JPS6337197A - Method for regenerating desulfurizing agent in coal gasification - Google Patents
Method for regenerating desulfurizing agent in coal gasificationInfo
- Publication number
- JPS6337197A JPS6337197A JP18094886A JP18094886A JPS6337197A JP S6337197 A JPS6337197 A JP S6337197A JP 18094886 A JP18094886 A JP 18094886A JP 18094886 A JP18094886 A JP 18094886A JP S6337197 A JPS6337197 A JP S6337197A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- air
- coal
- desulfurizing agent
- pipe
- 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
- 239000003795 chemical substances by application Substances 0.000 title claims abstract description 39
- 239000003245 coal Substances 0.000 title claims abstract description 30
- 230000003009 desulfurizing effect Effects 0.000 title claims abstract description 15
- 230000001172 regenerating effect Effects 0.000 title claims abstract description 9
- 238000002309 gasification Methods 0.000 title claims description 22
- 238000000034 method Methods 0.000 title claims description 17
- 239000002893 slag Substances 0.000 claims abstract description 14
- 235000019738 Limestone Nutrition 0.000 claims abstract description 6
- 239000006028 limestone Substances 0.000 claims abstract description 6
- 150000003464 sulfur compounds Chemical class 0.000 claims abstract description 6
- 150000004763 sulfides Chemical class 0.000 claims abstract 3
- 239000007789 gas Substances 0.000 claims description 46
- 230000008929 regeneration Effects 0.000 claims description 32
- 238000011069 regeneration method Methods 0.000 claims description 32
- 238000006477 desulfuration reaction Methods 0.000 claims description 23
- 230000023556 desulfurization Effects 0.000 claims description 23
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 abstract description 7
- 239000002245 particle Substances 0.000 abstract description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 3
- 229910052799 carbon Inorganic materials 0.000 abstract description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 15
- 239000011593 sulfur Substances 0.000 description 13
- 229910052717 sulfur Inorganic materials 0.000 description 13
- 238000006243 chemical reaction Methods 0.000 description 10
- 238000010586 diagram Methods 0.000 description 7
- 239000000428 dust Substances 0.000 description 7
- 238000010248 power generation Methods 0.000 description 7
- 238000000605 extraction Methods 0.000 description 5
- 238000004064 recycling Methods 0.000 description 4
- 238000011161 development Methods 0.000 description 3
- 230000018109 developmental process Effects 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 235000010216 calcium carbonate Nutrition 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000010459 dolomite Substances 0.000 description 1
- 229910000514 dolomite Inorganic materials 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000005445 natural material Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000002250 progressing effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
- 238000004383 yellowing Methods 0.000 description 1
- 239000011787 zinc oxide Substances 0.000 description 1
Abstract
Description
【発明の詳細な説明】
（産業上の利用分野）
本発明は石炭ガス化における脱硫剤の再生方法に関し、
特に石炭をガス化して生成したガス中の流黄化合物を効
率良く除去し、ガス化発電用のガスとする石炭ガス化に
おける脱硫剤の再生方法に関するものである。[Detailed Description of the Invention] (Industrial Application Field) The present invention relates to a method for regenerating a desulfurization agent in coal gasification,
In particular, the present invention relates to a method for regenerating a desulfurization agent in coal gasification, which efficiently removes yellowing compounds from the gas produced by gasifying coal to provide gas for gasification power generation.
（従来の技術）
近年、エネルギー源としての石炭利用が急速に進んでお
り、石炭をそのまま燃料として燃境させる方法、または
石炭をガス化、液化して無公害な流体燃料として利用す
る技術の開発が盛んになっている。我が国では石炭をガ
ス化する技術として、原料ガスまたは燃料ガスを得る高
カロリーガス化プロセスおよび発電用を目的とした低カ
ロリーガス化プロセスの開発が主に進められている。さ
らに最近では、酸素または空気とスチームを用い、石炭
を噴流層でスラグガス化し、灰をスラグとして排出する
プロセスの開発が進められている。(Conventional technology) In recent years, the use of coal as an energy source has been rapidly progressing, and there is a need for the development of methods to burn coal directly as fuel, or to gasify and liquefy coal to use it as non-polluting fluid fuel. is becoming popular. In Japan, as technologies for gasifying coal, the main developments are a high-calorie gasification process for obtaining raw material gas or fuel gas, and a low-calorie gasification process for power generation. More recently, progress has been made in the development of a process in which coal is gasified into slag in a spouted bed using oxygen or air and steam, and the ash is discharged as slag.
このスラグガス化プロセスでは、炉内の温度を１５００
℃以上にすることにより石炭中の天分を熔融して、炉底
からスラグとして排出するため、石炭中のカーボンのガ
ス化反応速度が大きくなり、また石炭を高温高圧でガス
化するため、生成ガスはＣＯとＨ２を多く含んでいる。In this slag gasification process, the temperature inside the furnace is set to 1500
By heating the temperature above ℃, the natural substances in the coal are melted and discharged from the bottom of the furnace as slag, which increases the gasification reaction rate of carbon in the coal.Also, since the coal is gasified at high temperature and pressure, The gas contains a lot of CO and H2.
これをガス化発電と組み合わせる場合、この生成粗ガス
を高温のまま処理することがエネルギーの有効利用の面
から望ましく、したがってガス化炉で主にＨ２Ｓとなる
石炭中の硫黄成分を高温状態で脱硫することが大きな課
題となっている。When this is combined with gasification power generation, it is desirable from the standpoint of effective energy use to process the generated crude gas at a high temperature. Therefore, the sulfur components in the coal, which mainly become H2S, are desulfurized at high temperatures in the gasifier. It is a big challenge to do so.
第５図は、従来のガス化発電装置の一例を示す系統図で
ある。図において、供給された石炭３はガス化炉１でガ
ス化され、生成ガス中の未反応チャーと、生成ガス中の
硫黄化合物と反応した脱硫剤とは排出管６からサイクロ
ン７に導かれ、ここで粒径の大きいチャーがまず分離さ
れ、次に熱交換器２０でガスは冷却され、２次サイクロ
ン２２で前記反応脱硫剤が分離される。硫黄化合物が除
去された精製ガスはコンパスタ１７に送り込まれ、ガス
タービン１８で発電に使用される。FIG. 5 is a system diagram showing an example of a conventional gasification power generation device. In the figure, supplied coal 3 is gasified in a gasification furnace 1, and unreacted char in the generated gas and desulfurization agent that has reacted with sulfur compounds in the generated gas are led to a cyclone 7 from a discharge pipe 6. Here, char having a large particle size is first separated, then the gas is cooled in a heat exchanger 20, and the reactive desulfurization agent is separated in a secondary cyclone 22. The purified gas from which sulfur compounds have been removed is sent to the comparator 17 and used by the gas turbine 18 for power generation.
この方法によれば、ガスタービン１８に入るガス温度が
高く、ガスタービン１８の発電効率が高くなるが、２次
サイクロン２２で回収した反応脱硫剤が再生塔９で空気
供給管１１からの空気により再生させる際、再生ガスと
して高濃度のＳ０２ガスが発生し、通常の石灰石−石膏
法による吸収除去が困難となる。またＳ０２を還元して
硫黄として回収するには、還元ガスが必要となり、装置
が複雑化し、コスト高となる。According to this method, the temperature of the gas entering the gas turbine 18 is high, and the power generation efficiency of the gas turbine 18 is increased. During regeneration, a high concentration of S02 gas is generated as regeneration gas, making it difficult to absorb and remove it by the usual limestone-gypsum method. Further, reducing S02 and recovering it as sulfur requires a reducing gas, which complicates the equipment and increases costs.
（発明が解決しようとする問題点）
本発明の目的は、上記従来技術の問題点を解決し、再生
塔で効率良く反応脱硫剤を再生して、脱硫剤と硫黄とに
分離し、回収することのできる石炭ガス化における脱硫
剤の再生方法を提供することにある。(Problems to be Solved by the Invention) The purpose of the present invention is to solve the above-mentioned problems of the prior art, to efficiently regenerate the reactive desulfurizing agent in a regeneration tower, and to separate and recover the desulfurizing agent and sulfur. An object of the present invention is to provide a method for regenerating a desulfurization agent in coal gasification.
（問題点を解決するための手段）
上記目的は、脱硫剤として微粉石灰石を用い、ガス化炉
で生じた未反応チャーと、石灰石と反応した硫化物とを
サイクロンで捕集して再生塔に導き、空気または／およ
びスチームとにより反応させ、脱硫剤と硫黄に分離し、
回収することにより達せられる。(Means for solving the problem) The above purpose is to use pulverized limestone as a desulfurization agent, and collect unreacted char generated in the gasifier and sulfide reacted with limestone with a cyclone and send it to the regeneration tower. and react with air or/and steam to separate the desulfurization agent and sulfur,
Achieved by collecting.
すなわち本発明は、微粉炭を用いて酸素または空気によ
るエントレイン方式によりスラグガス化し、精製したガ
スを必要に応じてガスタービンに導いてガス化発電する
方法において、ガス化炉に脱硫剤を供給し、ガス中の硫
黄化合物を硫化物として、未反応チャーとともに再生塔
に導き、空気または／およびスチームで脱硫剤を再生す
ることを特徴とする。That is, the present invention is a method of gasifying slag gas using pulverized coal by entraining with oxygen or air, and guiding the purified gas to a gas turbine as necessary to generate gasification power. , the sulfur compounds in the gas are introduced as sulfides together with unreacted char to a regeneration tower, and the desulfurization agent is regenerated with air and/or steam.
本発明における再生塔の温度は、７５０〜９５０℃が望
ましく、特に８００℃前後が最適である。The temperature of the regeneration tower in the present invention is preferably 750 to 950°C, and particularly optimally around 800°C.
また、本発明における再生塔に供給する空気とスチーム
の供給量の割合（ａｉｒ／ｓｔｍｉｉｉ量比）は２以下
が望ましい。空気の供給量を増加しすぎると、再生ガス
中の硫黄濃度が増加するが、系の反応温度が低下する傾
向がある。Further, in the present invention, the ratio of the amounts of air and steam supplied to the regeneration tower (air/stmiii amount ratio) is preferably 2 or less. If the air supply amount is increased too much, the sulfur concentration in the regeneration gas will increase, but the reaction temperature of the system will tend to decrease.
再生塔より回収した脱硫剤ＣａＯは、ガス化炉にリサイ
クルして再利用することができる。The desulfurization agent CaO recovered from the regeneration tower can be recycled and reused in the gasification furnace.
（作用）
本発明で使用される再生塔では、石灰石の硫化物は以下
の反応により硫黄として回収される。(Operation) In the regeneration tower used in the present invention, limestone sulfide is recovered as sulfur through the following reaction.
先ず、ガス化炉で
Ｈ２Ｓ＋ＣａＣＯ３→ＣａＳ＋Ｈ２０＋ＣＯ２の反応に
より作られた硫化物は、再生塔に供給された空気により
一部燃焼してＳＯ２を生成する。First, sulfide produced by the reaction of H2S+CaCO3→CaS+H20+CO2 in the gasifier is partially combusted by air supplied to the regeneration tower to generate SO2.
ＣａＳ＋３／２０２−”ＣａＯ＋５Ｏ２一方、チャーと
Ｓ０２またはスチームは次の反応によりＨ２Ｓとなる。CaS+3/202-"CaO+5O2 On the other hand, char and S02 or steam become H2S through the following reaction.
ｃ＋ｓｏ２→ｓ＋ｃｏ２ Ｃ＋Ｈ２０−＝Ｈ２＋ＣＯ ３＋Ｈ２→Ｈ２Ｓ さらにＨ２ＳとＳＯ２は以下の反応により硫黄となる。c+so2→s+co2 C+H20-=H2+CO 3+H2→H2S Furthermore, H2S and SO2 become sulfur through the following reaction.
２Ｈ２Ｓ＋ＳＯ２→３Ｓ＋Ｈ２０
以上の反応により硫化物は単体Ｓ（硫黄）となり、再生
塔出口ガスを冷却すれば容易に硫黄として回収すること
ができる。2H2S+SO2→3S+H20 The above reaction turns sulfide into elemental S (sulfur), which can be easily recovered as sulfur by cooling the regeneration tower outlet gas.
（実施例）
第１図は、本発明の一実施例を示す石炭ガス化および脱
硫剤の再生装置の系統図である。この装置は、石炭をス
ラグガス化するガス化炉１と、該ガス化炉１の生成ガス
から脱硫剤等の粒子を除去するサイクロン７と、該脱硫
剤の再生塔９と、サイクロンを出たガスを除塵する脱塵
器８と、該脱塵器８からのガスにより一発電を行なうた
めのガスタービン１８とから成っている。上記構成にお
いて、ガス化する微粉炭は石炭供給管３よりガス化炉１
の下部に供給され、同時にガス化剤である酸素または空
気が酸素供給管４から供給される。(Example) FIG. 1 is a system diagram of a coal gasification and desulfurization agent regeneration apparatus showing an example of the present invention. This device consists of a gasification furnace 1 that turns coal into slag gas, a cyclone 7 that removes particles such as a desulfurization agent from the gas produced by the gasification furnace 1, a regeneration tower 9 for the desulfurization agent, and a gas exiting from the cyclone. It consists of a dust remover 8 for removing dust, and a gas turbine 18 for generating electricity using the gas from the dust remover 8. In the above configuration, pulverized coal to be gasified is supplied to the gasifier 1 from the coal supply pipe 3.
At the same time, oxygen or air as a gasifying agent is supplied from the oxygen supply pipe 4.
ガス化炉１で石炭はガス化され、有害成分であるＨ２Ｓ
を含む生成ガスを発生する。また石炭中の灰は溶融して
スラグとしてスラグ排出管５から系外に排出する。Coal is gasified in gasifier 1, and H2S, a harmful component, is
Generates product gas containing. Further, the ash in the coal is melted and discharged as slag to the outside of the system through the slag discharge pipe 5.
一方、生成ガス中の硫黄化合物であるＨ２Ｓを除去する
ため、ガス化炉１の脱硫剤供給管２から微粉の脱硫剤、
例えば石灰石、ドロマイト、酸化亜鉛、酸化鉄等が供給
される。ガス化炉１で生成した硫化物ＣａＳとカーボン
を含む未反応チャーは塔頂から排出管６を通ってサイク
ロン７に入り、ガスと分離される。サイクロン７で分離
された粒子は再生塔９に入り、空気供給管１１およびス
チーム供給管１２からの空気とスチームによりＣａＳは
Ｃａ０（脱硫剤）とＳ（硫黄）に再生される。On the other hand, in order to remove H2S, which is a sulfur compound in the generated gas, a fine powder of desulfurization agent is supplied from the desulfurization agent supply pipe 2 of the gasification furnace 1.
For example, limestone, dolomite, zinc oxide, iron oxide, etc. are supplied. Unreacted char containing CaS sulfide and carbon produced in the gasifier 1 enters the cyclone 7 from the top of the tower through the exhaust pipe 6, where it is separated from the gas. The particles separated by the cyclone 7 enter the regeneration tower 9, where CaS is regenerated into Ca0 (desulfurizing agent) and S (sulfur) by air and steam from the air supply pipe 11 and the steam supply pipe 12.
再生した硫黄蒸気を含むガスは再生ガス出口管１０から
系外に排出され、冷却して単体硫黄として回収される。The regenerated gas containing sulfur vapor is discharged from the system through the regenerated gas outlet pipe 10, cooled, and recovered as elemental sulfur.
一方、再生塔９で再生された脱硫剤ＣａＯは脱硫剤抜出
管１３から抜出され、灰分離器１４で天分を抜出した後
、脱硫剤リサイクル管１６によりガス化炉１ヘリサイク
ルされる。On the other hand, the desulfurization agent CaO regenerated in the regeneration tower 9 is extracted from the desulfurization agent extraction pipe 13, and after the ash separator 14 extracts the contents, it is recycled to the gasification furnace 1 through the desulfurization agent recycling pipe 16. .
またサイクロン７を出た精製されたガスは脱塵器８でダ
ストを分離した後、コンパスタ１７に入りガスタービン
１８で発電を行ない、排ガス管１９から系外に放出され
る。Further, the purified gas leaving the cyclone 7 separates dust in a dust remover 8, enters a comparator 17, generates electricity in a gas turbine 18, and is discharged from the system through an exhaust gas pipe 19.
以上の方法により容易に硫化物ＣａＳから硫黄に再生処
理することが可能となった。By the above method, it has become possible to easily regenerate sulfide CaS into sulfur.
次に第２図ないし第４図は、本発明を実証するために小
型実験装置を用いてＣａＳとチャーの混合物の再生実験
を行なった結果を示すものである。Next, FIGS. 2 to 4 show the results of a regeneration experiment of a mixture of CaS and char using a small experimental device in order to demonstrate the present invention.
第２図は、供給ガスとして空気とスチームの重量比（ａ
ｉｒ／ｓｔｍ）をθ〜２に変化したガスを用い、再生塔
の温度を７００〜１０００℃に変えたときのＣａＳ再生
率（ＣａＳがＣａＯに再生される割合）を示したもので
あるが、温度８００℃でＣａＳ再生率が最大となること
がわかる。また第３図は、再生塔の温度を同様に変化し
た場合のチャーの反応率を示したものであるが、温度が
高いほどスチームとチャーの反応が進み、チャーの反応
率が高（なる傾向を示している。以上の結果から再生塔
の最適温度は７５０から９５０℃、好ましくは８００℃
前後であることがわかった。Figure 2 shows the weight ratio (a
The graph shows the CaS regeneration rate (the rate at which CaS is regenerated into CaO) when the temperature of the regeneration tower is changed from 700 to 1000°C using a gas whose ir/stm) has been changed to θ ~ 2. It can be seen that the CaS regeneration rate is maximum at a temperature of 800°C. Figure 3 shows the reaction rate of char when the temperature of the regeneration tower is similarly changed. From the above results, the optimum temperature for the regeneration tower is 750 to 950°C, preferably 800°C.
I found out that it was before and after.
第４図は、温度８５０℃、常圧下で空気とスチーム比（
ａ ｉｒ／ｓ ｔｍ）を変化した場合の再生ガス出口の
ガス中のＳ濃度を示したものであるが、空気の供給量を
増してａｉｒ／ｓｔｍ比を上げた方がｓ４度が高くなる
ことがわかる。しかしａｉｒ／ｓｔｍ比が２を超えると
Ｓ濃度はそれ以上を増加せず、またその反応濃度が低下
するので、ａｉｒ／ｓｔｍ比は２以下が適当であること
がわかった。Figure 4 shows the air and steam ratio (
This shows the S concentration in the gas at the regeneration gas outlet when changing the air/stm ratio, and it shows that increasing the air supply amount and raising the air/stm ratio will result in a higher s4 degree. I understand. However, when the air/stm ratio exceeds 2, the S concentration does not increase any more and the reaction concentration decreases, so it has been found that an air/stm ratio of 2 or less is appropriate.
（発明の効果）
本発明によれば、再生塔で効率良く反応脱硫剤を再生し
て、脱硫剤と硫黄に分離し、回収することができ、装置
の複雑化や、コスト高を防止することができる。(Effects of the Invention) According to the present invention, the reactive desulfurization agent can be efficiently regenerated in the regeneration tower, separated into the desulfurization agent and sulfur, and recovered, thereby preventing complication of the equipment and high cost. Can be done.
第１図は本発明の一実施例を示す装置系統図、第２図は
再生塔でのＣａＳ再生率と温度の関係を示す図、第３図
には再生塔でのチャー反応率と温度の関係を示す図、第
４図は再生ガス出口の硫黄濃度と空気とスチーム比の関
係を示す図、第５図は従来のガス化発電装置を示す装置
系統図である。
１・・・ガス化炉１．２・・・脱硫剤供給管、３・・・
石炭供給管、４・・・酸素供給管、５・・・スラグを友
出管、６・・・排出管、７・・・サイクロン、８・・・
脱塵器、９・・・再生塔、１０・・・再生ガス出口管、
１１・・・空気供給管、１２・・・スチーム供給管、１
３・・・脱硫剤抜出管、１４・・・灰分離器、１５・・
・灰抜出前、１６・・・脱硫剤リサイクル管、１７・・
・コンパスタ、１８・・・ガスタービン、１９・・・排
ガス管、２０・・・熱交換器、２１・・・リサイクル管
、２２・・・２次サイクロン。
代理人 弁理士 川 北 武 長
第１図
１ガス化炉 ８脱塵器 １５灰抜出管
２脱硫剤供給管 ９再生塔 １６脱硫剤
リサイクル管３石炭供給管 １０再生ガス出口管
１７コンパスタ４酸石供給管 １１空気供給
管 １８ガスタービン５スラグ抜出管 １２
スチーム供給管 １９排ガス管６排出管
１３脱硫剤抜出管７サイクロン １４灰分離器
第２図
温度（°Ｃ）
第３図
温度（°Ｃ）Figure 1 is an equipment system diagram showing an embodiment of the present invention, Figure 2 is a diagram showing the relationship between the CaS regeneration rate and temperature in the regeneration tower, and Figure 3 is a diagram showing the relationship between the char reaction rate and temperature in the regeneration tower. FIG. 4 is a diagram showing the relationship between the sulfur concentration at the regeneration gas outlet and the air to steam ratio, and FIG. 5 is a system diagram showing a conventional gasification power generation device. 1...Gasifier 1.2...Desulfurizing agent supply pipe, 3...
Coal supply pipe, 4... Oxygen supply pipe, 5... Slag removal pipe, 6... Discharge pipe, 7... Cyclone, 8...
Dust remover, 9... Regeneration tower, 10... Regeneration gas outlet pipe,
11...Air supply pipe, 12...Steam supply pipe, 1
3... Desulfurizing agent extraction pipe, 14... Ash separator, 15...
・Before ash removal, 16... Desulfurization agent recycling pipe, 17...
- Compaster, 18... Gas turbine, 19... Exhaust gas pipe, 20... Heat exchanger, 21... Recycling pipe, 22... Secondary cyclone. Agent Patent Attorney Takenaga Kawakita Figure 1 1 Gasifier 8 Dust remover 15 Ash extraction pipe 2 Desulfurizing agent supply pipe 9 Regeneration tower 16 Desulfurizing agent recycling pipe 3 Coal supply pipe 10 Regenerated gas outlet pipe 17 Compaster 4 Acid Stone supply pipe 11 Air supply pipe 18 Gas turbine 5 Slag extraction pipe 12
Steam supply pipe 19 Exhaust gas pipe 6 Discharge pipe
13 Desulfurizing agent extraction pipe 7 Cyclone 14 Ash separator Figure 2 Temperature (°C) Figure 3 Temperature (°C)
Claims (2)
グガス化する方法において、ガス化炉に脱硫剤を供給し
、ガス中の硫黄化合物を硫化物として、未反応チャーと
ともに再生塔に導き、空気または／およびスチームで脱
硫剤を再生することを特徴とする石炭ガス化における脱
硫剤の再生方法。(1) In a method of slag gasifying pulverized coal with oxygen or air in a gasifier, a desulfurization agent is supplied to the gasifier, and sulfur compounds in the gas are converted into sulfides and guided to a regeneration tower along with unreacted char. A method for regenerating a desulfurizing agent in coal gasification, comprising regenerating the desulfurizing agent with air and/or steam.
粉の石灰石を用いることを特徴とする石炭ガス化におけ
る脱硫剤の再生方法。(2) A method for regenerating a desulfurization agent in coal gasification according to claim 1, characterized in that finely powdered limestone is used as the desulfurization agent.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61180948A JPH083103B2 (en) | 1986-07-31 | 1986-07-31 | Regeneration method of desulfurizing agent in coal gasification |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61180948A JPH083103B2 (en) | 1986-07-31 | 1986-07-31 | Regeneration method of desulfurizing agent in coal gasification |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6337197A true JPS6337197A (en) | 1988-02-17 |
| JPH083103B2 JPH083103B2 (en) | 1996-01-17 |
Family
ID=16092073
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61180948A Expired - Fee Related JPH083103B2 (en) | 1986-07-31 | 1986-07-31 | Regeneration method of desulfurizing agent in coal gasification |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH083103B2 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104762105A (en) * | 2015-03-13 | 2015-07-08 | 李毅强 | Biomass gasifier flue gas self-purification device |
| CN113600246A (en) * | 2021-08-23 | 2021-11-05 | 中冶赛迪上海工程技术有限公司 | Desulfurization catalyst regeneration method and system |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4872202A (en) * | 1971-11-12 | 1973-09-29 | ||
| JPS55808A (en) * | 1978-06-14 | 1980-01-07 | Babcock Hitachi Kk | Desulfurizing agent regenerating method |
-
1986
- 1986-07-31 JP JP61180948A patent/JPH083103B2/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4872202A (en) * | 1971-11-12 | 1973-09-29 | ||
| JPS55808A (en) * | 1978-06-14 | 1980-01-07 | Babcock Hitachi Kk | Desulfurizing agent regenerating method |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104762105A (en) * | 2015-03-13 | 2015-07-08 | 李毅强 | Biomass gasifier flue gas self-purification device |
| CN113600246A (en) * | 2021-08-23 | 2021-11-05 | 中冶赛迪上海工程技术有限公司 | Desulfurization catalyst regeneration method and system |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH083103B2 (en) | 1996-01-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP5166443B2 (en) | Electric energy generation method and equipment in gas / steam turbine (combined cycle) power plant | |
| US20080202985A1 (en) | Method for recovery of hydrocarbon oils from oil shale and other carbonaceous solids | |
| CN101802143A (en) | Method for purifying the crude gas from a solid matter gasification | |
| BRPI0722330B1 (en) | PROCESS AND INSTALLATION TO PRODUCE COAL AND FUEL GAS | |
| CN1212730A (en) | Process for production of liquid pig iron or liquid intermediate products of steel and plant for carrying out said process | |
| JPH0653206B2 (en) | Removal method of sulfur from exhaust gas of reduction blast furnace | |
| JP4250472B2 (en) | Method for producing reduced iron and reducing gas for blast furnace charge, method for using reduced iron, and method for using reducing gas | |
| JPS621784A (en) | Gasification of hydrocarbon fuel | |
| JPS6150995B2 (en) | ||
| JPS6337197A (en) | Method for regenerating desulfurizing agent in coal gasification | |
| JPS63191894A (en) | Treatment of fly slag | |
| JP2635652B2 (en) | Dry desulfurization of coal gas | |
| US4064222A (en) | Nitrogen fixation and molecular magneto hydrodynamic generation using a coal gasification gas stream | |
| JP2000212620A (en) | Production of reduced iron | |
| KR101149601B1 (en) | Carbon dioixde sequester using molten slag | |
| JPS63297496A (en) | Sulfur recover in high-temperature desulfurization process | |
| JP2007277479A (en) | Method and apparatus for producing hydrogen gas and carbon monoxide gas from inflammable waste | |
| JPH06293888A (en) | Method for recovering sulfur from plant for gasifying coal and device therefor | |
| CA2413563C (en) | Power generation from sulphur-containing fuels | |
| JPS62260889A (en) | Method of desulfurization in gasifying oven | |
| JP2604430B2 (en) | Coal gasification method | |
| KR20070067830A (en) | Method of production of hydrogen and pig-iron utilizing coal and iron ore | |
| JPH01272693A (en) | Method for desulfurizing coat gas and apparatus therefor | |
| KR20160071573A (en) | The apparatus for removing hydrogen sulfide from coke oven gas and the method thereof | |
| JPH0832894B2 (en) | Spouted bed coal gasifier |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| LAPS | Cancellation because of no payment of annual fees |