JPH07136458A - Method for removing mercury in acidic exhaust gas - Google Patents
Method for removing mercury in acidic exhaust gasInfo
- Publication number
- JPH07136458A JPH07136458A JP5309753A JP30975393A JPH07136458A JP H07136458 A JPH07136458 A JP H07136458A JP 5309753 A JP5309753 A JP 5309753A JP 30975393 A JP30975393 A JP 30975393A JP H07136458 A JPH07136458 A JP H07136458A
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- absorption tower
- absorbent
- absorption
- mercury
- 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
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
(57)【要約】
【目的】 吸収塔の吸収剤を効率的に使用できるように
し、吸収塔を通過する排ガスの圧力損失及び吸収塔を通
過した後の排ガス中の水銀濃度の変動を小さくする。
【構成】 無機物質担体に金属硫化物を担持させてなる
吸収剤を入れた吸収塔に水銀を含む酸性排ガスを通過せ
しめて、排ガス中の水銀を除去する方法において、排ガ
スの通路に４個以上の吸収塔が並列に装入され、吸収塔
の全部に同時に排ガスを通過せしめ、その内の圧力損失
の最も増加した吸収塔のみを排ガスの通過を停止してそ
の中の吸収剤を交換し、再び排ガスを通過させ、次いで
同様にして順次に他の吸収塔の排ガスの通過の停止、吸
収剤の交換、排ガスの通過を行うか、１部の吸収塔を常
時待機させ、他の４個以上の吸収塔がいつも使用されて
いるようにする。(57) [Summary] [Purpose] To enable efficient use of the absorbent in the absorption tower, and to reduce fluctuations in pressure loss of the exhaust gas passing through the absorption tower and mercury concentration in the exhaust gas after passing through the absorption tower. . [Constitution] In a method for removing mercury in exhaust gas by passing acidic exhaust gas containing mercury through an absorption tower containing an absorbent in which a metal sulfide is supported on an inorganic substance carrier, four or more are provided in the exhaust gas passage. The absorption towers are charged in parallel and allow the exhaust gas to pass through all of the absorption towers at the same time, and only the absorption tower in which the pressure loss has increased most is stopped the passage of the exhaust gas and the absorbent therein is replaced, Pass the exhaust gas again, and then similarly stop the passage of the exhaust gas of the other absorption tower, exchange the absorbent, and pass the exhaust gas in the same manner, or let one absorption tower stand by at all times Make sure that the absorption tower is always used.
Description
【０００１】[0001]
【産業上の利用分野】本発明は非鉄精錬排ガス等の酸性
排ガス中に気体又はミスト状で含有される微量な水銀の
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 removing a trace amount of mercury contained in a gas or mist form in an acidic exhaust gas such as a non-ferrous refining exhaust gas.
【０００２】[0002]
【従来の技術】硫化鉱を処理した精錬排ガス中には、一
般に亜硫酸ガスを４〜１０容量％含有し、原料鉱物中に
水銀が含まれている場合には、ガス状又はミスト状の水
銀が含まれている。この酸性排ガス中の微量の水銀は、
水を散水するスクラバー方式、バグフイルター方式、電
気的に集塵するコットレルなどによる除去方法では除去
が困難である。2. Description of the Related Art Refining flue gas treated with sulfide ores generally contains 4 to 10% by volume of sulfurous acid gas, and when mercury is contained in a raw material mineral, gaseous or mist-like mercury is contained. include. The trace amount of mercury in this acidic exhaust gas is
It is difficult to remove by a scrubber method that sprays water, a bag filter method, or a cotrel that electrically collects dust.
【０００３】このため、非炭素質の無機多孔性物質担体
上に、金属硫化物を担持せしめた吸収剤と上記の水銀含
有酸性排ガスとを接触させて水銀を除去する方法（特公
昭５４−８４５７号公報）、天然硫化鉱物や人工硫化鉱
物を無機質の多孔性物質に付着させた吸収剤による水銀
除去方法（特開昭５３−２３８８８号公報）、多孔質物
質に単体硫黄を付着させた吸収剤による水銀除去方法
（特公昭６３−２６５５号公報）等が提案されている。For this reason, a method of removing mercury by contacting an absorbent supporting metal sulfides with the above-mentioned mercury-containing acidic exhaust gas on a non-carbonaceous inorganic porous material carrier (Japanese Patent Publication No. 54-8457). Japanese Patent Laid-Open Publication No. 1993-242242), a method for removing mercury by an absorbent in which a natural sulfide mineral or an artificial sulfide mineral is attached to an inorganic porous material (Japanese Patent Laid-Open No. 53-23888), and an absorbent in which elemental sulfur is attached to the porous material. A method of removing mercury (Japanese Patent Publication No. 63-2655) is proposed.
【０００４】上記の吸収剤を入れた吸収塔に、水銀を含
む酸性排ガスを通過させて排ガス中の水銀を除去する場
合、排ガス中の水銀は水銀硫化物となって吸収剤に沈着
するので、排ガス通過時間の経過に従い、吸収剤の水銀
吸着性能が低下してくる。このため従来は、吸収塔を２
個設け、その内の１個の吸収塔に排ガスを流し、他の１
個の吸収塔は予備としておき、排ガスを流していた吸収
塔の水銀吸収性能が低下すると、他の１個の吸収塔に流
路を切り替えてこの吸収塔に排ガスを流し、排ガスの流
通を止めた１個の吸収塔の吸収剤を新しい吸収剤に取り
替えていた。When the acidic exhaust gas containing mercury is passed through the absorption tower containing the absorbent to remove the mercury in the exhaust gas, the mercury in the exhaust gas becomes mercury sulfide and is deposited on the absorbent. As the exhaust gas passage time passes, the mercury adsorption performance of the absorbent decreases. Therefore, in the past, two absorption towers were used.
The exhaust gas is made to flow through one of the absorption towers, and the other one
Keep one absorption tower as a spare, and when the mercury absorption performance of the absorption tower that was flowing the exhaust gas deteriorates, switch the flow path to another absorption tower and let the exhaust gas flow to this absorption tower to stop the flow of the exhaust gas. Also, the absorbent in one absorption tower was replaced with a new absorbent.
【０００５】吸収剤に付着した水銀硫化物等の増加によ
り、吸収塔を通過する排ガスの圧力損失も増加する。吸
収剤は、水銀の吸着が出来なくなるまで使用するのが最
も経済的である。しかし、水銀の吸着が出来なくなるま
で使用しようとすると、排ガスの通過抵抗の増加により
処理ガス量が減少し、精錬炉等で発生する排ガスを処理
仕切れなくなるので、吸収塔の吸収剤を水銀吸収性能が
残っているにも拘らず取り替える必要があった。Due to the increase of mercury sulfide and the like adhering to the absorbent, the pressure loss of the exhaust gas passing through the absorption tower also increases. It is most economical to use absorbents until mercury adsorption is no longer possible. However, if you try to use it until mercury can no longer be adsorbed, the amount of treated gas will decrease due to an increase in exhaust gas passage resistance, and the exhaust gas generated in the refining furnace, etc. will not be able to be treated. Had to be replaced despite the remaining.
【０００６】又、この従来方法では１個の吸収塔に処理
排ガスを全量流すことになるので、吸収塔が大きくなる
と共に収容する吸収剤の量も多量となる。従って、水銀
吸着性能の低下した吸収剤を新しい吸収剤に取り替える
のに数週間を要するだけでなく、吸収塔を通過した後の
排ガス中の残留水銀濃度や圧力損失が、取り替えたばか
りの吸収剤に排ガスを流し始めた時と、吸収剤を取り替
えなければならなくなった時とでは大きく変化する問題
がある。Further, in this conventional method, the total amount of the treated exhaust gas is passed through one absorption tower, so that the absorption tower becomes large and the amount of the absorbent contained therein also becomes large. Therefore, it takes not only several weeks to replace the absorbent with reduced mercury adsorption performance with a new absorbent, but also the residual mercury concentration and pressure loss in the exhaust gas after passing through the absorption tower can be changed to the absorbent just replaced. There is a problem that there is a big difference between when the exhaust gas starts flowing and when the absorbent has to be replaced.
【０００７】[0007]
【発明が解決しようとする課題】本発明は吸収塔の吸収
剤を効率的に使用でき、同時に吸収塔を通過する排ガス
の圧力損失及び吸収塔を通過した後の排ガス中の水銀濃
度の変動を小さくできる方法を提供することを課題とす
る。DISCLOSURE OF THE INVENTION The present invention enables efficient use of the absorbent in the absorption tower, and at the same time reduces the pressure loss of the exhaust gas passing through the absorption tower and the fluctuation of the mercury concentration in the exhaust gas after passing through the absorption tower. It is an object to provide a method that can be reduced.
【０００８】[0008]
【課題を解決するための手段】本発明は、この課題を達
成するため、排ガスの通路に４個以上の吸収塔が並列に
装入され、この吸収塔の全部に同時に排ガスを通過せし
め、その内の圧力損失の最も増加した吸収塔のみを排ガ
スの通過を停止してその中の吸収剤を交換し、再び排ガ
スを通過させ、次いで同様にして順次に他の吸収塔の排
ガスの通過の停止、吸収剤の交換、排ガスの通過を行う
ことにある。According to the present invention, in order to achieve this object, four or more absorption towers are charged in parallel in the exhaust gas passage, and the exhaust gas is allowed to pass through all of the absorption towers at the same time. Stop the passage of the exhaust gas only in the absorption tower with the largest increase in pressure loss, exchange the absorbent in it, and let the exhaust gas pass through again, and then similarly stop the passage of the exhaust gas of other absorption towers in the same manner. , To replace the absorbent and to pass the exhaust gas.
【０００９】本発明は、又、排ガスの通路に５個以上の
吸収塔が並列に装入され、この吸収塔の１部を除く残部
に同時に排ガスを通過せしめ、その内の圧力損失の最も
増加した吸収塔のみを排ガスの通過を停止し、前記の１
部の吸収塔に前記の排ガスを通過せしめ、前記の排ガス
の通過を停止した吸収塔中の前記吸収剤を交換し、次い
で同様にして順次に他の吸収塔の排ガスの通過の停止、
排ガスの通過、吸収剤の交換を行うことにある。According to the present invention, five or more absorption towers are loaded in parallel in the exhaust gas passage, and the exhaust gas is allowed to pass through the rest of the absorption tower except one part at the same time, so that the pressure loss therein increases the most. The passage of exhaust gas is stopped only in the absorption tower
Pass the exhaust gas to the absorption tower of the part, replace the absorbent in the absorption tower that has stopped the passage of the exhaust gas, then similarly stop the passage of the exhaust gas of other absorption tower,
The purpose is to pass the exhaust gas and exchange the absorbent.
【００１０】[0010]
【作用】本発明では、排ガス全量を１個の吸収塔に流す
場合に比べて、その容積の小さいものを用いることがで
きる。例えば直径４ｍ以下、高さ６ｍ以下のような汎用
の耐酸容器を使用できる。このように、従来用いられて
いた直径、高さ共に１０ｍを超える耐酸容器を１個使用
するよりも、これより小さな容器を多数用いることによ
って、排ガス全体に生ずる圧力損失を小さくでき、同時
に１個の吸収塔に収容する吸収剤の量が少なくなるの
で、吸収剤の取り替え時間を短縮できる。In the present invention, it is possible to use an exhaust gas having a smaller volume as compared with the case where the entire amount of exhaust gas is passed through one absorption tower. For example, a general-purpose acid resistant container having a diameter of 4 m or less and a height of 6 m or less can be used. As described above, by using a number of smaller acid-resistant containers than the one conventionally used, which has both a diameter and a height of more than 10 m, it is possible to reduce the pressure loss generated in the exhaust gas as a whole. Since the amount of the absorbent stored in the absorption tower is reduced, the replacement time of the absorbent can be shortened.
【００１１】本発明で使用する吸収塔の数を４個以上と
するのは、処理全排ガス量が少ない時には吸収塔の全数
を４個とし、１個を休止し、排ガスを残りの３個の吸収
塔を通過させるようにしても、全排ガス中の水銀濃度及
び圧力損失の変動は小さいが、吸収塔の全数を３個とす
ると、その内の２個の圧力損失が大きくなっている場合
には、その２個の内の１個を休止すると、残りの２個に
よる圧力損失が急に大きくなり、排ガスの処理に停滞を
生ずる恐れが生ずるためである。本発明で排ガスを通過
させつつある吸収塔の内から圧力損失の最も増加した吸
収塔の排ガスの流通を停止してその中の吸収剤を取り替
えるのは、残りの吸収塔の中に圧力損失が大きくなって
いないものがあるために、１個を停止しても停止前と圧
力損失の変動があまり大きくならないからである。The reason why the number of absorption towers used in the present invention is 4 or more is that when the total amount of exhaust gas treated is small, the total number of absorption towers is set to 4 and one is stopped and the remaining 3 exhaust gases are used. Even if it passes through the absorption tower, the fluctuations in mercury concentration and pressure loss in the total exhaust gas are small, but if the total number of absorption towers is three, the pressure loss of two of them is large. The reason is that if one of the two is stopped, the pressure loss due to the remaining two suddenly increases, and there is a possibility that the processing of the exhaust gas will be delayed. In the present invention, the pressure loss in the remaining absorption tower is changed by stopping the flow of the exhaust gas in the absorption tower where the pressure loss is most increased from the inside of the absorption tower passing the exhaust gas and replacing the absorbent therein. This is because, because there are some that have not become large, even if one is stopped, the fluctuation in pressure loss is not so large as before the stop.
【００１２】処理排ガスの処理量が同じであれば、全吸
収塔の数が多いほど、その一部の吸収塔を休止したとき
の圧力損失の変動は小さくなる。従って、全吸収塔の数
を多くすれば、一部の吸収塔の圧力損失がかなり大きく
なり、水銀吸着性能がかなりなくなるまで使用してか
ら、吸収剤の取り替えを行えるので、吸収剤の使用を経
済的にすることができる。吸収塔の吸収剤取り替えのた
めの時間間隔は、処理排ガス中の水銀濃度や、処理後の
排ガス中に残留する水銀濃度をどの程度に抑えるかによ
り異なる。If the amount of treated exhaust gas is the same, the larger the total number of absorption towers, the smaller the fluctuation of pressure loss when some of the absorption towers are stopped. Therefore, if the number of all absorption towers is increased, the pressure loss of some of the absorption towers will be considerably large, and it will be possible to replace the absorbent after it has been used until the mercury adsorption performance is considerably lost. Can be economical. The time interval for replacing the absorbent in the absorption tower varies depending on the mercury concentration in the treated exhaust gas and how much the mercury concentration remaining in the treated exhaust gas is suppressed.
【００１３】[0013]
【実施例】直径３.８ｍ、高さ５.９２ｍ、壁厚１３ｍｍ
のＦＲＰ製耐酸容器内に、上下２段に吸収剤層を設け
た。上段の吸収剤層は厚さを１０８０ｍｍ、下段の吸収
剤層の厚さを６８０ｍｍとした。吸収剤は硫化鉛を担持
させた粒径４〜９ｍｍのものを主体とし、他に粒径１０
〜１５ｍｍ及び１５〜２５ｍｍの粒状物を用いた。この
吸収塔を１０個並列に排ガスの通路に接続し、全吸収塔
に同時に亜硫酸ガス濃度７容量％、水銀濃度２.０ｍｇ
／Ｎｍ3、温度３７℃（水分飽和）の排ガスを５３００
０Ｎｍ3／Ｈｒ（乾燥基準）の割合で通過させた。[Example] Diameter 3.8 m, height 5.92 m, wall thickness 13 mm
In the FRP acid-resistant container of No. 3, the absorbent layers were provided in two upper and lower stages. The upper absorbent layer had a thickness of 1080 mm, and the lower absorbent layer had a thickness of 680 mm. The absorbent is mainly composed of lead sulfide having a particle size of 4 to 9 mm, and another particle size of 10
Granules of -15 mm and 15-25 mm were used. Ten of these absorption towers were connected in parallel to the exhaust gas passage, and all of the absorption towers simultaneously had a sulfur dioxide gas concentration of 7% by volume and a mercury concentration of 2.0 mg.
/ Nm 3 and temperature of 37 ° C (water saturated) exhaust gas 5300
It was passed through at a ratio of 0 Nm 3 / Hr (dry basis).
【００１４】排ガス通過開始時の全圧力損失は１００ｍ
ｍＨ2Ｏで、全吸収塔を通過した排ガス中の水銀濃度は
０.１ｍｇ／Ｎｍ3以下であった。使用開始後１６カ月
で、全圧力損失が２００ｍｍＨ2Ｏに増加したので、圧
力損失の最も大きい１個の吸収塔を休止し、吸収剤の交
換を行った。残りの９個の吸収塔の全圧力損失は２２０
ｍｍＨ2Ｏであった。吸収剤の交換を終わった１個の吸
収塔を使用し１０個の吸収塔の使用した後の全圧力損失
は１７０ｍｍＨ2Ｏであった。The total pressure loss at the start of passing the exhaust gas is 100 m
With mH 2 O, the mercury concentration in the exhaust gas that passed through the entire absorption tower was 0.1 mg / Nm 3 or less. Sixteen months after the start of use, the total pressure loss increased to 200 mmH 2 O, so one absorption tower with the largest pressure loss was stopped and the absorbent was replaced. The total pressure loss of the remaining 9 absorption towers is 220
It was mmH 2 O. The total pressure loss after using 10 absorption towers was 170 mmH 2 O after using 1 absorption tower after the replacement of the absorbent.
【００１５】次に、圧力損失の最も大きい吸収塔１個を
休止して吸収剤の交換を行った。残りの９個の吸収塔の
全圧力損失は１８０ｍｍＨ2Ｏであった。吸収剤の交換
を終わった吸収塔を使用し、１０個の吸収塔の使用した
後の全圧力損失は１６０ｍｍＨ2Ｏであった。Next, one of the absorption towers having the largest pressure loss was stopped to exchange the absorbent. The total pressure loss of the remaining 9 absorption towers was 180 mmH 2 O. The total pressure loss after using the absorption tower after the replacement of the absorbent and using 10 absorption towers was 160 mmH 2 O.
【００１６】従って、圧力損失の最も大きくなった吸収
塔の吸収剤を取り替える時の圧力損失を幾らに設定する
かにより、全圧力損失の変動を１８０〜１６０ｍｍＨ2
Ｏの範囲としたり、２００〜１６０ｍｍＨ2Ｏの範囲と
したりすることができる。全圧力損失の最大限度を例え
ば２２０ｍｍＨ2Ｏに設定した場合には、個々の吸収塔
の圧力損失は２２０ｍｍＨ2Ｏより大きいものも、小さ
いものもあるので、その中の最も圧力損失の大きい吸収
塔の吸収剤は圧力損失が２２０ｍｍＨ2Ｏよりも大きく
なるまで使用出来る。２個の吸収塔を交互に使用する場
合では、圧力損失が２２０ｍｍＨ2Ｏになれば吸収剤を
取り替えねばならないので、本発明の場合よりも吸収剤
の使用効率が低くなり、圧力損失の変動も大きくなる。Therefore, the fluctuation of the total pressure loss is 180 to 160 mmH 2 depending on how much the pressure loss is set when replacing the absorbent in the absorption tower having the largest pressure loss.
It may be in the range of O or in the range of 200 to 160 mmH 2 O. When the maximum limit of total pressure loss is set to 220 mmH 2 O, for example, the pressure loss of each absorption tower may be larger or smaller than 220 mmH 2 O, so that the absorption tower with the largest pressure loss among them This absorbent can be used until the pressure loss exceeds 220 mmH 2 O. In the case of using two absorption towers alternately, if the pressure loss reaches 220 mmH 2 O, the absorbent has to be replaced, so the efficiency of use of the absorbent is lower than in the case of the present invention, and fluctuations in pressure loss also occur. growing.
【００１７】[0017]
【発明の効果】本発明方法によれば、酸性排ガス中の水
銀を吸収剤を用いて除去するに当たり、吸収塔の吸収剤
を効率的に使用でき、同時に吸収塔を通過する排ガスの
圧力損失及び吸収塔を通過した後の排ガス中の水銀濃度
の変動を小さくできる。According to the method of the present invention, when the mercury in the acidic exhaust gas is removed by using the absorbent, the absorbent in the absorption tower can be used efficiently and, at the same time, the pressure loss of the exhaust gas passing through the absorption tower and Fluctuations in mercury concentration in the exhaust gas after passing through the absorption tower can be reduced.
Claims (2)
なる吸収剤を入れた吸収塔に水銀を含む酸性排ガスを通
過せしめて、該排ガス中の水銀を除去する方法におい
て、前記の排ガスの通路に４個以上の吸収塔が並列に装
入され、該吸収塔の全部に同時に前記の排ガスを通過せ
しめ、その内の圧力損失の最も増加した吸収塔のみを前
記の排ガスの通過を停止してその中の前記吸収剤を交換
し、再び前記の排ガスを通過させ、次いで同様にして順
次に他の吸収塔の排ガスの通過の停止、吸収剤の交換、
排ガスの通過を行う酸性排ガス中の水銀の除去方法。1. A method for removing mercury in an exhaust gas by passing an acidic exhaust gas containing mercury through an absorption tower containing an absorbent made by supporting a metal sulfide on an inorganic substance carrier, In the passage, four or more absorption towers are charged in parallel, the exhaust gas is allowed to pass through all of the absorption towers at the same time, and only the absorption tower having the largest pressure loss therein is stopped from passing the exhaust gas. The exchange of the absorbent in it, let the exhaust gas pass again, and then similarly stop the passage of the exhaust gas of the other absorption tower, replace the absorbent,
A method for removing mercury in an acidic exhaust gas that allows the exhaust gas to pass through.
なる吸収剤を入れた吸収塔に水銀を含む酸性排ガスを通
過せしめて、該排ガス中の水銀を除去する方法におい
て、前記の排ガスの通路に５個以上の吸収塔が並列に装
入され、該吸収塔の１部を除く残部に同時に前記の排ガ
スを通過せしめ、その内の圧力損失の最も増加した吸収
塔のみを前記の排ガスの通過を停止し、前記の１部の吸
収塔に前記の排ガスを通過せしめ、前記の排ガスの通過
を停止した吸収塔中の前記吸収剤を交換し、次いで同様
にして順次に他の吸収塔の排ガスの通過の停止、排ガス
の通過、吸収剤の交換を行う酸性排ガス中の水銀の除去
方法。2. A method of removing mercury in an exhaust gas by passing an acidic exhaust gas containing mercury through an absorption tower containing an absorbent comprising a metal sulfide supported on an inorganic material carrier, Five or more absorption towers are charged in parallel in the passages, and the exhaust gas is allowed to pass through the rest of the absorption tower except one part at the same time. The passage is stopped, the exhaust gas is allowed to pass through the part of the absorption tower, the absorbent in the absorption tower where the passage of the exhaust gas is stopped is exchanged, and then similarly in the other absorption towers. A method for removing mercury in acidic exhaust gas by stopping passage of exhaust gas, passage of exhaust gas, and exchange of absorbent.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5309753A JP2662768B2 (en) | 1993-11-16 | 1993-11-16 | Method for removing mercury from acidic exhaust gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5309753A JP2662768B2 (en) | 1993-11-16 | 1993-11-16 | Method for removing mercury from acidic exhaust gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH07136458A true JPH07136458A (en) | 1995-05-30 |
| JP2662768B2 JP2662768B2 (en) | 1997-10-15 |
Family
ID=17996878
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5309753A Expired - Fee Related JP2662768B2 (en) | 1993-11-16 | 1993-11-16 | Method for removing mercury from acidic exhaust gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2662768B2 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2010021053A1 (en) * | 2008-08-22 | 2010-02-25 | 株式会社日立製作所 | Mercury removing system for equipment for carbon dioxide recovery from combustion exhaust gas and method of mercury removing operation for equipment for carbon dioxide recovery from combustion exhaust gas |
| US9375679B2 (en) | 2013-08-30 | 2016-06-28 | Haldex Brake Products Corporation | Air dryer assembly with manifold system |
| CN111748388A (en) * | 2019-03-26 | 2020-10-09 | 珠海巨涛海洋石油服务有限公司 | Natural gas demercuration device |
-
1993
- 1993-11-16 JP JP5309753A patent/JP2662768B2/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2010021053A1 (en) * | 2008-08-22 | 2010-02-25 | 株式会社日立製作所 | Mercury removing system for equipment for carbon dioxide recovery from combustion exhaust gas and method of mercury removing operation for equipment for carbon dioxide recovery from combustion exhaust gas |
| JP5253509B2 (en) * | 2008-08-22 | 2013-07-31 | 株式会社日立製作所 | Mercury removal system for carbon dioxide recovery equipment in combustion exhaust gas, and mercury removal operation method for carbon dioxide recovery equipment in combustion exhaust gas |
| US9375679B2 (en) | 2013-08-30 | 2016-06-28 | Haldex Brake Products Corporation | Air dryer assembly with manifold system |
| CN111748388A (en) * | 2019-03-26 | 2020-10-09 | 珠海巨涛海洋石油服务有限公司 | Natural gas demercuration device |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2662768B2 (en) | 1997-10-15 |
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