JPS63270524A - Two-stage gas separation for hydrocarbon vapor - Google Patents
Two-stage gas separation for hydrocarbon vaporInfo
- Publication number
- JPS63270524A JPS63270524A JP62103105A JP10310587A JPS63270524A JP S63270524 A JPS63270524 A JP S63270524A JP 62103105 A JP62103105 A JP 62103105A JP 10310587 A JP10310587 A JP 10310587A JP S63270524 A JPS63270524 A JP S63270524A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- hydrocarbon vapor
- vapor
- stage
- hydrocarbon
- 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
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 37
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 37
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 36
- 238000000926 separation method Methods 0.000 title claims description 21
- 239000012528 membrane Substances 0.000 claims abstract description 27
- 239000007788 liquid Substances 0.000 claims abstract description 13
- 238000011084 recovery Methods 0.000 claims abstract description 11
- 239000012466 permeate Substances 0.000 claims description 10
- 238000010521 absorption reaction Methods 0.000 claims description 5
- 239000003502 gasoline Substances 0.000 abstract description 18
- 239000007789 gas Substances 0.000 description 58
- 238000000034 method Methods 0.000 description 10
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 238000007796 conventional method Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
炭化水素蒸気と空気との混合ガスから炭化水素蒸気を分
離する・ための技術に関する。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to a technique for separating hydrocarbon vapor from a mixed gas of hydrocarbon vapor and air.
ガソリン、灯油、ベンゼン、アルコール類等の揮発性変
化水素を貯蔵タンク、タンクロー９、タンク車等に充填
し、或いは気温に、昇時などに発生する炭化水素ガスを
含む混合ガスは従来大気中にそのまま放散されていた。Traditionally, volatile hydrogen such as gasoline, kerosene, benzene, alcohols, etc. is filled into storage tanks, tank rows, tank cars, etc., or mixed gases containing hydrocarbon gases that are generated when the temperature rises are released into the atmosphere. It was just being dissipated.
しかし、このように大気中に放散されたガスは、光化学
スモッグの生成物質として大気汚染の重賞原因の工つに
挙げられており、各地方自治体などで前記ガスの排出濃
度が規制されつつある。However, the gases released into the atmosphere in this way are listed as one of the major causes of air pollution as photochemical smog generators, and local governments are beginning to regulate the emission concentration of these gases. .
近年ガス分離膜の発展に伴い、前記炭化水素蒸気の分離
についてもこのガス分離膜の利用が検討されるようにな
り、これはガス分離膜を中間に入れた混合ガスに圧力差
をつけると、圧力の高い側から低い側にガスが透過して
行き、このときのガス透過速度は同一の膜に対してもガ
ス成分ごとに異ることを利用したものである。In recent years, with the development of gas separation membranes, the use of gas separation membranes has been considered for the separation of hydrocarbon vapors. This method takes advantage of the fact that gas permeates from the high-pressure side to the low-pressure side, and the gas permeation rate at this time differs depending on the gas component even through the same membrane.
ここでは空気と炭化水素蒸気との混合ガスをガス分！ａ
膜の透過側を低圧として炭化水素蒸気を主とした透過を
図り、この炭化水素蒸気を主とした混合ガスを加圧して
回収塔に送ると共に炭化水素濃度の低減された処理済み
ガスを大気中に放散させ、前記の炭化水素蒸気を主とし
た混合ガスを加圧して回収塔に送りタンク貯蔵液を吸収
液として該炭化水素蒸気を吸収させる方法に例えば特願
昭８１−１２０３１１等がある。Here, a mixture of air and hydrocarbon vapor is used as a gas! a
The permeation side of the membrane is kept under low pressure to allow mainly hydrocarbon vapor to permeate, and this mixed gas, mainly consisting of hydrocarbon vapor, is pressurized and sent to the recovery tower, while the treated gas with reduced hydrocarbon concentration is released into the atmosphere. For example, Japanese Patent Application No. 81-120311 discloses a method in which a mixed gas mainly consisting of hydrocarbon vapor is pressurized and sent to a recovery tower, and the liquid stored in a tank is used as an absorption liquid to absorb the hydrocarbon vapor.
ガス分離膜１段で前記混合ガスから炭化水素蒸気を透過
分離するためには、約３０Ｔｏｒｒ程度の高真空が必要
であり、真空ポンプの容量が大きくなるので、１段で炭
化水素蒸気を透過分離することは、大容量の真空ポンプ
を運転しなければならない。In order to permeate and separate hydrocarbon vapor from the mixed gas in one stage of gas separation membrane, a high vacuum of about 30 Torr is required, and the capacity of the vacuum pump becomes large, so it is not possible to permeate and separate hydrocarbon vapor in one stage. To do this, a large capacity vacuum pump must be operated.
空気と炭化水素蒸気との混合ガスをガス分離膜により、
真空ポンプで負正にした側に炭化水素蒸気を選択的に透
過させ、ついでこの炭化水素蒸気を大気圧以−ヒに加圧
して、タンク貯蔵液を吸収液とした回収塔に送り、混合
ガ、スから炭化水素蒸気を分離する方法において、ガス
分離膜と真空ポンプとを直列に２段以上にして混合ガス
から炭化水素２人気を透過分離することを特徴とする炭
化水素蒸気の２段ガス分離方法にある。A mixed gas of air and hydrocarbon vapor is separated by a gas separation membrane.
The hydrocarbon vapor is selectively permeated through the negative and positive sides of the vacuum pump, and then this hydrocarbon vapor is pressurized above atmospheric pressure and sent to the recovery tower where the tank storage liquid is used as the absorption liquid, and the mixed gas is , a two-stage method for separating hydrocarbon vapor from a gas mixture, characterized in that two or more stages of gas separation membranes and vacuum pumps are connected in series to permeate and separate two hydrocarbons from a mixed gas. It's in the separation method.
本発明は一ヒ記ガス分離膜と真空ポンプの組合せを直列
に２段以上にして前述ガスから炭化水素蒸気を透過除去
することにより動力の低減がはかられる。In the present invention, the power consumption can be reduced by arranging two or more stages of the gas separation membrane and vacuum pump in series to permeate and remove hydrocarbon vapor from the gas.
に記回収塔で吸収液に回収されなかった炭化水素蒸気含
有の混合ガスは前記ガス分離膜に対する入側に戻されて
再循環される。The hydrocarbon vapor-containing mixed gas that is not recovered into the absorption liquid in the recovery column is returned to the inlet side of the gas separation membrane and recirculated.
本発明の一実施例のａ要を第１図に示す、４０マＯ１％
のガソリン蒸気とＢＯマ０１％の空気を含む４２０ ｍ
’／Ｈの混合ガスを処理して、出口排ガスを５７０１％
のガソリン蒸気にする場合について述べる。The main points of an embodiment of the present invention are shown in FIG.
420 m containing 1% gasoline vapor and 01% BO
'/H mixed gas to reduce outlet exhaust gas to 5701%
Let us discuss the case of converting gasoline into vapor.
常圧のガソリンタンクなどから排出されたガソリン蒸気
濃度４０マＯ１％を含む４２０ｍ”／Ｈの混合ガスｌは
、ブロワ−２で加圧された後にリターンガス１４と混合
される。このガスは、フィルターセパレータ３でミスト
やダストを除去された後に第１段［１のガス分離膜４に
入る。A mixed gas l of 420 m''/H containing a gasoline vapor concentration of 40 mO1% discharged from a normal pressure gasoline tank is pressurized by the blower 2 and then mixed with the return gas 14. This gas is After the mist and dust are removed by the filter separator 3, the gas enters the gas separation membrane 4 of the first stage [1].
ここで混合ガスは、ガス分１ｌｌｌ膜を相対的に透過し
やすいガソリン蒸気が多く除かれ、ガソリン蒸気濃度ｌ
Ｏ数マｏ１％の混合ガスとなる。Here, from the mixed gas, much of the gasoline vapor that is relatively easy to permeate through the 1llll gas membrane is removed, and the gasoline vapor concentration is
It becomes a mixed gas of several O and O1%.
次にこのガスは、２段目のガス分離膜５に入り、ガソリ
ン蒸気濃度５マｏ１％以下の混合ガス６となって、大気
中に放散される。Next, this gas enters the second-stage gas separation membrane 5, becomes a mixed gas 6 with a gasoline vapor concentration of 5 mmol or less, and is dissipated into the atmosphere.
一方第１段目のガス分離膜４を透過したガソリン蒸気濃
度が８０数マｏ１％ぐらいに高くなった混合ガス７は、
第１段真空ポンプ８で１１０Ｔｏｒｒ程度で吸引された
後に、加圧されて回収塔９に入る。On the other hand, the mixed gas 7 that has passed through the first stage gas separation membrane 4 and has a gasoline vapor concentration as high as about 80 Mao1%,
After being suctioned at about 110 Torr by the first stage vacuum pump 8, it is pressurized and enters the recovery tower 9.
回収塔は若干大気圧より高い圧力で運転され、底部より
入ってきた混合ガスは、充填層を上昇しながら頂部に供
給されたガソリン液ｌＯと直接接触して吸収され、ガソ
リンとして回収される。The recovery tower is operated at a pressure slightly higher than atmospheric pressure, and the mixed gas entering from the bottom is absorbed by directly contacting the gasoline liquid 1O supplied to the top while rising through the packed bed, and is recovered as gasoline.
回収されたガソリンは、ガソリンリターンポンプ１１に
よってガソリンタンクに戻される。The recovered gasoline is returned to the gasoline tank by the gasoline return pump 11.
ここで吸収されなかったガスはガソリン蒸気濃度５０マ
ｏ１％ぐらいで、２段目のガス分ａ膜５を透過した６０
マ０１％のガソリン蒸気を含む混合ガス１２と共にフィ
ルターセパレータ３に戻される。The gas not absorbed here has a gasoline vapor concentration of about 50 mO1%, and has passed through the second stage gas separation membrane 5.
It is returned to the filter separator 3 together with a mixed gas 12 containing 01% gasoline vapor.
また、上記の方法において、１段目の透過ガス７と２段
目の透過ガス１２とを真空ポンプ昨日で合流させて回収
塔９に供給するようにしても性能的にはほとんど変らな
い。Furthermore, in the above method, even if the first-stage permeate gas 7 and the second-stage permeate gas 12 are combined using the vacuum pump and then supplied to the recovery column 9, there is almost no difference in performance.
この発明と従来の方法である特願昭８１−１２０３１１
の１段ガス分離脱法とを比較すると、２段式は１段目は
低真空で充分であり、２段目は高真空であるが小官？で
充分である。これに対し１段式は初段が高真空でかつ大
容量であるので不経済である。Patent application No. 81-120311 which describes this invention and the conventional method
Comparing with the one-stage gas separation and desorption method, the two-stage method has a low vacuum sufficient for the first stage, and a high vacuum for the second stage, but is this a minor issue? is sufficient. On the other hand, the one-stage type is uneconomical because the first stage is under high vacuum and has a large capacity.
−例を下に示す。- Examples are shown below.
１、真空ポンプ容量は、
本発明： ２５ｒｎ”／ｓｉｎ １１０Ｔｏｒｒ １
台、２５ｒｎ”／ｓｉｎ ３５Ｔｏｒｒ １台１段
膜法： ５０ｒｎ’／ｓｉｎ ３５Ｔｏｒｒ ２台
となり、真、空ポンプの総容量は、本発明と１段ガス分
離膜法を比べると半分程度となっている。1. Vacuum pump capacity is: Invention: 25rn”/sin 110Torr 1
25rn'/sin 35Torr, 1 unit, 1-stage membrane method: 50rn'/sin 35Torr, 2 units, and the total capacity of the vacuum and air pumps is about half of that of the present invention and the 1-stage gas separation membrane method. .
以上説明した通り、本発明によれば真空ポンプの総合計
を従来法の約１／２に品減することができ、吸収塔、循
環ポンプ等の設備も簡便なものとすることができると同
時に設備費、動力費を軽減できる等優れた効果を有する
。As explained above, according to the present invention, the total number of vacuum pumps can be reduced to about half of the conventional method, and equipment such as absorption towers and circulation pumps can be simplified. It has excellent effects such as reducing equipment costs and power costs.
１固層は本発明の方法を実施する設備の１例について４
１！要を示した説明図である。
この図面において、ｌは処理すべき混合ガス、２・・・
ブロワ−１３・・・フィルターセパレータ、４・・・第
１段ガス分Ｒ１膜、５・・・第２段ガス分＃膜、６・・
・濃度の低い処理済みガス、７・・・第１段ガス分離膜
で分離された炭化水素濃度の高い混合ガス、８・・・第
１段真空ポンプ、９・・・回収塔、ｌＯ・・・炭化水素
液、１１・・・炭化水素液リターンポンプ、１２・・・
第２段処理済みの中濃度炭化水素ガス、１３・・・第２
段ガス分離膜の真空ポンプ、１４・・・リターンガスを
示すものである。1 solid phase for one example of equipment carrying out the method of the invention 4
1! It is an explanatory diagram showing the main points. In this drawing, l is the mixed gas to be treated, 2...
Blower 13... Filter separator, 4... 1st stage gas R1 membrane, 5... 2nd stage gas # membrane, 6...
- Processed gas with low concentration, 7... Mixed gas with high hydrocarbon concentration separated by the first stage gas separation membrane, 8... First stage vacuum pump, 9... Recovery tower, lO...・Hydrocarbon liquid, 11...Hydrocarbon liquid return pump, 12...
Medium-concentration hydrocarbon gas processed in the second stage, 13...2nd
Vacuum pump for staged gas separation membrane, 14...represents return gas.
Claims (1)
真空ポンプで負圧にした側に炭化水素蒸気を選択的に透
過させ、ついでこの炭化水素蒸気を大気圧以上に加圧し
て、タンク貯蔵液を吸収液とした回収塔に送り、混合ガ
スから炭化水素蒸気を分離する方法において、ガス分離
膜と真空ポンプとを直列に２段以上にして混合ガスから
炭化水素蒸気を透過分離することを特徴とする炭化水素
蒸気の２段ガス分離方法。A mixed gas of air and hydrocarbon vapor is separated by a gas separation membrane.
Hydrocarbon vapor is selectively permeated through the negative pressure side of the vacuum pump, and then this hydrocarbon vapor is pressurized above atmospheric pressure and sent to a recovery tower using tank storage liquid as an absorption liquid, where it is carbonized from the mixed gas. A two-stage gas separation method for hydrocarbon vapor, characterized in that a gas separation membrane and a vacuum pump are arranged in two or more stages in series to permeate and separate hydrocarbon vapor from a mixed gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62103105A JPS63270524A (en) | 1987-04-28 | 1987-04-28 | Two-stage gas separation for hydrocarbon vapor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62103105A JPS63270524A (en) | 1987-04-28 | 1987-04-28 | Two-stage gas separation for hydrocarbon vapor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS63270524A true JPS63270524A (en) | 1988-11-08 |
Family
ID=14345339
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62103105A Pending JPS63270524A (en) | 1987-04-28 | 1987-04-28 | Two-stage gas separation for hydrocarbon vapor |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63270524A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6772740B2 (en) | 2002-04-17 | 2004-08-10 | Toyota Jidosha Kabushiki Kaisha | Evaporative fuel treating device and method |
| US6786207B2 (en) | 2002-04-17 | 2004-09-07 | Toyota Jidosha Kabushiki Kaisha | Evaporative fuel emission control system |
| US7958652B2 (en) * | 2005-01-07 | 2011-06-14 | Bissell Homecare Inc. | Extraction cleaning with plenum and air outlets facilitating air flow drying |
| JP2014117687A (en) * | 2012-12-19 | 2014-06-30 | Ube Ind Ltd | Gas separation recovery system and gas separation recovery method |
-
1987
- 1987-04-28 JP JP62103105A patent/JPS63270524A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6772740B2 (en) | 2002-04-17 | 2004-08-10 | Toyota Jidosha Kabushiki Kaisha | Evaporative fuel treating device and method |
| US6786207B2 (en) | 2002-04-17 | 2004-09-07 | Toyota Jidosha Kabushiki Kaisha | Evaporative fuel emission control system |
| DE10317583B4 (en) * | 2002-04-17 | 2012-03-01 | Toyota Jidosha Kabushiki Kaisha | Apparatus and method for treating vaporized fuel for an internal combustion engine |
| US7958652B2 (en) * | 2005-01-07 | 2011-06-14 | Bissell Homecare Inc. | Extraction cleaning with plenum and air outlets facilitating air flow drying |
| JP2014117687A (en) * | 2012-12-19 | 2014-06-30 | Ube Ind Ltd | Gas separation recovery system and gas separation recovery method |
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