JP2000117048A - Adsorptive capturing device and adsorptive recovering device of volatile petroleum compound - Google Patents
Adsorptive capturing device and adsorptive recovering device of volatile petroleum compoundInfo
- Publication number
- JP2000117048A JP2000117048A JP10208572A JP20857298A JP2000117048A JP 2000117048 A JP2000117048 A JP 2000117048A JP 10208572 A JP10208572 A JP 10208572A JP 20857298 A JP20857298 A JP 20857298A JP 2000117048 A JP2000117048 A JP 2000117048A
- Authority
- JP
- Japan
- Prior art keywords
- adsorption
- hydrocarbons
- air
- tower
- adsorptive
- 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.)
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Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
- B01D53/0438—Cooling or heating systems
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/10—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
- B01J20/103—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate comprising silica
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/20—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising free carbon; comprising carbon obtained by carbonising processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/702—Hydrocarbons
- B01D2257/7022—Aliphatic hydrocarbons
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/702—Hydrocarbons
- B01D2257/7027—Aromatic hydrocarbons
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は揮発性石油化合物の
吸着式捕集装置と吸着回収装置に係るものであり、特
に、揮発性石油化合物の精製施設、貯蔵施設あるいは取
扱施設から排出されて大気環境汚染と資源損失を誘発す
る揮発性石油化合物を効率的に捕集できる吸着式捕集装
置と、この吸着式捕集装置によって吸着捕集した炭化水
素類を大気圧より低い圧力で洗浄する低圧洗浄法により
脱着して揮発性石油化合物を得て、この揮発性石油化合
物を空気と混合して処理する２塔式の吸着回収装置とで
構成した揮発性石油化合物の捕集装置と吸着回収装置に
関するものである。本発明の装置では、炭化水素類を液
状で回収して再活用することにより大気環境汚染を防止
するようにしている。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a volatile petroleum compound adsorptive trapping device and an adsorptive recovery device, and more particularly to a volatile petroleum compound discharged from a refining facility, a storage facility, or a handling facility. An adsorptive collection device that can efficiently collect volatile petroleum compounds that cause environmental pollution and resource loss, and a low-pressure system that cleans hydrocarbons adsorbed and collected by the adsorptive collection device at a pressure lower than atmospheric pressure A volatile petroleum compound is obtained by desorption by a washing method, and the volatile petroleum compound is collected and adsorbed and collected by a two-tower adsorption / recovery device which mixes the volatile petroleum compound with air for treatment. It is about. In the apparatus of the present invention, the hydrocarbons are collected in a liquid state and reused to prevent air pollution.
【０００２】[0002]
【従来の技術】炭化水素類の中でレイド蒸気圧が１０．
３ｋＰａ（または１．５ｐｓｉａ、１ｋＰａ＝０．０１
０２ｋｇ／ｃｍ２）以上である石油化学物質や、有機溶
剤を排出する石油精製施設、石油化学製造施設、貯蔵施
設及び出荷施設、貯油所の貯蔵施設及び出荷施設、注油
所の貯蔵施設塔から排出される揮発性石油化合物は大気
環境汚染と資源損失を誘発する。2. Description of the Related Art Among hydrocarbons, raid vapor pressure is 10.
3 kPa (or 1.5 psia, 1 kPa = 0.01
Emission from petrochemicals, organic petrochemicals, petrochemical manufacturing facilities, storage and shipping facilities, storage and shipping facilities in oil storages, and storage and storage towers in oil filling stations that emit petrochemicals and organic solvents of at least 02 kg / cm2). Volatile petroleum compounds cause air pollution and resource loss.
【０００３】アメリカやヨーロッパ統合国家では、石油
化合物の中でも揮発性が高いガソリンに関して、１００
０リットルのガソリンを取扱う時に大気に揮発する炭化
水素量を１０ｇ以下に、ドイツでは０．１５ｇ（メタン
成分除外）以下に規制する法規を制定して施行してい
る。[0003] In the United States and the European integrated nations, gasoline, which is a highly volatile petroleum compound, is 100%.
When handling 0 liters of gasoline, the law regulates the amount of hydrocarbons that evaporate to the atmosphere to 10 g or less, and in Germany it regulates to 0.15 g (excluding methane components) and enforces it.
【０００４】一般的にガソリンの蒸気により汚染された
空気の主な汚染成分は脂肪族炭化水素であり、この他少
量の芳香族化合物とナフテン類等で構成されている。[0004] In general, the main polluting components of air polluted by gasoline vapor are aliphatic hydrocarbons, and are also composed of small amounts of aromatic compounds and naphthenes.
【０００５】ガソリンで汚染された空気中に含まれる脂
肪族炭化水素の一般的な成分別体積濃度は、メタン０．
０５％、エタン０．１％、プロパン０．６２％、ブタン
類１１．１〜１８．６％、ペンタン類８．１〜１４．５
％、ヘキサン類２．６〜３．０％、ヘプタン類以上０．
１９〜０．９％であり、その他は空気である。[0005] The general volumetric concentration of aliphatic hydrocarbons contained in gasoline-contaminated air is 0.1% methane.
05%, ethane 0.1%, propane 0.62%, butanes 11.1-18.6%, pentanes 8.1-14.5
%, Hexanes 2.6 to 3.0%, heptane and more.
19 to 0.9%, and the others are air.
【０００６】汚染空気の炭化水素濃度は、季節によって
変化し、またガソリンの種類によっても異なるが、炭化
水素類が占める総体積比は約２０〜４０％である。１０
００リットルのガソリンを取扱う時に揮発するガソリン
で汚染された空気中の炭化水素の体積濃度は４０％であ
り、平均分子量６８．５％ｍｏｌ、密度０．７ｇ／ｃｍ
３とすると、約１．７５リットルの液体ガソリンが損失
することになる。これはガソリン取扱量の０．１７５％
に相当する。[0006] The hydrocarbon concentration of the polluted air varies with the season and also varies depending on the type of gasoline, but the total volume ratio occupied by hydrocarbons is about 20 to 40%. 10
The volume concentration of hydrocarbons in the air contaminated with gasoline that evaporates when handling 00 liters of gasoline is 40%, the average molecular weight is 68.5% mol, and the density is 0.7 g / cm.
As a result of 3, about 1.75 liters of liquid gasoline will be lost. This is 0.175% of gasoline handling volume
Is equivalent to
【０００７】１０００リットルのガソリンを取扱う時大
気に排出される総炭化水素量を０．１５〜１０ｇに規制
する条件を満足するためには回収設備の回収率が９９．
１８〜９９．９８％でなくてはならない。In order to satisfy the condition that the total amount of hydrocarbons discharged into the atmosphere when handling 1000 liters of gasoline is regulated to 0.15 to 10 g, the recovery rate of the recovery equipment must be 99.
It must be 18-99.98%.
【０００８】大気中に揮発される揮発性石油化合物を回
収して大気汚染を防止しつつ、資源を回収して再活用す
る技術としては、膜分離装置、深冷分離装置、吸収装
置、吸着装置とこれらを相互に組み合わせた混合分離装
置がある。Techniques for collecting and reusing resources while collecting volatile petroleum compounds volatilized in the air to prevent air pollution include membrane separation devices, cryogenic separation devices, absorption devices, and adsorption devices. And a mixing / separating apparatus in which these are combined with each other.
【０００９】しかし、最近は排出許容基準が厳格になっ
ているため吸着分離装置を使用するかまたは吸着分離装
置と他の分離装置を組み合わせた回収工程を利用しなけ
ればならない。However, recently, due to stricter discharge allowance standards, it is necessary to use an adsorption / separation apparatus or a recovery step in which an adsorption / separation apparatus is combined with another separation apparatus.
【００１０】膜分離回収装置は、ＰＶＣ製造工程で排出
されるビニルクロライド単量体または化学工場から排出
されるデクロメタン等を回収するため開発されたもの
で、ガソリン蒸気の回収、ポリオレピン洗浄過程で排出
されるエチレン、プロピレン、ブテン等のオレピン類の
回収、精油工場の附生ガスから水素を回収する時にこの
膜分離装置を利用している。（K. Ohlrogge et al./ In
dustrial Applicationsto Separate Volatile Organic
Compounds from Industrial Off-gas Stream, AlChE Sp
ring National Meeting March 9-13, 1997）。[0010] The membrane separation and recovery apparatus has been developed to recover vinyl chloride monomer discharged in the PVC manufacturing process or dechloromethane discharged from a chemical plant, etc., and recovers gasoline vapor and discharges in the polyolepine washing process. This membrane separation device is used when recovering olepines such as ethylene, propylene, butene, etc., and recovering hydrogen from auxiliary gas of an refinery. (K. Ohlrogge et al./ In
dustrial Applicationsto Separate Volatile Organic
Compounds from Industrial Off-gas Stream, AlChE Sp
ring National Meeting March 9-13, 1997).
【００１１】しかしながら、前記膜分離装置だけでガソ
リン成分を回収するためには多段式システムを構成して
分離膜間に大きな圧力差を維持する必要がある。However, in order to recover gasoline components using only the membrane separation device, it is necessary to configure a multistage system to maintain a large pressure difference between the separation membranes.
【００１２】吸着技術は、主に活性炭、シリカゲル、ゼ
オライト等を充填した複数の吸着塔を用いて縮圧、吸着
除去と脱着過程を連続的に行って、揮発性石油化合物で
汚染された空気を処理してこの汚染空気から炭化水素類
を回収するのに使用されている。[0012] The adsorption technique is to continuously perform pressure reduction, adsorption removal and desorption processes using a plurality of adsorption towers filled with activated carbon, silica gel, zeolite, etc., to remove air contaminated with volatile petroleum compounds. It has been used to treat and recover hydrocarbons from this contaminated air.
【００１３】例えば、精油工場と貯油所等から排出され
る汚染空気から炭化水素を回収する吸着工程では、減
圧、低圧洗浄と加熱脱着により吸着剤を再生するように
している。（特開平７−２８４６２３号公報、特開平９
−１４１０３９号公報）また、乳棒式真空ポンプを使用
して減圧と低圧洗浄によって吸着塔を再生して、この時
脱着される揮発性有機化合物の成分が真空ポンプオイル
に吸収されないようにするためにポンプオイルを露点以
上で加熱して使用する方法もある。（ＵＳＰ４，８５
７，０８４）。For example, in the adsorption step of recovering hydrocarbons from polluted air discharged from an oil refinery and a storage, etc., the adsorbent is regenerated by decompression, low pressure washing and heat desorption. (JP-A-7-284623, JP-A-9-284
In addition, in order to prevent the components of the volatile organic compound desorbed at this time from being absorbed by the vacuum pump oil, the adsorption tower is regenerated by vacuum and low pressure washing using a pestle type vacuum pump. There is also a method in which the pump oil is heated above the dew point and used. (USP 4,85
7,084).
【００１４】また、揮発性石油化合物の取扱施設から排
出される汚染空気を貯蔵タンクに捕集した後、吸収、膜
分離、吸着分離方法を組合せた回収装置でこれを回収す
る方法も使用されている（Hydrocarbon Processing, Au
g. 1996）。Further, a method is also used in which contaminated air discharged from a volatile petroleum compound handling facility is collected in a storage tank, and then collected by a recovery apparatus combining absorption, membrane separation and adsorption separation methods. (Hydrocarbon Processing, Au
g. 1996).
【００１５】[0015]
【発明が解決しようとする課題】しかし、揮発性石油化
合物の精製施設、貯蔵施設あるいは取扱施設では石油類
を給油する短時間の間に多量の汚染空気が不規則、かつ
散発的に大気中に放出される。従来は汚染空気捕集量に
よってレベルが変わる流動式貯蔵タンクに汚染空気を捕
集した後、その捕集した汚染空気を回収設備に供給して
炭化水素成分を回収して清浄空気を大気に排出するよう
にしている。しかし、短時間に高速で散発的に排出され
る汚染空気を流動式貯蔵タンクを使用して捕集するには
大型の貯蔵タンクが必要である。However, in a refining facility, a storage facility or a handling facility for volatile petroleum compounds, a large amount of polluted air is irregularly and sporadically released into the atmosphere during a short time of refueling petroleum. Released. Conventionally, after collecting contaminated air in a fluidized storage tank whose level changes according to the amount of contaminated air collected, the collected contaminated air is supplied to a recovery facility to recover hydrocarbon components and discharge clean air to the atmosphere. I am trying to do it. However, a large storage tank is required to collect contaminated air discharged sporadically at high speed in a short time by using a fluid storage tank.
【００１６】また、揮発性石油化合物の汚染空気は脂肪
族炭化水素が主成分であり、この他芳香族化合物とナフ
テン類等で構成されているが、このうちの炭化水素類が
占める体積比は約２０〜４０％であり、他は空気であ
る。この時、炭化水素成分と空気を吸着分離するには、
吸着剤を連続的に使用して、回収に必要なエネルギ量を
減らす必要がある。即ち、吸着分離技術では一般的にゼ
オライトまたは活性炭を吸着剤として使用している。こ
れらの吸着剤に対するペンタン類とヘキサン類以上の成
分の吸着特性は低い分圧でも吸着量が大きい凸形吸着等
温線を示すため、吸着塔を加熱して再生するかまたは吸
着塔の圧力を大気圧より低い圧力で維持して炭化水素を
脱着するようにしている。The polluted air of volatile petroleum compounds is mainly composed of aliphatic hydrocarbons, and is also composed of aromatic compounds and naphthenes. Of these, the volume ratio of hydrocarbons is limited. About 20-40%, the other being air. At this time, in order to adsorb and separate the hydrocarbon component and air,
The adsorbent must be used continuously to reduce the amount of energy required for recovery. That is, in the adsorption separation technique, zeolite or activated carbon is generally used as an adsorbent. Since the adsorption characteristics of pentanes and hexane and higher components to these adsorbents show a convex adsorption isotherm with a large amount of adsorption even at a low partial pressure, the adsorption tower is heated to regenerate or the adsorption tower pressure is increased. The system is maintained at a pressure lower than the atmospheric pressure to desorb hydrocarbons.
【００１７】しかし、装置を連続運転する間にこれら炭
化水素成分を可逆的に脱着できないと吸着剤に炭化水素
成分が漸次累積されるため、吸着剤を長時間使用するこ
とができず頻繁に交換する必要がある。したがって、多
大な補修費がかかるという問題があった。However, if these hydrocarbon components cannot be reversibly desorbed during the continuous operation of the apparatus, the hydrocarbon components are gradually accumulated in the adsorbent, so that the adsorbent cannot be used for a long time and is frequently replaced. There is a need to. Therefore, there is a problem that a large repair cost is required.
【００１８】本発明はこのような問題点を解決するため
案出されたもので、その第１目的は、揮発性石油化合物
を貯蔵または取扱う施設において、大気環境汚染と資源
損失を誘発する揮発性石油化合物で汚染された空気をシ
リカゲルと活性炭を充填した捕集塔に供給して処理する
ことにより、炭化水素成分を効率的に除去するととも
に、炭化水素成分濃度０．１５〜１０ｇ／ｍ３以下の排
出許容値を満足する清浄空気を大気に排出できる吸着捕
集装置を提供することにある。SUMMARY OF THE INVENTION The present invention has been made to solve the above problems, and a first object of the present invention is to provide a facility for storing or handling volatile petroleum compounds, which is a volatile substance which causes air pollution and resource loss. The air contaminated with petroleum compounds is supplied to a collection tower filled with silica gel and activated carbon for treatment, whereby hydrocarbon components are efficiently removed and the hydrocarbon component concentration is 0.15 to 10 g / m3 or less. It is an object of the present invention to provide an adsorption trapping device capable of discharging clean air satisfying a discharge allowable value to the atmosphere.
【００１９】本発明の第２目的は、シリカゲルと活性炭
を兼用してシリカゲル層ではペンタン類の一部とヘキサ
ン類以上の炭化水素成分を除去して、活性炭層ではメタ
ン、エタン類、プロパン類、ブタン類とペンタン類の一
部を除去して、減圧と低圧洗浄だけで吸着塔を可逆的に
再生できる吸着塔を提供することにある。A second object of the present invention is to use both silica gel and activated carbon to remove part of pentanes and hexane or more hydrocarbon components in the silica gel layer, and to remove methane, ethanes, propanes, and the like in the activated carbon layer. An object of the present invention is to provide an adsorption tower capable of reversibly regenerating an adsorption tower by removing only a part of butanes and pentanes and performing only reduced pressure and low pressure washing.
【００２０】本発明の第３目的は、炭化水素成分を吸着
した捕集塔を大気圧より低い圧力に減圧して低圧洗浄に
より脱着して、この時得られる揮発性石油化合物と空気
の混合物を２塔式吸着回収装置で処理して炭化水素類を
液状で回収して再活用することにより、大気汚染と資源
損失を防止するようにした揮発性有機化合物の吸着回収
装置を提供することにある。[0020] A third object of the present invention is to desorb the trapping column adsorbing the hydrocarbon component to a pressure lower than the atmospheric pressure and desorb it by low pressure washing, and to obtain a mixture of the volatile petroleum compound and air obtained at this time. It is an object of the present invention to provide a volatile organic compound adsorption / recovery apparatus which prevents air pollution and resource loss by collecting and reusing hydrocarbons in a liquid state by treating the liquid with a two-column adsorption / recovery apparatus. .
【００２１】[0021]
【課題を解決するための手段】前記の目的を達成するた
めに本発明による揮発性石油化合物の吸着式捕集装置と
吸着回収装置は、石油類を生産する精油工場、石油類を
貯蔵して取扱する貯油所あるいは注油所、油類を使用す
る工場の貯蔵施設あるいは取扱施設から排出される汚染
空気を捕集するためのシリカゲルと活性炭が充填された
吸着式捕集塔１機と、この吸着式捕集塔を再生して得ら
れる汚染空気を処理するシリカゲルと活性炭が充填され
た吸着塔機２機と、これらの吸着塔を再生して得られた
高濃度炭化水素を凝縮回収する熱交換機１機と、貯蔵槽
２機と、乳棒式またはドライ真空ポンプ２機とで構成さ
れる。SUMMARY OF THE INVENTION In order to achieve the above object, the present invention provides a volatile petroleum compound adsorption-type collecting apparatus and an adsorption-recovering apparatus, which are used in a refinery for producing petroleum and for storing petroleum. One adsorption-type collection tower filled with silica gel and activated carbon for collecting polluted air discharged from the storage facility or oil-filling station that handles the oil, the storage facility or the handling facility of the factory that uses oils, and the adsorption tower Two adsorption towers filled with silica gel and activated carbon for treating polluted air obtained by regenerating the trapping tower, and a heat exchanger for condensing and recovering high-concentration hydrocarbons obtained by regenerating these adsorption towers It consists of one machine, two storage tanks, and two pestle or dry vacuum pumps.
【００２２】また、吸着式捕集塔の運転は、貯油所また
は精油工場で石油類を貯蔵タンクに充填する時、または
貯蔵タンクで石油類を貯蔵タンクローリに充填する時タ
ンクローリで石油類を貯蔵タンクに充填する時などに所
要の短時間で行われる。The operation of the adsorptive collection tower is performed when the petroleum is filled in the storage tank in a storage tank or an refinery, or when the petroleum is filled in the storage tank in the storage tank. It is carried out in a required short time, for example, when filling into a container.
【００２３】[0023]
【発明の実施の形態】まず、不規則に大気中に排出され
る揮発性石油化合物で汚染された空気を流路３０を通し
て吸着式捕集塔１１に供給する。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS First, air contaminated with a volatile petroleum compound, which is irregularly discharged into the atmosphere, is supplied to an adsorption type collection tower 11 through a flow path 30.
【００２４】この過程で石油化合物の中でも吸着性が大
きいペンタン類の一部、ヘキサン類、ヘプタン類以上の
炭化水素はシリカゲル層で吸着除去して、吸着性が低い
メタン、エタン、プロパン、ブタン類、ペンタン類の一
部は活性炭層で吸着除去して排出許容値である０．１５
〜１０ｇ／ｍ３を満足する清浄空気だけを流路３２と弁
３１を通して外部へ排出する。In this process, among the petroleum compounds, some of the pentanes, which are highly adsorbable, and hydrocarbons more than hexanes and heptane are adsorbed and removed by the silica gel layer, and methane, ethane, propane, butanes, which have low adsorbability, are removed. Some of the pentanes are adsorbed and removed by the activated carbon layer, and the allowable discharge value is 0.15.
Only clean air satisfying を 10 g / m 3 is discharged to the outside through the flow path 32 and the valve 31.
【００２５】揮発性石油化合物を捕集する時、吸着捕集
塔の１１／１２地点に熱伝導帯を設置してこの地点での
温度変化幅が約１５〜５０°Ｃになると捕集工程を中止
して吸着捕集塔１１の脱着を開始する。When collecting volatile petroleum compounds, a heat conduction zone is installed at the 11/12 point of the adsorption collecting tower, and when the temperature change width at this point becomes about 15 to 50 ° C., the collecting step is performed. The operation is stopped and the desorption of the adsorption collection tower 11 is started.
【００２６】吸着式捕集塔１１では、真空ポンプ１６を
稼動させて最終圧力を３０から１００ｍｍＨｇに維持
し、一方貯蔵層１５に入っている炭化水素類を含まない
清浄ガスを流路３３を経由して吸着式捕集塔１１に供給
して炭化水素成分を脱着させる。この時、活性炭層の再
生に使用する低圧洗浄ガスは流路３４を通して供給し
て、シリカゲル層の再生に使用する低圧洗浄ガスは流路
３５を通して供給するようにして炭化水素成分の脱着効
率を高めるようにする。In the adsorption type collection tower 11, the vacuum pump 16 is operated to maintain the final pressure at 30 to 100 mmHg, while the clean gas containing no hydrocarbons contained in the storage layer 15 is passed through the flow path 33. Then, the hydrocarbon component is supplied to the adsorption type collection tower 11 to desorb the hydrocarbon component. At this time, the low-pressure cleaning gas used for regeneration of the activated carbon layer is supplied through the flow path 34, and the low-pressure cleaning gas used for regeneration of the silica gel layer is supplied through the flow path 35, thereby increasing the desorption efficiency of the hydrocarbon component. To do.
【００２７】また、２塔式吸着回収装置の運転周期は、
縮圧、吸着、減圧、低圧洗浄の４つの過程からなる。縮
圧過程では、吸着式捕集塔１１を再生する時流路３６を
通して得られる高濃度炭化水素類と凝縮用熱交換機１４
上端で流路３７を通して排出される未凝縮ガスとを混合
したガスを流路３８と弁１ａを通して吸着塔１２に供給
して吸着塔１２の圧力を初期の圧力３０〜１００ｍｍＨ
ｇから吸着圧力である８００〜１０００ｍｍＨｇまで昇
圧する。The operation cycle of the two-column adsorption / recovery apparatus is as follows:
It consists of four processes: reduced pressure, adsorption, reduced pressure, and low pressure washing. In the pressure-reducing process, the high-concentration hydrocarbons obtained through the passage 36 and the heat exchanger 14 for condensation
A gas mixed with uncondensed gas discharged through the flow path 37 at the upper end is supplied to the adsorption tower 12 through the flow path 38 and the valve 1a, and the pressure of the adsorption tower 12 is increased to an initial pressure of 30 to 100 mmH.
g to the adsorption pressure of 800 to 1000 mmHg.
【００２８】吸着過程では吸着式捕集塔１１を再生する
時得られた高濃度炭化水素類と凝縮用熱交換機１４ａ上
端で流路３７を通して排出される未凝縮ガスとを混合し
たガスを流路３８と弁１ａを介して吸着塔１２に供給さ
れ、この時、ペンタン類の一部、ヘキサン類、ヘプタン
類以上の炭化水素成分をシリカゲル層で吸着除去して、
吸着性が低いメタン、エタン、プロパン、ブタン類、ペ
ンタン類の一部を活性炭層で吸着除去する。In the adsorption step, a gas obtained by mixing high-concentration hydrocarbons obtained when regenerating the adsorption-type trapping tower 11 and uncondensed gas discharged through the flow path 37 at the upper end of the condensing heat exchanger 14a is passed through the flow path. 38, and supplied to the adsorption tower 12 via the valve 1a. At this time, a part of pentanes, hexanes, and hydrocarbon components such as heptane or more are adsorbed and removed by the silica gel layer,
Part of methane, ethane, propane, butanes and pentanes with low adsorptivity are adsorbed and removed by the activated carbon layer.
【００２９】ここで、炭化水素を含有していない清浄ガ
スは流路３９と弁３ａを通して貯蔵槽１５に送られて吸
着式捕集塔１１の脱着に使用する。Here, the clean gas containing no hydrocarbon is sent to the storage tank 15 through the flow path 39 and the valve 3a, and is used for desorption of the adsorption type collecting tower 11.
【００３０】吸着塔１２で縮圧と吸着が行われる間、吸
着塔１３は減圧と低圧洗浄によって脱着が行われる。減
圧工程では弁２ｂを開放して真空ポンプ１７を作動さ
せ、吸着塔の圧力を１００〜２００ｍｍＨｇまで減圧し
て、シリカゲルと活性炭に吸着された炭化水素成分を脱
着させる。While pressure reduction and adsorption are performed in the adsorption tower 12, the adsorption tower 13 is desorbed by depressurization and low-pressure washing. In the depressurizing step, the valve 2b is opened and the vacuum pump 17 is operated to reduce the pressure of the adsorption tower to 100 to 200 mmHg to desorb the hydrocarbon component adsorbed on the silica gel and the activated carbon.
【００３１】低圧洗浄工程は吸着塔１２で吸着工程を行
う間に弁３ａを経由して排出される清浄ガスの一部を流
路４０と弁４ｂを介して吸着塔１３の活性炭層に供給す
ると共に、一部を流路４１と弁４ｂを介してシリカゲル
層に供給して、吸着塔１３の真空圧力３０〜１００ｍｍ
Ｈｇとし、この分圧差を利用して炭化水素成分の脱着効
率を高めるようにする。In the low pressure washing step, a part of the clean gas discharged through the valve 3a during the adsorption step in the adsorption tower 12 is supplied to the activated carbon layer of the adsorption tower 13 through the flow path 40 and the valve 4b. At the same time, a part is supplied to the silica gel layer through the flow path 41 and the valve 4b, and the vacuum pressure of the adsorption tower 13 is 30 to 100 mm.
Hg, and the desorption efficiency of the hydrocarbon component is increased by utilizing this partial pressure difference.
【００３２】真空ポンプ１７を通して脱着した高濃度炭
化水素成分は清浄ガスと混合されこの混合物は流路４２
を通して凝縮熱交換機１４に供給される。The high-concentration hydrocarbon component desorbed through the vacuum pump 17 is mixed with a clean gas,
To the condensing heat exchanger 14.
【００３３】熱交換機１４では温度５〜２５°Ｃの冷却
水（流路４４から供給される）との熱交換で炭化水素類
を凝縮回収し、凝縮回収された炭化水素類を流路４３を
経由して貯蔵タンクに再循環させる。この凝縮ガスは吸
着式捕集塔１１を脱着して得られる汚染空気と混合して
２塔式吸着回収装置に供給して再利用する。凝縮熱交換
機は温度１２００°Ｃ、圧力１８００ｍｍＨｇで運転す
る。In the heat exchanger 14, hydrocarbons are condensed and recovered by heat exchange with cooling water (supplied from the flow path 44) at a temperature of 5 to 25 ° C., and the condensed and recovered hydrocarbons are passed through the flow path 43. Recirculated via storage tanks. This condensed gas is mixed with contaminated air obtained by desorbing the adsorption-type collection tower 11 and supplied to a two-column adsorption and recovery device for reuse. The condensing heat exchanger operates at a temperature of 1200 ° C. and a pressure of 1800 mmHg.
【００３４】[0034]
【発明の実施の形態】以下、添付図面を参照して本発明
の一実施例について詳細に説明する。図１は揮発性石油
化合物の吸着式捕集装置と吸着回収装置図、図２は揮発
性石油化合物の吸着回収装置の連続運転図、図３は吸着
回収装置で処理した汚染空気、低圧洗浄ガスと清浄空気
の流速を示すグラフ、図４は吸着回収装置で処理した揮
発性石油化合物の汚染空気組成図である。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS An embodiment of the present invention will be described below in detail with reference to the accompanying drawings. Fig. 1 is a diagram of a volatile petroleum compound adsorption type trapping device and adsorption and recovery device, Fig. 2 is a continuous operation diagram of a volatile petroleum compound adsorption and recovery device, and Fig. 3 is contaminated air and low-pressure cleaning gas treated by the adsorption and recovery device. FIG. 4 is a graph showing the composition of contaminated air of volatile petroleum compounds treated by the adsorption and recovery apparatus.
【００３５】図１に示す揮発性石油化合物の吸着式捕集
装置と回収装置を揮発性石油化合物で汚染された空気に
適用して次のような結果を得た。The following results were obtained by applying the volatile petroleum compound adsorption type collector and recovery device shown in FIG. 1 to air contaminated with volatile petroleum compounds.
【００３６】即ち、図３に示すように、シリカゲルと活
性炭を各々０．８５ｋｇと０．４２ｋｇ充填した体積２
１００ｃｍ３の吸着塔２機と凝縮熱交換機とで構成され
た吸着回収装置を利用して揮発性石油化合物の体積比が
１５〜５３％である汚染空気を処理した。That is, as shown in FIG. 3, a volume 2 filled with 0.85 kg and 0.42 kg of silica gel and activated carbon, respectively.
Contaminated air having a volatile petroleum compound volume ratio of 15% to 53% was treated using an adsorption recovery apparatus including two 100 cm3 adsorption towers and a condensation heat exchanger.
【００３７】汚染空気を１１〜１８ＮＩ／分の流速で吸
着回収塔に供給して炭化水素を吸着除去して、ガスクロ
マト分析器（ＦＩＤ：Flame Ionization Detector検出
器）で吸着時に塔出口から排出されるガスを分析した
時、炭化水素が検出されなかった清浄空気だけを流速４
〜１２ＮＩ／分で排出できた。Contaminated air is supplied to the adsorption recovery tower at a flow rate of 11 to 18 NI / min to adsorb and remove hydrocarbons, and is discharged from the tower outlet during adsorption by a gas chromatography analyzer (FID: Flame Ionization Detector). The flow rate of only clean air from which no hydrocarbons were detected when analyzing
It could be discharged at ~ 12 NI / min.
【００３８】吸着回収塔では吸着塔圧力を３０〜１００
ｍｍＨｇで維持しながら吸着過程で汚染空気が供給され
てくる方向と反対方向に約１．２〜４ＮＩ／分で低圧洗
浄空気を供給して脱着した。In the adsorption recovery tower, the pressure of the adsorption tower is 30 to 100
While maintaining the pressure at mmHg, low-pressure washing air was supplied at about 1.2 to 4 NI / min in a direction opposite to the direction in which the contaminated air was supplied during the adsorption process, and desorption was performed.
【００３９】図４は総１７４０周期の連続運転の間に処
理された揮発性有機化合物の汚染空気の流速、回収装置
から排出された清浄空気の流速と吸着塔の脱着過程で供
給された低圧洗浄ガス流速の変化を示す。FIG. 4 shows the flow rate of the contaminated air of the volatile organic compounds treated during the continuous operation for a total of 1740 cycles, the flow rate of the clean air discharged from the recovery unit, and the low pressure washing supplied in the desorption process of the adsorption tower. 3 shows a change in gas flow rate.
【００４０】図５は揮発性石油化合物の吸着回収装置の
性能を示す。図５に示すように、代表的な結果としては
炭化水素類の体積比が約２１〜２７％である汚染空気を
平均流速１１ＮＩ／分で図１の回収装置に供給した時、
約８週期運転、即ち、２時間の間に凝縮回収された炭化
水素類は約１１５０ｍｌであった。FIG. 5 shows the performance of the adsorption and recovery apparatus for volatile petroleum compounds. As shown in FIG. 5, a typical result is that when the contaminated air having a hydrocarbon volume ratio of about 21 to 27% is supplied to the recovery apparatus of FIG. 1 at an average flow rate of 11 NI / min,
About 8 weeks of operation, ie, about 1150 ml of hydrocarbons condensed and recovered during 2 hours.
【００４１】また、吸着回収装置の連続運転の間２００
番目の周期と１６７３番目の周期でシリカゲル層と活性
炭層の各層で測定された温度変化を図６に各々示す。In addition, during continuous operation of the adsorption and recovery apparatus, 200
FIG. 6 shows temperature changes measured in each of the silica gel layer and the activated carbon layer in the second cycle and the 1673-th cycle.
【００４２】吸着回収装置の連続運転時は吸着期間は４
〜８分で、活性炭層の５／６地点の温度変化幅は１５〜
５０°Ｃである時に該当する。活性炭層の機能はブタン
類以下の成分とペンタン類の一部成分を除去すること
で、これら炭化水素が吸着されることによって吸着塔の
７／１２、９／１２、１１／１２の地点での温度が順次
上がる。１１／１２地点での温度が急激に上昇する理由
はブタン類以下の炭化水素成分が吸着されるのためで、
その地点で脱着と吸着過程間の温度変化幅が１５〜５０
°Ｃのとき、すぐ脱着過程に進行するように運転方法が
調節されている。During continuous operation of the adsorption and recovery apparatus, the adsorption period is 4
Within 8 minutes, the temperature change range at 5/6 point of the activated carbon layer is 15-
This applies when the temperature is 50 ° C. The function of the activated carbon layer is to remove components below butanes and some components of pentanes, so that these hydrocarbons are adsorbed, and as a result, 7/12, 9/12, and 11/12 of the adsorption tower are adsorbed. Temperature rises sequentially. The reason why the temperature at 11/12 point rises sharply is that hydrocarbon components below butanes are adsorbed.
At that point, the temperature change between desorption and adsorption process is 15-50
At the time of ° C, the operation method is adjusted so as to proceed to the desorption process immediately.
【００４３】[0043]
【発明の効果】以上のようによる揮発性石油化合物の吸
着式捕集装置と回収装置及びその運転方法によると、揮
発性石油化合物の貯蔵施設または取扱施設から排出され
る汚染空気で炭化水素類は除去して清浄空気だけを排出
することにより大気環境汚染が防止できる。As described above, according to the volatile petroleum compound adsorption type trapping apparatus and recovery apparatus and the operation method thereof, hydrocarbons are contained in polluted air discharged from a volatile petroleum compound storage facility or handling facility. By removing and discharging only clean air, air pollution can be prevented.
【００４４】また、散発的で不規則的に排出される汚染
空気を捕集するための吸着式捕集塔を利用することによ
り従来の捕集用貯蔵槽を大幅縮小させることができ、シ
リカゲルと活性炭を充填した吸着塔を使用した結果シリ
カゲル層でペンタン類一部とヘキサン類以上の炭化水素
成分を除去して活性炭層でペンタン類一部とブタン類以
下の炭化水素成分を除去して加熱再生方法を使用せず減
圧と低圧洗浄方法だけで吸着塔を再生できる効果があ
る。In addition, by using an adsorption type collection tower for collecting sporadic and irregularly discharged contaminated air, the conventional storage tank for collection can be significantly reduced, and silica gel and silica gel can be used. As a result of using an adsorption tower filled with activated carbon, the silica gel layer removes some pentanes and hydrocarbon components above hexanes, and the activated carbon layer removes some pentanes and hydrocarbon components below butanes to heat and regenerate. There is an effect that the adsorption tower can be regenerated only by reduced pressure and low pressure washing methods without using any method.
【００４５】また、精油工場、貯油所、注油所で揮発性
石油化合物を取扱する時大気に排出される炭化水素類を
凝縮回収することにより資源損失と大気環境汚染が防止
できる装置を提供する。Further, there is provided an apparatus capable of preventing resource loss and air environment pollution by condensing and recovering hydrocarbons discharged to the atmosphere when volatile petroleum compounds are handled at an refinery, a storage station, and an oil filling station.
【図１】 揮発性石油化合物の吸着式捕集装置と吸着回
収装置図である。FIG. 1 is a diagram of a volatile petroleum compound adsorption type adsorption device and an adsorption recovery device.
【図２】 揮発性石油化合物の吸着回収装置の連続運転
図である。FIG. 2 is a continuous operation diagram of the adsorption and recovery device for volatile petroleum compounds.
【図３】 吸着回収装置で処理された汚染空気、低圧洗
浄ガスと清浄空気の流速図である。FIG. 3 is a flow chart of contaminated air, low-pressure cleaning gas, and clean air processed by the adsorption and recovery device.
【図４】 揮発性石油化合物の吸着回収装置で処理され
た揮発性石油化合物の汚染空気組成図である。FIG. 4 is a contaminated air composition diagram of a volatile petroleum compound treated by the volatile petroleum compound adsorption and recovery apparatus.
【図５】 揮発性石油化合物の吸着回収装置の性能を示
す図である。FIG. 5 is a diagram showing the performance of a volatile petroleum compound adsorption and recovery apparatus.
【図６】 連続運転で吸着塔の温度変化を示す図であ
る。FIG. 6 is a diagram showing a temperature change of an adsorption tower in a continuous operation.
１ａ、２ｂ、３ａ、４ｂ、４ｄ 弁 １１ 吸着式捕集塔 １２ 吸着塔 １４ 凝縮用熱交換機 １５ 貯蔵槽 １６、１７ 真空ポンプ ３０、３２、３３、３４、３５、３６、３７、３８、３
９、４０、４１ 流路 ３１ 弁1a, 2b, 3a, 4b, 4d Valve 11 Adsorption type collection tower 12 Adsorption tower 14 Condensing heat exchanger 15 Storage tank 16, 17 Vacuum pump 30, 32, 33, 34, 35, 36, 37, 38, 3
9, 40, 41 Flow path 31 valve
───────────────────────────────────────────────────── フロントページの続き (72)発明者 チョ サンチュル 大韓民国デジョン市セオ区ドンサン洞908 −３ユンチョロンアパート1505 (72)発明者 キム ヨンナム 大韓民国デジョン市ヨーサン区ヨン洞99 ハンビットアパート116−305 (72)発明者 ハン サンスプ 大韓民国ソウル市ガムチェオン区シフン１ 洞109−１ ムジガエアパート２−318 (72)発明者 パク ヨンギ 大韓民国デジョン市セオ区ドンサン洞ハン シンドンジアパート104−1205 (72)発明者 ヤン ジョンイル 大韓民国ソウル市カンナム区イルウォン洞 625−５ (72)発明者 ブン ヒータエ 大韓民国ガンジュ市ブク区センヨン洞180 Ｆターム(参考） 4D002 AA34 AA40 AC07 BA02 BA04 BA13 DA41 DA46 EA02 EA03 EA04 EA08 GA01 GA03 GB04 4D012 BA01 BA03 CA10 CA12 CB15 CB16 CD07 CD10 CE01 CE03 CF03 CG01 CH06 CJ02 ──────────────────────────────────────────────────続 き Continuing on the front page (72) Inventor Cho Sangchul, 908-3, Dongsan-dong Apartment, Seo-gu, Dejong-City, Republic of Korea 150-3 Yuncho-lon Apartment 1505 (72) Inventor Kim Yong-nam, 116-305 (72) ) Inventor Han Sang-sup, 102-1 Mujigae Apartment 2-318, Si-Hung 1-dong, Gamcheon-gu, Seoul, South Korea (72) Inventor Park Yong-Gi 104-1205 Han Sin-dong Dong-dong, Seo-gu, Seo-gu, Dejong City, Republic of Korea (72) Inventor Yang Jong-il 625-5 Ilwon-dong, Gangnam-gu, Seoul, Korea (72) Inventor Bun-Hitae F-term (reference) 4D002 AA34 AA40 AC07 BA02 BA04 BA13 DA41 DA46 EA02 EA08 G A01 GA03 GB04 4D012 BA01 BA03 CA10 CA12 CB15 CB16 CD07 CD10 CE01 CE03 CF03 CG01 CH06 CJ02
Claims (2)
される炭化水素類の汚染空気を吸着式捕集塔に供給処理
して清浄空気を大気中に排出し、 前記吸着式捕集塔の圧力を３０〜１００ｍｍＨｇに維持
して、貯蔵槽にある清浄ガスを当該吸着式捕集塔に供給
して前記汚染空気の脱着を行い、 この脱着したガスを凝縮用熱交換機の上段から排出され
るガスとを混合して吸着塔に供給して、当該吸着塔にて
炭化水素類を除去して得られた清浄ガスを前記貯蔵槽に
送出し、 前記吸着塔の圧力を３０〜１００ｍｍＨｇで維持してこ
の吸着塔に清浄ガスを供給処理して得られる混合物を真
空ポンプを経て凝縮用熱交換機の下段に送出し、 前記凝縮用熱交換機で、当該混合物を冷却水と熱交換し
て炭化水素類を凝縮回収し、この凝縮回収した炭化水素
類を貯蔵タンクに再循環させるようにした一連の装置で
構成したことを特徴とする揮発性石油化合物の吸着式捕
集装置及び吸着回収装置。1. A process for supplying contaminated air of hydrocarbons discharged from a facility handling volatile petroleum compounds to an adsorption type trap tower to discharge clean air into the atmosphere, and a pressure of the adsorption type trap tower. Is maintained at 30 to 100 mmHg, and the clean gas in the storage tank is supplied to the adsorption-type trapping tower to desorb the contaminated air. The desorbed gas is discharged from the upper stage of the condensing heat exchanger. And the mixture is supplied to an adsorption tower, and a clean gas obtained by removing hydrocarbons in the adsorption tower is sent to the storage tank. The pressure of the adsorption tower is maintained at 30 to 100 mmHg. The mixture obtained by supplying the clean gas to the adsorption tower is sent to the lower stage of a condensing heat exchanger via a vacuum pump, and the condensing heat exchanger exchanges the mixture with cooling water to convert hydrocarbons. Condensed and recovered hydrocarbons Adsorption type collecting device and the suction recovery device of volatile oil compound characterized by being configured of a series of apparatus that is recycled to the storage tank.
空気に含有された脂肪族炭化水素中のペンタン類の一部
とヘキサン類以上を除去するためシリカゲルを充填した
第１の吸着部と、ペンタン類の一部とブタン類以下を除
去するため活性炭を充填した第２の吸着部とを設置して
汚染空気の炭化水素類を除去することを特徴とする請求
項１に記載の揮発性石油化合物回収装置。2. A first adsorption section filled with silica gel for removing a part of pentanes and hexanes or more in aliphatic hydrocarbons contained in air contaminated with volatile petroleum compounds, said adsorption tower having: The volatile matter according to claim 1, wherein a second adsorber filled with activated carbon for removing a part of pentanes and butanes or less is installed to remove hydrocarbons in polluted air. Petroleum compound recovery equipment.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| KR98-14769 | 1998-04-24 | ||
| KR1019980014769A KR100266479B1 (en) | 1998-04-24 | 1998-04-24 | Adsorptive collection and recovery of volatile petroleum compounds |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JP2000117048A true JP2000117048A (en) | 2000-04-25 |
Family
ID=19536681
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP10208572A Pending JP2000117048A (en) | 1998-04-24 | 1998-07-09 | Adsorptive capturing device and adsorptive recovering device of volatile petroleum compound |
Country Status (2)
| Country | Link |
|---|---|
| JP (1) | JP2000117048A (en) |
| KR (1) | KR100266479B1 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100374008B1 (en) * | 2000-07-31 | 2003-03-03 | 박경렬 | A method for regeneration and separate recovery of waste water, waste absorbent, waste absorbent oil and waste organic solvent etc. which have been involved odor and VOCs. |
| KR100375079B1 (en) * | 2000-10-17 | 2003-03-07 | 안창덕 | Method for recovery of volatile organic compounds by adsorption-condensation and apparatus therefor |
| CN107413168A (en) * | 2017-05-19 | 2017-12-01 | 海湾环境科技（北京）股份有限公司 | Gas recovery system for oil and its control method |
| CN112843984A (en) * | 2021-01-13 | 2021-05-28 | 东莞博联核技术有限公司 | Oil refining waste gas recovery device and method based on mixed gas hydrate |
| CN115141648A (en) * | 2022-06-29 | 2022-10-04 | 上海冠卓企业发展有限公司 | Oil gas recovery system and method |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100759529B1 (en) * | 2006-02-23 | 2007-09-18 | 이경호 | VOC recovering system by using nitrogen gas |
| KR20230064356A (en) | 2021-11-03 | 2023-05-10 | 한화솔루션 주식회사 | Unreacted monomer recovery method and recovery device |
| KR102552725B1 (en) * | 2022-10-31 | 2023-07-06 | 주식회사 빈텍코리아 | THC Treatment Process Controlling System of Petro-chemicals Solid Storage Facilities Capable of IoT based Smart Management Using Sensor network |
-
1998
- 1998-04-24 KR KR1019980014769A patent/KR100266479B1/en not_active IP Right Cessation
- 1998-07-09 JP JP10208572A patent/JP2000117048A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100374008B1 (en) * | 2000-07-31 | 2003-03-03 | 박경렬 | A method for regeneration and separate recovery of waste water, waste absorbent, waste absorbent oil and waste organic solvent etc. which have been involved odor and VOCs. |
| KR100375079B1 (en) * | 2000-10-17 | 2003-03-07 | 안창덕 | Method for recovery of volatile organic compounds by adsorption-condensation and apparatus therefor |
| CN107413168A (en) * | 2017-05-19 | 2017-12-01 | 海湾环境科技（北京）股份有限公司 | Gas recovery system for oil and its control method |
| CN112843984A (en) * | 2021-01-13 | 2021-05-28 | 东莞博联核技术有限公司 | Oil refining waste gas recovery device and method based on mixed gas hydrate |
| CN115141648A (en) * | 2022-06-29 | 2022-10-04 | 上海冠卓企业发展有限公司 | Oil gas recovery system and method |
Also Published As
| Publication number | Publication date |
|---|---|
| KR100266479B1 (en) | 2000-09-15 |
| KR19990081068A (en) | 1999-11-15 |
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