JPS62238893A - Combustion product recovery apparatus using alkali pulp waste liquor as fuel - Google Patents
Combustion product recovery apparatus using alkali pulp waste liquor as fuelInfo
- Publication number
- JPS62238893A JPS62238893A JP7983286A JP7983286A JPS62238893A JP S62238893 A JPS62238893 A JP S62238893A JP 7983286 A JP7983286 A JP 7983286A JP 7983286 A JP7983286 A JP 7983286A JP S62238893 A JPS62238893 A JP S62238893A
- Authority
- JP
- Japan
- Prior art keywords
- alkaline
- iron oxide
- combustion
- waste liquid
- exhaust gas
- 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.)
- Granted
Links
- 238000002485 combustion reaction Methods 0.000 title claims description 29
- 239000002699 waste material Substances 0.000 title claims description 17
- 238000011027 product recovery Methods 0.000 title claims description 6
- 239000000446 fuel Substances 0.000 title claims description 5
- 239000003513 alkali Substances 0.000 title claims 2
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims description 60
- 238000000034 method Methods 0.000 claims description 18
- 239000007788 liquid Substances 0.000 claims description 16
- 238000009993 causticizing Methods 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 13
- 239000000843 powder Substances 0.000 claims description 10
- 238000001035 drying Methods 0.000 claims description 8
- 239000003795 chemical substances by application Substances 0.000 claims description 7
- 239000008187 granular material Substances 0.000 claims description 7
- 239000002918 waste heat Substances 0.000 claims description 7
- 238000010411 cooking Methods 0.000 claims description 6
- 229920002522 Wood fibre Polymers 0.000 claims description 5
- 239000002025 wood fiber Substances 0.000 claims description 5
- 238000004061 bleaching Methods 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims description 2
- 230000000717 retained effect Effects 0.000 claims description 2
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 21
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 16
- 239000000428 dust Substances 0.000 description 11
- 238000002347 injection Methods 0.000 description 7
- 239000007924 injection Substances 0.000 description 7
- 229910052742 iron Inorganic materials 0.000 description 7
- 235000011121 sodium hydroxide Nutrition 0.000 description 7
- 239000011734 sodium Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 229910000462 iron(III) oxide hydroxide Inorganic materials 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000012256 powdered iron Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 150000003464 sulfur compounds Chemical class 0.000 description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000005469 granulation Methods 0.000 description 2
- 230000003179 granulation Effects 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 101100501252 Caenorhabditis elegans elo-4 gene Proteins 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- 235000012255 calcium oxide Nutrition 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000002655 kraft paper Substances 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000011819 refractory material Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
Landscapes
- Paper (AREA)
Abstract
(57)【要約】本公報は電子出願前の出願データであるた
め要約のデータは記録されません。(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、木材繊維、非木材繊維のアルカリ蒸解工程お
工び／またはこの繊維のアルカリ蒸解工程にヴ１き続く
漂白工程から排出される黒液と称される実質的に硫黄化
合物を含まない含水アルカリ性廃液を、酸化鉄（Ｆｅｗ
Ｏｓ ）を苛性化剤とする燃焼炉に導入して燃焼・反
応させ鉄酸ソーダ（ＮａｔＦｅ＊Ｏｎ）を生成せしめ、
この鉄酸ソーダを温水抽出して直接苛性ソーダ液を回収
する燃焼生成物回収装置に関するものである。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention is directed to the use of wood fibers and non-wood fibers in the alkaline cooking process and/or the bleaching process that follows the alkaline cooking process of these fibers. A water-containing alkaline waste liquid called black liquor, which is substantially free of sulfur compounds, is treated with iron oxide (Few).
Os ) is introduced into a combustion furnace using a causticizing agent to burn and react to produce sodium ferrate (NatFe*On),
The present invention relates to a combustion product recovery device that directly recovers a caustic soda solution by extracting this ferric acid sodium with hot water.
従来、クラフトパルプ法（ＫＰ法）での木材繊維の蒸解
工程から排出される黒液を濃縮して回収ボイラ炉内で還
元燃焼させ、Ｎａ、Ｉｓ、 Ｎａ１ＣＯ１などの薬品を
溶融状態で回収し、それを苛性化工程において苛性ソー
ダとして回収する方法として、石灰法が実用化されてい
る。Conventionally, the black liquor discharged from the wood fiber cooking process in the kraft pulp process (KP process) is concentrated and reduced and burned in a recovery boiler furnace to recover chemicals such as Na, Is, and Na1CO1 in a molten state. The lime method has been put into practical use as a method for recovering it as caustic soda in the causticizing process.
しかしこの石灰法においては、工程が複雑であること、
生石灰の再生にキルンを必要とし重油を用いること、さ
らには黒液中に硫黄化合物を含むので、臭気対策および
装置の腐食対策などが必要であった。However, in this lime method, the process is complicated,
Since quicklime regeneration requires a kiln and uses heavy oil, and the black liquor contains sulfur compounds, it was necessary to take measures against odor and equipment corrosion.
これらの欠点を解消するために、本発明者らは、回収ボ
イラ炉内で硫黄化合物を含まない黒液と苛性化剤を燃焼
・反応させ、反応生成物を温水抽出して直接パルプ蒸解
薬品とする苛性ソーダ液を回収し、沈殿した苛性化剤を
乾燥した後、回収ボイラへ循環再使用する直接苛性化法
を開発している。In order to overcome these drawbacks, the present inventors burned and reacted black liquor, which does not contain sulfur compounds, with a causticizing agent in a recovery boiler furnace, and extracted the reaction product with hot water to directly convert it into pulp cooking chemicals. We have developed a direct causticizing method in which the caustic soda solution is collected, the precipitated causticizing agent is dried, and then recycled to the recovery boiler for reuse.
すなわち、この方法は第３図に示すように、アルカリ性
廃液を濃縮装置１に導入し、蒸発、濃縮して７０〜８０
％の濃黒液とした後、 この濃黒液を流動床炉などの燃
焼炉２に供給するとともに、燃焼炉２に粒状酸化鉄（Ｆ
ｅｌｏｎ）を供給する。乙は酸化鉄バンカである。That is, in this method, as shown in Fig. 3, alkaline waste liquid is introduced into the concentrator 1, evaporated and concentrated to a concentration of 70 to 80%.
% of concentrated black liquor, this concentrated black liquor is supplied to a combustion furnace 2 such as a fluidized bed furnace, and granular iron oxide (F
elon). B is iron oxide banca.
燃焼炉２からの鉄酸ソーダを粒状物苛性化装置４に導入
して苛性ソーダと回収酸化鉄（粒状）とに抽出、分離し
、この回収酸化鉄を乾燥機５で乾燥して前記バンカ６へ
投入する。Ferric acid soda from the combustion furnace 2 is introduced into a granular material causticizing device 4 to extract and separate caustic soda and recovered iron oxide (granules), and this recovered iron oxide is dried in a dryer 5 and sent to the bunker 6. throw into.
一方、集じん機６で捕集されたダストの一部を粉状物苛
性化装置７に導入して苛性ソーダと回収酸化鉄（粉状）
とに抽出、分離し、この回収酸化鉄を乾燥部８ａおよび
造粒部８ｂからなる乾燥・造粒機８で乾燥・造粒して造
粒酸化鉄とし、これを燃焼炉２に供給する。また前記ダ
ストの残部を乾燥・造粒機８の造粒部８ｂに導入して造
粒酸化鉄とし、これを燃焼炉２に供給する。なおこれら
の反応式はつぎの如くである。On the other hand, a part of the dust collected by the dust collector 6 is introduced into the powder causticizing device 7 to produce caustic soda and recovered iron oxide (powder).
The recovered iron oxide is dried and granulated in a drying/granulating machine 8 consisting of a drying section 8a and a granulating section 8b to form granulated iron oxide, which is then supplied to the combustion furnace 2. Further, the remaining part of the dust is introduced into the granulating section 8b of the drying/granulating machine 8 to form granulated iron oxide, which is then supplied to the combustion furnace 2. Incidentally, these reaction formulas are as follows.
Ｎａ１ＯＯ１−）−’Ｆｅ１Ｏ１−＋ ＮａＪｅｌＯａ
＋ Ｃｏｔ （１）ＮａｌＯ＋ Ｆｅ２Ｏ２
−＋ＮａＪ’ｅｌＯ４（２）Ｎａ！Ｆｅ１０４ ＋Ｈ，
ｏ→２ Ｎａｏａ −１−ｐｅ、ｏ、 （３）〔
発明が解決しようとする問題点〕
しかし上記従来の方式は、濃縮装置で黒液濃度７０〜８
０％まで濃縮しなければならないので、多量の加熱蒸気
を必要とし、また粒状酸化鉄用の乾燥機、粉状酸化鉄用
の乾燥・造粒機を必要とするので、設備が複雑になって
設備費が高価となり、このためバルブ生産量１００Ｔ／
Ｄ前後以上の大容１規模の工場には適用できるが、パル
プ生産量３０〜１００Ｔ／Ｄ前後の比較的小容量規模の
工場には適さないという問題点を有している。Na1OO1-)-'Fe1O1-+ NaJelOa
+ Cot (1) NalO+ Fe2O2
-+NaJ'elO4(2)Na! Fe104 +H,
o → 2 Naoa -1-pe, o, (3) [
[Problems to be Solved by the Invention] However, in the above conventional system, the black liquor concentration is 70 to 8 in the concentrator.
Since it must be concentrated to 0%, a large amount of heated steam is required, and a dryer for granular iron oxide and a dryer/granulator for powdered iron oxide are required, making the equipment complicated. The equipment cost is high, so the valve production volume is 100T/
Although it can be applied to a single-scale factory with a large capacity of around D or more, it has the problem that it is not suitable for a relatively small-scale factory with a pulp production rate of around 30 to 100 T/D.
本発明は上記の問題点を解決するためになされたもので
、黒液濃縮装置での加熱蒸気使用量が少なくなり、かつ
設備の簡略化を図ることができ、したがって設備費が安
価な比較的小容量規模の工場に設置するのに適したアル
カリ決ルプ廃液を燃料とする燃焼生成物回収装置の提供
を目的とするものである。The present invention was made in order to solve the above problems, and it is possible to reduce the amount of heated steam used in a black liquor concentrator and to simplify the equipment. The object of the present invention is to provide a combustion product recovery device that uses alkaline liquid waste as fuel and is suitable for installation in small-scale factories.
〔問題点を解決するための手段および作用〕本発明の装
置は、図面を参照して説明すれば、木材繊維、非木材繊
維のアルカリ蒸解工程および／またはこのアルカリ蒸解
工程に引き続く漂白工程から排出されるアルカリ性廃液
を、酸化鉄を苛性化剤とする燃焼炉２に導入して燃焼・
反応させ、燃焼生成物を回収するとともに、燃焼排ガス
の保有熱を廃熱ボイラ１１で回収する装置において、燃
焼炉２の排ガス出口と廃熱ボイラ１１の排ガス入口との
間に、苛性化剤とアルカリ性廃液とを単独にまたは混合
して供給し、微粉酸「ヒ鉄の造粒・乾燥およびアルカリ
性廃液の濃縮を行うためのロークリドライヤ１４を設け
たことを特徴としている。[Means and effects for solving the problems] The apparatus of the present invention will be described with reference to the drawings. The alkaline waste liquid is introduced into a combustion furnace 2 that uses iron oxide as a causticizing agent to burn it.
In an apparatus for reacting and recovering combustion products and recovering heat retained in combustion exhaust gas in a waste heat boiler 11, a causticizing agent and The present invention is characterized in that it is provided with a rotary dryer 14 for granulating and drying the finely powdered acid "arsenic" and concentrating the alkaline waste liquid by supplying the alkaline waste liquid alone or in combination.
ロータリドライヤ１４内では、微粉酸化鉄の造粒および
乾燥、ならびに燃焼炉からの高温の排ガスとの接触によ
り、アルカリ性廃液の濃縮が行われる。In the rotary dryer 14, the alkaline waste liquid is concentrated by granulation and drying of finely divided iron oxide and contact with high-temperature exhaust gas from the combustion furnace.
以下、本発明の実施例を第１図および第２図に基づいて
説明する。第１図は本発明の装置の一例を示している。Embodiments of the present invention will be described below with reference to FIGS. 1 and 2. FIG. 1 shows an example of the apparatus of the present invention.
２は水冷壁１０を有する燃焼扉、１１は廃熱ボイラで、
燃焼炉２の排ガス出口１２と廃熱ボイラ１１の排ガス人
口１６との間に、ロータリドライヤ１４が設けられてい
る。１５はロータリドライヤ１４を回転させるための駆
動装置、１６はアルカリ性廃液と酸化鉄との混合物を噴
射するための噴射ノズルである。2 is a combustion door having a water cooling wall 10, 11 is a waste heat boiler,
A rotary dryer 14 is provided between the exhaust gas outlet 12 of the combustion furnace 2 and the exhaust gas outlet 16 of the waste heat boiler 11. 15 is a drive device for rotating the rotary dryer 14, and 16 is an injection nozzle for injecting a mixture of alkaline waste liquid and iron oxide.
また噴射ノズル１６からアルカリ性廃液のみを噴射する
場合があり、この場合は酸化鉄を供給するだめの他の噴
射ノズル１７を設ける。１８は上部伝熱管、２０は耐火
材層である。In some cases, only the alkaline waste liquid is injected from the injection nozzle 16, and in this case, another injection nozzle 17 for supplying iron oxide is provided. 18 is an upper heat exchanger tube, and 20 is a refractory material layer.
つぎに上記のように構成された装置の使用方法を第２図
に基づいて説明する。まずアルカリ性廃液を真空蒸発器
、回転ディスク型蒸発器などの濃縮装置１に導入し、蒸
発、濃縮して黒液澄明５５〜６０％の黒液とした後、こ
の黒液を予混合機２１または直接ロータリドライヤ１４
に噴射ノズルを介して供給する。Next, a method of using the apparatus configured as described above will be explained based on FIG. 2. First, the alkaline waste liquid is introduced into a concentrator 1 such as a vacuum evaporator or a rotating disk type evaporator, and is evaporated and concentrated to obtain a black liquor with a clear black liquor of 55 to 60%. Direct rotary dryer 14
through an injection nozzle.
黒液を直接ロークリドライヤ１４に供給する場合は、一
つの噴射ノズルから噴射された黒液と他の噴射ノズルか
ら噴射された酸化鉄とが混合しながら、燃焼炉２からの
高温の排ガスとが対向流接触して、黒液の濃度が７０〜
８０％に濃縮されるとともに、微粉酸化鉄が造粒される
。この濃縮黒液が燃焼炉２内に供給されるとともに、燃
焼炉２には粒状酸化鉄（Ｆｅ、ｌＯｓ’）が供給される
。 ６は酸化鉄バンカである。When the black liquor is directly supplied to the raw dryer 14, the black liquor injected from one injection nozzle and the iron oxide injected from the other injection nozzle are mixed while being mixed with the high temperature exhaust gas from the combustion furnace 2. are in countercurrent contact, and the concentration of black liquor is 70~
While concentrating to 80%, fine powdered iron oxide is granulated. This concentrated black liquor is supplied into the combustion furnace 2, and granular iron oxide (Fe, lOs') is also supplied to the combustion furnace 2. 6 is iron oxide banka.
燃焼炉２が流動床炉の場合、層温度は８００〜１１００
°Ｃ１望ましくは９００〜１０００°Ｃとし、Ｆｅ／Ｎ
ａは１．０以上となるようにする。流動層形成材として
は、純鉄、鉄鉱石（Ｆｅ＝０３、Ｆｅ、０４）、焼結鉱
、還元ペレット、製鉄ダストを造粒したものなどの粒状
の鉄系化合物、３１０２ 、Ａｌ鵞０．、Ｏｒｌｏｇ、
ＭｇＯ１ＣａＯなどの粒状の化合物が用いられる。本例
においては、酸化鉄として鉄鉱石を使用し、補給は粒状
鉄鉱石で行う。補給粒状鉄鉱石は、流動層形成材と同じ
ものな用いる。When the combustion furnace 2 is a fluidized bed furnace, the bed temperature is 800 to 1100.
°C1 desirably 900 to 1000 °C, Fe/N
Set a to be 1.0 or more. Examples of fluidized bed forming materials include granular iron-based compounds such as pure iron, iron ore (Fe=03, Fe, 04), sintered ore, reduced pellets, iron-making dust granules, 3102, Al 0. , Orlog,
Particulate compounds such as MgO1CaO are used. In this example, iron ore is used as the iron oxide, and granular iron ore is used for replenishment. The supplementary granular iron ore is the same as the fluidized bed forming material.
燃焼炉２からの鉄酸ソーダは粒状物苛性化装置４に導入
され、苛性ソーダと回収酸化鉄（粒状）とに抽出、分離
され、この回収酸化鉄は乾燥機を経ることなくそのまま
予混合機２１、あるいはバンカ６またはロータリドライ
ヤ１４へ送られる。The ferric acid soda from the combustion furnace 2 is introduced into the granular material causticizing device 4, where it is extracted and separated into caustic soda and recovered iron oxide (granules), and this recovered iron oxide is directly transferred to the premixer 21 without passing through the dryer. , or sent to the bunker 6 or rotary dryer 14.
廃熱ボイラ１１および集じん機６からのダスト（微粉Ｆ
ｅ、Ｏｙ）の一部は、粉状物苛性化装置７に導入され、
苛性ソーダと回収酸化鉄（粉状）とに抽出、分離され、
この回収酸化鉄は、前記ダスト（微粉Ｆｅ１Ｏｓ ）の
残りとともに微粉Ｆθ、０３として予混合機２１に供給
される。Dust from waste heat boiler 11 and dust collector 6 (fine powder F
e, Oy) is introduced into the powder causticizing device 7,
Extracted and separated into caustic soda and recovered iron oxide (powder),
This recovered iron oxide is supplied to the premixer 21 as fine powder Fθ,03 together with the rest of the dust (fine powder Fe1Os).
予混合機２１内では、濃度５５〜６０％の黒液と微粉Ｆ
ｅ、０３、または濃度５５〜６０％の黒液と微粉Ｆｅｇ
Ｏ＠と粒状Ｆθ、０３が混合され、噴射ノズルからロー
タリドライヤ１４内に噴射され、燃焼炉２からの高温の
排ガスと対向流接触して、濃度７０〜８０％の濃黒液に
濃縮されるとともに、微粉酸化鉄が造粒され、燃焼炉２
内に落下する。In the premixer 21, black liquor with a concentration of 55 to 60% and fine powder F
e, 03, or black liquor with a concentration of 55-60% and fine powder Feg
O@ and granular Fθ, 03 are mixed, injected into the rotary dryer 14 from an injection nozzle, brought into countercurrent contact with high-temperature exhaust gas from the combustion furnace 2, and concentrated into a concentrated black liquor with a concentration of 70 to 80%. At the same time, fine powdered iron oxide is granulated and sent to the combustion furnace 2.
fall inside.
〔発明の効果〕
本発明は上記のように構成されているので、つぎのよう
な種々の優れた効果を有している。[Effects of the Invention] Since the present invention is configured as described above, it has the following various excellent effects.
（１） 濃度５５〜６０％の黒液をロータリドライヤ
で高温の排ガスの顕熱により、濃度７０〜８０％の濃黒
液に濃縮することができるので、黒液濃縮装置での加熱
蒸気使用量を低減することができ省エネルギを図ること
ができる。(1) Black liquor with a concentration of 55 to 60% can be concentrated to a concentrated black liquor with a concentration of 70 to 80% using a rotary dryer using the sensible heat of high-temperature exhaust gas, so the amount of heated steam used in the black liquor concentrator is It is possible to reduce energy consumption and save energy.
（２） ロータリドライヤ内で、酸化鉄と高温の排ガ
スとが対向流接触するので、酸化鉄の乾燥および微粉酸
化鉄の造粒が行われ、従来方式におけるように、粒状物
乾燥機および粉状物乾燥・造粒機を必要としなくなるの
で、設備が簡略化し、設備費の低減を図ることができる
。(2) In the rotary dryer, the iron oxide and the high-temperature exhaust gas come into contact with each other in countercurrent flow, so that drying of the iron oxide and granulation of the finely divided iron oxide are performed. Since a material drying/granulating machine is not required, the equipment can be simplified and the equipment cost can be reduced.
（３） ロータリドライヤ内で、排ガスと噴射黒液と
が接触するので、排ガス中のダストの一部が黒液中に捕
集され、集じん機入口のダスト量が少なくなる。このた
め集じん機の容量を減少させることができる。(3) Since the exhaust gas and the injected black liquor come into contact within the rotary dryer, some of the dust in the exhaust gas is collected in the black liquor, reducing the amount of dust at the dust collector inlet. Therefore, the capacity of the dust collector can be reduced.
（４）上記（１）〜（３）のように運転費、設備費が低
減されるので、バルブ生産量６０〜１００ Ｔ／Ｄ級の
比佼的小容量規模のパルプ工場に適用することができる
。(4) As mentioned in (1) to (3) above, operating costs and equipment costs are reduced, so it can be applied to relatively small pulp mills with valve production of 60 to 100 T/D class. can.
（５）またパルプ工場以外にも、カブロラクタム工場な
どのアルカリ性廃液を取り扱う工場にも適用することが
できる。(5) In addition to pulp factories, it can also be applied to factories that handle alkaline waste liquid, such as cabrolactam factories.
第１図は本発明のアルカリバルブ廃液を燃料とする燃焼
生成物回収装置の一例を示す説明図、第２図は第１図に
示す装置まわりの一例を示すフローシート、第３図は従
来の方法の一例を示すフローシートである。Fig. 1 is an explanatory diagram showing an example of a combustion product recovery device using alkaline valve waste liquid as fuel according to the present invention, Fig. 2 is a flow sheet showing an example of the surroundings of the device shown in Fig. 1, and Fig. 3 is a conventional It is a flow sheet showing an example of the method.
Claims (1)
またはこのアルカリ蒸解工程に引き続く漂白工程から排
出されるアルカリ性廃液を、酸化鉄を苛性化剤とする燃
焼炉に導入して燃焼・反応させ、燃焼生成物を回収する
とともに、燃焼排ガスの保有熱を廃熱ボイラで回収する
装置において、 燃焼炉の排ガス出口と廃熱ボイラの排ガス入口との間に
、苛性化剤とアルカリ性廃液とを単独にまたは混合して
供給し、微粉酸化鉄の造粒・乾燥およびアルカリ性廃液
の濃縮を行うためのロータリドライヤを設けたことを特
徴とするアルカリパルプ廃液を燃料とする燃焼生成物回
収装置。 ２ 燃焼炉が水冷壁構造を有する流動床炉である特許請
求の範囲第１項記載のアルカリパルプ廃液を燃料とする
燃焼生成物回収装置。[Claims] 1. Alkaline cooking process of wood fibers and non-wood fibers and/or
Alternatively, the alkaline waste liquid discharged from the bleaching process that follows this alkaline cooking process is introduced into a combustion furnace using iron oxide as a causticizing agent, where it is combusted and reacted, and the combustion products are recovered, and the heat retained in the combustion exhaust gas is recovered. In a device for recovering waste heat from a waste heat boiler, a causticizing agent and an alkaline waste liquid are supplied alone or in a mixture between the exhaust gas outlet of the combustion furnace and the exhaust gas inlet of the waste heat boiler to granulate and granulate iron oxide powder. A combustion product recovery device using alkaline pulp waste liquid as fuel, characterized in that it is equipped with a rotary dryer for drying and concentrating alkaline waste liquid. 2. A combustion product recovery device using alkali pulp waste liquid as fuel according to claim 1, wherein the combustion furnace is a fluidized bed furnace having a water-cooled wall structure.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7983286A JPH0665798B2 (en) | 1986-04-07 | 1986-04-07 | Combustion product recovery device using alkaline pulp waste liquid as fuel |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7983286A JPH0665798B2 (en) | 1986-04-07 | 1986-04-07 | Combustion product recovery device using alkaline pulp waste liquid as fuel |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS62238893A true JPS62238893A (en) | 1987-10-19 |
| JPH0665798B2 JPH0665798B2 (en) | 1994-08-24 |
Family
ID=13701179
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7983286A Expired - Fee Related JPH0665798B2 (en) | 1986-04-07 | 1986-04-07 | Combustion product recovery device using alkaline pulp waste liquid as fuel |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0665798B2 (en) |
-
1986
- 1986-04-07 JP JP7983286A patent/JPH0665798B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0665798B2 (en) | 1994-08-24 |
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