JPH0345505A - Method for purifying liquid sulfur - Google Patents
Method for purifying liquid sulfurInfo
- Publication number
- JPH0345505A JPH0345505A JP17912689A JP17912689A JPH0345505A JP H0345505 A JPH0345505 A JP H0345505A JP 17912689 A JP17912689 A JP 17912689A JP 17912689 A JP17912689 A JP 17912689A JP H0345505 A JPH0345505 A JP H0345505A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- sulfur
- liquid sulfur
- solid catalyst
- sweep 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
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 48
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 48
- 239000011593 sulfur Substances 0.000 title claims abstract description 47
- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000007788 liquid Substances 0.000 title claims abstract description 25
- 239000007789 gas Substances 0.000 claims abstract description 44
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 41
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 41
- 239000011949 solid catalyst Substances 0.000 claims abstract description 10
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 7
- 238000006243 chemical reaction Methods 0.000 abstract description 13
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 abstract description 5
- 229910001882 dioxygen Inorganic materials 0.000 abstract description 5
- 239000011261 inert gas Substances 0.000 abstract description 3
- -1 inexpensive air Chemical compound 0.000 abstract description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract 3
- 239000001257 hydrogen Substances 0.000 abstract 3
- 229910052739 hydrogen Inorganic materials 0.000 abstract 3
- 229920001021 polysulfide Polymers 0.000 abstract 3
- 239000005077 polysulfide Substances 0.000 abstract 3
- 150000008117 polysulfides Polymers 0.000 abstract 3
- 230000001590 oxidative effect Effects 0.000 abstract 1
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 28
- 239000003054 catalyst Substances 0.000 description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 229910001873 dinitrogen Inorganic materials 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 229910003296 Ni-Mo Inorganic materials 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- 230000010718 Oxidation Activity Effects 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000012993 chemical processing Methods 0.000 description 1
- WHDPTDWLEKQKKX-UHFFFAOYSA-N cobalt molybdenum Chemical compound [Co].[Co].[Mo] WHDPTDWLEKQKKX-UHFFFAOYSA-N 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000010408 sweeping Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Landscapes
- Catalysts (AREA)
Abstract
Description
【発明の詳細な説明】
イ２発明の目的
の１
この発明は、主としてクラウス法によりＨ２Ｓ（硫化水
素）とＳＯ２（二酸化硫黄）から製造される液体硫黄の
精製方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION A2.Objective 1 of the Invention The present invention relates to a method for purifying liquid sulfur produced from H2S (hydrogen sulfide) and SO2 (sulfur dioxide) mainly by the Claus method.
クラウス法硫黄回収装置からの元素硫黄は液体状で生産
されることから、この形態で輸送あるいけ毬逆ＬｆＴ輩
的に伸田される７
しかし、クラウス法からの液体硫黄中には、その生成過
程においてＨ２Ｓ及びＨ２ＳＸ （ポリ硫化水素）がＨ
２Ｓに換算して通常２００〜８００ｐｐｍ溶存しており
、貯蔵又は輸送中に液体硫黄中からＨ２Ｓが気化、拡散
するため、人体への影響やガス爆発の危険がある。また
Ｈ２ＳＸは徐々に分解してＨ２Ｓになるので同様に有害
である。Since elemental sulfur from the Claus process sulfur recovery equipment is produced in liquid form, it can be transported in this form or transported in a reverse LfT manner.7 However, the liquid sulfur from the Claus process contains In the process, H2S and H2SX (polyhydrogen sulfide)
H2S is normally dissolved in an amount of 200 to 800 ppm in terms of 2S, and since H2S vaporizes and diffuses from liquid sulfur during storage or transportation, there is a risk of impact on the human body and gas explosion. H2SX is also harmful as it gradually decomposes into H2S.
従って液体硫黄中のＨ２Ｓ及びＨ２ＳＸのＨ２Ｓ換算濃
度は１０ｐｐｍ以下であることが要求されている。Therefore, the concentration of H2S and H2SX in liquid sulfur in terms of H2S is required to be 10 ppm or less.
鎧迷」月ｉ量
液体硫黄中に溶存しているＨ２Ｓ及びＨ２ＳＸを除去す
る方法としては、液体硫黄を障害物に吹きつけたり、ス
イープガスと呼ばれる空気等の気体と液体硫黄を無触媒
で接触させたりして、Ｈ２Ｓｘを分解してＨ２Ｓの形と
し溶存Ｈ２Ｓと共に気化して除去する方法があるが、い
ずれも処理時間が長く且つ除去効率が悪い。特にＨ２Ｓ
Ｘの分解が遅く、スイープガスの使用のみでは一日以上
の机理皓聞２騨オろ−
そこで処理時間を短縮しようとする見地から、化学的に
処理するための研究が行われており、種々の方法が知ら
れている。Monthly amount of H2S and H2SX dissolved in liquid sulfur can be removed by spraying liquid sulfur onto obstacles or by bringing liquid sulfur into contact with a gas such as air called sweep gas without a catalyst. There is a method of decomposing H2Sx to form H2S and vaporizing it together with dissolved H2S to remove it, but all of these methods require a long processing time and have poor removal efficiency. Especially H2S
The decomposition of X is slow, and it would take more than a day to use only a sweep gas.Therefore, from the perspective of shortening the processing time, research is being conducted on chemical processing, and various methods are being conducted. method is known.
例えば特公昭５６−５２８４７号には、液体硫黄をクラ
ウス反応器からの最終残留ガスでスウイーブし、さらに
アンモニアやアミンを添加してＨ２Ｓ及びＨ２ＳＸを除
去する方法が開示されている。また特公昭５９−４０７
６２号には液体硫黄をアルミナ又はコバルト−モリブデ
ン含浸アルミナからなる触媒と接触させて、空気又は酸
素富化空気でスウイーブしてＨ２Ｓ及びＨ２ＳＸを除去
する方法が記載されている。For example, Japanese Patent Publication No. 56-52847 discloses a method in which liquid sulfur is swept with the final residual gas from a Claus reactor and further ammonia or amine is added to remove H2S and H2SX. In addition, the special public service 59-407
No. 62 describes a method for removing H2S and H2SX by contacting liquid sulfur with a catalyst consisting of alumina or cobalt-molybdenum impregnated alumina and sweeping with air or oxygen-enriched air.
さらに本発明者等はその改良法として、Ｎｉ−Ｍｏ系の
触媒を使用し、酸素含有ガス及び窒素ガスよりなる群か
ら選ばれるスイープガスと接触させることにより、より
迅速に除去しつる方法について特願昭６０−９６８０５
号にて提案している。Furthermore, as an improved method, the present inventors have specifically developed a method for more rapid removal by using a Ni-Mo catalyst and bringing it into contact with a sweep gas selected from the group consisting of an oxygen-containing gas and a nitrogen gas. Gansho 60-96805
It is proposed in the issue.
が ′ しよ とする
前記の特公昭５９−４０７６２号や特願昭６０−９６８
０５号に開示されたモリブデン系触媒を用いる方法は、
共に、スイープガスとして空気のような分子状酸素含有
ガスの利用が可能とされている。The above-mentioned Japanese Patent Publication No. 59-40762 and Japanese Patent Application No. 60-968 which
The method using a molybdenum catalyst disclosed in No. 05 is as follows:
In both cases, it is possible to use a molecular oxygen-containing gas such as air as the sweep gas.
しかしこれらの方法では、スイープガスとして空気のよ
うな分子状酸素含有ガスを用いた場合、液体硫黄中のＨ
２Ｓ及びＨ２ＳＸ除去に関する本来の性能は高いが、反
応中にＨ２Ｓが微量酸化すると共に、原料硫黄の供給停
止後空気を流し続けると接触層内に滞留していた硫黄の
酸化反応が起き、加速度的に温度上昇する危険性がある
。このため停止時には不活性ガスへの切替など複雑な操
作を必要とする。However, in these methods, when a molecular oxygen-containing gas such as air is used as a sweep gas, H
Although the original performance for removing 2S and H2SX is high, a small amount of H2S is oxidized during the reaction, and if air continues to flow after the feedstock sulfur supply is stopped, the oxidation reaction of the sulfur accumulated in the contact layer occurs, resulting in an accelerated reaction. There is a risk of temperature rise. Therefore, when the system is stopped, complicated operations such as switching to inert gas are required.
ことに装置の緊急停止時などに対応が遅れると危険であ
る。It is especially dangerous if the response is delayed, such as during an emergency stop of the equipment.
本発明は、スイープガスとして、不活性ガスはもとより
、安価な空気などの分子状酸素を含有するガスをも使用
でき、しかも硫黄の酸化反応を抑制して、安全且つ効率
的に溶存している硫化水素及びポリ硫化水素を除去でき
る液体硫黄の精製方法を提供することを目的とする。The present invention can use not only an inert gas but also an inexpensive gas containing molecular oxygen such as air as the sweep gas, and suppresses the oxidation reaction of sulfur to safely and efficiently dissolve it. An object of the present invention is to provide a method for purifying liquid sulfur that can remove hydrogen sulfide and polyhydrogen sulfide.
口０発明の構成
を ゛するための
本発明に係わる液体硫黄の精製方法は、硫化水素及びポ
リ硫化水素を含有する液体硫黄をスイープガスと固体触
媒層で接触させて硫化水素及びポリ硫化水素を除去する
方法において、固体触媒としてＺｎＯを用いることを特
徴とする。The method for purifying liquid sulfur according to the present invention for achieving the configuration of the present invention is to contact liquid sulfur containing hydrogen sulfide and polyhydrogen sulfide with a sweep gas through a solid catalyst layer to purify hydrogen sulfide and polyhydrogen sulfide. The removing method is characterized by using ZnO as a solid catalyst.
スイープガスとしては、窒素ガス、クラウス法硫黄回収
装置におけるインシネレータ−オフガスやテールガス処
理装置（例えばスコツトオフガス法）などのほか、空気
をも安全に使用できる。スイープガスとして空気を用い
た場合、従来の固体触媒では硫黄の酸化反応が起きるの
に対し、ＺｎＯではこの反応が実質的に起きないので安
全で有利である。As the sweep gas, in addition to nitrogen gas, incinerator off gas in a Claus method sulfur recovery device, tail gas treatment device (for example, Scott off gas method), and the like, air can also be safely used. When air is used as the sweep gas, sulfur oxidation reaction occurs with conventional solid catalysts, but this reaction does not substantially occur with ZnO, so it is safe and advantageous.
スイープガスの流量は処理される液体硫黄に対し１０〜
１００ＮＪ２／βが好適である。The flow rate of the sweep gas is 10 to 10% for the liquid sulfur being treated.
100NJ2/β is suitable.
処理条件は前記の公知技術で採用されている条件と同様
で良い。即ち処理温度は液体硫黄の特性上１２０〜１６
５℃の範囲内に保持することが必尊で＄、スー帆狸圧力
は通當當庫乃卒若千の加庫下で行う。The processing conditions may be similar to those employed in the above-mentioned known techniques. That is, the processing temperature is 120 to 16
It is essential to maintain the temperature within the range of 5°C, and the pressure must be maintained at a constant temperature.
以下実施例により本発明を具体的に説明する。The present invention will be specifically explained below using Examples.
［実施例１］
押出成型法により製造した直径３ｍｍ、長さ５〜１０ｍ
ｍのＺｎＯ触媒１１８６ｍｇを、内径２８．６ｍｍ、長
さ２２００ｍｍのスチームジャケット付反応管に充填し
、１４５±１０℃に溶解した原料硫黄０．５９β／ Ｈ
ｒを窒素ガス５ＯＮＱ／ Ｈｒと共に供給し反応温度１
４５℃で液体硫黄中のＨ２Ｓ及びＨ２ＳＸの除去反応を
行った。原料硫黄としては全Ｈ２Ｓとして３３０ｗｔ、
ｐｐｍ、そのうちＨ２ＳＸ態として１７０ｗｔ、ｐｐｍ
が含まれているものを使用した。[Example 1] Diameter 3 mm and length 5 to 10 m manufactured by extrusion molding method
A steam-jacketed reaction tube with an inner diameter of 28.6 mm and a length of 2200 mm was filled with 1186 mg of ZnO catalyst of
r is supplied together with nitrogen gas 5ONQ/Hr, and the reaction temperature is 1
A reaction for removing H2S and H2SX in liquid sulfur was carried out at 45°C. The raw material sulfur is 330wt as total H2S,
ppm, of which 170wt as H2SX state, ppm
I used the one that included.
反応管出口の硫黄中のＨ２Ｓ濃度及びガス中のＨ２Ｓと
ＳＯ２の濃度を分析したところ、次の結果を得た。When the concentration of H2S in the sulfur at the outlet of the reaction tube and the concentration of H2S and SO2 in the gas were analyzed, the following results were obtained.
■精製硫黄の分析結果
全Ｈ２Ｓ 濃度： ８ｗｔ、ｐｐｍ内Ｈ２ＳＸ濃度
： ６ｗｔ、ｐｐｍ
■出ロガス中の分析結果
Ｈ２Ｓ 濃度： ０．４５ｖｏｆ２．％ＳＯ２ｉ
農度 ： ０．０２ｖｏ ℃ 、 ％［実施
例２］
窒素ガスの代りに空気５ＯＮβ／ Ｈｒを用いた以外は
実施例１と同様にして液体硫黄中のＨ２Ｓ及びＨ２ＳＸ
の除去反応を行い、反応管出口の硫黄中のＨ２Ｓ濃度及
びガス中のＨ２ＳとＳＯ２の濃度を分析したところ、次
の結果を得た。■Analysis results of purified sulfur Total H2S concentration: 8wt, ppm H2SX concentration: 6wt, ppm ■Analysis results of output log gas H2S concentration: 0.45vof2. %SO2i
Agricultural degree: 0.02vo °C, % [Example 2] H2S and H2SX in liquid sulfur were prepared in the same manner as in Example 1 except that air 5ONβ/Hr was used instead of nitrogen gas.
When the H2S concentration in the sulfur at the outlet of the reaction tube and the H2S and SO2 concentrations in the gas were analyzed, the following results were obtained.
■精製硫黄の分析結果
全Ｈ２Ｓ 濃度： ’ｙＷｔ、ｐｐｍ内Ｈ２ＳＸ濃
度： ６ｗｔ、ｐｐｍ
■出ロガス中の分析結果
Ｈ２Ｓ ａ度： ０．４６ｖｏｆｆ、％ＳＯ２濃
度： ０．０２ｖｏｆｆ、％次いで原料硫黄の供給を
停止し、空気５ＯＮβ／ Ｈｒのみを流し続けたところ
、出口ガス中のＳＯ２は０．０３ｖｏｊ２．％を維持し
た。その後−旦空気量を４倍にして３時間残留硫黄をパ
ージしてから元の流量に戻したところ、出口ガス中のＳ
０２は０．０３〜０．０３２ｖｏ氾９％の範囲で維持さ
れ、硫黄の残留量による影響は見られなかった。■Analysis results of refined sulfur Total H2S concentration: 'yWt, ppmH2SX concentration: 6wt, ppm ■Analysis results of H2S in output log gas a degree: 0.46voff, %SO2 concentration: 0.02voff,%Next supply of raw material sulfur When the gas was stopped and only air 5ONβ/Hr continued to flow, the SO2 in the outlet gas was 0.03voj2. % was maintained. After that, the amount of air was quadrupled to purge the residual sulfur for 3 hours, and then the original flow rate was returned to the original flow rate.
02 was maintained in the range of 0.03 to 0.032vo flood 9%, and no influence by the residual amount of sulfur was observed.
［比較例１］
粒径ｌ／１６インチのＮｉ−Ｍｏ系脱硫触媒を用いて実
施例２と同様に実験した。原料硫黄としては全Ｈ２Ｓと
して３６０ｗｔ、ｐｐｍ、そのうちＨ２ＳＸ態として１
９０ｗｔ、ｐｐｍが含まれているものを使用した。[Comparative Example 1] An experiment was carried out in the same manner as in Example 2 using a Ni-Mo desulfurization catalyst having a particle size of 1/16 inches. The raw material sulfur is 360wt, ppm as total H2S, of which 1 is in H2SX form.
The one containing 90wt, ppm was used.
反応管出口の硫黄中のＨ２Ｓａ度及びガス中のＨ２Ｓと
ＳＯ２の濃度を分析したところ、次の結果を得た。When the H2Sa degree in the sulfur at the outlet of the reaction tube and the concentrations of H2S and SO2 in the gas were analyzed, the following results were obtained.
■精製硫黄の分析結果
全Ｈ２Ｓ 濃度： ２ｗｔ、ｐｐｍ内Ｈ２ＳＸ濃度
： １ｗｔ、ｐｐｍ
■出ロガス中の分析結果
Ｈ２Ｓ 濃度： ０．２４ｖｏｊ２．％ＳＯ２濃
度： ０．０８ｖｏｆｆ、％その後、スィ−ブガスを
空気から窒素に切替えて出口ガス中のＨ２Ｓ及びＳＯ２
を測定したところ、Ｈ２Ｓは０．３３ｖｏＩ２．％、Ｓ
Ｏ２は０％であった。このことから出口ガス中のＳＯ２
はＨ２Ｓの燃焼によることが明らかである。■Analysis results of purified sulfur Total H2S concentration: 2wt, ppm H2SX concentration: 1wt, ppm ■Analysis results of output log gas H2S concentration: 0.24voj2. %SO2 concentration: 0.08voff, %Then, the sweep gas was switched from air to nitrogen to reduce H2S and SO2 in the outlet gas.
When measured, H2S was 0.33voI2. %, S
O2 was 0%. From this, SO2 in the outlet gas
It is clear that this is due to the combustion of H2S.
次いでスィ−ブガスを元の空気に戻した後原料硫黄の供
給を停止し、空気５ＯＮβ／ Ｈｒを流し続けたところ
、出口ガス中のＳＯ２は０．１６ＶＯＷ、％で継続した
。−旦空気量を４倍にして３時間流した後５０ Ｎ Ｉ
２／ Ｈｒに戻したところ、ＳＯ２濃度は０．７ｖｏβ
１％まで上昇し、継続した。空気量を一時的に増やすこ
とによって液体硫黄がパージされた結果、触媒表面に空
気が触れ易くなり硫黄の酸化反応が促進されたためと思
われる。Next, after returning the sieve gas to the original air, the supply of raw material sulfur was stopped, and when air was continued to flow at 5ONβ/Hr, SO2 in the outlet gas continued at 0.16 VOW, %. - After quadrupling the air volume and flowing for 3 hours, 50 N I
When the temperature was returned to 2/Hr, the SO2 concentration was 0.7voβ
It rose to 1% and continued. This seems to be because liquid sulfur was purged by temporarily increasing the amount of air, which made it easier for air to come into contact with the catalyst surface, promoting the oxidation reaction of sulfur.
［実施例３］
小型のスチームジャケット付反応管に第１表に示した各
種触媒を各１０ｒｎＪ２充填し、１４５℃で溶解した）
（２Ｓを含まない液体硫黄を５０ｍβ流し触媒を硫黄で
漏らした後、空気を流して出口ガス中のＳＯ２を分析し
た。その・結果、第１表のようになり、硫黄の酸化活性
についてはＺｎＯがもわかった。[Example 3] A small steam-jacketed reaction tube was filled with 10rnJ2 of each of the various catalysts shown in Table 1, and dissolved at 145°C.)
(After flowing 50 mβ of liquid sulfur that does not contain 2S to make the catalyst leak with sulfur, air was flowed to analyze the SO2 in the outlet gas. The results are as shown in Table 1, and the sulfur oxidation activity of ZnO I also understood.
第
表
艷且
ＺｎＯ触媒は、十分実用的なポリ硫化水素の分解性能を
有すると共に、空気のように分子状酸素を含有するガス
の存在下で使用しても硫黄を酸化してＳＯ２にする程度
が公知触媒に比して小さいので、スイープガスとして安
価な空気を支障なく使用できる。Table 1: The ZnO catalyst has sufficient performance to decompose polyhydrogen sulfide for practical use, and even when used in the presence of a gas containing molecular oxygen, such as air, it only oxidizes sulfur to SO2. is smaller than that of known catalysts, so cheap air can be used as the sweep gas without any problems.
ハ１発明の効果
ｌ）反応停止時にスイープガスを切替える必要がなく、
運転操作が簡易になる。C1 Effects of the invention l) There is no need to switch the sweep gas when the reaction is stopped,
Driving operations become easier.
２）緊急停止時に危険を伴わない。2) No danger during emergency stop.
Claims (1)
イープガスと固体触媒層で接触させて硫化水素及びポリ
硫化水素を除去する方法において、固体触媒としてＺｎ
Ｏを用いることを特徴とする液体硫黄の精製方法。 ２ スイープガスとして空気を用いる請求項第１項記載
の液体硫黄の精製方法。[Claims] 1. A method for removing hydrogen sulfide and polyhydrogen sulfide by contacting liquid sulfur containing hydrogen sulfide and polyhydrogen sulfide with a sweep gas through a solid catalyst layer, in which Zn is used as the solid catalyst.
A method for purifying liquid sulfur, characterized by using O. 2. The method for purifying liquid sulfur according to claim 1, wherein air is used as the sweep gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP17912689A JPH0345505A (en) | 1989-07-13 | 1989-07-13 | Method for purifying liquid sulfur |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP17912689A JPH0345505A (en) | 1989-07-13 | 1989-07-13 | Method for purifying liquid sulfur |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0345505A true JPH0345505A (en) | 1991-02-27 |
| JPH0567561B2 JPH0567561B2 (en) | 1993-09-27 |
Family
ID=16060449
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP17912689A Granted JPH0345505A (en) | 1989-07-13 | 1989-07-13 | Method for purifying liquid sulfur |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0345505A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102134061A (en) * | 2010-01-25 | 2011-07-27 | 气体产品与化学公司 | A reactor, a structured packing, and a method for improving oxidation of hydrogen sulfide or polysulfides in liquid sulfur |
| WO2013006040A1 (en) | 2011-06-21 | 2013-01-10 | Jacobs Nederland B.V. | Catalytic sulfur degassing |
-
1989
- 1989-07-13 JP JP17912689A patent/JPH0345505A/en active Granted
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102134061A (en) * | 2010-01-25 | 2011-07-27 | 气体产品与化学公司 | A reactor, a structured packing, and a method for improving oxidation of hydrogen sulfide or polysulfides in liquid sulfur |
| EP2347995A1 (en) * | 2010-01-25 | 2011-07-27 | Air Products and Chemicals, Inc. | A reactor, a structures packing, and a method for improving oxidation of hydrogen sulfide or polysulfides in liquid sulfur |
| AU2011200201B2 (en) * | 2010-01-25 | 2013-08-22 | Fluor Technologies Corporation | A reactor, a structured packing, and a method for improving oxidation of hydrogen sulfide or polysulfides in liquid sulfur |
| US8663596B2 (en) | 2010-01-25 | 2014-03-04 | Fluor Enterprises, Inc. | Reactor, a structure packing, and a method for improving oxidation of hydrogen sulfide or polysulfides in liquid sulfur |
| WO2013006040A1 (en) | 2011-06-21 | 2013-01-10 | Jacobs Nederland B.V. | Catalytic sulfur degassing |
| US9260307B2 (en) | 2011-06-21 | 2016-02-16 | Jacobs Nederland B.V. | Catalytic sulfur degassing |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0567561B2 (en) | 1993-09-27 |
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