put into the cooling device 17 consisting of and is cooled down to around 100 ° C.
【０００３】前記ロータリーキルン６は、仮焼炉５側が
高く、冷却装置１７側が低い状態に傾斜配置された大型
の管形状を有しており、長手方向複数箇所を対の回転駆
動ローラ１８上に支持されて回転駆動されるようになっ
ている。The rotary kiln 6 has a large tubular shape in which the calcination furnace 5 side is high and the cooling device 17 side is low, and it has a large pipe shape, and a plurality of longitudinal positions are supported on a pair of rotary drive rollers 18. It is driven to rotate.
【０００４】従って、仮焼炉５にて仮焼されてプレヒー
タ３からロータリーキルン６の上端側に供給されたセメ
ント原料４は、ロータリーキルン６の回転によってロー
タリーキルン６内の一側に偏った位置において重力によ
り崩れ落ちる運動を繰り返しつつ下端側へ移動し、ロー
タリーキルン６の下端側に備えた焼成バーナ１０の燃焼
により焼成されてセメントクリンカ７とされ、ロータリ
ーキルン６下端の落下口１９から冷却装置１７に落下投
入されるようになっている。Therefore, the cement raw material 4 which has been calcined in the calcining furnace 5 and supplied from the preheater 3 to the upper end side of the rotary kiln 6 is gravitated to one side in the rotary kiln 6 by the rotation of the rotary kiln 6 due to gravity. While repeating the falling motion, it moves to the lower end side, is burned by the combustion of the burning burner 10 provided at the lower end side of the rotary kiln 6, and becomes a cement clinker 7, which is dropped into the cooling device 17 from the drop port 19 at the lower end of the rotary kiln 6. It is like this.
【０００５】更に、前記冷却装置１７に落下投入された
セメントクリンカ７は、グレート式クーラ８の可動格子
板の往復移動により徐々に図３の右方に送られながら、
可動格子板のスリットから噴出する冷却空気９によって
冷却され、冷却されたセメントクリンカ７はグレート式
クーラ８の右端の取出口から外部へ取り出される。Further, the cement clinker 7 dropped into the cooling device 17 is gradually sent to the right side in FIG. 3 by the reciprocating movement of the movable grid plate of the great type cooler 8,
The cement clinker 7 cooled by the cooling air 9 ejected from the slits of the movable lattice plate is taken out from the outlet of the great type cooler 8 at the right end.
【０００６】一方、グレート式クーラ８でセメントクリ
ンカ７を冷却して高温となった空気９の一部は、ロータ
リーキルン６の焼成バーナ１０の燃焼用に、又他の一部
はダスト沈降室１１を有する燃焼空気送入管１２を通っ
て６００℃前後の温度で前記仮焼炉５の仮焼バーナ１３
に供給され、又低温側の余剰の空気（２３０℃前後）は
電気集塵機１４及びクーラー排ガス管１４’を介して煙
突１５から大気に捨てている。On the other hand, a part of the air 9 heated to a high temperature by cooling the cement clinker 7 with the great type cooler 8 is used for combustion of the burning burner 10 of the rotary kiln 6, and the other part is stored in the dust settling chamber 11. The calcination burner 13 of the calcination furnace 5 passes through the combustion air inlet pipe 12 and has a temperature of about 600 ° C.
The excess air on the low temperature side (around 230 ° C.) is discharged to the atmosphere from the chimney 15 via the electrostatic precipitator 14 and the cooler exhaust gas pipe 14 ′.
【０００７】上記のロータリーキルン６の焼成バーナ１
０の燃焼用に供給された空気９及びダスト沈降室１１を
有する燃焼空気送入管１２を通って前記仮焼炉５の仮焼
バーナ１３に供給された空気９は、共に高温の燃焼排ガ
スとなって多段のサイクロン２からなるプレヒータ３を
予熱用高温ガスとして上昇し、セメント原料４を予熱し
て３２０℃前後に降温された後、排風機１から排ガス２
０として大気に放出されている。Firing burner 1 of the above rotary kiln 6
The air 9 supplied for combustion of 0 and the air 9 supplied to the calcination burner 13 of the calcination furnace 5 through the combustion air inlet pipe 12 having the dust settling chamber 11 are both high temperature combustion exhaust gas. After that, the preheater 3 composed of multi-stage cyclones 2 rises as a high-temperature gas for preheating, preheats the cement raw material 4 and cools it down to around 320 ° C.
It is released to the atmosphere as 0.
【０００８】斯かるセメント製造設備において、ロータ
リーキルン６でセメント原料４からセメントクリンカ７
を焼成する時には多量の二酸化炭素が発生し、更に焼成
バーナ１０の燃焼によっても二酸化炭素が発生する為、
プレヒータ３から大気に放出される排ガス２０中には、
重量比で２８％もの二酸化炭素が含まれており、地球温
暖化等の一要因となっている二酸化炭素を大気中に放出
しない対策が検討されている。In such a cement manufacturing facility, the rotary kiln 6 is used to move the cement raw material 4 to the cement clinker 7.
Since a large amount of carbon dioxide is generated when firing, and carbon dioxide is also generated by the combustion of the firing burner 10,
In the exhaust gas 20 emitted from the preheater 3 to the atmosphere,
As much as 28% by weight of carbon dioxide is contained, measures to prevent the release of carbon dioxide, which is one of the factors contributing to global warming, to the atmosphere are being studied.
【０００９】また、従来の二酸化炭素処理装置として
は、図４に示すような二酸化炭素処理装置が既にあり、
二酸化炭素を吸収し得る炭酸カリウム水溶液等の吸収液
２３を下部に貯留した吸収塔２１と、該吸収塔２１で二
酸化炭素を吸収した吸収液２３を再生する再生塔２２と
が設けられており、該再生塔２２内の吸収液２３は蒸気
等を加熱源として使用した加熱器２５で加熱され、導管
２６のポンプ２７により、熱交換器２８、冷却器２９を
通されて冷却された後、吸収塔２１内の上部に設けられ
ている噴霧器３０から吸収塔２１内に噴霧されるように
なっている。As a conventional carbon dioxide treatment device, there is already a carbon dioxide treatment device as shown in FIG.
An absorption tower 21 in which an absorption liquid 23 such as an aqueous solution of potassium carbonate capable of absorbing carbon dioxide is stored in the lower portion, and a regeneration tower 22 for regenerating the absorption liquid 23 that has absorbed carbon dioxide in the absorption tower 21 are provided. The absorption liquid 23 in the regeneration tower 22 is heated by a heater 25 that uses steam or the like as a heating source, cooled by a pump 27 of a conduit 26 through a heat exchanger 28 and a cooler 29, and then absorbed. The atomizer 30 provided at the upper part of the tower 21 is adapted to spray the absorption tower 21.
【００１０】一方、吸収塔２１内の吸収液２３は、導管
３１のポンプ３２により前記熱交換器２８に送られ、導
管２６を通って来た吸収液２３と熱交換して加熱された
後、再生塔２２内の上部に設けられている噴霧器３３か
ら再生塔２２内に噴霧されるようになっている。On the other hand, the absorption liquid 23 in the absorption tower 21 is sent to the heat exchanger 28 by the pump 32 of the conduit 31, is heat-exchanged with the absorption liquid 23 that has passed through the conduit 26, and is then heated. A sprayer 33 provided in the upper part of the regeneration tower 22 is adapted to spray the inside of the regeneration tower 22.
【００１１】更に吸収塔２１には、下部に排ガス導入管
３４、頂部に処理ガス排出管３５が夫々取り付けられて
おり、再生塔２２の頂部には、二酸化炭素回収管３６が
取り付けられている。Further, the absorption tower 21 is provided with an exhaust gas introduction pipe 34 at the bottom and a treated gas discharge pipe 35 at the top, and a carbon dioxide recovery pipe 36 is attached at the top of the regeneration tower 22.
【００１２】而して、図４に示す二酸化炭素処理装置を
使用した場合、排ガス導入管３４を通して排ガス２０を
吸収塔２１内の吸収液２３の中に導入すると、該排ガス
２０に含まれている二酸化炭素が吸収液２３に吸収さ
れ、二酸化炭素の除去されたガスは吸収液２３内を上昇
し、処理ガス排出管３５から排出される。When the carbon dioxide treatment apparatus shown in FIG. 4 is used, when the exhaust gas 20 is introduced into the absorbing liquid 23 in the absorption tower 21 through the exhaust gas introducing pipe 34, it is contained in the exhaust gas 20. Carbon dioxide is absorbed by the absorption liquid 23, and the gas from which the carbon dioxide has been removed rises in the absorption liquid 23 and is discharged from the processing gas discharge pipe 35.
【００１３】一方、吸収塔２１内で二酸化炭素を吸収し
た吸収液２３は、導管３１のポンプ３２により熱交換器
２８に送られ、加熱された後、噴霧器３３から再生塔２
２内に噴霧され、二酸化炭素の揮発を促進される。On the other hand, the absorption liquid 23 which has absorbed carbon dioxide in the absorption tower 21 is sent to the heat exchanger 28 by the pump 32 of the conduit 31 and heated, and then is sprayed from the sprayer 33 to the regeneration tower 2.
2 is sprayed and the volatilization of carbon dioxide is promoted.
【００１４】更に、再生塔２２の下部に貯留した吸収液
２３は加熱器２５で加熱され、７０℃〜１１０℃の範囲
の温度で吸収液２３中の二酸化炭素が揮発され、再生塔
２２内を上昇して二酸化炭素回収管３６により回収さ
れ、ドライアイス等の原料に活用される。Further, the absorption liquid 23 stored in the lower portion of the regeneration tower 22 is heated by the heater 25, and the carbon dioxide in the absorption liquid 23 is volatilized at a temperature in the range of 70 ° C. to 110 ° C. It rises and is recovered by the carbon dioxide recovery pipe 36, and is utilized as a raw material such as dry ice.
【００１５】また、二酸化炭素を除かれて再生された吸
収液２３は、導管２６のポンプ２７により、熱交換器２
８、冷却器２９を通されて冷却された後、吸収塔２１内
の上部に設けられている噴霧器３０から吸収塔２１内に
噴霧され、再び二酸化炭素の吸収に使用される。The absorption liquid 23 regenerated by removing carbon dioxide is supplied to the heat exchanger 2 by the pump 27 of the conduit 26.
8. After being cooled by being passed through the cooler 29, it is sprayed into the absorption tower 21 from the sprayer 30 provided in the upper part of the absorption tower 21 and used again for absorbing carbon dioxide.
【００１６】[0016]
【発明が解決しようとする課題】しかしながら、図３に
示した如きセメント製造設備に対し、図４に示した如き
従来の二酸化炭素処理装置を単純に付設しただけでは、
再生塔２２において吸収液２３を再生する際に熱エネル
ギーが必要となる為、セメント製造設備の運転コストが
嵩むという問題があった。However, if the conventional carbon dioxide treatment device as shown in FIG. 4 is simply attached to the cement production facility as shown in FIG.
Since heat energy is required to regenerate the absorbing liquid 23 in the regeneration tower 22, there is a problem that the operating cost of the cement manufacturing facility increases.
【００１７】また、プレヒータ３から排出される排ガス
２０中には、５０ｍｇ／Ｎｍ3 程度のセメント原料粉が
含まれている為、このような排ガス２０を吸収塔２１内
の吸収液２３の中に導入して処理していると、吸収液２
３のセメント原料粉含有濃度が次第に高くなり、吸収液
２３が早期に劣化して排ガス２０の二酸化炭素除去が十
分に行えなくなるという問題もあった。Further, since the exhaust gas 20 discharged from the preheater 3 contains about 50 mg / Nm 3 of cement raw material powder, such exhaust gas 20 is contained in the absorption liquid 23 in the absorption tower 21. Absorbing liquid 2 when introduced and treated
There was also a problem that the concentration of the cement raw material powder of No. 3 gradually increased, and the absorbing liquid 23 deteriorated at an early stage, so that carbon dioxide removal of the exhaust gas 20 could not be sufficiently performed.
【００１８】本発明は、上述の実情に鑑みてなしたもの
で、セメント製造設備で生ずる排ガスの熱エネルギーを
利用して前記排ガスから二酸化炭素を安価に除去するこ
とができ、且つ二酸化炭素処理装置の吸収液の劣化を抑
制できるようにしたセメント製造設備を提供することを
目的とするものである。The present invention has been made in view of the above circumstances, and carbon dioxide can be removed from the exhaust gas at low cost by utilizing the thermal energy of the exhaust gas generated in the cement manufacturing facility, and the carbon dioxide treatment device. It is an object of the present invention to provide a cement production facility capable of suppressing the deterioration of the absorbent.
【００１９】[0019]
【課題を解決するための手段】本発明は、セメント原料
を高温ガスと熱交換して予熱するプレヒータと、該プレ
ヒータからのセメント原料を焼成バーナにより焼成して
セメントクリンカとし且つ前記焼成バーナの燃焼排ガス
を前記プレヒータに予熱用高温ガスとして導くセメント
焼成炉と、該セメント焼成炉からのセメントクリンカを
冷却空気と熱交換して冷却し且つ前記セメントクリンカ
との熱交換により高温となった空気の一部を前記セメン
ト焼成炉にバーナ燃焼用空気として導く冷却装置とを備
えたセメント製造設備であって、二酸化炭素を吸収する
吸収液を貯留した吸収塔と、該吸収塔から熱交換器を介
して導いた吸収液を加熱することにより二酸化炭素を揮
発させ且つ前記熱交換器を介して吸収液を吸収塔に戻す
再生塔とを備え、前記プレヒータからの排ガスを前記再
生塔を経由させて加熱源として利用してから前記吸収塔
に導く排ガス導入管を設けたことを特徴とするセメント
製造設備、に係るものである。The present invention is directed to a preheater for preheating heat exchange of a cement raw material with a high temperature gas, a cement raw material from the preheater is fired by a firing burner into a cement clinker, and combustion of the firing burner. A cement firing furnace that guides the exhaust gas to the preheater as a high-temperature gas for preheating, and one of the air that has been heated to a high temperature by heat exchange with the cement clinker and cooling the cement clinker from the cement firing furnace with cooling air. A cement manufacturing facility comprising a cooling unit for guiding a portion to the cement firing furnace as burner combustion air, the absorption tower storing an absorbing liquid that absorbs carbon dioxide, and a heat exchanger from the absorption tower. And a regeneration tower for evaporating carbon dioxide by heating the led absorption liquid and returning the absorption liquid to the absorption tower via the heat exchanger, Those of the cement production facility, characterized in that the exhaust gas from the serial preheater from using as a heat source by way of the regeneration tower is provided an exhaust gas inlet pipe leading to the absorption column.
【００２０】このようにすれば、プレヒータからの排ガ
スが、排ガス導入管を介し再生塔を経由され、加熱源と
して利用されてから前記吸収塔に導かれるので、該吸収
塔で排ガスから二酸化炭素を吸収して熱交換器を介し再
生塔に導かれた吸収液を再生する際の熱エネルギーを著
しく軽減することが可能となる。In this way, the exhaust gas from the preheater is passed through the exhaust gas introduction pipe through the regeneration tower and used as a heating source before being guided to the absorption tower, so that carbon dioxide is emitted from the exhaust gas in the absorption tower. It is possible to remarkably reduce the heat energy when regenerating the absorbing liquid which is absorbed and introduced into the regeneration tower through the heat exchanger.
【００２１】更に、冷却装置でセメントクリンカとの熱
交換により高温となった空気の一部を迂回させて再生塔
の下部を経由させる高温空気導入管を設けるようにして
も良く、このようにすれば、前記再生塔に導かれた吸収
液を再生する際の熱エネルギーを一層軽減することが可
能となる。Further, a high temperature air introducing pipe may be provided which bypasses a part of the air heated to a high temperature due to heat exchange with the cement clinker in the cooling device and passes through the lower part of the regeneration tower. In this case, it becomes possible to further reduce the heat energy when regenerating the absorbing liquid guided to the regeneration tower.
【００２２】また、前記再生塔には、再生塔内の吸収液
中の粉末を除去する濾過機を備えることが好ましく、こ
のようにすれば、再生塔内の吸収液中に混入したセメン
ト原料粉を濾過機によって除去し、吸収液の長期使用を
図ることが可能となる。Further, the regeneration tower is preferably equipped with a filter for removing the powder in the absorption liquid in the regeneration tower. By doing so, the cement raw material powder mixed in the absorption liquid in the regeneration tower is mixed. Can be removed by a filter and the absorbent can be used for a long period of time.
【００２３】[0023]
【発明の実施の形態】以下、本発明の実施の形態を図を
参照しつつ説明する。Embodiments of the present invention will be described below with reference to the drawings.
【００２４】図１及び図２は本発明を実施する形態の一
例を示すもので、図３及び図４と同一部分には同一符号
を付し、その説明を省略する。1 and 2 show an example of a mode for carrying out the present invention. The same parts as those in FIGS. 3 and 4 are designated by the same reference numerals and the description thereof will be omitted.
【００２５】前述した図３と略同様にプレヒータ３、セ
メント焼成炉１６、冷却装置１７を備えたセメント製造
設備２４において、図４と略同様に吸収塔２１及び再生
塔２２を備えた二酸化炭素処理装置３７を付設し、前記
プレヒータ３の排風機１の吐出側を大気に開口せずに、
排ガス導入管３４の一端に接続し、該排ガス導入管３４
の他端は、再生塔２２下部の吸収液２３中を経由させて
から吸収塔２１下部に接続するようにしてある。In a cement production facility 24 equipped with a preheater 3, a cement firing furnace 16 and a cooling device 17 as in the case of FIG. 3 described above, a carbon dioxide treatment provided with an absorption tower 21 and a regeneration tower 22 in the same manner as in FIG. A device 37 is attached, and the discharge side of the preheater 3 of the exhaust fan 1 is not opened to the atmosphere,
The exhaust gas introducing pipe 34 is connected to one end of the exhaust gas introducing pipe 34.
The other end is connected to the lower part of the absorption tower 21 after passing through the absorbent 23 under the regeneration tower 22.
【００２６】更に、本形態例においては、セメント製造
設備２４のクーラー排ガス管１４’に高温空気導入管３
８の一端が接続されており、この高温空気導入管３８の
他端は、送風機３９を介し再生塔２２下部の吸収液２３
中を経由させてから再びクーラー排ガス管１４’に接続
されている。Further, in this embodiment, the high temperature air introducing pipe 3 is connected to the cooler exhaust gas pipe 14 'of the cement manufacturing facility 24.
8 is connected to one end, and the other end of the high temperature air introduction pipe 38 is connected to the absorption liquid 23 in the lower part of the regeneration tower 22 via a blower 39.
After passing through the inside, it is again connected to the cooler exhaust gas pipe 14 '.
【００２７】また、再生塔２２の外部には濾過機４１が
設置されていて、濾過機４１の処理液導入管４２と分離
液吐出管４３とが再生塔２２の下部に接続されている。A filter 41 is installed outside the regeneration tower 22, and a treatment liquid introducing pipe 42 and a separated liquid discharge pipe 43 of the filter 41 are connected to the lower portion of the regeneration tower 22.
【００２８】図２は濾過機４１の一例を示す断面図であ
って、同心に配置されている内軸４４と外軸４５とが、
伝動装置４６，４７により夫々同方向に異なる回転速度
で回転駆動されるようになっていて、内軸４４の端部に
は、コーン状のスクリュー４８が固着されており、外軸
４５の端部には、スクリュー４８の外側に間隔をおいて
配置されているコーン状に形成された透水構造のバスケ
ット４９が固着されており、スクリュー４８の外面に
は、螺旋状のスクレーパ５０が形成されている。FIG. 2 is a sectional view showing an example of the filter 41, in which an inner shaft 44 and an outer shaft 45 arranged concentrically are
The transmissions 46 and 47 are rotationally driven in the same direction at different rotational speeds, and a cone-shaped screw 48 is fixed to the end of the inner shaft 44 and the end of the outer shaft 45. A cone-shaped basket 49 having a water-permeable structure, which is arranged on the outside of the screw 48 at a distance, is fixed to the screw 48, and a spiral scraper 50 is formed on the outer surface of the screw 48. .
【００２９】而して、再生塔２２内の吸収液２３を処理
液導入管４２を通してスクリュー４８とバスケット４９
の間に供給すると、吸収液２３は遠心力でバスケット４
９の内面に飛ばされ、液体分はバスケット４９を通過し
て分離液吐出管４３から排出され、吸収液２３中の固形
分はバスケット４９の内面に付着して、異速で回転して
いるスクレーパ５０で掻き落とされ、固形分吐出管５１
から吐出されるようになっている。Then, the absorption liquid 23 in the regeneration tower 22 is passed through the processing liquid introducing pipe 42 and the screw 48 and the basket 49.
When it is supplied to the basket 4, the absorption liquid 23 is centrifugally applied.
9, the liquid content passes through the basket 49 and is discharged from the separated liquid discharge pipe 43, and the solid content in the absorbing liquid 23 adheres to the inner surface of the basket 49 and rotates at a different speed. Solid content discharge pipe 51 scraped off with 50
It is designed to be discharged from.
【００３０】以下、本形態例の作用について説明する。The operation of this embodiment will be described below.
【００３１】セメント製造設備２４においては、従来の
セメント製造設備と同様に、粉末のセメント原料４がプ
レヒータ３で上昇してくる高温ガスと熱交換されること
により予熱され、仮焼炉５により仮焼された後にセメン
ト焼成炉１６で焼成されてセメントクリンカ７とされ、
該セメントクリンカ７が冷却装置１７で冷却空気９と熱
交換されることにより冷却される。In the cement manufacturing equipment 24, as in the conventional cement manufacturing equipment, the powdered cement raw material 4 is preheated by exchanging heat with the rising high temperature gas in the preheater 3 and is temporarily heated in the calcining furnace 5. After being fired, it is fired in the cement firing furnace 16 to obtain the cement clinker 7,
The cement clinker 7 is cooled by exchanging heat with the cooling air 9 in the cooling device 17.
【００３２】一方、冷却装置１７でセメントクリンカ７
との熱交換により高温となった空気９は、セメント焼成
炉１６及び燃焼空気送入管１２を通って仮焼炉５の仮焼
バーナ１３に供給され、更にプレヒータ３を上昇しなが
らセメント原料４を予熱した後、排風機１から３２０℃
前後の温度の排ガス２０として排ガス導入管３４に排出
される。On the other hand, the cement clinker 7 is cooled by the cooling device 17.
The air 9 having a high temperature due to heat exchange with the cement raw material 4 is supplied to the calcination burner 13 of the calcination furnace 5 through the cement calcination furnace 16 and the combustion air inlet pipe 12, and the cement raw material 4 is further raised while rising the preheater 3. After preheating, the blower 1 to 320 ℃
The exhaust gas 20 having the temperatures around the exhaust gas is discharged to the exhaust gas introduction pipe 34.
【００３３】前記排ガス導入管３４に入った排ガス２０
は、再生塔２２内の吸収液２３中にを経由して再生塔２
２内の吸収液２３を加熱し、１００℃前後に温度が降下
した状態で吸収塔２１内の吸収液２３の中に導入され
る。Exhaust gas 20 entering the exhaust gas introduction pipe 34
Via the absorption liquid 23 in the regeneration tower 22 via the regeneration tower 2
The absorption liquid 23 in 2 is heated and introduced into the absorption liquid 23 in the absorption tower 21 in a state where the temperature is lowered to around 100 ° C.
【００３４】吸収塔２１内の吸収液２３の中に導入され
た排ガス２０は、前記吸収液２３により二酸化炭素を吸
収され、二酸化炭素の除去されたガスは吸収液２３内を
上昇し、処理ガス排出管３５から大気中に放出される。The exhaust gas 20 introduced into the absorption liquid 23 in the absorption tower 21 absorbs carbon dioxide by the absorption liquid 23, and the gas from which the carbon dioxide has been removed rises in the absorption liquid 23 and is treated gas. It is discharged from the discharge pipe 35 into the atmosphere.
【００３５】一方、吸収塔２１内で二酸化炭素を吸収し
た吸収液２３は、導管３１のポンプ３２により熱交換器
２８に送られ、加熱された後、噴霧器３３から再生塔２
２内に噴霧され、二酸化炭素の揮発を促進される。On the other hand, the absorption liquid 23 which has absorbed carbon dioxide in the absorption tower 21 is sent to the heat exchanger 28 by the pump 32 of the conduit 31 and heated, and then is sprayed from the sprayer 33 to the regeneration tower 2.
2 is sprayed and the volatilization of carbon dioxide is promoted.
【００３６】更に、再生塔２２の下部に貯留した吸収液
２３は、再生塔２２の下部を経由する排ガス導入管３４
を流れる排ガス２０によって加熱され、７０℃〜１１０
℃の範囲の温度で吸収液２３中の二酸化炭素が揮発さ
れ、再生塔２２内を上昇して二酸化炭素回収管３６によ
り回収され、ドライアイス等の原料に活用される。Further, the absorption liquid 23 stored in the lower portion of the regeneration tower 22 is exhaust gas introduction pipe 34 passing through the lower portion of the regeneration tower 22.
Heated by the exhaust gas 20 flowing through
Carbon dioxide in the absorbing liquid 23 is volatilized at a temperature in the range of ° C, rises in the regeneration tower 22 and is recovered by the carbon dioxide recovery pipe 36, and is utilized as a raw material such as dry ice.
【００３７】また、二酸化炭素を除かれて再生された吸
収液２３は、導管２６のポンプ２７により、熱交換器２
８、冷却器２９を通されて冷却された後、吸収塔２１内
の上部に設けられている噴霧器３０から吸収塔２１内に
噴霧され、再び二酸化炭素の吸収に使用される。The absorption liquid 23 regenerated by removing carbon dioxide is supplied to the heat exchanger 2 by the pump 27 of the conduit 26.
8. After being cooled by being passed through the cooler 29, it is sprayed into the absorption tower 21 from the sprayer 30 provided in the upper part of the absorption tower 21 and used again for absorbing carbon dioxide.
【００３８】ここで、排ガス導入管３４を流れる排ガス
２０のみでは、再生塔２２内の吸収液２３の加熱が不十
分で、吸収液２３中の二酸化炭素を揮発しきれない時に
は、高温空気導入管３８の送風機３９を作動させ、クー
ラー排ガス管１４’を通る２３０℃前後の温度になって
いる高温の空気９の一部を、再生塔２２下部を経由する
高温空気導入管３８に通し、再生塔２２内の吸収液の加
熱度を高める。Here, when the heating of the absorption liquid 23 in the regeneration tower 22 is insufficient with only the exhaust gas 20 flowing through the exhaust gas introduction pipe 34 and the carbon dioxide in the absorption liquid 23 cannot be completely volatilized, the high temperature air introduction pipe The blower 39 of 38 is operated to pass a part of the high temperature air 9 passing through the cooler exhaust gas pipe 14 ′ and having a temperature of around 230 ° C. through the high temperature air introduction pipe 38 passing through the lower part of the regeneration tower 22 and The degree of heating of the absorbing liquid in 22 is increased.
【００３９】また、排ガス導入管３４を流れる排ガス２
０による加熱と、高温空気導入管３８を流れる高温の空
気９による加熱とを併用しても、なお再生塔２２内の吸
収液の加熱が不十分な場合があれば、初めて従来と同様
に蒸気等を使用した加熱器２５で加熱する。Further, the exhaust gas 2 flowing through the exhaust gas introducing pipe 34
Even if the heating by the high temperature air 9 flowing through the high temperature air introducing pipe 38 is used in combination with the heating by 0, if the heating of the absorbing liquid in the regeneration tower 22 is still insufficient, the steam will be used for the first time as in the conventional case. It is heated by the heater 25 using the above.
【００４０】このように、排ガス２０並びに高温の空気
９の熱を有効利用して再生塔２２内の吸収液２３を加熱
することが可能な為、蒸気等の熱源が必要な加熱器２５
の使用は激減し、再生塔２２に導かれた吸収液２３を再
生する際の熱エネルギーを著しく軽減することができ、
排ガス２０から二酸化炭素を安価に除去することができ
る。As described above, since the heat of the exhaust gas 20 and the high temperature air 9 can be effectively used to heat the absorbing liquid 23 in the regeneration tower 22, the heater 25 requiring a heat source such as steam is required.
Is drastically reduced, and the heat energy at the time of regenerating the absorption liquid 23 guided to the regeneration tower 22 can be remarkably reduced.
Carbon dioxide can be removed from the exhaust gas 20 at low cost.
【００４１】また、プレヒータ３を上昇しながらセメン
ト原料４を予熱する空気は、ダスト沈降室１１やサイク
ロン２で粉末のセメント原料４を除去してはいるが、排
風機１から排ガス導入管３４に排出される排ガス２０中
には、なお５０ｍｇ／Ｎｍ3程度のセメント原料粉を含
んでいる。The air for preheating the cement raw material 4 while raising the preheater 3 removes the powdered cement raw material 4 in the dust settling chamber 11 and the cyclone 2, but from the exhauster 1 to the exhaust gas introducing pipe 34. The exhaust gas 20 discharged still contains about 50 mg / Nm 3 of cement raw material powder.
【００４２】このような排ガス２０を吸収塔２１内の吸
収液２３の中に排出し、更に吸収塔２１内の吸収液２３
を再生塔２２内の吸収液２３に混入して、排ガス２０の
二酸化炭素除去に循環使用していると、吸収液２３のセ
メント原料粉含有濃度が次第に高くなり、吸収液２３の
性能が劣化して排ガス２０の二酸化炭素除去が十分に行
えなくなる。The exhaust gas 20 is discharged into the absorption liquid 23 in the absorption tower 21, and the absorption liquid 23 in the absorption tower 21 is further discharged.
When mixed with the absorption liquid 23 in the regeneration tower 22 and circulated and used for removing carbon dioxide of the exhaust gas 20, the cement raw material powder content concentration of the absorption liquid 23 gradually increases and the performance of the absorption liquid 23 deteriorates. As a result, the carbon dioxide in the exhaust gas 20 cannot be sufficiently removed.
【００４３】そこで濾過機４１を作動させると、再生塔
２２内の吸収液２３は処理液導入管４２を通って濾過機
４１内に入り、図２に示すスクリュー４８とバスケット
４９の間に供給され、バスケット４９を通過してセメン
ト原料粉が除去された液体分のみが、分離液吐出管４３
から再び再生塔２２内に戻され、吸収液２３中に混入し
ていたセメント原料粉はスクレーパ５０で掻き落とさ
れ、固形分吐出管５１から吐出されて処分される。Then, when the filter 41 is operated, the absorption liquid 23 in the regeneration tower 22 enters the filter 41 through the treatment liquid introducing pipe 42 and is supplied between the screw 48 and the basket 49 shown in FIG. Only the liquid component which has passed through the basket 49 and from which the cement raw material powder has been removed is separated liquid discharge pipe 43.
Is returned to the inside of the regeneration tower 22 again, the cement raw material powder mixed in the absorbing liquid 23 is scraped off by the scraper 50, discharged from the solid content discharge pipe 51, and disposed of.
【００４４】これによって、吸収液２３中のセメント原
料粉が除去される為、吸収液２３はセメント原料粉含有
濃度が高くならず、長期にわたって使用することが可能
になる。As a result, the cement raw material powder in the absorbing liquid 23 is removed, so that the absorbing liquid 23 does not have a high cement raw material powder content concentration and can be used for a long period of time.
【００４５】尚、本発明のセメント製造設備は、上述の
形態例にのみ限定されるものではなく、本発明の要旨を
逸脱しない範囲内において種々変更を加え得ることは勿
論である。The cement production equipment of the present invention is not limited to the above-mentioned embodiment, and various modifications can be made without departing from the gist of the present invention.
【００４６】[0046]
【発明の効果】上記した本発明のセメント製造設備によ
れば、下記の如き種々の優れた効果を奏し得る。According to the cement production facility of the present invention described above, various excellent effects as described below can be obtained.
【００４７】（Ｉ）本発明の請求項１に記載の発明によ
れば、プレヒータからの排ガスが、排ガス導入管を介し
再生塔を経由され、加熱源として利用されてから前記吸
収塔に導かれるので、該吸収塔で排ガスから二酸化炭素
を吸収して再生塔に導かれた吸収液を再生する際の熱エ
ネルギーを著しく軽減することができ、排ガスから二酸
化炭素を安価に除去することができる。(I) According to the invention described in claim 1 of the present invention, the exhaust gas from the preheater is introduced into the absorption tower after being used as a heating source after passing through the regeneration tower through the exhaust gas introduction pipe. Therefore, it is possible to remarkably reduce the thermal energy when the absorption tower absorbs carbon dioxide from the exhaust gas and regenerates the absorption liquid guided to the regeneration tower, and it is possible to remove the carbon dioxide from the exhaust gas at a low cost.
【００４８】（ＩＩ）本発明の請求項２に記載の発明に
よれば、冷却装置でセメントクリンカとの熱交換により
高温となった空気の一部を迂回させて再生塔の下部を経
由させることにより、前記再生塔に導かれた吸収液を再
生する際の熱エネルギーを一層軽減することができる。(II) According to the invention described in claim 2 of the present invention, a part of the air heated to a high temperature due to heat exchange with the cement clinker in the cooling device is diverted to pass through the lower part of the regeneration tower. This makes it possible to further reduce the heat energy when regenerating the absorption liquid guided to the regeneration tower.
【００４９】（ＩＩＩ）本発明の請求項３に記載の発明
によれば、再生塔内の吸収液中に混入したセメント原料
粉を濾過機によって除去し、吸収液を長期にわたって使
用することができる。(III) According to the invention described in claim 3 of the present invention, the cement raw material powder mixed in the absorption liquid in the regeneration tower can be removed by a filter, and the absorption liquid can be used for a long time. .
【図１】本発明を実施する形態の一例を示す系統図であ
る。FIG. 1 is a system diagram showing an example of an embodiment for implementing the present invention.
【図２】本発明に使用する濾過機の一例を示す概略断面
図である。FIG. 2 is a schematic sectional view showing an example of a filter used in the present invention.
【図３】従来のセメント製造設備の一例を示す系統図で
ある。FIG. 3 is a system diagram showing an example of a conventional cement manufacturing facility.
【図４】従来から使用されている二酸化炭素処理装置の
一例を示す系統図である。FIG. 4 is a system diagram showing an example of a carbon dioxide treatment device that has been conventionally used.
３ プレヒータ ４ セメント原料 ７ セメントクリンカ ９ 冷却空気 １０ 焼成バーナ １６ セメント焼成炉 １７ 冷却装置 ２０ 排ガス ２１ 吸収塔 ２２ 再生塔 ２３ 吸収液 ２４ セメント製造設備 ２８ 熱交換器 ３４ 排ガス導入管 ３８ 高温空気導入管 ４１ 濾過機 3 Preheater 4 Cement raw material 7 Cement clinker 9 Cooling air 10 Burning burner 16 Cement burning furnace 17 Cooling device 20 Exhaust gas 21 Absorption tower 22 Regeneration tower 23 Absorption liquid 24 Cement manufacturing facility 28 Heat exchanger 34 Exhaust gas introduction pipe 38 High temperature air introduction pipe 41 Filter
Claims (3)
熱するプレヒータと、 該プレヒータからのセメント原料を焼成バーナにより焼
成してセメントクリンカとし且つ前記焼成バーナの燃焼
排ガスを前記プレヒータに予熱用高温ガスとして導くセ
メント焼成炉と、 該セメント焼成炉からのセメントクリンカを冷却空気と
熱交換して冷却し且つ前記セメントクリンカとの熱交換
により高温となった空気の一部を前記セメント焼成炉に
バーナ燃焼用空気として導く冷却装置とを備えたセメン
ト製造設備であって、 二酸化炭素を吸収する吸収液を貯留した吸収塔と、 該吸収塔から熱交換器を介して導いた吸収液を加熱する
ことにより二酸化炭素を揮発させ且つ前記熱交換器を介
して吸収液を吸収塔に戻す再生塔とを備え、 前記プレヒータからの排ガスを前記再生塔を経由させて
加熱源として利用してから前記吸収塔に導く排ガス導入
管を設けたことを特徴とするセメント製造設備。1. A preheater for preheating a cement raw material by exchanging heat with a high-temperature gas, a cement raw material from the preheater being burned by a burning burner into a cement clinker, and combustion exhaust gas of the burning burner being preheated to the preheater. A cement calcination furnace that is introduced as a gas, and a cement clinker from the cement calcination furnace is cooled by exchanging heat with cooling air, and a part of the air heated to a high temperature by heat exchange with the cement clinker is burned to the cement calcination furnace. A cement manufacturing facility comprising a cooling device for guiding as combustion air, wherein an absorption tower storing an absorption liquid that absorbs carbon dioxide, and heating the absorption liquid guided from the absorption tower via a heat exchanger. And a regeneration tower that volatilizes carbon dioxide by means of the heat exchanger and returns the absorption liquid to the absorption tower via the heat exchanger. Cement manufacturing facility to a scan from using as a heat source by way of the regeneration tower characterized in that a gas inlet pipe leading to the absorption column.
により高温となった空気の一部を迂回させて再生塔の下
部を経由させる高温空気導入管を設けたことを特徴とす
る請求項１に記載のセメント製造設備。2. A high-temperature air introduction pipe is provided in the cooling device, which bypasses a part of the air heated to a high temperature by heat exchange with the cement clinker and passes through the lower part of the regeneration tower. Cement production equipment described.
過機を前記再生塔に備えたことを特徴とする請求項１又
は２に記載のセメント製造設備。3. The cement manufacturing facility according to claim 1, wherein the regeneration tower is equipped with a filter for removing powder in the absorption liquid in the regeneration tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP26146195A JPH09110485A (en) | 1995-10-09 | 1995-10-09 | Cement production equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP26146195A JPH09110485A (en) | 1995-10-09 | 1995-10-09 | Cement production equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH09110485A true JPH09110485A (en) | 1997-04-28 |
Family
ID=17362225
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP26146195A Pending JPH09110485A (en) | 1995-10-09 | 1995-10-09 | Cement production equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH09110485A (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6908507B2 (en) | 2001-04-13 | 2005-06-21 | Co2 Solution Inc. | Process and a plant for the production of Portland cement clinker |
| WO2008056068A1 (en) * | 2006-11-09 | 2008-05-15 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process for manufacturing clinker with controlled co2 emission |
| CN100451519C (en) * | 2006-12-31 | 2009-01-14 | 北京市琉璃河水泥有限公司 | Residual heat generating system used for new type nonaqueous cement production line |
| FR2921059A1 (en) * | 2007-09-14 | 2009-03-20 | Rech S Geol Et Minieres Brgm E | Production of clinker, comprises preparing calcium oxide material by producing flue gases that are used for direct/indirect heating of reactor for decarbonation of calcium carbonate, and blending calcium oxide material to form the clinker |
| WO2009136485A1 (en) * | 2008-05-07 | 2009-11-12 | 三菱マテリアル株式会社 | Method and apparatus for recovering co2 gas in cement production equipment |
| JP2009269785A (en) * | 2008-05-07 | 2009-11-19 | Mitsubishi Materials Corp | Method and apparatus for recovering co2 gas in cement production equipment |
| JP2009269784A (en) * | 2008-05-07 | 2009-11-19 | Mitsubishi Materials Corp | Recovery method and recovery equipment of co2 gas in cement manufacturing facility |
| JP2009292715A (en) * | 2008-05-07 | 2009-12-17 | Mitsubishi Materials Corp | Method and apparatus for recovering co2 gas in cement production equipment |
| WO2010012880A1 (en) * | 2008-08-01 | 2010-02-04 | Fives Fcb | Process for manufacturing cement clinker in a plant, and cement clinker manufacturing plant as such |
| WO2011048770A1 (en) * | 2009-10-20 | 2011-04-28 | 三菱マテリアル株式会社 | Methods and systems for recovery of co2 gas in cement-manufacturing facilities, and processes for manufacturing cement |
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| JP2011529845A (en) * | 2008-08-01 | 2011-12-15 | フィーヴ エフセーベー | Cement clinker manufacturing method in equipment and such cement clinker manufacturing equipment |
-
1995
- 1995-10-09 JP JP26146195A patent/JPH09110485A/en active Pending
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| US6908507B2 (en) | 2001-04-13 | 2005-06-21 | Co2 Solution Inc. | Process and a plant for the production of Portland cement clinker |
| WO2008056068A1 (en) * | 2006-11-09 | 2008-05-15 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process for manufacturing clinker with controlled co2 emission |
| FR2908327A1 (en) * | 2006-11-09 | 2008-05-16 | Air Liquide | PROCESS FOR MANUFACTURING CLINKER WITH CONTROLLED CO2 EMISSION |
| JP2010509166A (en) * | 2006-11-09 | 2010-03-25 | レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Method for producing clinker with controlled CO2 release |
| US8187374B2 (en) | 2006-11-09 | 2012-05-29 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process for manufacturing clinker with controlled CO2 emission |
| CN100451519C (en) * | 2006-12-31 | 2009-01-14 | 北京市琉璃河水泥有限公司 | Residual heat generating system used for new type nonaqueous cement production line |
| FR2921059A1 (en) * | 2007-09-14 | 2009-03-20 | Rech S Geol Et Minieres Brgm E | Production of clinker, comprises preparing calcium oxide material by producing flue gases that are used for direct/indirect heating of reactor for decarbonation of calcium carbonate, and blending calcium oxide material to form the clinker |
| JP2009269785A (en) * | 2008-05-07 | 2009-11-19 | Mitsubishi Materials Corp | Method and apparatus for recovering co2 gas in cement production equipment |
| JP2009292715A (en) * | 2008-05-07 | 2009-12-17 | Mitsubishi Materials Corp | Method and apparatus for recovering co2 gas in cement production equipment |
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| WO2009136485A1 (en) * | 2008-05-07 | 2009-11-12 | 三菱マテリアル株式会社 | Method and apparatus for recovering co2 gas in cement production equipment |
| CN102015568A (en) * | 2008-05-07 | 2011-04-13 | 三菱综合材料株式会社 | Method and apparatus for recovering co2 gas in cement production equipment |
| US8617506B2 (en) | 2008-05-07 | 2013-12-31 | Mitsubishi Materials Corporation | Method and facility for recovering CO2 gas in cement manufacturing facility |
| FR2934589A1 (en) * | 2008-08-01 | 2010-02-05 | Fives Fcb | METHOD FOR MANUFACTURING CEMENT CLINKER IN AN INSTALLATION, AND CEMENT CLINKER MANUFACTURING PLANT AS SUCH |
| CN102112834A (en) * | 2008-08-01 | 2011-06-29 | 菲弗斯有限公司 | Process for manufacturing cement clinker in plant, and cement clinker manufacturing plant as such |
| JP2011529844A (en) * | 2008-08-01 | 2011-12-15 | フィーヴ エフセーベー | Method for producing cement clinker in the facility and such cement clinker production facility |
| JP2011529845A (en) * | 2008-08-01 | 2011-12-15 | フィーヴ エフセーベー | Cement clinker manufacturing method in equipment and such cement clinker manufacturing equipment |
| US8647430B2 (en) | 2008-08-01 | 2014-02-11 | Fives Fcb | Process for manufacturing cement clinker in a plant, and cement clinker manufacturing plant as such |
| WO2010012880A1 (en) * | 2008-08-01 | 2010-02-04 | Fives Fcb | Process for manufacturing cement clinker in a plant, and cement clinker manufacturing plant as such |
| JP2011088760A (en) * | 2009-10-20 | 2011-05-06 | Mitsubishi Materials Corp | Recovery method and recovery equipment of co2 gas in cement producing equipment and method for producing cement |
| WO2011048770A1 (en) * | 2009-10-20 | 2011-04-28 | 三菱マテリアル株式会社 | Methods and systems for recovery of co2 gas in cement-manufacturing facilities, and processes for manufacturing cement |
| US9028249B2 (en) | 2009-10-20 | 2015-05-12 | Mitsubishi Materials Corporation | Methods and systems for recovery of CO2 gas in cement-manufacturing facilities, and processes for manufacturing cement |
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