JPH06277439A - Tail gas treatment apparatus in claus process - Google Patents
Tail gas treatment apparatus in claus processInfo
- Publication number
- JPH06277439A JPH06277439A JP5088181A JP8818193A JPH06277439A JP H06277439 A JPH06277439 A JP H06277439A JP 5088181 A JP5088181 A JP 5088181A JP 8818193 A JP8818193 A JP 8818193A JP H06277439 A JPH06277439 A JP H06277439A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- separation membrane
- membrane module
- tail gas
- waste heat
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、クラウス法テールガス
の処理装置に関するものであり、詳しくは、分離膜モジ
ュールを利用することにより、設備費が安価で且つ運転
管理が容易なクラウス法テールガスの処理装置に関する
ものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a Claus tail gas treatment apparatus, and more particularly, to a Claus tail gas treatment with low equipment cost and easy operation management by using a separation membrane module. It relates to the device.
【０００２】[0002]
【従来の技術】周知の通り、クラウス法硫黄回収装置
は、Ｈ2 Ｓガスから単体硫黄を回収するための装置であ
る。その反応工程は、Ｈ2 Ｓガスの３分の１を空気酸化
してＨ2Ｓ：ＳＯ2 の比率を２：１に調整する第１工程
と、アルミナ触媒によりＨ2 ＳとＳＯ2 とを反応させて
単体硫黄に変換させる第２工程とから成る。第２工程の
反応は、通常、２００〜３００℃の温度で行われ、単体
硫黄は、第２工程の反応器流出ガスを冷却することによ
り、硫黄分を凝縮して回収される。As is well known, the Claus Claus sulfur recovery device is a device for recovering elemental sulfur from H 2 S gas. In the reaction step, the first step in which one-third of H 2 S gas is air-oxidized to adjust the ratio of H 2 S: SO 2 to 2: 1, and H 2 S and SO 2 are mixed with an alumina catalyst. A second step of reacting and converting to elemental sulfur. The reaction in the second step is usually carried out at a temperature of 200 to 300 ° C., and elemental sulfur is recovered by condensing the sulfur content by cooling the reactor outflow gas in the second step.
【０００３】第２工程の反応器の段数を増加させること
により、単体硫黄の回収率はある程度にまで高めること
が出来、例えば、反応器段数が２段の場合の回収率は約
９５％、反応器段数が３段の場合の回収率は約９７％と
なる。The recovery rate of elemental sulfur can be increased to some extent by increasing the number of reactor stages in the second step. For example, when the number of reactor stages is 2, the recovery rate is about 95%. When the number of plates is 3, the recovery rate is about 97%.
【０００４】近時、石油製品の中においては、ガソリン
等の軽質留分の需要が増大しおり、これがために、製油
所においては重質留分の水素化分解による軽質化が盛ん
に行なわれている。その結果、多量のＨ2 Ｓガスが水素
化分解工程において発生する。また、トラックやバス等
のデーゼルエンジン用軽油の窒素分および硫黄分の規制
が強化され、軽油の深度脱硫装置が数多く設置されるよ
うになってきた。その結果、上記と同様に、多量のＨ2
Ｓガスが脱硫工程において発生する自体になっている。Recently, in petroleum products, demand for light distillates such as gasoline has been increasing, and for this reason, heavy distillates have been actively lightened by hydrocracking in heavy oil distillates. There is. As a result, a large amount of H 2 S gas is generated in the hydrocracking process. Further, regulations on nitrogen content and sulfur content of light oil for diesel engines such as trucks and buses have been strengthened, and a large number of deep oil desulfurization devices have been installed. As a result, a large amount of H 2
S gas is itself generated in the desulfurization process.
【０００５】上記のような製油所におけるＨ2 Ｓ含有ガ
スは、ガス吸収装置で処理され、高濃度のＨ2 Ｓガス
（アシッドガスと呼ばれる）として集められ、前記のク
ラウス法硫黄回収装置に供給されて単体硫黄として回収
される。ところで、アシッドガスの発生量が多量になる
に従い、クラウス法硫黄回収装置からのテールガスの処
理が一層重要となる。例えば、硫黄回収量３００Ｔ／Ｄ
の装置において、単体硫黄の回収率が９７％の場合に
は、硫黄換算で９Ｔ／Ｄの多量の硫黄化合物が大気に放
出される結果となる。The H 2 S-containing gas in the refinery as described above is processed by a gas absorption device, collected as a high-concentration H 2 S gas (called acid gas), and supplied to the Claus sulfur recovery device. It is recovered as elemental sulfur. By the way, as the amount of generated acid gas increases, the treatment of tail gas from the Claus sulfur recovery device becomes more important. For example, sulfur recovery amount 300T / D
In the apparatus described above, when the recovery rate of elemental sulfur is 97%, a large amount of sulfur compound of 9 T / D in terms of sulfur is released to the atmosphere.
【０００６】従来、クラウス法テールガスの処理装置と
しては、所謂ビーボン法とスコット法とが知られてい
る。ビーボン法は、米国パーソンズ社のビーボン氏によ
って開発された方法である（特公昭４９−１１１４２号
公報参照）。スコット法は、オランダのシエル社によっ
て開発された方法である（特公昭５７−１５８４６号公
報参照）。Conventionally, the so-called Biebon method and Scott method are known as a Claus gas tail gas processing apparatus. The Bevon method is a method developed by Mr. Bevon of Parsons, Inc. (see Japanese Patent Publication No. 49-11142). The Scott method is a method developed by Ciel GmbH of the Netherlands (see Japanese Patent Publication No. 57-15846).
【０００７】ビーボン法の概要は次の通りである。すな
わち、先ず、クラウス法硫黄回収装置からのテールガス
に水素含有ガスを添加し、３５０℃に予熱してからＣＯ
ＭＯＸ（コバルト−モリブデン）触媒に通し、テールガ
ス中の硫黄化合物を還元してＨ2 Ｓに転換する。次い
で、Ｈ2 Ｓ含有ガスをストレトフオード法と呼ばれる吸
収法で処理する。ストレトフオード法の吸収液は、炭酸
ナトリウムをベースとし酸化触媒を含有しており、再生
工程において、Ｈ2 Ｓ含有吸収液を空気酸化することに
より、Ｈ2 Ｓは単体硫黄に変換される。The outline of the Beebon method is as follows. That is, first, a hydrogen-containing gas is added to the tail gas from the Claus sulfur recovery device, preheated to 350 ° C., and then CO
It passes through a MOX (cobalt-molybdenum) catalyst to reduce the sulfur compound in the tail gas and convert it into H 2 S. Next, the H 2 S-containing gas is treated by an absorption method called the Stretford method. The absorption liquid of the Strethode method contains sodium carbonate as a base and contains an oxidation catalyst, and in the regeneration step, H 2 S-containing absorption liquid is air-oxidized to convert H 2 S to elemental sulfur.
【０００８】上記の場合の単体硫黄は液中のスカム状で
あるため、濾過機やフイルタープレス等を使用した通常
の固液分離設備により、固体硫黄として回収される。一
方、再生された吸収液は吸収塔に循環されて再使用され
る。ビーボン法によれば、吸収塔からのテールガス中の
Ｈ2 Ｓ濃度を約１００ｐｐｍまで低減することが出来
る。In the above case, the elemental sulfur is in the form of scum in the liquid, and thus it is recovered as solid sulfur by the usual solid-liquid separation equipment using a filter, a filter press or the like. On the other hand, the regenerated absorption liquid is circulated to the absorption tower for reuse. According to the Bevon method, the H 2 S concentration in the tail gas from the absorption tower can be reduced to about 100 ppm.
【０００９】スコット法の概要は次の通りである。すな
わち、先ず、ビーボン法の場合と同様にしてテールガス
中の硫黄化合物を還元してＨ2 Ｓに転換する。次いで、
吸収液としてジイソプロパノールアミンの水溶液を使用
する吸収法でＨ2 Ｓ含有ガスを処理する。吸収塔におい
て、ガス中のＨ2 Ｓは選択的に吸収され、再生塔におい
てストリツピングして回収されたＨ2 Ｓは、クラウス法
硫黄回収装置に循環され、アシッドガスと共に原料Ｈ2
Ｓとして使用される。スコット法によれば、吸収塔から
のテールガス中のＨ2 Ｓ濃度を約１５０ｐｐｍまで低減
することが出来る。The outline of the Scott method is as follows. That is, first, the sulfur compound in the tail gas is reduced and converted into H 2 S in the same manner as in the Bevon method. Then
The H 2 S-containing gas is treated by an absorption method using an aqueous solution of diisopropanolamine as the absorption liquid. In the absorption tower, H 2 S in the gas is selectively absorbed, H 2 S recovered by Sutoritsupingu in the regeneration tower is recycled to the Claus process sulfur recovery unit, the raw material H 2 with Acid Gas
Used as S. According to the Scott method, the H 2 S concentration in the tail gas from the absorption tower can be reduced to about 150 ppm.
【００１０】[0010]
【発明が解決しようとする課題】しかしながら、ビーボ
ン法の場合、液中のスカム状の単体硫黄の回収のため、
運転や保守が一般に困難な固液分離設備を必要とし、し
かも、単体硫黄其自体がスカム状であるために取り扱い
が容易ではないと言う欠点がある。一方、スコット法の
場合は、上記の欠点はないものの、設備費が一般に高額
である吸収塔や再生塔を必要とし、しかも、吸収液の再
生に相当量のスチームを必要としてランニングコストが
高いと言う欠点がある。本発明は、上記実情に鑑みなさ
れたものであり、その目的は、設備費が安価で且つ運転
管理が容易なクラウス法テールガスの処理装置を提供す
ることにある。However, in the case of the Bevon method, in order to recover scum-like elemental sulfur in the liquid,
It has the drawback that it requires solid-liquid separation equipment that is generally difficult to operate and maintain, and that it is not easy to handle because the elemental sulfur itself is scum-like. On the other hand, in the case of the Scott method, although the above-mentioned drawbacks are not present, an absorption tower and a regeneration tower, which are generally expensive in equipment cost, are required, and further, a considerable amount of steam is required to regenerate the absorption liquid, resulting in high running cost. There is a drawback to say. The present invention has been made in view of the above circumstances, and an object of the present invention is to provide a Claus tail gas treatment apparatus that has a low equipment cost and is easy to operate and manage.
【００１１】[0011]
【課題を解決するための手段】すなわち、本発明の要旨
は、クラウス法硫黄回収装置におけるテールガスの処理
装置であって、テールガス及び還元ガスが導入される昇
温炉と、当該昇温炉から導出される混合ガスが導入され
る還元触媒反応器と、当該反応器から導出される反応排
ガスが導入される廃熱回収設備と、当該廃熱回収設備か
ら導出されるガスを昇圧する圧縮機と、当該圧縮機から
導出される昇圧ガスが導入され且つＨ2Ｓガスが選択的
に透過される分離膜モジュールと、当該分離膜モジュー
ルの透過ガスをクラウス法硫黄回収装置に供給する循環
管路と、上記分離膜モジュールの非透過ガスを焼却炉に
供給する管路とを包含することを特徴とするクラウス法
テールガスの処理装置に存する。That is, the gist of the present invention is a tail gas treating apparatus in a Claus Claus sulfur recovery apparatus, in which a tail gas and a reducing gas are introduced, and a temperature raising furnace is derived from the temperature raising furnace. A reduction catalyst reactor into which the mixed gas is introduced, a waste heat recovery facility into which the reaction exhaust gas derived from the reactor is introduced, and a compressor that pressurizes the gas derived from the waste heat recovery facility, A separation membrane module into which the pressurized gas derived from the compressor is introduced and through which H 2 S gas is selectively permeated; and a circulation line for supplying the permeation gas of the separation membrane module to a Claus sulfur recovery device, And a pipeline for supplying the non-permeable gas of the separation membrane module to an incinerator.
【００１２】[0012]
【作用】本発明の処理装置においては、先ず、テールガ
ス中の硫黄化合物を還元してＨ2 Ｓに転換する。次い
で、テールガスを昇圧し、分離膜モジュールで処理し、
透過ガス側に得られた高濃度のＨ2 Ｓを硫黄回収装置に
循環し、アシッドガスと共に原料ガスとして処理する。
一方、分離膜モジュールの非透過ガス側に得られる窒素
を主体とするガスは、焼却炉で処理し、残存している微
量のＨ2 ＳをＳＯ2として大気放出する。In the treatment apparatus of the present invention, first, the sulfur compound in the tail gas is reduced and converted into H 2 S. Then, the tail gas is pressurized and treated with a separation membrane module,
The high-concentration H 2 S obtained on the permeate gas side is circulated to the sulfur recovery device and treated as a raw material gas together with the acid gas.
On the other hand, the gas mainly containing nitrogen obtained on the non-permeable gas side of the separation membrane module is treated in the incinerator, and the trace amount of remaining H 2 S is released to the atmosphere as SO 2 .
【００１３】[0013]
【実施例】以下、本発明の実施例を添付図面に基づいて
説明する。図１は、本発明のクラウス法テールガスの処
理装置の説明図である。本発明の処理装置は、昇温炉
（１０）、還元触媒反応器（２０）、廃熱回収設備（３
０）、圧縮機（４０）及び分離膜モジュール（５０）か
ら主として構成される。Embodiments of the present invention will be described below with reference to the accompanying drawings. FIG. 1 is an explanatory view of a Claus tail gas treating apparatus of the present invention. The processing apparatus of the present invention comprises a heating furnace (10), a reduction catalyst reactor (20), a waste heat recovery facility (3
0), a compressor (40) and a separation membrane module (50).
【００１４】昇温炉（１０）は、クラウス法硫黄回収装
置からのテールガス及び還元ガスを所定の温度に高める
機能を有する。昇温炉（１０）としては、例えば、燃焼
加熱方式などの従来公知の形式の昇温炉を採用すること
が出来る。硫黄化合物（Ｈ2Ｓ、ＳＯ2 、ＣＯＳ、ＣＳ
2 等）を含有するテールガスは、クラウス法硫黄回収装
置（１００）から管路（１）を通し、還元ガス（水素、
一酸化炭素など）は、管路（２）を通して昇温炉（１
０）に導入される。The temperature raising furnace (10) has a function of raising the tail gas and the reducing gas from the Claus sulfur recovery device to a predetermined temperature. As the temperature raising furnace (10), for example, a conventionally known type temperature raising furnace such as a combustion heating system can be adopted. Sulfur compounds (H 2 S, SO 2 , COS, CS
The tail gas containing ( 2 etc.) is passed through the pipeline (1) from the Claus sulfur recovery device (100) and the reducing gas (hydrogen,
Carbon monoxide, etc., is passed through the pipe (2) to the heating furnace (1
0).
【００１５】テールガス及び還元ガスは、昇温炉（１
０）に導入され、管路（３）から供給される燃料ガスの
燃焼熱によって加熱される。テールガス及び還元ガスの
混合ガスは、昇温炉（１０）において、通常、３００〜
４００℃の範囲の還元反応に好適な温度に加熱される。The tail gas and the reducing gas are supplied to the heating furnace (1
0) and is heated by the combustion heat of the fuel gas supplied from the pipe (3). The mixed gas of the tail gas and the reducing gas is usually 300 to 300 in the temperature raising furnace (10).
It is heated to a temperature suitable for the reduction reaction in the range of 400 ° C.
【００１６】還元触媒反応器（２０）は、昇温炉（１
０）から導出される混合ガスの還元反応を行なう機能を
有する。還元触媒反応器（２０）としては、通常、還元
触媒を固定床として内蔵する反応器が採用される。触媒
としては、周知の還元触媒を使用することが出来る。触
媒は必要に応じて耐火性担体に担持させて使用する。耐
火性担体としては、シリカ、アルミナ、シリカ−アルミ
ナ担体などが使用される。好適な触媒は、コバルト、モ
リブデン、鉄、クロム、バナジウム、トリウム、ニッケ
ル、タングステン、ウランの１種または２種以上を含有
する触媒である。The reduction catalyst reactor (20) is a heating furnace (1
It has a function of performing a reduction reaction of the mixed gas derived from 0). As the reduction catalyst reactor (20), a reactor containing a reduction catalyst as a fixed bed is usually adopted. As the catalyst, a known reduction catalyst can be used. The catalyst is used by supporting it on a refractory carrier as needed. As the refractory carrier, silica, alumina, silica-alumina carrier or the like is used. Suitable catalysts are catalysts containing one or more of cobalt, molybdenum, iron, chromium, vanadium, thorium, nickel, tungsten, uranium.
【００１７】特に好適な触媒は、コバルト−モリブデン
触媒またはニッケル−モリブデン触媒であり、混合ガス
の還元触媒反応器（２０）における空間速度は、一般的
には、１０００〜２０００Ｈｒ-1の範囲から選択され
る。る。昇温炉（１０）において約３５０℃に予熱され
た混合ガスは、管路（４）を通して還元触媒反応器（２
０）に導入され、混合ガス中の硫黄化合物は、例えば、
次の反応式に従って硫化水素に転換される。Particularly preferred catalysts are cobalt-molybdenum catalysts or nickel-molybdenum catalysts, the space velocity of the mixed gas reduction catalytic reactor (20) is generally selected from the range of 1000 to 2000 Hr -1. To be done. It The mixed gas preheated to about 350 ° C. in the temperature raising furnace (10) passes through the pipe (4) and the reduction catalyst reactor (2).
0), the sulfur compound in the mixed gas is, for example,
It is converted to hydrogen sulfide according to the following reaction formula.
【００１８】[0018]
【化１】 [Chemical 1]
【００１９】廃熱回収設備（３０）は、還元反応によっ
て温度上昇した反応排ガスの温度を常温付近まで冷却す
る機能を有する。廃熱回収設備（３０）としては、特に
制限はないが、通常は、自然循環式の廃熱ボイラー（３
０ａ）と冷却器（３０ｂ）を組み合わせた設備が好適に
使用される。斯かる廃熱回収設備によれば、廃熱ボイラ
ー（３０ａ）の出口における反応排ガスの温度を１７０
℃程度に設定することにより、廃熱ボイラー（３０ａ）
において低圧スチームを発生させて利用することが出来
る。還元触媒反応器（２０）から導出される反応排ガス
は、管路（５）通して廃熱回収設備（３０）に導入さ
れ、常温付近まで冷却される。The waste heat recovery equipment (30) has a function of cooling the temperature of the reaction exhaust gas whose temperature has risen due to the reduction reaction to near room temperature. The waste heat recovery equipment (30) is not particularly limited, but is usually a natural circulation type waste heat boiler (3
0a) and a cooler (30b) in combination are preferably used. According to such waste heat recovery equipment, the temperature of the reaction exhaust gas at the outlet of the waste heat boiler (30a) is set to 170
Waste heat boiler (30a) by setting at about ℃
At, low pressure steam can be generated and used. The reaction exhaust gas discharged from the reduction catalytic reactor (20) is introduced into the waste heat recovery facility (30) through the pipe line (5) and cooled to near room temperature.
【００２０】圧縮機（４０）は、廃熱回収設備（３０）
から導出されるガスを所定の圧力まで昇圧する機能を有
する。圧縮機（４０）としては、公知の遠心式圧縮機ま
たは往復動式圧縮機を使用することが出来る。管路
（６）通して圧縮機（４０）に導入されたガスは、通
常、２〜５ａｔＧ、好ましくは３ａｔＧ程度に昇圧され
る。好ましい態様として、管路（６）の途中に設けられ
た分離器（６０）は、ガス中のドレンを除去する機能を
有する。The compressor (40) is a waste heat recovery facility (30).
It has a function of increasing the pressure of the gas derived from the gas to a predetermined pressure. As the compressor (40), a known centrifugal compressor or a reciprocating compressor can be used. The gas introduced into the compressor (40) through the pipe (6) is normally pressurized to 2 to 5 atG, preferably about 3 atG. In a preferred embodiment, the separator (60) provided in the middle of the pipe (6) has a function of removing drain in the gas.
【００２１】分離膜モジュール（５０）は、圧縮機（４
０）から導出される昇圧ガスからＨ2 Ｓガスを選択的に
分離する機能を有する。分離膜モジュール（５０）とし
ては、特に制限されないが、一般的には、分離膜として
中空糸を使用した分離膜モジュールが使用される。斯か
る中空糸分離膜モジュールは、通常０．１〜１．０ｍｍ
径の多数の中空糸を管束状に束ねて圧力容器に収納して
構成される。そして、中空糸分離膜の外側（高圧側）と
内側（低圧側）の各々のガス成分の分圧差を推進力と
し、透過速度の差により、比較的速いガスと比較的遅い
ガスの分離を行なう。The separation membrane module (50) includes a compressor (4
0) has a function of selectively separating H 2 S gas from the boosted gas. The separation membrane module (50) is not particularly limited, but generally, a separation membrane module using a hollow fiber as the separation membrane is used. Such a hollow fiber separation membrane module usually has a thickness of 0.1 to 1.0 mm.
A large number of hollow fibers having a large diameter are bundled into a tube bundle and housed in a pressure vessel. Then, the difference in partial pressure between the gas components on the outside (high pressure side) and the inside (low pressure side) of the hollow fiber separation membrane is used as the propulsion force, and a relatively fast gas and a relatively slow gas are separated by the difference in permeation speed. .
【００２２】中空糸分離膜モジュールを使用する場合、
本発明においては、中空糸分離膜として、Ｈ2 Ｓガスが
選択的に透過される膜材料で構成された中空糸分離膜を
使用する。斯かる中空糸分離膜としては、例えば、ポリ
スルホン系、セルローズ系、ポリイミド系またはポリア
ラミド系の中空糸分離膜が挙げられる。何れにしても、
中空糸分離膜で処理する場合、透過するガス中のＨ2 Ｓ
の含有量は数％と少ないため、膜面積は小さくて済むと
言う利点がある。なお、本発明においては、分離膜モジ
ュール（５０）としては、上記のような有機系中空糸分
離膜を使用した分離膜モジュールの他に、Ｈ2 Ｓガスを
選択的に透過し得る限り、例えば、セラミックスや金属
などの無機系材料で構成される気体分離膜を使用するこ
とも出来る。When using the hollow fiber separation membrane module,
In the present invention, as the hollow fiber separation membrane, a hollow fiber separation membrane composed of a membrane material that allows H 2 S gas to selectively permeate is used. Examples of such hollow fiber separation membranes include polysulfone-based, cellulose-based, polyimide-based, or polyaramid-based hollow fiber separation membranes. Whatever it is,
When treating with a hollow fiber separation membrane, H 2 S
Since the content of is as small as several percent, there is an advantage that the film area can be small. In the present invention, as the separation membrane module (50), in addition to the separation membrane module using the organic hollow fiber separation membrane as described above, as long as H 2 S gas can be selectively permeated, for example, Alternatively, a gas separation membrane composed of an inorganic material such as ceramics or metal can be used.
【００２３】管路（７）を通して分離膜モジュール（中
空糸分離膜モジュール）（５０）のシエル側に導入され
た昇圧ガスは、その中のＨ2 Ｓガスが選択的に透過さ
れ、Ｈ2 Ｓ濃縮ガスと、Ｎ2 を主成分とし、ＣＯ2 等の
他の成分を含有する非透過ガスとに分離される。そし
て、Ｈ2 Ｓ濃縮ガスは、分離膜の低圧側（内側）から透
過ガスとして導出される。Ｎ2 を主成分とし微量のＨ2
Ｓを含有するガスは、中空糸分離膜の高圧側（外側）か
ら非透過ガスとして導出される。好ましい態様として、
管路（７）の途中に設けられた冷却器（７０）及び分離
器（８０）は、圧縮ガス中のドレンを除去する機能を有
する。The separation membrane module (hollow fiber separation membrane module) through a line (7) (50) boosting gas introduced into the shell side of, H 2 S gas therein is selectively permeable, H 2 S It is separated into a concentrated gas and an impermeable gas containing N 2 as a main component and other components such as CO 2 . Then, the H 2 S concentrated gas is derived as a permeated gas from the low pressure side (inside) of the separation membrane. N 2 as a main component and a trace amount of H 2
The gas containing S is discharged as a non-permeable gas from the high pressure side (outside) of the hollow fiber separation membrane. In a preferred embodiment,
The cooler (70) and the separator (80) provided in the middle of the pipe (7) have a function of removing drain in the compressed gas.
【００２４】分離膜モジュール（５０）の透過ガスは、
循環管路（８）を通し、アシッドガスとして、クラウス
法硫黄回収装置（１００）に供給され、非透過ガスは、
管路（９）を通して焼却炉（２００）に供給される。The permeation gas of the separation membrane module (50) is
The acid gas is supplied to the Claus sulfur recovery device (100) through the circulation line (8), and the non-permeated gas is
It is supplied to the incinerator (200) through the line (9).
【００２５】一般に、前述の分離膜モジュール（５０）
は次のような特徴を有する。 ガスの分圧を推進力として分離を行なうため、供給ガ
スの圧力以外には分離のためのエネルギーやユーティリ
ティーは殆ど不要である（省エネルギー）。 管束状のモジュールを使用しているため、配管、計装
などのシステム全体をコンパクトにまとめることが出来
て設置スペースが小さい（省スペース）。 スタートアップやシャットダウンが極めて容易であ
り、通常運転中は殆ど操作の必要がなく、しかも、負荷
変動に対しても容易に操作を行なうことが出来る（優れ
た操作性）。 駆動部がない（メンテナンス・フリー）。Generally, the separation membrane module (50) described above.
Has the following features. Since the separation is performed by using the partial pressure of the gas as a driving force, almost no energy or utility for separation other than the pressure of the supply gas is needed (energy saving). Since a tube bundle type module is used, the entire system such as piping and instrumentation can be compactly packed, and the installation space is small (space saving). Startup and shutdown are extremely easy, almost no operation is required during normal operation, and it is possible to easily operate even for load fluctuations (excellent operability). There is no drive (maintenance free).
【００２６】[0026]
【発明の効果】本発明は、上記の分離膜モジュール（５
０）をクラウス法テールガスの処理装置に巧みに利用し
たことにより、従来公知のビーボン法やスコット法に比
し、設備費が安価で且つ運転管理が容易であると言う工
業的に顕著な効果を発揮することが出来る。よって、本
発明の工業的価値は顕著である。The present invention provides the separation membrane module (5
Skillfully using 0) as a Claus tail gas treatment device, the industrially remarkable effect that the equipment cost is lower and the operation management is easier than the conventionally known Biebon method or Scott method is achieved. Can be demonstrated. Therefore, the industrial value of the present invention is remarkable.
【図１】本発明のクラウス法テールガスの処理装置の説
明図である。FIG. 1 is an explanatory view of a Claus tail gas processing apparatus of the present invention.
１０：昇温炉 ２０：還元触媒反応器 ３０：廃熱回収設備 ４０：圧縮機 ５０：分離膜モジュール １００：クラウス法硫黄回収装置 ２００：焼却炉 10: Temperature rising furnace 20: Reduction catalytic reactor 30: Waste heat recovery equipment 40: Compressor 50: Separation membrane module 100: Claus sulfur recovery device 200: Incinerator
Claims (1)
ガスの処理装置であって、テールガス及び還元ガスが導
入される昇温炉と、当該昇温炉から導出される混合ガス
が導入される還元触媒反応器と、当該反応器から導出さ
れる反応排ガスが導入される廃熱回収設備と、当該廃熱
回収設備から導出されるガスを昇圧する圧縮機と、当該
圧縮機から導出される昇圧ガスが導入され且つＨ2 Ｓガ
スが選択的に透過される分離膜モジュールと、当該分離
膜モジュールの透過ガスをクラウス法硫黄回収装置に供
給する循環管路と、上記分離膜モジュールの非透過ガス
を焼却炉に供給する管路とを包含することを特徴とする
クラウス法テールガスの処理装置。1. A device for treating tail gas in a Claus sulfur recovery device, comprising a temperature rising furnace into which a tail gas and a reducing gas are introduced, and a reduction catalyst reactor into which a mixed gas derived from the temperature rising furnace is introduced. And a waste heat recovery facility into which the reaction exhaust gas derived from the reactor is introduced, a compressor for increasing the pressure of the gas derived from the waste heat recovery facility, and a boosted gas derived from the compressor. Further, a separation membrane module through which H 2 S gas is selectively permeated, a circulation line for supplying the permeation gas of the separation membrane module to the Claus sulfur recovery device, and the non-permeation gas of the separation membrane module to an incinerator. Clause tail gas treatment device characterized by including a supply line.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5088181A JP2745099B2 (en) | 1993-03-23 | 1993-03-23 | Klaus tail gas treatment equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5088181A JP2745099B2 (en) | 1993-03-23 | 1993-03-23 | Klaus tail gas treatment equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH06277439A true JPH06277439A (en) | 1994-10-04 |
| JP2745099B2 JP2745099B2 (en) | 1998-04-28 |
Family
ID=13935743
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5088181A Expired - Fee Related JP2745099B2 (en) | 1993-03-23 | 1993-03-23 | Klaus tail gas treatment equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2745099B2 (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100494135B1 (en) * | 2000-12-05 | 2005-06-10 | 주식회사 포스코 | Method for treating tail gas in sintering process |
| CN102989268A (en) * | 2011-09-15 | 2013-03-27 | 中国石油化工股份有限公司 | Method for processing Claus tail gas through membrane separation |
| WO2018169918A1 (en) * | 2017-03-13 | 2018-09-20 | Saudi Arabian Oil Company | Enhancement of claus tail gas treatment with membrane and reducing step |
| CN110603087A (en) * | 2017-03-10 | 2019-12-20 | 沙特阿拉伯石油公司 | Enhancing Claus tail gas treatment using sulfur dioxide selective membrane technology |
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| CN102631827A (en) * | 2012-04-11 | 2012-08-15 | 山东三维石化工程股份有限公司 | Zero-emission sulfur recovery technology combined with low-temperature methanol washing acid gas treatment |
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1993
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100494135B1 (en) * | 2000-12-05 | 2005-06-10 | 주식회사 포스코 | Method for treating tail gas in sintering process |
| CN102989268A (en) * | 2011-09-15 | 2013-03-27 | 中国石油化工股份有限公司 | Method for processing Claus tail gas through membrane separation |
| CN102989268B (en) * | 2011-09-15 | 2015-11-25 | 中国石油化工股份有限公司 | A kind of method adopting membrane separation Claus tail gases |
| US10898885B2 (en) | 2016-04-11 | 2021-01-26 | Saudi Arabian Oil Company | Nano-sized zeolite supported catalysts and methods for their production |
| US11084992B2 (en) | 2016-06-02 | 2021-08-10 | Saudi Arabian Oil Company | Systems and methods for upgrading heavy oils |
| CN110603087A (en) * | 2017-03-10 | 2019-12-20 | 沙特阿拉伯石油公司 | Enhancing Claus tail gas treatment using sulfur dioxide selective membrane technology |
| WO2018169918A1 (en) * | 2017-03-13 | 2018-09-20 | Saudi Arabian Oil Company | Enhancement of claus tail gas treatment with membrane and reducing step |
| CN110612150A (en) * | 2017-03-13 | 2019-12-24 | 沙特阿拉伯石油公司 | Enhanced Claus tail gas treatment with membrane and reduction steps |
| US10689587B2 (en) | 2017-04-26 | 2020-06-23 | Saudi Arabian Oil Company | Systems and processes for conversion of crude oil |
| US10696910B2 (en) | 2017-07-17 | 2020-06-30 | Saudi Arabian Oil Company | Systems and methods for processing heavy oils by oil upgrading followed by distillation |
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| US10689585B2 (en) | 2017-07-17 | 2020-06-23 | Saudi Arabian Oil Company | Systems and methods for processing heavy oils |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2745099B2 (en) | 1998-04-28 |
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