JPH0223210B2 - - Google Patents
Info
- Publication number
- JPH0223210B2 JPH0223210B2 JP55080956A JP8095680A JPH0223210B2 JP H0223210 B2 JPH0223210 B2 JP H0223210B2 JP 55080956 A JP55080956 A JP 55080956A JP 8095680 A JP8095680 A JP 8095680A JP H0223210 B2 JPH0223210 B2 JP H0223210B2
- Authority
- JP
- Japan
- Prior art keywords
- clinker
- gas
- air chamber
- layer
- malodorous
- 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 - Lifetime
Links
- 239000007789 gas Substances 0.000 claims description 32
- 238000011084 recovery Methods 0.000 claims description 14
- 239000002918 waste heat Substances 0.000 claims description 12
- 238000001816 cooling Methods 0.000 claims description 10
- 238000011144 upstream manufacturing Methods 0.000 claims description 9
- 238000000354 decomposition reaction Methods 0.000 claims description 3
- 239000000112 cooling gas Substances 0.000 claims 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 14
- 235000012255 calcium oxide Nutrition 0.000 description 7
- 239000000292 calcium oxide Substances 0.000 description 7
- 238000002485 combustion reaction Methods 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 239000000446 fuel Substances 0.000 description 4
- 238000010411 cooking Methods 0.000 description 3
- 238000005192 partition Methods 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- QMMFVYPAHWMCMS-UHFFFAOYSA-N Dimethyl sulfide Chemical compound CSC QMMFVYPAHWMCMS-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- WQOXQRCZOLPYPM-UHFFFAOYSA-N dimethyl disulfide Chemical compound CSSC WQOXQRCZOLPYPM-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 241000202567 Fatsia japonica Species 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 1
- 230000009965 odorless effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
Description
【発明の詳細な説明】
この発明は廃熱回収装置に係り、特に製紙プラ
ントにおいて焼成された生石灰を冷却する際工場
内他の工程において発生した悪臭ガスを同時に熱
分解する廃熱回収装置に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a waste heat recovery device, and more particularly to a waste heat recovery device that simultaneously thermally decomposes malodorous gases generated in other processes within the factory when cooling calcined lime in a paper manufacturing plant.
製紙プラントにおける苛性プロセスの一部とし
て石灰石（CaCO3）を焼成して生石灰（CaO）
を製造するが、この際キルンより排出されるCaO
は例えば約1000〜1100℃の高温となつている。こ
のためCaOの有する熱を回収するとともにCaOを
冷却し、かつキルンで消費する燃料の節減を図る
装置が提供されている。第１図は現在使用されて
いる装置を示し、ロータリキルン１から排出され
たCaO等の焼塊（以下「クリンカ」と称する）は
スロート部２を経て廃熱回収装置本体３内に落下
する。廃熱回収装置本体３には油圧シリンダ等の
駆動装置５により作動する可動グレート４ａと、
固定グレート４ｂが交互に配置してある。装置内
に落下し層を形成したクリンカ８はこのグレート
４ａ，４ｂにより徐々に排出端（図の右側）に移
動される。この移動の間にグレート４ａ，４ｂの
下部に形成した空気室７内の冷却空気は各グレー
トを経てクリンカ８の層内を通過し、クリンカ８
を冷却する。一方昇温した冷却用空気はロータリ
キルン１に燃焼用二次空気として流入し、ロータ
リキルン１で使用する燃料の量を節減する。一方
パルプの蒸解過程からは種々の成分から成る悪臭
ガスが発生するが、この悪臭ガス処理の一つとし
て悪臭ガスを燃焼用空気としてロータリキルンに
直接供給し熱分解する方法がある。しかしこの悪
臭ガスの供給はクリンカの熱回収には何等役立つ
ていないのみならず、比較的低温であるため、キ
ルン内の燃焼にかえつて悪影響を与える。さらに
はキルンに供給する二次空気（クリンカと熱交換
を行つた冷却用空気）の導入量を減少させること
になり、熱回収効率の低下をきたすことになる。 Calcining limestone (CaCO 3 ) to produce quicklime (CaO) as part of the caustic process in paper plants
The CaO discharged from the kiln is
For example, the temperature is about 1000-1100℃. For this reason, devices have been provided that recover the heat possessed by CaO, cool CaO, and reduce the amount of fuel consumed in the kiln. FIG. 1 shows an apparatus currently in use, in which baked ingots such as CaO (hereinafter referred to as "clinker") discharged from a rotary kiln 1 pass through a throat section 2 and fall into a waste heat recovery apparatus main body 3. The waste heat recovery device main body 3 includes a movable grate 4a operated by a drive device 5 such as a hydraulic cylinder,
Fixed grates 4b are arranged alternately. The clinker 8 that has fallen into the apparatus and formed a layer is gradually moved to the discharge end (to the right in the figure) by the grates 4a and 4b. During this movement, the cooling air in the air chamber 7 formed at the bottom of the grates 4a and 4b passes through each grate and through the layer of clinker 8.
to cool down. On the other hand, the heated cooling air flows into the rotary kiln 1 as secondary combustion air, thereby reducing the amount of fuel used in the rotary kiln 1. On the other hand, a malodorous gas composed of various components is generated from the pulp cooking process, and one method for treating this malodorous gas is to directly supply the malodorous gas as combustion air to a rotary kiln and thermally decompose it. However, the supply of this foul-smelling gas not only does not help in any way to recover heat from the clinker, but also has a negative effect on the combustion within the kiln since the temperature is relatively low. Furthermore, the amount of secondary air (cooling air that has exchanged heat with the clinker) introduced to the kiln is reduced, resulting in a decrease in heat recovery efficiency.
この発明の目的は上述した従来技術の欠点をな
くし、クリンカの冷却に際し悪臭ガス自身の燃焼
熱を利用し、装置のクリンカの冷却と同時に熱回
収効率を高める廃熱回収装置に関する。 The object of the present invention is to eliminate the above-mentioned drawbacks of the prior art, and to relate to a waste heat recovery device that utilizes the combustion heat of malodorous gas itself to cool the clinker, thereby increasing heat recovery efficiency at the same time as cooling the clinker of the device.
要するにこの発明はグレート下部、特にクリン
カの移動方向の上流側、すなわち高温部側に悪臭
ガスと冷却空気の混合した気体を導入する空気室
を形成し、この気体と熱交換させ、かつこの高温
側クリンカにより悪臭ガスを熱分解して二次空気
を昇温させ分解熱を利用するよう構成したもので
ある。 In short, this invention forms an air chamber in which a mixture of foul-smelling gas and cooling air is introduced into the lower part of the grate, particularly on the upstream side in the direction of clinker movement, that is, on the high-temperature side, and exchanges heat with this gas, and also on the high-temperature side. The structure is such that clinker thermally decomposes foul-smelling gas, raises the temperature of secondary air, and utilizes the heat of decomposition.
以下この発明の実施例を図面により説明する。 Embodiments of the present invention will be described below with reference to the drawings.
第２図において、ヒータ１１に対して供給した
蒸気Ｓにより加熱された蒸解液は蒸解缶１０に流
入し内部に充填したチツプパルプを通過して循環
流動する。これにより蒸解缶１０内のパルプは最
高温度約130℃〜145℃で所定時間で蒸解される。
この蒸解過程においては、通常悪臭ガスと総称さ
れるガスが排出される。このガスの組成物として
はメチルメルカブタン（CH3SH）硫化メチル
〔（CH3）2S〕、二硫化メチル（CH3SSCH3）、硫化
水素（H2S）等がある。この悪臭ガスは悪臭ガス
排出ダクト１２、フアン１３を経て廃熱回収装置
３に至る。廃熱回収装置３のグレート下部に形成
した空気室はクリンカ流れの上流側と下流側の二
つに分割されている。このうち上流側空気室７ａ
に対しては前記悪臭ガス排出ダクト１２が接続し
ている。つまり悪臭ガスを高温のクリンカ層（ク
リンカ流れの上流側）を通過させることにより効
果的に熱分解させるよう構成している。ここで例
えば硫化メチルの発火点は205℃、硫化水素は260
℃であるので悪臭ガスの熱分解可能域はクリンカ
温度が前記発火点以上の部分ということになる。
従つて上流側空気室７ａの形成範囲は好ましくは
空気室仕切壁１７は前記発火点温度に対応する位
置に選定する。即ちクリンカ流れに従つてみると
最大限前記発火点までの上流側部分である。また
悪臭ガスの処理量に応じて形成範囲を適当に設定
してもよい。なお、冷却すべきクリンカは、通常
ロータリキルン１から排出された時点で約1000
℃、廃熱回収装置から排出される際の温度は200
℃程度である。以上の装置において、上流側空気
室７ａ内の悪臭ガスはグレート４ａ，４ｂを経て
クリンカ８の層中を通過し、クリンカ８を冷却し
悪臭ガス自身は昇温してクリンカ８の表面におい
て燃焼して悪臭の分解を行う。クリンカ８と熱交
換し、かつ主としてクリンカ層上で燃焼すること
により昇温し分解したガスはロータリキルン１に
二次空気として流入し、ロータリキルン１の燃料
使用量を節減する一方クリンカによりなお熱分解
されなかつた悪臭成分はキルン内で完全分解され
無臭ガスとなる。またクリンカ８に対して供給す
る悪臭ガスの量が多すぎる場合にはダクト１２ａ
により一部を別の処理システムに送つても良い。
また反対に処理量が少い場合、および悪臭ガス自
体の酸素含有量が少い場合にはフアン１４から供
給される冷却空気Ａを導入する。次に下流側空気
室７ｂに対してはこのフアン１４から供給される
冷却空気Ａが供給されクリンカ８を所定温度まで
冷却した後CaO層上空間でかつ仕切壁１７に対応
する位置にある仕切壁１５より右方の悪臭ガスと
は反対に排出口１６から外部に排出される。この
昇温した空気は悪臭ガスを含まぬ故大気放出に支
障はない。 In FIG. 2, the cooking liquor heated by the steam S supplied to the heater 11 flows into the digester 10 and circulates through the chip pulp filled inside. As a result, the pulp in the digester 10 is cooked at a maximum temperature of about 130° C. to 145° C. for a predetermined period of time.
During this cooking process, gases generally referred to as malodorous gases are emitted. The composition of this gas includes methyl mercabutane (CH3SH), methyl sulfide [(CH 3 ) 2 S], methyl disulfide (CH 3 SSCH 3 ), hydrogen sulfide (H 2 S), and the like. This malodorous gas reaches the waste heat recovery device 3 via the malodorous gas discharge duct 12 and the fan 13. The air chamber formed in the lower part of the grate of the waste heat recovery device 3 is divided into two, an upstream side and a downstream side of the clinker flow. Of these, the upstream air chamber 7a
The foul-smelling gas exhaust duct 12 is connected to. In other words, it is configured to effectively thermally decompose the foul-smelling gas by passing it through a high-temperature clinker layer (on the upstream side of the clinker flow). For example, the ignition point of methyl sulfide is 205℃, and that of hydrogen sulfide is 260℃.
℃, the range where malodorous gas can be thermally decomposed is the area where the clinker temperature is above the ignition point.
Therefore, the formation range of the upstream air chamber 7a is preferably such that the air chamber partition wall 17 is located at a position corresponding to the ignition point temperature. That is, when looking at the clinker flow, it is the maximum upstream portion up to the ignition point. Further, the formation range may be appropriately set depending on the amount of malodorous gas to be processed. The amount of clinker to be cooled is usually about 1000 ml when it is discharged from rotary kiln 1.
℃, the temperature when discharged from the waste heat recovery device is 200
It is about ℃. In the above device, the malodorous gas in the upstream air chamber 7a passes through the layers of the clinker 8 via the grates 4a and 4b, cools the clinker 8, and the malodorous gas itself heats up and burns on the surface of the clinker 8. to decompose the bad odor. The gas, which is heated and decomposed by exchanging heat with the clinker 8 and burning mainly on the clinker layer, flows into the rotary kiln 1 as secondary air, reducing the amount of fuel used in the rotary kiln 1, while still allowing heat to be generated by the clinker. Undecomposed malodorous components are completely decomposed in the kiln and become odorless gas. In addition, if the amount of malodorous gas supplied to the clinker 8 is too large, the duct 12a
A portion may be sent to another processing system.
On the other hand, when the amount to be treated is small or when the oxygen content of the malodorous gas itself is low, cooling air A supplied from the fan 14 is introduced. Next, the cooling air A supplied from this fan 14 is supplied to the downstream air chamber 7b, and after cooling the clinker 8 to a predetermined temperature, a partition wall located in the space above the CaO layer and at a position corresponding to the partition wall 17 Opposite to the foul-smelling gas to the right of 15, it is discharged to the outside from the discharge port 16. This heated air does not contain any foul-smelling gases, so there is no problem with releasing it into the atmosphere.
この発明によれば悪臭ガスをクリンカと熱交換
させることにより悪臭成分を熱分解して二次空気
として使用するので、二次空気温度が高くなり焼
成炉の燃料使用量を大巾に低減でき、しかもキル
ン内の燃焼を安定させることができる。また悪臭
成分の分解はクリンカおよび焼成炉（キルン）の
二段階で行われるのでより完全なものとなる。 According to this invention, the malodorous gas is thermally exchanged with the clinker to thermally decompose the malodorous components and used as secondary air, which increases the temperature of the secondary air and greatly reduces the amount of fuel used in the kiln. Furthermore, combustion within the kiln can be stabilized. Furthermore, the decomposition of malodorous components is carried out in two stages: clinker and kiln, making it more complete.
第１図は従来の廃熱回収装置の縦断面図、第２
図はこの発明に係る廃熱回収装置の系統図であ
る。
１……ロータリキルン、３……廃熱回収装置本
体、４ａ，４ｂ……グレート、７ａ……上流側空
気室、７ｂ……下流側空気室、８……クリンカ、
１２……悪臭ガス排出管。
Figure 1 is a vertical cross-sectional view of a conventional waste heat recovery device;
The figure is a system diagram of a waste heat recovery device according to the present invention. 1...Rotary kiln, 3...Waste heat recovery device main body, 4a, 4b...Grate, 7a...Upstream air chamber, 7b...Downstream air chamber, 8...Clinker,
12...Odor gas exhaust pipe.
Claims (1)
する間にクリンカ層下部に形成した空気室より冷
却気体をこの層を通過させクリンカを冷却し、冷
却気体はロータリキルン等の焼成炉用二次空気と
して利用するものにおいて、悪臭ガスの熱分解可
能な温度域におけるクリンカ層に悪臭ガスを含む
冷却気体を供給する上流側空気室を形成し、下流
側空気室には悪臭ガスを含まない冷却用空気を供
給するように構成したことを特徴とする悪臭ガス
分解廃熱回収装置。1 While the clinker such as CaO forms a layer and is transferred a certain distance, cooling gas is passed through this layer from the air chamber formed at the bottom of the clinker layer to cool the clinker. For those used as air, an upstream air chamber is formed that supplies cooling gas containing malodorous gas to the clinker layer in the temperature range where malodorous gas can be thermally decomposed, and a downstream air chamber is used for cooling that does not contain malodorous gas. A malodorous gas decomposition waste heat recovery device characterized by being configured to supply air.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP8095680A JPS577226A (en) | 1980-06-17 | 1980-06-17 | Apparatus for decomposing malodorant gas and recovering waste heat |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP8095680A JPS577226A (en) | 1980-06-17 | 1980-06-17 | Apparatus for decomposing malodorant gas and recovering waste heat |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS577226A JPS577226A (en) | 1982-01-14 |
| JPH0223210B2 true JPH0223210B2 (en) | 1990-05-23 |
Family
ID=13732952
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP8095680A Granted JPS577226A (en) | 1980-06-17 | 1980-06-17 | Apparatus for decomposing malodorant gas and recovering waste heat |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS577226A (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63173411A (en) * | 1987-01-12 | 1988-07-18 | Murata Mfg Co Ltd | Veramic resonator |
| DE10113516A1 (en) * | 2001-03-20 | 2002-09-26 | Bmh Claudius Peters Gmbh | Cooling a pourable material, eg cement clinker, on an advancing grid, comprises passing a gas stream through the grid and the material |
| DE10117226A1 (en) * | 2001-04-06 | 2002-10-10 | Bmh Claudius Peters Gmbh | Cooling grate for bulk goods |
| DE102008010235B4 (en) * | 2008-02-21 | 2010-07-01 | Siemens Ag Österreich | Process for litter feeding in furnaces and firing plant |
| CN102124293B (en) * | 2008-06-26 | 2013-10-23 | Fl史密斯公司 | Method and cooler for cooling hot particulate material |
-
1980
- 1980-06-17 JP JP8095680A patent/JPS577226A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS577226A (en) | 1982-01-14 |
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