JPS63305916A - Separation of component contained in by-product gas - Google Patents
Separation of component contained in by-product gasInfo
- Publication number
- JPS63305916A JPS63305916A JP13968187A JP13968187A JPS63305916A JP S63305916 A JPS63305916 A JP S63305916A JP 13968187 A JP13968187 A JP 13968187A JP 13968187 A JP13968187 A JP 13968187A JP S63305916 A JPS63305916 A JP S63305916A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- membrane
- components
- separation
- product 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.)
- Pending
Links
- 239000006227 byproduct Substances 0.000 title claims abstract description 20
- 238000000926 separation method Methods 0.000 title claims description 14
- 239000012528 membrane Substances 0.000 claims abstract description 28
- 239000005373 porous glass Substances 0.000 claims abstract description 15
- 239000000428 dust Substances 0.000 claims abstract description 14
- 229920005597 polymer membrane Polymers 0.000 claims description 25
- 238000000034 method Methods 0.000 claims description 16
- 238000000746 purification Methods 0.000 claims 1
- 239000012141 concentrate Substances 0.000 abstract description 7
- 239000000571 coke Substances 0.000 abstract description 5
- 229920002301 cellulose acetate Polymers 0.000 abstract description 3
- 238000001179 sorption measurement Methods 0.000 abstract description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 abstract 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 51
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 27
- 229910002092 carbon dioxide Inorganic materials 0.000 description 13
- 239000011148 porous material Substances 0.000 description 11
- 239000001569 carbon dioxide Substances 0.000 description 10
- 239000001257 hydrogen Substances 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- 239000012466 permeate Substances 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000004642 Polyimide Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 229910002090 carbon oxide Inorganic materials 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 229920001721 polyimide Polymers 0.000 description 2
- 238000004094 preconcentration Methods 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 1
- 239000005062 Polybutadiene Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229920000620 organic polymer Polymers 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 229920002857 polybutadiene Polymers 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 239000010409 thin film Substances 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Filtering Of Dispersed Particles In Gases (AREA)
Abstract
Description
【発明の詳細な説明】
産業上の利用分野
本発明は、例えば製鉄所内のコークス炉や熱風炉等の加
熱炉で発生する副生ガス中の任意成分を高効率・高精度
に分離する方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION Field of Industrial Application The present invention relates to a method for highly efficient and highly accurate separation of arbitrary components in by-product gases generated in heating furnaces such as coke ovens and hot blast ovens in steel plants. It is something.
従来の技術
従来、副生ガス中の成分を分離しその成分を有効利用す
るために、高分子膜に導入し抽出することが実験的に行
われている。このような技術として例えば、特開昭５９
−１４０３２１号公報に示されるように燃焼排ガスを非
多孔質高分子膜内装のガス分離装置に導いて二酸化炭素
を濃縮分離し、そのガスを他に有効利用するものがある
。BACKGROUND OF THE INVENTION Conventionally, in order to separate components in by-product gases and utilize them effectively, experiments have been carried out to introduce them into a polymer membrane and extract them. As an example of such technology, for example, Japanese Patent Application Laid-open No. 59
As shown in Japanese Patent No. 140321, there is a method in which combustion exhaust gas is introduced into a gas separation device equipped with a non-porous polymer membrane to concentrate and separate carbon dioxide, and the resulting gas is effectively used for other purposes.
発明が解決しようとする問題点
従来用いられている非多孔質高分子膜の特長の一つであ
る高効率・高精度を生かし任意成分を分離するには、膜
の形状・材質等から事前に導入ガス中に含有するダスト
をトレース程度にする必要がある。ダストの除去が完全
でない場合、膜表面への衝突・付着のため充分な分離効
果が発揮でき無くなるばかりか、寿命も大幅に短縮して
しまう。Problems that the invention aims to solve In order to separate arbitrary components by taking advantage of the high efficiency and high precision that are one of the features of conventionally used non-porous polymer membranes, it is necessary to It is necessary to reduce the amount of dust contained in the introduced gas to a trace level. If dust is not completely removed, it will collide with and adhere to the membrane surface, making it impossible to achieve a sufficient separation effect, and will also significantly shorten the life of the membrane.
さらに、非多孔質高分子膜に導く副生ガス中の分離対象
成分の濃度が高ければ高い程、高効率な分離が可能とな
り、回収率、膜面積、動力等の減少が図られ、大幅なコ
ストダウンが図られるが、現状ではこのような予＠濃縮
装置はなく、非多孔質高分子膜装置を２段にして用いれ
ば予備濃縮−濃縮工程は可能であるが、予＠濃縮工程後
膜分離の原理から分離ガス圧は常圧となってしまい、再
度予備濃縮前と同等まで加圧しなければならず非常に非
経済的になってしまう。Furthermore, the higher the concentration of the components to be separated in the by-product gas that leads to the non-porous polymer membrane, the more efficient separation becomes possible, reducing the recovery rate, membrane area, power, etc. Although cost reduction is attempted, there is currently no such pre-concentration equipment, and if a non-porous polymer membrane device is used in two stages, the pre-concentration-concentration process is possible; Due to the principle of separation, the pressure of the separated gas is normal pressure, and it has to be pressurized again to the same level as before preconcentration, which is extremely uneconomical.
しかしながら、これまでこの問題を有利に解決する方法
はなく、現状の非多孔質高分子膜分離装置を用い高効率
に分離する標準的システム構成は、導入副生ガス中ダス
トを除去する工程、非多孔質高分子膜を２段以上の編成
とする必要が生じてしまっている。However, there is no method to advantageously solve this problem so far, and the standard system configuration for highly efficient separation using current non-porous polymer membrane separation equipment is It has become necessary to organize porous polymer membranes into two or more stages.
問題点を解決するための手段
本発明はこれらの問題点を解決することを目的とするも
ので、非多孔質高分子膜の性能を十分に発揮できるよう
導入する副生ガス中の有害物であるダストを除去し、か
つ任意成分のみをある程度まで濃縮するという２つの工
程を同時におこなえるよう、多孔質ガラス膜の細孔径を
コントロールして、非多孔質高分子膜ガス分離装置の事
前処理として用い、高効率・高精度・低コストの任意成
分分離を可能とした副生ガス中の成分分離方法を提供し
ようとするものである。Means for Solving the Problems The purpose of the present invention is to solve these problems.It is an object of the present invention to solve these problems by eliminating harmful substances in the by-product gas introduced in order to fully demonstrate the performance of the non-porous polymer membrane. The pore diameter of the porous glass membrane is controlled so that the two processes of removing certain dust and concentrating optional components to a certain extent can be performed simultaneously, and the membrane is used as a pre-treatment for a non-porous polymer membrane gas separation device. The present invention aims to provide a method for separating components in by-product gases, which enables separation of arbitrary components with high efficiency, high precision, and low cost.
すなわち、本発明は、副生ガスを多孔質ガラス膜に導入
し、ガス中に含まれるダストを除去、且つ分離対象成分
のみをある一定以上の濃度に濃縮し、次いでこれを非多
孔質高分子膜に導入し、高効率・高精度に精製分離する
ことを特徴とする副生ガス中任意成分分離方決である。That is, the present invention introduces a by-product gas into a porous glass membrane, removes dust contained in the gas, concentrates only the components to be separated to a certain concentration or higher, and then converts this into a non-porous polymer. This is a method for separating arbitrary components in by-product gas, which is introduced into a membrane and purified and separated with high efficiency and precision.
作用
本発明は、副生ガスを物理的損傷に強く、細孔径の大き
さにより副生ガス中の任意成分を分離でき、その時の圧
損も非多孔質高分子膜に比べ非常に少ない多孔質ガラス
膜に導き、非多孔質高分子膜で有害となるガス中のダス
トを９９％以上除去すると共に、５〜２０％程度、任意
成分の予＠濃縮を行わせ、これを次工程の非多孔質高分
子膜に導く副生ガス中の成分分離方法であって、本発明
によれば非多孔質高分子膜を単体で利用する場合に比べ
、回収率、動力費、膜面積ともに改善でき、非常に低コ
ストで任意成分を分離することができる。Function The present invention uses porous glass that is resistant to physical damage to by-product gases, can separate arbitrary components in the by-product gases depending on the size of the pores, and has significantly less pressure loss than non-porous polymer membranes. The non-porous polymer membrane removes more than 99% of the harmful dust in the gas, and pre-concentrates optional components by about 5-20%, which is then transferred to the non-porous membrane in the next step. This is a method for separating components in a by-product gas that is introduced into a polymer membrane, and according to the present invention, compared to the case where a non-porous polymer membrane is used alone, the recovery rate, power cost, and membrane area can be significantly improved. Any component can be separated at low cost.
以下さらに本発明の詳細な説明する。The present invention will be further explained in detail below.
本発明において、多孔質ガラス膜とは、気体分子の平均
自由工程とほぼ同じか、もしくはそれより小さい細孔を
持つものであって、さらに空隙率が大きく、薄い膜状の
ものであり、その膜の細孔の大きさを利用し、分子径差
により、対象成分を分離することができるものである。In the present invention, a porous glass membrane is one that has pores that are approximately the same as or smaller than the mean free path of gas molecules, has a large porosity, and is thin. By utilizing the size of the pores in the membrane, target components can be separated based on the difference in molecular diameter.
具体的には、５ｉ０２系ガラスに熱処理を加えある一定
の細孔径分布を持ったもので、ある任意成分のみを透過
分離されるように目的に応じて細孔径分布を調整したも
のである。Specifically, 5i02 glass is heat-treated to have a certain pore size distribution, and the pore size distribution is adjusted according to the purpose so that only certain arbitrary components can be permeated and separated.
一方非多孔質高分子膜とは、各気体を透過する機能を有
し、かつ使用条件下で、熱、圧力、化学的安定などに対
する耐性を有し、薄膜化された高分子膜のことであって
、各気体の高分子膜への溶解度係数と高分子膜中の拡散
係数の差を利用して、混合ガス成分を分離するものであ
る。具体的には酢酸セルローズ、ポリイミド、ポリブタ
ジェン、ブロイミド等の有機系高分子を極めて薄い膜状
にしたものであり、そのモデュールとしては、チューブ
ハンドル型、積層型、二流積層型などがある。両者とも
導入する副生ガスをある圧まで昇圧して膜に導き、混合
ガス成分を分離する。On the other hand, a non-porous polymer membrane is a thin polymer membrane that has the ability to permeate various gases and has resistance to heat, pressure, chemical stability, etc. under the conditions of use. The mixed gas components are separated using the difference between the solubility coefficient of each gas in the polymer membrane and the diffusion coefficient in the polymer membrane. Specifically, it is an extremely thin film made of organic polymers such as cellulose acetate, polyimide, polybutadiene, and bromide, and its modules include tube handle type, laminated type, and two-flow laminated type. In both cases, the introduced by-product gas is boosted to a certain pressure and introduced into the membrane to separate the mixed gas components.
本発明者らはこれらの特長を生かすべく、多孔質ガラス
膜の細孔径をコントロールし、非多孔質高分子膜の分離
機能に影響を及ぼさないよう一定値以下迄ダスト（量・
径）を除去でき、かつ一定値以上にガス成分中の任意成
分のみを濃縮できるようにした。In order to take advantage of these features, the present inventors controlled the pore diameter of the porous glass membrane and kept the dust (amount and amount) below a certain value so as not to affect the separation function of the non-porous polymer membrane.
diameter), and it is now possible to concentrate only arbitrary components in the gas components above a certain value.
すなわち、多孔質ガラス膜の細孔径を平均１００人で、
かつシャープな分布をもたせることにより、副生ガス中
のダストの８８％以上が除去され、製鉄所内の加熱炉で
発生する副生ガスを５〜２０％程度濃縮するのにほとん
ど数ｋｇ／ｃｍ’の圧損で可能とすることができた。In other words, the pore diameter of the porous glass membrane was determined by an average of 100 people.
Moreover, by providing a sharp distribution, more than 88% of the dust in the by-product gas is removed, and it takes just a few kg/cm' to concentrate the by-product gas generated in the heating furnace in a steelworks by 5 to 20%. This was possible with a pressure drop of .
また分離対象成分により非透過側に分離されることもあ
るが、この場合も多孔質ガラス膜内偏流板への衝突によ
り同程度のダストが除去でき、圧損も数ｋｇ／ｃｒｒｆ
以下で、５〜１０％程度のガス濃縮が可能であった。In addition, depending on the component to be separated, it may be separated to the non-permeate side, but in this case as well, the same amount of dust can be removed by collision with the drift plate in the porous glass membrane, and the pressure loss is also several kg/crrf.
Gas concentration of about 5 to 10% was possible below.
本発明において、適用可能な副生ガスとじては、たとえ
ば製鉄所内で発生する熱風炉燃焼排ガス、コークス炉燃
焼排ガス、ボイラー燃焼排ガス、鋼材加熱炉燃焼ガス等
があげられる。In the present invention, applicable by-product gases include, for example, hot-blast furnace combustion exhaust gas, coke oven combustion exhaust gas, boiler combustion exhaust gas, steel heating furnace combustion gas, etc. generated in a steelworks.
これらの副生ガスの成分としては、代表的には水素、メ
タン、−酸化炭素、二酸化炭素、窒素などが挙げられる
。本発明を適用することにより、これらの１種以上のガ
スを高効率、高精度に分離回収することができる。Components of these by-product gases typically include hydrogen, methane, carbon oxide, carbon dioxide, and nitrogen. By applying the present invention, one or more of these gases can be separated and recovered with high efficiency and precision.
実施例
以下実施例をあげて、本発明を具体的に説明するが、本
発明はこれら実施例により限定されるものではない。EXAMPLES The present invention will be specifically explained with reference to Examples, but the present invention is not limited to these Examples.
実施例１
コークス炉ガスより水素を分離する場合、第１図に示す
ようにマークス炉ガスを活性炭などを挿入しである吸着
塔１に導き、コークス炉ガス中のタール、ナフタリン、
ＮＯｘガムを吸着させ、これらの不純物の含量をトレー
スとした。次に、不純物を除去したガスをコンプレッサ
ー２に導き、その圧力２〜２０ｋｇ／ｃｒｎ’Ｇに昇圧
すると共に、コンプレッサー内装クーラーによりガス温
度４０〜１５０℃とした後、例えば管状アルミナ多孔体
からなり透過係数Ｈ２：５７、ＣＯ２：１５、Ｎ２ ：
ＩＩＸ １０−’ｃｍ３／ ｃｍ・ｓ ｅ ｃｍＨｇ
を有するような多孔質ガラス膜３に導入した。このとき
のガス成分は水素５０〜６０％程度、メタン２０％程度
、−酸化炭素、二酸化炭素等からなり、ダストは活性炭
を含めｌ ｍｇ／Ｎｍ”程度であった。Example 1 When separating hydrogen from coke oven gas, as shown in FIG.
NOx gum was adsorbed and the content of these impurities was traced. Next, the gas from which impurities have been removed is led to the compressor 2, where the pressure is increased to 2 to 20 kg/crn'G, and the gas temperature is set to 40 to 150 degrees Celsius by a cooler inside the compressor. Coefficient H2: 57, CO2: 15, N2:
IIX 10-'cm3/cm・s e cmHg
was introduced into the porous glass membrane 3 having the following properties. The gas components at this time consisted of about 50 to 60% hydrogen, about 20% methane, -carbon oxide, carbon dioxide, etc., and the amount of dust including activated carbon was about 1 mg/Nm''.
このガスを平均細孔径５０〜８０人程度の多孔質ガラス
膜３に導入すると、ダストは完全にトレースまで除去さ
れ、一方透過側平均水素儂縮度は１０〜２０％上昇し、
その透過側圧力は１５〜８ ｋｇ／ｃｍ″Ｇとなった。When this gas is introduced into the porous glass membrane 3 with an average pore diameter of about 50 to 80 pores, the dust is completely removed to the trace level, while the average hydrogen shrinkage degree on the permeate side increases by 10 to 20%.
The pressure on the permeate side was 15-8 kg/cm''G.
次いでこれを例えば酢酸セルロースからなり透過係数Ｈ
７： ３５．９、ＣＯ２： ３．０５、Ｎ２ ： ０．
２１Ｘ １０−１１ｃｍ” ／ ｃｍ ＊ ｓ ｍ ｃ
ｍＨｇを有するような非多孔質高分子膜４に導入すると
、９９．８％以上の水素濃度のガスが得られた。This is then made of, for example, cellulose acetate and has a permeability coefficient H.
7: 35.9, CO2: 3.05, N2: 0.
21X 10-11cm” / cm * s m c
When introduced into a non-porous polymer membrane 4 having mHg, a gas with a hydrogen concentration of 99.8% or more was obtained.
この実施例の方法は従来の非多孔質高分子膜単独分離装
置を用いた場合に比べて、回収率で数１０％上昇し、膜
所要面積も届〜１１５減少し、動力費も数１０％減少し
、非常に効率のよいプロセスであった。Compared to the case of using a conventional non-porous polymer membrane separation device, the method of this example increases the recovery rate by several tens of percent, reduces the required membrane area by ~115, and reduces power costs by several tens of percent. It was a very efficient process.
実施例２
熱風炉の排ガス中の二酸化炭素を分離する場合、第２図
に示すように水冷式ドレンカット５に導き、現状１００
〜２００℃程度の排ガスを温度５０〜１００℃に冷却し
てドレンをカットし、ガス中の水分を飽和濃度以下にし
てコンプレッサー２に導入し、その圧力を９〜２０ｋｇ
／ｃｍ２に昇圧すると共にコンプレッサー内装クーラー
により温度５０〜１００℃の範囲に冷却し、排ガス飽和
点以下の温度にならないようにコントロールした。Example 2 When separating carbon dioxide from the exhaust gas of a hot air stove, as shown in FIG.
The exhaust gas at ~200℃ is cooled to a temperature of 50~100℃, the drain is cut, the moisture in the gas is reduced to below the saturation concentration, and the gas is introduced into the compressor 2, and the pressure is set to 9~20kg.
The pressure was increased to /cm2, and the temperature was cooled to a range of 50 to 100°C using a cooler built into the compressor, and the temperature was controlled so as not to fall below the exhaust gas saturation point.
この時の排ガス中の成分は窒素ガス７０〜８０％、二酸
化炭素２０〜３０％、ダストはｌ −１０＋ａｇ／Ｎｒ
ｎ’であった。The components in the exhaust gas at this time are 70-80% nitrogen gas, 20-30% carbon dioxide, and the dust is 1 -10 + ag/Nr.
It was n'.
このガスを平均細孔径１００人程度で、非常にシャープ
な分布をもたせた多孔質ガラス膜３に導くと、透過側に
二酸化炭素は流れ、ダス） ０．１ｍｇ／Ｎｍ’以下、
二酸化炭素濃度は５〜１０％程度上昇、圧力は８〜１９
ｋｇ／ｃｎｆどなった。When this gas is introduced into the porous glass membrane 3, which has an average pore diameter of about 100 mm and a very sharp distribution, carbon dioxide flows to the permeate side, and the carbon dioxide is less than 0.1 mg/Nm'.
Carbon dioxide concentration rose by about 5-10%, pressure 8-19
What happened to kg/cnf?
これを例えばポリイミドからなり透過係数Ｈ２：５７、
ＣＯ２： １０．５、Ｎ２ ： ０．５８Ｘ １０−
” ｃｍ３７ｃｍ ｅ ｓ・ｅｍＨｇを有するよう
な非多孔質高分子膜４に導き、二酸化炭素８０〜９９％
程度とした。この実施例の方法は従来の非多孔質高分子
膜単独分離装６を用いた場合に比べて、回収率で数１０
％上昇、膜所要面積も局〜１７５減少し、動力費も数１
０％減少し、非常に効率のよいプロセスであった。For example, it is made of polyimide, with a transmission coefficient H2: 57,
CO2: 10.5, N2: 0.58X 10-
” cm 37 cm e s em Hg, and carbon dioxide 80 to 99%.
degree. The method of this example has a recovery rate of several tens of times higher than that of the conventional non-porous polymer membrane separation device 6.
% increase, the required membrane area decreased by ~175, and the power cost decreased by several points.
It was a very efficient process with a reduction of 0%.
発明の効果
本発明は、副生ガスを多孔質ガラス膜に導入して、その
不要成分を減少させるとともに、目的成分を予備濃縮さ
せ、これを非多孔質高分子膜に導入して目的成分を分＃
（回収）する方法であって、本発明によれば非多孔質高
分子膜単体で用いる場合に比べて、回収率、動力費、膜
面積ともに改善され非常に低コストで目的成分を分離す
ることができる。Effects of the Invention The present invention introduces a by-product gas into a porous glass membrane to reduce its unnecessary components, pre-concentrates a target component, and introduces it into a non-porous polymer membrane to reduce the target component. Minute #
According to the present invention, compared to the case where a non-porous polymer membrane is used alone, the recovery rate, power cost, and membrane area are improved, and the target component can be separated at a very low cost. Can be done.
図面は本発明の実施例を示すものであって、第１図はコ
ークス炉ガス中の水素ガス成分を分離する工程のフロー
図、第２図は熱風炉の排ガス中の炭酸ガス成分を分離す
る工程のフロー図である。
１・・・吸着塔、２１１１１ ＠コンプレッサー、３・
・・多孔質ガラス膜、４・◆拳非多孔質高分子膜、５−
・・ドレンカット。The drawings show an embodiment of the present invention, in which Fig. 1 is a flow diagram of the process of separating hydrogen gas components from coke oven gas, and Fig. 2 is a flow diagram of a process for separating carbon dioxide gas components from hot blast oven exhaust gas. It is a flow diagram of a process. 1... Adsorption tower, 21111 @ Compressor, 3.
・・Porous glass membrane, 4・◆Fist non-porous polymer membrane, 5-
...Drain cut.
Claims (1)
ダストを除去、且つ分離対象成分のみをある一定以上の
濃度に濃縮し、次いでこれを非多孔質高分子膜に導入し
、高効率・高精度に精製分離することを特徴とする副生
ガス中任意成分分離方法。The by-product gas is introduced into a porous glass membrane, the dust contained in the gas is removed, and only the components to be separated are concentrated to a certain concentration or higher, and then this is introduced into a non-porous polymer membrane to remove the dust contained in the gas. A method for separating arbitrary components in by-product gas, which is characterized by efficient and highly accurate purification and separation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13968187A JPS63305916A (en) | 1987-06-05 | 1987-06-05 | Separation of component contained in by-product gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13968187A JPS63305916A (en) | 1987-06-05 | 1987-06-05 | Separation of component contained in by-product gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS63305916A true JPS63305916A (en) | 1988-12-13 |
Family
ID=15250949
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP13968187A Pending JPS63305916A (en) | 1987-06-05 | 1987-06-05 | Separation of component contained in by-product gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63305916A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0858826A2 (en) * | 1997-02-14 | 1998-08-19 | Praxair Technology, Inc. | Air separation system and method |
| JP2008157226A (en) * | 2006-12-19 | 2008-07-10 | General Electric Co <Ge> | Method and system for using low btu fuel gas in gas turbine |
-
1987
- 1987-06-05 JP JP13968187A patent/JPS63305916A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0858826A2 (en) * | 1997-02-14 | 1998-08-19 | Praxair Technology, Inc. | Air separation system and method |
| EP0858826A3 (en) * | 1997-02-14 | 1998-09-09 | Praxair Technology, Inc. | Air separation system and method |
| JP2008157226A (en) * | 2006-12-19 | 2008-07-10 | General Electric Co <Ge> | Method and system for using low btu fuel gas in gas turbine |
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