JPH0543207A - Method for degassing liquid sulfur - Google Patents
Method for degassing liquid sulfurInfo
- Publication number
- JPH0543207A JPH0543207A JP22123691A JP22123691A JPH0543207A JP H0543207 A JPH0543207 A JP H0543207A JP 22123691 A JP22123691 A JP 22123691A JP 22123691 A JP22123691 A JP 22123691A JP H0543207 A JPH0543207 A JP H0543207A
- Authority
- JP
- Japan
- Prior art keywords
- sulfur
- hydrogen sulfide
- combustion air
- tower
- supplied
- 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
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/0232—Purification, e.g. degassing
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は液体硫黄の脱ガス方法に
関し、さらに詳しくはクラウス式硫黄回収装置の製品液
体硫黄中の硫化水素の除去方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for degassing liquid sulfur, and more particularly to a method for removing hydrogen sulfide from product liquid sulfur in a Claus sulfur recovery apparatus.
【０００２】[0002]
【従来の技術】石油精製工場においては、クラウス式硫
黄回収装置によって大量の硫黄が回収，生産されてい
る。すなわち、各石油留分中の硫黄化合物は、脱硫のた
めに水素化処理を受けて硫化水素ガスに成り、次にガス
洗浄装置で吸収，分離されて硫化水素の濃度の高いアシ
ッドガスとして硫黄回収装置に供給される。硫黄回収装
置においては、次記のクラウス反応により、硫化水素の
３分の１が空気中の酸素と反応して二酸化硫黄になり、
これが残りの硫化水素と反応して単体硫黄を生成する。 Ｈ2 Ｓ＋3/2 Ｏ2 ＝ＳＯ2 ＋Ｈ2Ｏ ─── (1) ２Ｈ2 Ｓ＋ＳＯ2 ＝３Ｓ＋２Ｈ2 Ｏ ─── (2) これらの反応は、実際には従来の硫黄回収装置の系統図
である図２において、(1) 式の酸化反応は主に反応炉
（Ｆ−１）で、(2) 式の反応はアルミナ触媒充填のリア
クター（Ｒ−１，Ｒ−２）でそれぞれ起こる。そしてリ
アクターは、硫化水素の硫黄への転換率を高くして、装
置出口ガス（以下テイルガスという）中の硫黄化合物の
含有量を極力少なくするため２段以上の多段方式が用い
られる。これは各段で生成する気相の単体硫黄をコンデ
ンサー（Ｃ−１〜３）で凝縮して液状にして反応系より
除去し、次段のリアクターにおける反応が、(2) 式にお
いてより右に有利に進行させるためである。2. Description of the Related Art In an oil refinery, a large amount of sulfur is recovered and produced by a Claus type sulfur recovery device. In other words, the sulfur compounds in each petroleum fraction are hydrotreated for desulfurization and become hydrogen sulfide gas, which is then absorbed and separated by the gas cleaning device to recover sulfur as acid gas with high hydrogen sulfide concentration. Supplied to the device. In the sulfur recovery device, due to the Claus reaction described below, one-third of hydrogen sulfide reacts with oxygen in the air to form sulfur dioxide,
This reacts with the remaining hydrogen sulfide to produce elemental sulfur. H 2 S + 3/2 O 2 = SO 2 + H 2 O ─── (1) 2H 2 S + SO 2 = 3S + 2H 2 O ─── (2) These reactions are actually the system diagrams of conventional sulfur recovery equipment. In FIG. 2, the oxidation reaction of the formula (1) mainly occurs in the reactor (F-1), and the reaction of the formula (2) occurs in the reactors (R-1, R-2) packed with the alumina catalyst. The reactor uses a multi-stage system of two or more stages in order to increase the conversion rate of hydrogen sulfide to sulfur and minimize the content of sulfur compounds in the apparatus outlet gas (hereinafter referred to as tail gas). This is because the elemental sulfur in the gas phase produced at each stage is condensed by the condenser (C-1 to 3) to be liquefied and removed from the reaction system. This is for advancing advantageously.
【０００３】以上のようにして各コンデンサー（Ｃ−１
〜３）で凝縮して得られる液状の単体硫黄（以下液体硫
黄という）は、ヘッダー管路を介して地下に埋設される
硫黄ピット（Ｓ−１）に流入して貯留され、ポンプ（Ｐ
−１）にて製品タンクに送出される。この硫黄ピットに
流入する液体硫黄は、凝縮の際に硫化水素ガスと接触す
るため、このガスを相当溶存しておりその濃度は温度等
の条件によっても異なるが、一般には２００ppm 以上で
ある。この溶存している硫化水素は貯蔵又は輸送中に大
気中に気化し、拡散するので労働安全衛生上好ましくな
く、例えば１０ppm 程度まで除去する必要がある。As described above, each capacitor (C-1
Liquid elemental sulfur (hereinafter referred to as liquid sulfur) obtained by condensing in 3) to 3) flows into the sulfur pit (S-1) buried underground via the header pipe line, is stored, and is stored in the pump (P
In -1), it is sent to the product tank. The liquid sulfur flowing into the sulfur pit is in contact with the hydrogen sulfide gas at the time of condensation, so that this gas is considerably dissolved and its concentration is generally 200 ppm or more, although it varies depending on the conditions such as temperature. This dissolved hydrogen sulfide vaporizes in the atmosphere during storage or transportation and diffuses, which is not preferable in terms of occupational safety and health, and it is necessary to remove it to about 10 ppm, for example.
【０００４】従来、この溶存硫化水素の除去方法とし
て、いくつかの案が提案されているが、代表的なものに
ついて次に説明する。最も古くから用いられている方法
としては、空気スィープ方式がある。これは硫黄ピット
（Ｓ−１）中で液体硫黄をポンプ（Ｐ−２）及びスプレ
イノズルを介してミスト状に噴霧し、ピット内の空気中
に硫化水素を気化して除去するものである。そしてこの
硫化水素を含む空気をスチームエジェクター（Ｅ−１）
で抽気して、硫黄回収装置のテイルガストリータのオフ
ガスの焼却炉（Ｆ−２，以下インシネレータという）に
移送して焼却して大気放出するものである。Conventionally, several proposals have been proposed as a method for removing this dissolved hydrogen sulfide, but a typical one will be described below. The air sweep method is the oldest method used. In this method, liquid sulfur is sprayed in a mist form through a pump (P-2) and a spray nozzle in a sulfur pit (S-1) to vaporize and remove hydrogen sulfide in the air in the pit. Then, the air containing the hydrogen sulfide is used as a steam ejector (E-1).
It is extracted into the incinerator (F-2, hereinafter referred to as an incinerator) for off-gas of the tail gas treater of the sulfur recovery device, incinerated and released to the atmosphere.
【０００５】また最近用いられている方法として微量の
アンモニア等を液体硫黄中に噴霧と同時に注入して硫化
水素の気化を促進する方法もある。これは硫化水素は、
液体硫黄中に単に溶存してるのみでなく、一部は硫黄と
化合して多硫化物になっており、アンモニア等はこれら
の分解に触媒作用を有するといわれている。そして気化
された硫化水素は、前記と同じようにスィープ空気によ
ってインシネレータに移送され焼却される。しかしなが
ら、このアンモニアの注入量が多い場合には、アンモニ
アの硫化物が析出し、製品硫黄の品質低下の原因になる
とともに、液体硫黄の輸送管路の閉塞トラブルの原因に
もなる問題がある。As a recently used method, there is also a method of injecting a small amount of ammonia or the like into liquid sulfur at the same time as spraying to accelerate vaporization of hydrogen sulfide. This is hydrogen sulfide
Not only is it dissolved in liquid sulfur, but a part of it is combined with sulfur to form polysulfides, and ammonia and the like are said to have a catalytic action for their decomposition. Then, the vaporized hydrogen sulfide is transferred to the incinerator by the sweep air and incinerated as described above. However, when the injection amount of ammonia is large, there is a problem that a sulfide of ammonia is deposited, which causes deterioration of the quality of product sulfur and also causes a trouble of blocking the liquid sulfur transportation pipeline.
【０００６】また以上の二つの方法に共通のものとして
次の問題がある。現在の硫黄回収装置では、大気汚染防
止の観点から、旧来のクラウス式硫黄回収装置の後段に
ＳＣＯＴ法，ビーボン法等のテイルガストリータ（Ｔ−
１）と称する装置を設け、例えばテイルガス中の硫黄化
合物を還元して硫化水素にしてから吸収塔にてアミン系
の水溶液で洗浄して回収し、しかも吸収塔を出るテイル
ガス中に残存している硫化水素は、後続して設けられる
インシネレータ（Ｆ−２）で焼却し、無害化してスタッ
ク（Ｕ−１）を経由して大気放出している。このように
して現在の硫黄回収装置では、最終的な大気放出ガスで
あるスタックガス中の硫黄酸化物の濃度は１００〜２０
０ppm と少なくなっている。これに対して前記のよう
に、硫黄ピット（Ｓ−１）から抽気される硫化水素含有
のスィープ空気をインシネレータ（Ｆ−２）で焼却し、
スタックガスに混合した場合には、スタックガス中の硫
黄酸化物の濃度が、一般的には５０ppm 以上増加する。
これは設備費の嵩むテイルガストリータ設置の効果を減
少するものであり、好ましいことではない。The following problems are common to the above two methods. In the current sulfur recovery system, from the viewpoint of preventing air pollution, a tail gas treater (T-T
An apparatus referred to as 1) is provided, for example, a sulfur compound in tail gas is reduced to hydrogen sulfide, and then washed with an amine-based aqueous solution in an absorption tower to be recovered and still remains in tail gas leaving the absorption tower. Hydrogen sulfide is incinerated by an incinerator (F-2) provided subsequently, rendered harmless, and released into the atmosphere via the stack (U-1). Thus, in the present sulfur recovery apparatus, the concentration of sulfur oxide in the stack gas, which is the final atmospheric emission gas, is 100 to 20.
It is as low as 0 ppm. On the other hand, as described above, the sweep air containing hydrogen sulfide extracted from the sulfur pit (S-1) is incinerated by the incinerator (F-2),
When mixed with the stack gas, the concentration of sulfur oxides in the stack gas generally increases by 50 ppm or more.
This reduces the effect of installation of the tail gas treater, which requires high equipment cost, and is not preferable.
【０００７】[0007]
【発明が解決しようとする課題】本発明は、以上説明し
た従来の液体硫黄の脱ガス方法の問題点に基づいてなさ
れたものであって、簡単な設備でもって液体硫黄中の硫
化水素を効率よく脱ガスでき、しかもテイルガストリー
タのスタックガス中の硫黄酸化物の濃度を増加しない方
法を提供することを課題とする。SUMMARY OF THE INVENTION The present invention has been made on the basis of the problems of the conventional method for degassing liquid sulfur as described above, and the efficiency of hydrogen sulfide in liquid sulfur can be improved with simple equipment. An object of the present invention is to provide a method capable of degassing well and not increasing the concentration of sulfur oxides in the stack gas of a tail gas treater.
【０００８】[0008]
【課題を解決するための手段】本発明の要旨とするとこ
ろは、硫化水素を原料にしてクラウス反応によって液体
硫黄を生成する硫黄回収装置において、製品液体硫黄を
脱ガス塔内で噴霧するとともに、前記硫黄回収装置の反
応炉に供給される燃焼空気の一部を分流して前記脱ガス
塔に導入し、噴霧液体硫黄と接触せしめて液体硫黄中に
溶存している硫化水素を気化し、該硫化水素を含む燃焼
空気を前記反応炉に戻してクラウス反応に供することを
特徴とする液体硫黄の脱ガス方法である。すなわち、液
体硫黄をスプレイノズルを介して脱ガス塔内に噴霧して
ミスト状にして溶存している硫化水素が気化し易い状態
にするとともに、クラウス式硫黄回収装置の反応炉に供
給される燃焼空気の一部を分流して脱ガス塔に導入し前
記噴霧硫黄と接触させて、該空気中に硫化水素を気化さ
せて液体硫黄を脱ガスする。一方脱ガス塔を出る硫化水
素を含んだ燃焼空気は反応炉の燃焼室に供給され、通常
のクラウス式硫黄回収装置と同様に硫化水素の燃焼用に
供される。同時に燃焼空気に含まれる硫化水素も、他の
アシッドガス中の硫化水素と同様にクラウス反応の原料
ガスとして処理される。Means for Solving the Problems The gist of the present invention is that in a sulfur recovery apparatus for producing liquid sulfur by a Claus reaction from hydrogen sulfide as a raw material, the product liquid sulfur is sprayed in a degassing tower, and Part of the combustion air supplied to the reaction furnace of the sulfur recovery device is split and introduced into the degassing tower, and is brought into contact with atomized liquid sulfur to vaporize hydrogen sulfide dissolved in the liquid sulfur, A method for degassing liquid sulfur, characterized in that combustion air containing hydrogen sulfide is returned to the reactor and subjected to Claus reaction. That is, liquid sulfur is sprayed into the degassing tower through a spray nozzle to form a mist so that the dissolved hydrogen sulfide is easily vaporized, and the combustion is supplied to the reactor of the Claus sulfur recovery device. A part of the air is branched and introduced into a degassing tower and brought into contact with the atomized sulfur to vaporize hydrogen sulfide in the air to degas liquid sulfur. On the other hand, the combustion air containing hydrogen sulfide that exits the degassing tower is supplied to the combustion chamber of the reaction furnace and is used for combustion of hydrogen sulfide as in the case of a normal Claus sulfur recovery device. At the same time, hydrogen sulfide contained in the combustion air is treated as a raw material gas for the Claus reaction, like hydrogen sulfide in other acid gases.
【０００９】[0009]
【実施例】以下実施例に基づいて本発明の内容をさらに
説明する。図１は実施例の系統図である。図において、
図２と同じ機器については同じ符番で示してある。反応
炉（Ｆ−１）及び各リアクター（Ｒ−１〜３）内で、ク
ラウス反応により生成した単体硫黄は各コンデンサー
（Ｃ−１〜３）内で凝縮し液体硫黄となって硫黄ピット
（Ｓ−１）に流入する。硫黄ピット（Ｓ−１）内の液体
硫黄は、ポンプ（Ｐ−３）によって汲み出され、脱ガス
塔（Ｄ−１）に供給される。ブローワ（Ｂ−１）で昇圧
された燃焼空気の大部分は、流量指示調節計（ＦＩＣ−
１）で流量制御され、反応炉（Ｆ−１）の燃焼室にクラ
ウス反応用として供給される。そして一部は、例えばク
ラウス反応に必要な総空気量の５％前後の流量が流量指
示調節計（ＦＩＣ−２）によって流量制御されて脱ガス
塔（Ｄ−１）の下部に供給される。脱ガス塔において
は、ミスト状で流下する液体硫黄と上昇する燃焼空気が
効率よく接触し、液体硫黄中の硫化水素は燃焼空気中に
気化し拡散する。脱ガス塔頂を出る硫化水素を含んだ燃
焼空気は、反応炉（Ｆ−１）の燃焼室に供給され、空気
及び硫化水素は通常のクラウス反応に供される。この
際、前記の流量指示調節計（ＦＩＣ−１）によって流量
制御される空気量と脱ガス塔（Ｄ−１）を出る空気量の
和が、反応炉に供給されるアシッドガス中の硫化水素の
量に見合う量になる。The contents of the present invention will be further described based on the following examples. FIG. 1 is a system diagram of the embodiment. In the figure,
The same devices as those in FIG. 2 are denoted by the same reference numerals. In the reactor (F-1) and each reactor (R-1 to 3), elemental sulfur produced by the Claus reaction is condensed in each condenser (C-1 to 3) to become liquid sulfur, and sulfur pits (S -1). The liquid sulfur in the sulfur pit (S-1) is pumped out by the pump (P-3) and supplied to the degassing tower (D-1). Most of the combustion air boosted by the blower (B-1) is a flow rate indicating controller (FIC-
The flow rate is controlled in 1) and is supplied to the combustion chamber of the reactor (F-1) for Claus reaction. And a part of the total amount of air required for the Claus reaction is supplied to the lower part of the degassing column (D-1) with a flow rate of about 5% of the total air amount being controlled by a flow rate indicating controller (FIC-2). In the degassing tower, the liquid sulfur flowing in the form of mist and the rising combustion air efficiently contact each other, and hydrogen sulfide in the liquid sulfur vaporizes and diffuses in the combustion air. The combustion air containing hydrogen sulfide that exits the top of the degassing tower is supplied to the combustion chamber of the reactor (F-1), and the air and hydrogen sulfide are subjected to a normal Claus reaction. At this time, the sum of the amount of air whose flow rate is controlled by the flow rate indicating controller (FIC-1) and the amount of air which leaves the degassing tower (D-1) is the hydrogen sulfide in the acid gas supplied to the reactor. The amount will be commensurate with the amount of.
【００１０】脱ガス塔を出る硫化水素の濃度は0.5 ％以
下であり、爆発限界の下限値である3.5 ％を考慮すれば
充分に安全であるが、脱ガス塔の出口管路には硫化水素
の分析計（ＡＮ）を設けて、例えば１％を越えた場合は
警報を発し、２％を越えた場合は脱ガス塔への液体硫黄
の供給を停止する等の自動安全停止機構を設けることが
望ましい。本実施例では、反応炉の燃焼空気を用いて脱
ガスしたが、場合によってはインシネレータ（Ｆ−２）
を出る酸素濃度の少ないガスを用いて脱ガスすることも
可能である。硫黄の融点は１１５℃であり、また硫化水
素の液体硫黄に対する溶解度は、低温ほど減少すること
を考慮して脱ガス塔に供給される液体硫黄の温度は１２
０〜１４０℃の範囲で選定される。液体硫黄の温度は硫
黄ピット（Ｓ−１）に装着されるスチームコイルにより
調節され，そして脱ガス塔に入る空気の温度は，ブロ−
ワ（Ｂ−１）によって相当昇温するが必要な場合は空気
予熱噐（Ｈ−３）でさらに昇温する。また脱ガス塔（Ｄ
−１）に循環される液体硫黄の流量は、脱ガス気体と接
触をよくするため、硫黄ピットに流入する硫黄流量の数
倍とし実際には、３〜５倍の範囲である。また本実施例
においては、脱ガス塔（Ｄ−１）は空塔であるが、場合
によってはトレイ塔，充填塔等の使用も可能である。The concentration of hydrogen sulfide exiting the degassing tower is 0.5% or less, which is sufficiently safe considering the lower limit of the explosion limit of 3.5%. Analyzer (AN), for example, an alarm is issued when the amount exceeds 1%, and an automatic safety stop mechanism that stops the supply of liquid sulfur to the degassing column when the amount exceeds 2%. Is desirable. In this embodiment, the combustion air of the reactor was used for degassing, but in some cases, the incinerator (F-2) was used.
It is also possible to degas by using a gas having a low oxygen concentration that exits. Considering that the melting point of sulfur is 115 ° C., and the solubility of hydrogen sulfide in liquid sulfur decreases as the temperature decreases, the temperature of liquid sulfur supplied to the degassing column is 12
It is selected in the range of 0 to 140 ° C. The temperature of liquid sulfur is regulated by the steam coil installed in the sulfur pit (S-1), and the temperature of the air entering the degassing tower is controlled by the blower.
When it is necessary to raise the temperature considerably by using the wax (B-1), the temperature is further raised by the air preheater (H-3). The degassing tower (D
The flow rate of liquid sulfur circulated in -1) is several times the flow rate of sulfur flowing into the sulfur pit in order to improve the contact with the degassed gas, and is in the range of 3 to 5 times. Further, in the present embodiment, the degassing tower (D-1) is an empty tower, but it is also possible to use a tray tower, a packed tower or the like depending on the case.
【００１１】実施デ−タ：温度１４０℃で硫化水素を３
００ppm 含む液体硫黄を直径が１２cmのジャケット付の
空塔に１５０kg／Ｈの流量割合で、塔頂よりスプレイノ
ズルを用いて噴霧し、塔下部より温度１２０℃の空気を
5.5 Ｎｍ3 ／Ｈの割合で供給して脱ガス実験を行ったと
ころ、次の結果が得られた。 液体硫黄の残存硫化水素濃度 ： １２ppm 塔頂を出る空気中の硫化水素濃度 ： 0.50％Implementation data: Hydrogen sulfide 3 at a temperature of 140.degree.
Liquid sulfur containing 00 ppm was sprayed into a 12 cm diameter superficial tower with a jacket at a flow rate of 150 kg / H using a spray nozzle from the top of the tower, and air at a temperature of 120 ° C. from the bottom of the tower.
The following results were obtained when the degassing experiment was performed by supplying the gas at a rate of 5.5 Nm 3 / H. Residual hydrogen sulfide concentration of liquid sulfur: 12 ppm Hydrogen sulfide concentration in air exiting the tower top: 0.50%
【００１２】[0012]
【発明の効果】以上説明した構成と作用を有する本発明
によれば、次の効果が得られる。 （イ）液体硫黄より脱ガスされた硫化水素は、反応炉で
アシッドガス中の硫化水素と同様にクラウス反応に供さ
れるので、スタックガス中の硫黄酸化物の濃度を増加す
ることはない。 （ロ）脱ガス用の空気は反応炉の燃焼空気を利用できる
ので特別の空気源は不要である。 （ハ）液体硫黄の脱ガスの程度は、脱ガス塔に供給する
液体硫黄の循環量及び空気量を増減することにより容易
に調節できる。According to the present invention having the above-described structure and operation, the following effects can be obtained. (A) Since hydrogen sulfide degassed from liquid sulfur is subjected to the Claus reaction in the reaction furnace in the same manner as hydrogen sulfide in acid gas, it does not increase the concentration of sulfur oxides in the stack gas. (B) Since the degassing air can use the combustion air of the reactor, no special air source is required. (C) The degree of degassing of liquid sulfur can be easily adjusted by increasing or decreasing the circulating amount of liquid sulfur and the amount of air supplied to the degassing tower.
【図１】本発明の実施例の系統図FIG. 1 is a system diagram of an embodiment of the present invention.
【図２】従来の硫黄回収装置の系統図[Fig. 2] System diagram of a conventional sulfur recovery device
Ｂ−１：燃焼空気ブローク、Ｃ−１〜３：コンデンサ
ー、Ｄ−１：脱ガス塔、Ｅ−１：スチームエジェクタ
ー、Ｆ−１：反応炉、Ｆ−２：インシネレータ、Ｈ−１
〜２：予熱器、Ｈ−３：空気予熱器，Ｐ−１〜３：ポン
プ、Ｒ−１〜２：リアクター、Ｓ−１：硫黄ピット、Ｔ
−１：テイルガストリータ、Ｕ−１：スタック，Ａ．
Ｇ：アシッドガス，Ｃ．Ａ：燃焼空気，Ｔ．Ｇ：テイル
ガス，，Ｓ．Ｔ：スチ−ム，Ｌ．Ｓ：液体硫黄。B-1: Combustion air broke, C-1 to 3: Condenser, D-1: Degassing tower, E-1: Steam ejector, F-1: Reactor, F-2: Incinerator, H-1
-2: Preheater, H-3: Air preheater, P-1 to 3: Pump, R-1 to 2: Reactor, S-1: Sulfur pit, T
-1, tail gas treater, U-1: stack, A.I.
G: Acid gas, C.I. A: Combustion air, T.I. G: Tail gas, S.S. T: Steam, L.A. S: Liquid sulfur.
Claims (1)
て液体硫黄を生成する硫黄回収装置において、製品液体
硫黄を脱ガス塔内で噴霧するとともに、前記硫黄回収装
置の反応炉に供給される燃焼空気の一部を分流して前記
脱ガス塔に導入し、噴霧液体硫黄と接触せしめて液体硫
黄中に溶存している硫化水素を気化し、該硫化水素を含
む燃焼空気を前記反応炉に戻してクラウス反応に供する
ことを特徴とする液体硫黄の脱ガス方法。1. A sulfur recovery apparatus for producing liquid sulfur by a Claus reaction using hydrogen sulfide as a raw material, wherein the product liquid sulfur is sprayed in a degassing tower, and the combustion air is supplied to the reaction furnace of the sulfur recovery apparatus. A part of the gas is introduced into the degassing tower, the hydrogen sulfide dissolved in the liquid sulfur is vaporized by contacting with the spray liquid sulfur, and the combustion air containing the hydrogen sulfide is returned to the reactor. A method for degassing liquid sulfur, which comprises subjecting it to a Claus reaction.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP22123691A JPH0725522B2 (en) | 1991-08-07 | 1991-08-07 | Method of degassing liquid sulfur |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP22123691A JPH0725522B2 (en) | 1991-08-07 | 1991-08-07 | Method of degassing liquid sulfur |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0543207A true JPH0543207A (en) | 1993-02-23 |
| JPH0725522B2 JPH0725522B2 (en) | 1995-03-22 |
Family
ID=16763605
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP22123691A Expired - Lifetime JPH0725522B2 (en) | 1991-08-07 | 1991-08-07 | Method of degassing liquid sulfur |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0725522B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102923670A (en) * | 2012-11-22 | 2013-02-13 | 山东三维石化工程股份有限公司 | Liquid sulfur degasification process |
-
1991
- 1991-08-07 JP JP22123691A patent/JPH0725522B2/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102923670A (en) * | 2012-11-22 | 2013-02-13 | 山东三维石化工程股份有限公司 | Liquid sulfur degasification process |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0725522B2 (en) | 1995-03-22 |
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