TWI327164B - - Google Patents
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- TWI327164B TWI327164B TW095134421A TW95134421A TWI327164B TW I327164 B TWI327164 B TW I327164B TW 095134421 A TW095134421 A TW 095134421A TW 95134421 A TW95134421 A TW 95134421A TW I327164 B TWI327164 B TW I327164B
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- adsorption
- gasoline
- gasoline vapor
- desorption
- gas
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
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- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/38—Removing components of undefined structure
- B01D53/44—Organic components
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
- C10G5/02—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas with solid adsorbents
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
- C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Environmental & Geological Engineering (AREA)
- Treating Waste Gases (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Separation Of Gases By Adsorption (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Loading And Unloading Of Fuel Tanks Or Ships (AREA)
Description
1327164 九、發明說明: 【發明所屬之技術領域】 本發明係有關於大氣釋放氣體中所含之氣體狀碳氮 的處理、回收裝置及其方法,尤其係有關於在加油站等之供 油設施等,用以處理汽油等的富有揮發性之可燃性的汽油蒸 氣之裝置及方法。 … 【先前技術】 在以往之利用吸附解吸劑的氣體狀碳氫之除去方 法,利用送風器或本身壓力,由排氣送氣管將由排氣產生源 所產生的氣體(含有約40vol%之汽油蒸氣的排氣)向吸附塔 送氣,並將結束吸附步驟之已處理的排氣,由吸附塔(在切 換為解吸步驟後為解吸塔)之頂部經由排出管,作為含有低 於lvol%之汽油蒸氣的空氣(清淨之氣體)向大氣排出。 在此情況,吸附塔雖然一面交互地切換該吸附步驟和 後述之解吸步驟,一面進行運轉,但是將該切換時間設為約 5 分鐘(Switching Time) » 另一方面,藉由向吸附步驟結束後之吸附塔,經由沖 洗用氣體用送氣管將沖洗用氣體送氣,並以真空泵吸入而進 行解吸。作為沖洗用氣體,使用在吸附運轉時由吸附塔之頂 部所排出的清淨氣體之一部分,真空泵在約25Torr運轉。 解吸後之含有汽油蒸氣的沖洗用排氣,經由送氣管向 汽油回收器送氣’並經由分配管和液體汽油接觸,而作為液 體(汽油吸收液),回收沖洗用排氣中的汽油蒸氣β 在來自汽油回收器之排氣中,因為殘留微量的汽油蒸 2118-8326-PF 5 1327164 所以經由回送管再回到排氣管,和來自#氣產生源之排 孔起進打吸附處理,並為了冷卻吸附塔内之吸附劑層,而 使冷卻水在内管循環。 藉由如此地構成,可將汽油蒸氣大致作為全量液體汽 油回收,由吸附塔所排出之汽油蒸氣濃度报低,可變成不會 引起大氣污染的水準(例如,參照專利文獻〇。 [專利文獻1]特許第2766793號公報(第3〜6頁, 圖) 【發明内容】 【發明要解決之課題】 在專利文獻1之由真空果對汽油蒸氣進行解吸的回收 方法,泵之動能變成極大,而不切實際。 又,因為以對大量之排齑;隹彡-人曰 徘孔進仃全置吸附處理,需要使 吸附塔變大,或縮短吸附和解 鮮及之切換時間(Switching1327164 IX. Description of the Invention: [Technical Field] The present invention relates to a treatment and recovery apparatus for gas-like carbon and nitrogen contained in an atmosphere-releasing gas, and a method thereof, and more particularly to an oil supply facility at a gas station or the like And an apparatus and method for treating volatile flammable gasoline vapor such as gasoline. [Prior Art] In the conventional method for removing gaseous hydrocarbons using an adsorption desorbent, the gas generated by the exhaust gas generation source (containing about 40 vol% of gasoline vapor) is supplied from the exhaust gas supply pipe by the air blower or its own pressure. Exhaust gas) is supplied to the adsorption tower, and the treated exhaust gas at the end of the adsorption step is passed through the discharge pipe from the top of the adsorption tower (being the desorption step after the desorption step) as a gasoline vapor containing less than 1 vol%. The air (clean gas) is discharged to the atmosphere. In this case, the adsorption tower is operated while switching the adsorption step and the desorption step described later alternately, but the switching time is set to about 5 minutes (Switching Time) » On the other hand, after the adsorption step is completed In the adsorption tower, the flushing gas is supplied to the gas through the purge gas supply pipe, and is sucked by the vacuum pump to be desorbed. As the flushing gas, a part of the clean gas discharged from the top of the adsorption tower during the adsorption operation was used, and the vacuum pump was operated at about 25 Torr. The degassing rinsing exhaust gas containing gasoline vapor is supplied to the gasoline recovery device via the air supply pipe and is contacted with the liquid gasoline via the distribution pipe, and is used as a liquid (gasoline absorbing liquid) to recover the gasoline vapor β in the rinsing exhaust gas. In the exhaust gas from the gasoline recycler, because the residual trace of gasoline is steamed 2118-8326-PF 5 1327164, it is returned to the exhaust pipe via the return pipe, and the exhaust hole from the gas generating source is subjected to adsorption treatment, and The adsorbent layer in the adsorption tower is cooled, and the cooling water is circulated in the inner tube. With such a configuration, the gasoline vapor can be recovered as a full amount of liquid gasoline, and the concentration of the gasoline vapor discharged from the adsorption tower can be reduced to a level that does not cause atmospheric pollution (for example, refer to the patent document 〇. [Patent Document 1] [Problem to be Solved by the Invention] In the method of recovering gasoline vapor by vacuum fruit in Patent Document 1, the kinetic energy of the pump becomes extremely large, and It is impractical. In addition, because of the large amount of enthalpy; the 隹彡-human pupil is fully absorbed, it is necessary to make the adsorption tower bigger, or shorten the adsorption and thawing and switching time (Switching)
Time) ’但是在使用大的吸附技的声Time) ‘but using the sound of a large adsorption technique
了。的匱況,殘留設置面積之問 題’或吸附劑的費用之問題等。又始 又縮紐切換時間時,有無 法對所吸附之汽油蒸氣充分地進行解 疋订解及,或閥等之壽命變短 等的問題。 此外,在使吸附塔變大, 況,吸附塔之壓力損失變大,處 高效率地處理之問題。 並使用大量之吸附劑的情 理氣體流量變慢,而有無法 又,雖然汽油蒸氣中一定含右处名击以 3有空虱中的水分,但是在 以往之方式’因為和汽油蒸氣一起連 硬·这水;7亦同時吸附,所 以有吸附劑之吸附性能降低的問題。 2118-8326-PF 6 1327164 又,在用於由供油處之地下儲存槽漏出的汽油蒸氣之 回收的情況’在對地下儲存槽供油之時間帶需要處理大量產 生的汽油蒸氣。因而,需要配合尖峰量設計裝置性能,= 將裝置性能作成超出所需。 本發明係為解決上述之課題而開發者,其目的在於提 供一種氣體狀碳氫之處理、回收裝置及其方法,防止吸附劑 因汽油蒸氣中所含之水分的影響而受到毒害,且更小型、便 宜。 _ 【解決課題之手段】 本發明之氣體狀碳氫之處理、回收裝置,係用以處理 在供給汽油時漏出的汽油蒸氣之氣體狀碳氫的處理回收裝 置,其特徵在於包括:除去水分及汽油蒸氣之第一凝結裝 置,除去汽油蒸氣之第二凝結裝置,設置於該第一凝結裝置 之後段的氣體下游側;及汽油蒸氣之吸附解吸裝置,設置於 該第二凝結裝置之後段的氣體下游側。 又,本發明之氣體狀碳氫之處理、回收方法,在用以 •處理在供給汽油時漏出的汽油蒸氣之氣體狀碳氫的處理、回 收裝置,其係包括:除去水分及汽油蒸氣之第—凝結裝置; 除去 >飞油蒸氣之第一凝結裝置’設置於該第—凝結裝置之後 • 段的氣體下游側;及汽油蒸氣之吸附解吸裝置,設置於該第 . 二凝結裝置之後段的氣體下游側,其特徵在於: 該吸附解吸裝置具有至少各一個之吸附塔和解吸 塔,按照高於〇°C的空間、高於一 3(TC之空間、及充填吸附 劑的空間之順序處理汽油蒸氣。 【發明效果】 2118-8326-PF 7 1327164 本發明藉由配设:除去水分及汽油蒸氣之第一凝結裝 置、除去汽油蒸氣之第二凝結裝置、及吸附並除去汽油蒸氣 .之吸附解吸裝置,而可使排氣變成極清淨(汽油濃度低於 ,ivol%)’而且可實現小型且便宜的回收裝置。尤其,即使在 π油蒸氣中含有水分的情況,亦因為不必擔心吸附劑受到水 刀毒α而且在第一凝結裝置或吸附解吸塔之配管内不會結 冰,所以可實現安定的運轉動作。 又,藉由作成產生2個溫度帶,並將水分和汽油之回 •收的功能分離,而可減少水分結;東所引起之能源的浪費,可 實現省能源之汽油蒸氣回收裝置。此外,藉由作成在第一凝 、、裝置和吸附解吸塔進行間接冷卻,在第二凝結裝置進行直 接冷卻,不僅冷凍機之開閉運轉,而且藉由控制冷媒的流 動,而可控制凝結裝置之運轉,可實現省能源之汽油蒸氣回 收裝置。又,因為作成設置第二凝結裝置,高效率地回收汽 油蒸氣後,將汽油蒸氣供給第一吸附解吸塔,所以用極少量 之及附劑可吸附Κ油蒸氣,而可大幅度地減少吸附劑的使用 量。 此外,在汽油吸附動作結束後,藉由花時間實施第一 吸附解吸塔所儲存之汽油的回收操作,而可使第一吸附解吸 塔所附设之解吸相關機器的性能變小,可實現便宜之汽油蒸 ' 氣回收裝置。 【實施方式】 第1實施形態 第1圖係表示本發明之第1實施形態的氣體狀碳氫之 2118-8326-PF 8 丄〜164 處理、回收裝置的流程之整體構造圖。 在第1圖’ 1係儲存汽油 罐車等向汽油儲存槽,供給汽油係在由油 f換含有汽_之空;^=,二 利用二通換向閥3a向大氣排出汽油蒸氣之通路所° 調壓閥’ 5係冷凍機,6係和冷凍機 斤。括的 媒暂彳脑7 /粟機5連接並用以冷卻溫度 户媒;7之熱交換器,7係收容熱交換器6所冷卻之溫 ,媒質的溫度媒質槽,8係由溫度媒質槽7送出已冷卻之溫 -媒質的液體循環泵,9係利用液體循環泵8所送來之溫度 媒質冷卻的第-凝結裝置,1G係制冷;東機5冷卻之第二 凝結裝置’ 11係、利用液體循環& 8所送來之溫度媒質冷卻 的第—吸附解吸塔,12a、12b係已除去由第一吸附解吸塔 11及第二吸附解吸塔16所排出之汽油蒸氣的空氣通過之二 路閥’ 13係將第一吸附解吸塔i丨所吸附之汽油作為汽油蒸 氣由第一吸附解吸塔11取出的吸氣泵,14係將吸氣泵13 所取出之含有汽油蒸氣的空氣加壓壓縮之加壓泵,15係由 利用加壓泵14已加壓壓縮之含有汽油蒸氣的空氣將汽油加 以液化回收的第三凝結裝置,16係由第三凝結裝置15所排 出之含有汽油蒸氣的空氣將汽油加以吸附回收的第二吸附 解吸塔,17a、17b係第一吸附解吸塔11及第二吸附解吸塔 16所包括之流量調整閥,18係使已液化之汽油回到汽油儲 存槽1的汽油配管,19係調整第三凝結裝置15及第二吸附 解吸塔16内之壓力的壓力控制器。該第一凝結裝置9、第 二凝結裝置10、及第一吸附解吸塔11由汽油蒸氣之流向的 上游侧(前段)往下游侧(後段)依次配置,而且在安裝位置上 2118-8326-PF 9 1327164 由下部往上部疊層。 其次’說明第!圖之氣體狀碳氯的處理、回收裝置之 動作。本貫施%態所示之裝置的運轉一|係按㈣附製#、 第—再生製程、及第二再生製程之3個步驟進行。首先^說 明吸附製程…般,三通換向閥33和大氣排出側連接,’並 利用調壓閥4控制汽油健存槽工的壓力,以免汽油儲存槽! 之壓力超過既定之壓力。 在開始供油時,三通換向閥3&切換至回收裝置側,同 時二路閥12a打開。又,三通換向閥3a切換,由油罐車等 經由汽油配管2向汽油儲存槽!開始供油時,由汽油儲存槽 旧出充滿於汽油儲存^的汽油蒸氣。此時之汽油蒸氣的 >飞油濃度在常溫係約30〜40v〇1%。由汽油儲存槽Μ排出之 汽油蒸氣,經由三通換向閥3a,被送至第一凝結裝置9。第 一凝結裝置9藉由利用液體循環系8供給利用冷;東機5已冷 卻之溫度媒質,而被間接地冷卻。—般,第_凝結 : 之内部保持於由〇t至約5。〇,#法节产 、 5C,&油錢之—部分及氣體中 所含的水分凝結,並利用洛、泣八μ怒,* 關用轧液分離Μ未圖示)等分離成氣體 h油洛氣)和液體(汽油)。液體積存於第一凝結裂置9的下 侧’並經由汽油配管18被送至汽油儲存槽卜此外,在第i 圖,雖然作成汽油蒸氣由第—凝結裝置9之下側流通 藉由由第一凝結裝^的上方引人汽油蒸氣,並向下方一流 通’而所液化之汽油或水分利用重力和氣流高效率地向下方 流動,ϋ些液化物之回收變得容易。 …在糸第凝結裝置9之運轉條件之壓力O.IMPa、 冷部/皿度5 C之條件’汽油蒸氣濃度變成約浙。此外,It is. The problem of the residual set area or the cost of the adsorbent. When the switching time is changed again, there is a problem that the adsorbed gasoline vapor is sufficiently solved and the life of the valve or the like is shortened. Further, in the case where the adsorption tower is made large, the pressure loss of the adsorption tower becomes large, and the problem of high-efficiency treatment is caused. And the use of a large amount of adsorbent, the flow of the rational gas is slow, and there is no way, although the gasoline vapor must contain the right side of the name to hit 3 of the water in the air, but in the past way 'because it is hard with gasoline vapor · This water; 7 is also adsorbed at the same time, so there is a problem that the adsorption performance of the adsorbent is lowered. 2118-8326-PF 6 1327164 Further, in the case of recovery of gasoline vapor which is leaked from the underground storage tank of the oil supply station, a large amount of generated gasoline vapor needs to be treated in the time zone for supplying oil to the underground storage tank. Therefore, it is necessary to design the device performance in conjunction with the peak amount, = to make the device performance beyond what is required. The present invention has been made to solve the above problems, and an object of the present invention is to provide a gas-like hydrocarbon treatment and recovery apparatus and a method thereof, which prevent the adsorbent from being poisoned by the influence of moisture contained in gasoline vapor, and are smaller. Cheap. _ [Means for Solving the Problem] The gas-like hydrocarbon treatment and recovery device of the present invention is a treatment and recovery device for treating gaseous hydrocarbons of gasoline vapor leaked during supply of gasoline, characterized in that it includes: removing moisture and a first condensing device for gasoline vapor, a second condensing device for removing gasoline vapor, a gas downstream side disposed at a later stage of the first condensing device; and an adsorption and desorption device for gasoline vapor, a gas disposed at a later stage of the second condensing device Downstream side. Further, the method for treating and recovering gaseous hydrocarbons according to the present invention is a treatment and recovery apparatus for treating gaseous hydrocarbons of gasoline vapor leaking during the supply of gasoline, including: removal of moisture and gasoline vapor - a coagulation device; a first coagulation device that removes > fly oil vapor is disposed on the downstream side of the gas after the first coagulation device; and an adsorption desorption device for the gasoline vapor, which is disposed in the subsequent stage of the second coagulation device The downstream side of the gas is characterized in that: the adsorption desorption device has at least one adsorption tower and a desorption tower, which are processed in a sequence higher than 〇 ° C, higher than a space of 3 (the space of the TC, and the space filled with the adsorbent). [Invention Effect] 2118-8326-PF 7 1327164 The present invention is provided by: a first coagulation device for removing moisture and gasoline vapor, a second coagulation device for removing gasoline vapor, and adsorption and removal of gasoline vapor. The desorption device can make the exhaust gas extremely clean (gasoline concentration is lower than ivol%)' and can realize a small and inexpensive recovery device. Especially, even in π oil In the case where the gas contains moisture, it is also necessary to prevent the adsorbent from being subjected to water knife poisoning α and not to freeze in the piping of the first coagulation device or the adsorption desorption column, so that stable operation can be achieved. Two temperature zones separate the function of water and gasoline back and charge, which can reduce the moisture knot; the energy waste caused by the east can realize the energy-saving gasoline vapor recovery device. In addition, by making the first The coagulation, the device and the adsorption desorption column are indirectly cooled, and the second coagulation device performs direct cooling, which not only opens and closes the refrigerating machine, but also controls the operation of the coagulation device by controlling the flow of the refrigerant, thereby realizing energy-saving gasoline. a vapor recovery device. Further, since the second condensation device is provided to efficiently recover the gasoline vapor, the gasoline vapor is supplied to the first adsorption desorption column, so that the oil vapor can be adsorbed with a very small amount of the auxiliary agent. Reducing the amount of adsorbent used. Further, after the gasoline adsorption operation is completed, the first adsorption desorption tower is stored by taking time to store it. In the recovery operation of the gasoline, the performance of the desorption-related machine attached to the first adsorption-desorption column can be reduced, and an inexpensive gasoline-gas recovery device can be realized. [Embodiment] FIG. 1 is a view showing the present invention. 2118-8326-PF 8 丄 164 of the first embodiment of the present invention, the overall structure of the process of the treatment and recovery device. In the first figure, the gasoline storage tank is supplied to the gasoline storage tank, and the gasoline system is supplied. In the case of the oil f, the air is contained in the air_^; and the second two-way switching valve 3a is used to discharge the gasoline vapor to the atmosphere. The pressure regulating valve '5 series refrigerator, 6 series and the freezing machine. Temporary brain 7 / mill 5 connected to cool the temperature of the household medium; 7 heat exchanger, 7 series contain the temperature of the heat exchanger 6 cooling, medium temperature medium tank, 8 series sent by the temperature medium tank 7 has been cooled The temperature-media liquid circulation pump, the 9th system uses the temperature medium-cooled first-condensation device sent by the liquid circulation pump 8, the 1G system refrigeration, and the east machine 5 cools the second condensation device '11 series, using the liquid circulation &; 8 the temperature medium sent by the cooling - adsorption The desorption column, 12a, 12b is a second-way valve that has removed the gasoline vapor discharged from the first adsorption desorption column 11 and the second adsorption desorption column 16 through the second-way valve '13 system to adsorb the gasoline adsorbed by the first adsorption desorption column i As a getter pump for taking out the gasoline vapor from the first adsorption/desorption column 11, 14 is a pressurizing pump that pressurizes and compresses the air containing gasoline vapor taken out by the getter pump 13, and 15 is pressurized by the pressurizing pump 14. a third condensing device for liquefying and recovering gasoline by compressing the gas containing gasoline vapor, and a second adsorbing and desorbing tower for adsorbing and recovering the gasoline by the air containing gasoline vapor discharged from the third condensing device 15, 17a, 17b The flow regulating valve included in the first adsorption desorption column 11 and the second adsorption desorption column 16 is 18 for returning the liquefied gasoline to the gasoline piping of the gasoline storage tank 1, and the 19 series adjusting the third condensation device 15 and the second adsorption desorption A pressure controller for the pressure within the tower 16. The first condensing device 9, the second condensing device 10, and the first adsorption/desorption column 11 are arranged in order from the upstream side (front stage) of the flow of gasoline vapor to the downstream side (rear stage), and at the mounting position 2118-8326-PF 9 1327164 Laminated from the lower part to the upper part. Second, the description! The operation of the treatment and recovery device for gaseous carbon and chlorine in the figure. The operation of the device shown in the % state is performed in three steps of (4) attached #, the first-regeneration process, and the second regeneration process. First, the adsorption process is similar. The three-way reversing valve 33 is connected to the atmospheric discharge side, and the pressure regulating valve 4 is used to control the pressure of the gasoline storage tank to avoid the gasoline storage tank! The pressure exceeds the established pressure. When the oil supply is started, the three-way switching valve 3& switches to the recovery device side, and the two-way valve 12a is opened. Further, the three-way switching valve 3a is switched, and the gasoline tank or the like is transported to the gasoline storage tank via the gasoline pipe 2! When the oil supply starts, the gasoline vapor is stored in the gasoline storage tank. At this time, the > flying oil concentration of the gasoline vapor is about 30 to 40 v 〇 1% at a normal temperature. The gasoline vapor discharged from the gasoline storage tank is sent to the first condensing device 9 via the three-way switching valve 3a. The first condensing device 9 is indirectly cooled by the use of the liquid circulation system 8 to supply the temperature medium which has been cooled by the cold machine; In general, the first _ condensate: the internal is maintained from 〇t to about 5. 〇, #法制产, 5C, & oil money - part and the moisture contained in the gas condense, and use Luo, weeping eight μ anger, * use the rolling liquid separation Μ not shown) to separate into a gas h Oil gas) and liquid (gasoline). The liquid volume is stored on the lower side of the first condensation crack 9 and is sent to the gasoline storage tank via the gasoline piping 18. Further, in the first drawing, although the gasoline vapor is produced by the lower side of the first condensation device 9, The upper part of the condensing unit introduces gasoline vapor and flows downwards. The liquefied gasoline or water flows efficiently downward by gravity and airflow, and the recovery of these liquefied materials becomes easy. ...the pressure of the operating conditions of the first coagulation device 9 is O.IMPa, the cold portion/the degree of the dish 5 C. The gasoline vapor concentration becomes about Zhe. In addition,
2118-8326-PF 10 1327164 調查汽油蒸氣飽和濃度時,在壓力0.1 MPa、溫度51:,飽和 汽油蒸氣濃度係約20vol%,在此條件,汽油蒸氣濃度理論 上不會低於20vol%。又,藉由降低溫度,可降低在第—凝 . 結裝置9之出口的汽油蒸氣濃度《可是,將設定溫度設為冰 點以下時’氣體中所含的水在第一凝結裝置9結冰,因為增 • 加在第一凝結裝置9内部之壓力損失,所以第一凝結裝置9 之設定溫度設為由〇°C至5°C較佳。 接著’將在第一凝結裝置9無法處理之約20vol%的汽 _油蒸氣供給第二凝結裝置1〇。第二凝結裝置10藉由將冷凍 機5已冷卻之冷媒供給第二凝結裝置1〇,而被直接地冷卻。 一般’第一凝結裝置1 〇之内部保持在由—2〇。〇至約—丨〇。〇, 汽油瘵氣之一部分凝結,而分離成氣體(汽油蒸氣)和液體 (汽油)。液體積存於第一凝結裝置9的下側,並經由汽油配 官18被送至汽油儲存槽1 ^此外,雖然第二凝結裝置i 〇之 内部被冷卻至冰點以下,但是因為在第一凝結裝置9除去水 分的大部分,所以在第二凝結裝置1〇結冰之水分極少。又’ 鲁第1圖,雖然作成汽油蒸氣由第一凝結裝置9之下侧流通, 但是和第一凝結裝置9的情況一樣,藉由由第二凝結裝置 10之上方引入汽油蒸氣,並向下方流通,而所液化之汽油 或水分利用重力和氣流南效率地向下方流動,這些液化物之 • 回收變得容易。 而,在係第二凝結装置之運轉條件之壓力 O.IMPa、冷卻溫度一10°C之條件,汽油蒸氣濃度變成約 8vol%。此外,調查汽油蒸氣之飽和濃度時,在壓力〇 1Mpa、 溫度一io°c,飽和汽油蒸氣濃度係約8v〇1%,在此條件,汽 2118-8326-PF 11 1327164 油蒸氣濃度理論上不會低於8vol%。又,藉由降低溫度可 降低在第二凝結裝置10之出口的汽油蒸氣濃度。可是,即 •使冷卻至—3〇艺,汽油蒸氣濃度亦係約5vol%,得知即使冷 .卻至低於-3(TC,汽油蒸氣濃度亦幾乎不降低。因為即使冷 -卻至低於―赃時使用的能量增大,所以無法高效率地利用 •能源。因此,將第二凝結裝置10之設定溫度設為超過_3(rc 較佳。 接著,將在第二凝結裝置10無法處理之約8v〇1%的汽 •油蒸氣送至第一吸附解吸塔11加以處理。在第i圖,表示 —第一吸附解吸塔11作為吸附塔動作的情況。因此,二路閥 12a打開(塗黑),流量調整閥17a處於關閉(空白)之狀態。 作為吸附塔在任意的時間進行吸附處理後,用作解吸塔。在 此情況,二路閥12a在關閉、流量調整閥17a在打開之狀態 使用。 在第一吸附解吸塔11内封入吸附汽油蒸氣之吸附 劑。Ά油蒸氣之吸附劑使用石夕膠。尤其具有孔徑4〜1 〇〇埃之 •石夕膠或合成沸石的單體或這些的混合物係有效。藉由汽油蒸 氣通過該吸附劑中’而將汽油成分加以吸附除去,變成低於 1 vol%之汽油濃度的清淨空氣,並經由二路闊12a向大氣排 • 出。 • 第一吸附解吸塔11和汽油蒸氣之吸附解吸的功能無 關’總是利用液體循環泵8所供給之溫度媒質冷卻至固定溫 度。即’對第一凝結裝置9及第一吸附解吸塔11之冷卻系 統以總是保持係設定溫度的〇〜5 °C之方式進行運轉控制。這 是由於第一吸附解吸塔11所充填的矽膠係藉由來自凸片管 2118-8326-PF 12 ,父換器等之熱交換器(未圖式)的導熱而被冷卻,所以某程 度的冷卻時間係必要而不可或缺,無法應㈣間之運轉動。 又’為了可在短時間冷卻而包括冷卻性能大的冷;東機5,對 设備費用有不良的影響,因為無法提供便宜之汽油回收裝 f此外’藉由降低第一吸附解吸塔i (内部的溫度,而提 ^及付容量’可減少㈣的使用量。可是,使第—吸附解吸 塔11之内部溫度變成冰點以下時,因為在第一吸附解吸塔 η内水結冰’而冰逐漸儲存於♦膠等之吸附劑,所以發生 吸附劑的汽油吸附性能降柄 叹ιπ r王此降低之問題,因此,將第一吸附解吸 塔Π之内部溫度設為冰點以上較佳。 由以上之事項,藉由具有第一凝結裝置9及第一吸附 解吸塔11之冷卻系統和第二凝結裝置1〇的冷卻系統之溫度 帶相異的2種冷卻系統,而可高效率地回收汽油。 第吸附解吸塔11吸附大氣壓的氣體,雖然第一吸附 解吸塔11之外部構造的形狀不受限制,但是因為在解吸時 吸附塔内部之壓力變成約〇 02MPa,所以採用圓筒構造。藉 由採用圓筒構造,可使作用於壁面之壓力變成均勻,即使吸 附塔内之壓力變成約0.02MPa,亦可實現安全性高,即不會 發生形狀變形等之吸附解吸塔丨丨。又,關於第一吸附解吸 % 11之内部構造’考慮對石夕膠或合成沸石的導熱,配置凸 片管熱父換器(以Is散熱片使溫度媒質流向導熱管),將石夕膠 或合成沸石塞入鋁散熱片之間,同時在上下設置矽膠流出防 止網’防止矽膠向配管流出’而且改善氣體的流動。在此情 況,為了使矽膠對汽油蒸氣之吸附變成均勻,亦可設置以沖 孔金屬板等所製作的整流板,使汽油蒸氣均勻地流向第一吸 2118-8326-PF 13 1327164 附解吸塔11。凸片管熱 谀益之敢熱片的方向設定成和汽 ”、'氣之流向平行較佳,以免發生汽油蒸氣流動時的壓損。 .又’為了高效率地冷卻充填於外壁附近㈣膠,需要作成在 .凸片管熱交換器和外壁之間不會產生間隙。 ' 纟此情況’藉由對具有f曲之侧設置用以接觸彎曲部 分的格子狀或板狀之金屬(導熱特性優異之K銅最適 ,合)’對無彎曲之側延長凸片㈣交換器的散熱片本身之長 度,而對消除外壁和凸片管熱交換器之間的間隙有效。又, •為了消除外壁和凸片管熱交換器之間的間隙,亦可作成*** 金屬棒或具有散熱片之管等。又,在使溫度媒質流向凸片管 熱交換器之導熱管的情況,在進人導熱管之前將溫度媒質流 動的配管分支,並將凸片管熱交換器分成多個組,使溫度媒 質並列地流動較佳。因而,可減少溫度媒質流動之配管的壓 知,並可降低將溫度媒質供給第一吸附解吸塔丨〗之液體循 壞果8的容量。 此外,在本例,因為汽油蒸氣由下向上流動,所以配 參置成凸片管熱交換器和下部之矽膠流出防止網接觸較佳。因 而’在矽膠流出防止網和凸片管熱交換器之間可消除空間, 即僅充填矽膠的空間’在吸附時可充分地冷卻矽膠。結果, 可防止位於汽油濃度最咼之汽油蒸氣流入之部分的石夕膠之 溫度上昇’而可提供安全之第一吸附解吸塔11β此外,在 汽油蒸氣由上向下流動的情況,當然上部之矽膠流出防止網 和凸片管熱交換器接觸。 在第一吸附解吸塔11之前段未設置第一凝結裝置9 及第二凝結裝置10的情況,高濃度之汽油蒸氣流入第一吸 2118-8326-PF 14 1327164 附解吸塔11,而且吸附劑吸附汽油蒸氣中所含的水分,而 汽油蒸氣之吸附性能降低,需要量超出需要的吸附劑。又, 在將第一吸附解吸塔11之溫度降至冰點以下的情況,水分 " 結冰於吸附劑表面,可能發生充滿氣體等之大故障。 ' 本實施形態,在第一吸附解吸塔11之前段設置第一凝 • 結裝置9及第二凝結裝置10,因為和汽油蒸氣一起連水分 亦除去’所以可預防在第一吸附解吸塔11之水分的影響。 又’因為可大幅度降低在第一吸附解吸塔11處理之汽油 _ 量,所以可使第一吸附解吸塔11變小,而可便宜地製作。 又,在本實施形態,因為可用第一凝結裝置9將由汽油儲存 槽1所排出之高濃度(40vol%)的汽油降低至20vol%為止, 可用第二凝結裝置1 〇降低至8vol。/◦為止,所以在第一吸附 解吸塔11所處理的汽油量可降低至總吸入量之 20 /〇(-8%/40%)。即’藉由在第一吸附解吸塔1丨之前段設置 第一凝結裝置及第二凝結裝置1 〇,而可將第一吸附解吸塔 11之容積設為約1/5。 • 其次,說明第二凝結裝置10之冷卻溫度對第一吸附 解吸塔11的矽膠充填量之影響。第2圖係表示第二凝結裝 置10内。卩之冷卻溫度和在第一吸附解吸塔11之出口使汽油 蒸氣濃度變成lvol%以下的情況所需之膠充填量的關係。此 外,Μ在第二凝結裝置10之冷卻溫度為5t:的情況所需之 膠充填量為基準,表示矽膠減少量。如此,藉由降低第二凝2118-8326-PF 10 1327164 When investigating the saturated concentration of gasoline vapor, the saturated gasoline vapor concentration is about 20 vol% at a pressure of 0.1 MPa and a temperature of 51:. Under this condition, the gasoline vapor concentration is theoretically not lower than 20 vol%. Further, by lowering the temperature, the concentration of the gasoline vapor at the outlet of the first condensation device 9 can be lowered. However, when the set temperature is set below the freezing point, the water contained in the gas freezes in the first coagulation device 9, Since the pressure loss added to the inside of the first condensing device 9 is increased, the set temperature of the first condensing device 9 is preferably set to 〇 ° C to 5 ° C. Then, about 20 vol% of steam-oil vapor which cannot be processed by the first coagulation device 9 is supplied to the second coagulation device 1A. The second condensing device 10 is directly cooled by supplying the refrigerant cooled by the refrigerator 5 to the second condensing device 1 。. Generally, the inside of the first condensing device 1 is maintained at -2 〇. 〇到约—丨〇. 〇, one part of the gasoline helium is condensed and separated into gas (gasoline vapor) and liquid (gasoline). The liquid volume is stored on the lower side of the first condensing device 9, and is sent to the gasoline storage tank 1 via the gasoline dispenser 18. In addition, although the inside of the second condensing device i is cooled below the freezing point, because in the first condensing device 9 Most of the moisture is removed, so there is very little moisture in the second coagulation device 1 icing. Further, in the first drawing, although the gasoline vapor is made to flow from the lower side of the first condensing device 9, as in the case of the first condensing device 9, the gasoline vapor is introduced from above the second condensing device 10, and is downward. Circulating, and the liquefied gasoline or water flows efficiently downward by gravity and airflow, and the recovery of these liquefied materials becomes easy. On the other hand, the gasoline vapor concentration became about 8 vol% under the conditions of the operating pressure of the second condensing device of O.IMPa and the cooling temperature of 10 °C. In addition, when investigating the saturated concentration of gasoline vapor, the concentration of saturated gasoline vapor is about 8v〇1% at a pressure of 1Mpa and a temperature of io°c. Under this condition, the vapor concentration of steam 2118-8326-PF 11 1327164 is theoretically not Will be less than 8vol%. Further, the concentration of gasoline vapor at the outlet of the second condensing device 10 can be lowered by lowering the temperature. However, if the cooling is to -3, the gasoline vapor concentration is also about 5 vol%. It is known that even if it is cold, it is less than -3 (TC, the gasoline vapor concentration is hardly reduced. Because even if it is cold - it is low. Since the energy used in the 赃 is increased, the energy cannot be used efficiently. Therefore, the set temperature of the second condensing device 10 is set to exceed _3 (rc is preferable. Next, the second condensing device 10 cannot be used. About 8v〇1% of the steam and oil vapor to be treated is sent to the first adsorption/desorption column 11 for treatment. In the figure i, the first adsorption/desorption column 11 is operated as the adsorption column. Therefore, the two-way valve 12a is opened. (blackened), the flow rate adjusting valve 17a is in a closed state (blank). The adsorption tower is used as a desorption column after being subjected to adsorption treatment at an arbitrary timing. In this case, the two-way valve 12a is closed, and the flow rate adjusting valve 17a is It is used in the open state. The adsorbent for adsorbing gasoline vapor is sealed in the first adsorption desorption column 11. The adsorbent of the sulphur oil vapor is made of Shishijiao, especially having a pore diameter of 4~1 〇〇 之·石石胶 or synthetic zeolite. Monomer or a mixture of these Effectively, the gasoline component is adsorbed and removed by passing the gasoline vapor through the adsorbent, and becomes a clean air of less than 1 vol% of the gasoline concentration, and is discharged to the atmosphere via the second-way wide 12a. • The first adsorption desorption The column 11 is independent of the function of adsorption and desorption of the gasoline vapor. 'Always the temperature medium supplied by the liquid circulation pump 8 is cooled to a fixed temperature. That is, the cooling system for the first condensation device 9 and the first adsorption desorption column 11 is always The operation control is performed in such a manner that the temperature of the set system is maintained at 〇 5 ° C. This is because the silicone resin filled in the first adsorption/desorption column 11 is exchanged by heat from the fin tube 2118-8326-PF 12 , the parent exchanger or the like. The heat transfer of the device (not shown) is cooled, so a certain amount of cooling time is necessary and indispensable, and it is not possible to operate between (4). In addition, it can be cooled in a short time to include cooling performance. Machine 5, has a bad impact on equipment costs, because it can not provide cheap gasoline recovery equipment f In addition, by reducing the first adsorption desorption tower i (internal temperature, and increase the capacity) can be reduced (four) use However, when the internal temperature of the first adsorption desorption column 11 is changed to below the freezing point, since the water is frozen in the first adsorption desorption column η and the ice is gradually stored in the adsorbent such as ♦, the adsorption of the adsorbent occurs. The performance reduction handle sighs the problem of the reduction of the king, therefore, it is preferable to set the internal temperature of the first adsorption desorption tower to be above the freezing point. From the above, by having the first condensation device 9 and the first adsorption desorption tower The cooling system of the cooling system of 11 and the cooling system of the second condensing device 1 are different in temperature, and the gasoline can be efficiently recovered. The first adsorption desorption column 11 adsorbs atmospheric gas, although the first adsorption desorption column 11 The shape of the external structure is not limited, but since the pressure inside the adsorption tower becomes about MPa02 MPa at the time of desorption, a cylindrical structure is employed. By using the cylindrical structure, the pressure acting on the wall surface can be made uniform, and even if the pressure in the adsorption tower becomes about 0.02 MPa, the safety can be high, that is, the adsorption desorption tower such as shape deformation does not occur. Further, regarding the internal structure of the first adsorption desorption % 11 'considering the heat conduction to the Shiqi gum or the synthetic zeolite, the fin tube heat exchanger is arranged (the heat sink is used to make the temperature medium flow guide the heat pipe), and the Shixia gum or The synthetic zeolite is inserted between the aluminum fins, and at the same time, the silicone outflow is provided on the upper and lower sides to prevent the net from 'preventing the silicone to flow out to the pipe' and to improve the flow of the gas. In this case, in order to make the adsorption of the rubber vapor to the gasoline vapor uniform, a rectifying plate made of a punched metal plate or the like may be provided to uniformly flow the gasoline vapor to the first suction 2118-8326-PF 13 1327164 with the desorption column 11 . The direction of the heat pipe of the fin tube is set to be parallel with the flow of steam and gas, so as to avoid the pressure loss when the gasoline vapor flows. . . . 'In order to efficiently cool the filling near the outer wall (4) It is necessary to make a gap between the heat exchanger of the tab tube and the outer wall. ' 纟 情况 ' 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉Excellent K copper is optimal, combined with the length of the heat sink itself for the non-bending side extension tab (4), and is effective for eliminating the gap between the outer wall and the tube heat exchanger. Also, • To eliminate the outer wall The gap between the heat exchanger and the heat exchanger can also be made into a metal rod or a tube having a heat sink, etc. Further, in the case where the temperature medium flows to the heat pipe of the fin tube heat exchanger, the heat pipe is inserted into the heat pipe. The piping for flowing the temperature medium is branched, and the fin tube heat exchanger is divided into a plurality of groups, so that the temperature medium flows in parallel. Therefore, the piping of the temperature medium flowing can be reduced, and the temperature medium can be lowered. for The capacity of the liquid of the first adsorption desorption tower is the following. In addition, in this example, since the gasoline vapor flows from the bottom to the top, the reaction is placed into a fin tube heat exchanger and the lower portion of the silicone outflow prevents the mesh from coming into contact. Preferably, the space can be eliminated between the silicone outflow prevention net and the tab tube heat exchanger, that is, the space filled only with the silicone rubber can sufficiently cool the silicone rubber during adsorption. As a result, the gasoline at the lowest concentration of gasoline can be prevented. The temperature of the Shiqi gum in which the vapor flows in is increased, and the first adsorption desorption column 11β which is safe can be provided. In addition, in the case where the gasoline vapor flows from the top to the bottom, of course, the upper silicone outflow prevention net and the tab tube heat exchanger In the case where the first condensing device 9 and the second condensing device 10 are not disposed in the first stage of the first adsorption/desorption column 11, the high-concentration gasoline vapor flows into the first suction 2118-8326-PF 14 1327164 with the desorption column 11 and is adsorbed. The agent adsorbs the moisture contained in the gasoline vapor, and the adsorption performance of the gasoline vapor is lowered, and the amount of the adsorbent is required to be exceeded. Further, the temperature of the first adsorption desorption column 11 is lowered. In the case of freezing below, the moisture " icing on the surface of the adsorbent may cause a large failure such as full of gas. In the present embodiment, the first condensation device 9 and the second condensation are disposed in the first stage of the first adsorption/desorption column 11 Since the device 10 is removed together with the gasoline vapor, the influence of the moisture in the first adsorption/desorption column 11 can be prevented. Further, since the amount of gasoline processed in the first adsorption/desorption column 11 can be greatly reduced, The first adsorption/desorption column 11 is made smaller, and can be produced inexpensively. Further, in the present embodiment, since the first concentration device 9 can be used to reduce the high concentration (40 vol%) of gasoline discharged from the gasoline storage tank 1 to 20 vol%. Therefore, the second coagulation device 1 can be lowered to 8 vol. / ◦, so the amount of gasoline processed in the first adsorption/desorption column 11 can be reduced to 20 / 〇 (-8% / 40%) of the total intake amount. Namely, the volume of the first adsorption/desorption column 11 can be set to about 1/5 by providing the first condensation device and the second condensation device 1 in the first stage of the first adsorption-desorption column 1 . • Next, the influence of the cooling temperature of the second condensing device 10 on the amount of mash filling of the first adsorption/desorption column 11 will be explained. Fig. 2 shows the inside of the second coagulation device 10. The relationship between the cooling temperature of the crucible and the amount of the gel filling required for the case where the gasoline vapor concentration becomes 1 vol% or less at the outlet of the first adsorption/desorption column 11. Further, Μ is based on the amount of glue required for the case where the cooling temperature of the second condensing device 10 is 5t:, which indicates the amount of sputum reduction. So by lowering the second condensation
裝置10之冷卻溫度,而可使第一吸附解吸塔i 1所充填的 夕膠量變;。可是,得知即使冷卻至一30。(:以下矽膠量亦幾 "咸乂。對各種汽油以實驗調查之結果,得知和汽油蒸氣 2118-8326-PP 15 1327164 之成分無關,即使使冷卻溫度變成一 30°C以下,汽油蒸氣之 飽和濃度亦幾乎不降低的事實,這係由於矽膠降低量之減少 的影響。因此,在考慮投入能量的情況,將第二凝結裝置 10之冷卻溫度設為_30乞以下不是高效率,而將第二凝結 - 裝置10之冷卻溫度設為一30T:以上較佳。 ’ 其次’說明第一吸附解吸塔11之再生製程,即,汽油 . 蒸氣之解吸製程。第一吸附解吸塔π之再生製程包含:第 再生製程’由第一吸附解吸塔11將汽油加以解吸,並經 #由第二凝結裝置15及第二吸附解吸塔16向大氣排出;及第 二再生製程,由第二吸附解吸塔16將汽油解吸,並經由第 一凝結裝置9、第二凝結裝置10及第一吸附解吸塔11向大 氣排出。首先,說明第一再生製程。 在將吸附劑所吸附之汽油解吸的情況,利用吸氣泵13 經由三通換向閥3b由第一吸附解吸塔11吸入氣體並由吸附 劑將汽油加以解吸。此時,二路闊12a關閉。又,第一吸附 解吸塔11内之壓力降至既定的壓力時,打開流量調整閥 • 17a ’固定流量之空氣由大氣流入第一吸附解吸塔U,而使 第一吸附解吸塔u内部之壓力變成大致定值。雖然在吸附 時第一吸附解吸塔在〇.1MPa之大氣壓狀態動作,但是 在解吸時因為利用吸氣泵13降壓至大氣壓以下,所以利用 • 該壓力差在吸附劑所吸附之汽油被濃縮成高濃度的狀態解 及°在此情況’雖然和汽油蒸氣之氣體流量或吸附時之吸附 置亦有關,但是藉由將第一吸附解吸塔U内之壓力控制成 〇·〇2〜〇.〇4MPa ’而可使汽油蒸氣濃度變成2〇~4〇v〇1%。 解吸後之汽油蒸氣經由三通換向閥3c被引至加壓泵 2118-8326-PF 16 1327164 14 °利用加壓泵14將汽油蒸氣加壓至約0.3MPa,並供給第 二凝結裝置15。即,將汽油濃度30vol%、壓力〇 3MPa之 尚濃度、加壓汽油蒸氣供給第三凝結裝置15。藉由利用液 . 體循環泵8供給冷凍機5所冷卻之溫度媒質,間接地冷卻第 • 三凝結裝置15。一般,第三凝結裝置15内部保持在由〇r ’ 至約5。〇 ’汽油蒸氣之一部分及氣體中所含的水分凝結,並 利用氣液分離器(未圖示)等分離成氣體(汽油蒸氣)和液體 (汽油)^液體積存於第三凝結裝置15的下側,並經由汽油 _配管18被送回至汽油儲存槽1。此外,如第1圖所示,藉 由由第二凝結裝置丨5的上方引入汽油蒸氣,並向下方流 通,而所液化之汽油或水分利用重力和氣流高效率地向下方 流動,這些液化物之回收變得容易。 而,在係第三凝結裝置15之運轉條件之壓力 0.3MPa、冷卻溫度5。。之條件,出口的汽油蒸氣濃度變成約 8 vol%。此外,由汽油蒸氣之飽和濃度曲線圖得知,在壓力 0.3MPa、溫度5°C,飽和汽油蒸氣濃度係約8v〇1%,在此條 _件,π油蒸氣濃度理論上不會低於8v〇1%。X,藉由降低溫 度,可降低在第三凝結裝置15之出口的汽油蒸氣濃度。可 是,將設定溫度設為冰點以下時,氣體中所含的水在第三凝 •結裝置15結冰,因為增加在第三凝結裝置15内部之壓力損 '失,所以第二凝結裝置15之設定溫度設為由ot至約rc較 佳。又’在第二凝結裝置15,因為被加壓至約〇3Mpa,所 以採用圓筒構造。藉由採用圓筒構造,可使作用於壁面之壓 力變成均句’即使第三凝結裝置i…壓力變成約 0.3MPa’亦可實現安全性高,即不會發生形狀變形等之第 2118-8326-PF 17 1327164 三凝結裝置15。 接著’將在第三凝結裝置15無法處理之約8vol%的汽 油蒸氣送至第二吸附解吸塔16並處理。在第1圖,表示第 二吸附解吸塔16作為吸附塔動作的情況。因此,二路閥12b 打開(塗黑),流量調整閥17b處於關閉(空白)之狀態。作為 吸附塔在任意的時間進行吸附處理後,用作解吸塔。在此情 況’二路閥12b在關閉、流量調整閥i7b在打開之狀態使用。 在第二吸附解吸塔16亦封入吸附汽油蒸氣之吸附 劑,而和第一吸附解吸塔11 一樣。藉由汽油蒸氣通過該吸 附劑中,而將汽油成分加以吸附除去,變成低於丨v〇1%之汽 油濃度的清淨空氣,並經由二路閥12b向大氣排出。此外, 第一吸附解吸塔16亦和汽油蒸氣之吸附解吸的功能無關, 總是利用液體循環泵8所供給之溫度媒質冷卻至固定溫 度。即,和第一吸附解吸塔U 一樣以總是保持〇~5。〇之方 式進行運轉控制。又,第二吸附解吸塔16因為吸附壓力約 〇.3MPa之氣體’在解吸時吸附塔内部的壓力變成約 0.02MPa,所以受到壓力之影響。因此,採用圓筒構造。藉 由採用圓筒構造,可使作用於壁面之壓力變成均勻,即使第 —吸附解吸塔16内之壓力在由〇 〇3至約〇 3Mpa變動,亦 可實現安全性高,即不會發生形狀變形等之第二吸附解吸塔 16。此外,關於内部構造,採用和第一吸附解吸塔丨丨相同 的構造較佳。 依以上之方式,在第—再生製程,藉由在加壓狀態進 行冷部、吸附,而可將由第一吸附解吸塔丨丨所排出之汽油 蒸氣咼效率地進行液化回收。此外,在解吸時,雖然藉由提 2118-8326-PF 18 1327164 高第一吸附解吸塔u内部之溫度,而可提高解吸速度,或 使a油蒸氣濃度變高,但是因使溫度變動,消耗能量增大, 所以在解吸時不提高溫度,而在和吸附時相同之溫度進行解 • 吸,這在對省能源有效。 ' 其次’說明由第二吸附解吸塔16將汽油加以解吸, • 並&由第一凝結裝置9、第二凝結裝置1〇、及第—吸附解吸 塔11向大氣排出之第二再生製程。在將第二吸附解吸塔16 . 内之吸附劑所吸附之汽油解吸的情況,利用吸氣泵13經由 'φ 三通換向閥3b由第二吸附解吸塔16吸入氣體並由吸附劑將 ' 汽油加以解吸。此時’二路閥12b關閉。又,第二吸附解吸 塔16内之壓力降至既定的壓力時,打開流量調整閥i7b, 固定流量之空氣由大氣流入第二吸附解吸塔16,而使第二 吸附解吸塔16内部之壓力變成大致定值。雖然在吸附時第 二吸附解吸塔16在0.3MPa之大氣壓狀態動作,但是在解 吸時因為利用吸氣泵13降壓至大氣壓以下,所以利用該壓 力差在吸附劑所吸附之汽油被濃縮成高濃度的狀態解吸。在 • 此情況,雖然和汽油蒸氣之氣體流量或吸附時之吸附量亦有 關’但是藉由將第二吸附解吸塔16内之壓力控制成 0.〇2~0.04MPa,而可使汽油蒸氣漢度變成2〇~4〇vol%。 • 解吸後之汽油蒸氣經由三通換向閥3c被引至第一凝 - 結裝置9。即,將汽油濃度30vol%、壓力〇.1 MPa之高濃度、 汽油蒸氣供給第一凝結裝置9,如上述所示,第一凝結裝置 9之内部保持在由0°C至約5°C,汽油蒸氣之一部分及氣體中 所含的水分凝結,並利用氣液分離器(未圖示)等分離成氣體 (汽油蒸氣)和液體(汽油)。接著,在第一凝結裝置9無法處 2118-8326-PF 19 理之約20vol%的汽油蒸氣, 梦w 1n .. 和及附時一樣地供給第二凝結 裝置10。在此,又進行液化 Λ- ^ “ 收僅將在第二凝結裝置10 無法處理之約8%的汽油蒸氣 -吸附解吸塔u,藉由汽油二第—吸附解吸塔U。在第 / U氧通過吸附劑中,而將汽油 成分加以吸附除去,變成低 产 取低力lv〇1%之汽油濃度的清淨空 氣,並經由二路閥12a向大氣排出。 如以上所述,藉由實施吸附製程、第一再生製程、及 第-再生製程’而-連串之動作結束…般,每次對汽油儲 存槽i供油時,就重複這些一連串之動作。利用該動作,僅 向大氣排出最多1 v 〇 i %的汽油蒸氣,係環境負載很小之氣體 狀碳氫的處理、回收裝置。又,因為僅排出最多的汽 油蒸氣,可回收40v〇1%的汽油蒸氣之中的%%,回收效率 為97.5%,係效率很高的回收裝置。又,因為在之個溫度帶 進行凝結操作後進行吸附操作,所以可將第一吸附解吸塔 11大幅度地小型化,亦具有可使裝置整體小型化之效果。 此外’將解吸時來自第一吸附解吸塔u及第二吸附解 吸塔16之汽油蒸氣的排出口,作成設置於和吸附時對第一 吸附解吸塔11及第二吸附解吸塔16之汽油蒸氣濃度的供給 口同一部分。因為以吸附解吸塔u、16出口之汽油蒸氣濃 度變成低於lvol%的方式運用吸附解吸塔U、16,所以在 吸附時變成在吸附解吸塔i i、16之汽油蒸氣吸入口的附近 咼密度地吸附汽油蒸氣,在吸附解吸塔11、16之汽油蒸氣 排出口的附近不太吸附汽油蒸氣之狀態。為了在解吸時利用 凝結高效率地回收由吸附解吸塔11、16所排出之汽油蒸 氣’需要儘量提高汽油蒸氣濃度。因此’因為由高密度地吸 2118-8326-PF 20 1327164 :::分排出汽油蒸氣者可排出高濃度的汽油蒸氣,所以作 由南密度地吸附汽油蒸氣之部分,即在吸附解吸拔u、 油蒸氣吸入口的附近,而在解吸時吸入排出汽 僅靠_ W 13之壓力差的解吸方法,因為其效 不太向’所以由外部引人沖洗用氣體係、有效,在本實施形 也’藉由併用吸入和利用沖洗用氣體之氣體置換將來自吸 附解吸塔11、16之汽油蒸氣加以解吸。在本實施形態,被 运至吸附解吸塔11、16之沖洗用氣體係大氣中的空氣。因 為空氣中含有定量之水分,所以供給吸附解吸塔u、16之 沖洗用氣體需要儘量少。因此,如上述所示,在解吸時經過 某時間而吸附解吸塔11、16内之壓力降至既定的壓力時, 流量調整閥m、17b打開,藉由固定流量之空氣由大氣流 入吸附解吸塔u、16,以吸附解吸塔u、16内部之壓力變 成大致定值之方式進行解吸1 3圖係用以說明沖洗用氣體 量之控制方法的圖。藉由這種作法,可防止吸入氣體量隨著 時間經過而降低’可安定地進行汽油蒸氣之解吸操作。 作為沖洗用氣體之引入的時序,有使用定時器等由解 吸開始在經過固定時間後引入沖洗用氣體的方式(定時器方 式)、在吸附解吸塔11、16内部壓力達到設定值時引入沖洗 用氣體的方式(壓力量測方式)' 及在由吸附解吸塔u、|6 所排出之汽油蒸氣的氣體量達到設定值時引入沖洗用氣體 的方式(氣體量量測方式)。定時器方式雖然在起始費用上最 有利,但是引入沖洗用氣體之時序根據吸附解吸塔1 ^、16 所吸附之汽油的量而偏移,可能降低沖洗用氣體引入之有效 2118-8326-PF 21 ^27164 :二若吸附量多,在吸附解吸“I汽油蒸氣充分 氣氣體量變少。反之,若吸附量少,/6所排出之汽油蒸 所妯山 附里少,甴吸附解吸塔11、16 之汽油蒸氣氣體量變少的時間帶增加,由吸附解吸塔 量量>^法高效率地排出汽油蒸氣4力量測方式及氣體 效:1:決上述之定時器方式的問題點,並可實現高 ' 吸。此外,在本汽油回收裝置,在安全上,對^ =流動的配管系統安裝壓力計係不可欠缺。因此,::: =測方式可兼㈣些壓力計,所以在3種方式之中係= 對加油站之汽油儲存槽的供油—般定期地進行 因間,而產线油蒸氣這件事僅限於—天中之固定時間。 Η二站在提冋裝置之運轉率的觀點,在產生汽油蒸氣的時 待進行吸附操作,而在未產生汽油蒸氣的時間帶進行 解吸塔U、16之再生’這係有效的。其次,使用第 明藉由減少氣體量並進行長時間運轉之汽油回數的有效 性。如此,得知藉由減少氣體量,而回收率降低。又得知, 氣體流量變成40L/min以上時,回收率不增加。這係由于於广 體流量變多時,由流量調整閥17a所流入之空氣量變多:= 油蒸氣濃度被該空氣稀釋,在第三凝結裝置15之汽油凝妗 里降低的緣故。因此,得知在由第一吸附解吸塔丨丨將汽由 蒸氣解吸的情況,氣體流量設為至多4〇L/min較佳。由以 之事項,藉由以低流量花長時間對第一吸附解吸塔U進^ 再生,可高效率地進行回收。 其次,說明氣體狀碳氫之處理、回收裝置的控制方 2118-8326-PF 22 1327164 法。回收裝置停止時’吸氣泵13哎 A加壓泵14停止’二路閥 12a、12b處於全閉狀態,而流量 ^ 垔調整閥丨化、17b處於關閉 狀態。第一吸附解吸塔U及第二 及附解吸塔16利用冷凍機 5所冷卻之溫度媒質冷卻。變成 t /飞/由儲存槽1開始供油之 狀態時,三通換向閥3a切換’而 且—路閥12a打開,第二 凝結裝置10的冷卻開始。第二凝姓 < — 叹、,、σ裒置1〇内部之溫度達到 設定值時,汽油蒸氣的回收開始。對汽油儲存槽i之供油及 汽油蒸氣之產生結束時,三通換向閥3a切換,而且二路間 12 a關閉,第二凝結裝置! 0之冷卻停止。然後,二路閥工2 b 打開,而且吸氣泵13及加壓泵14進行運轉時,由第一吸附 解吸塔11將汽油蒸氣加以解吸,並通過第三凝結裝置15 及第二吸附解吸塔16後向大氣排出。此時,藉由吸氣泵13 之運轉而第一吸附解吸塔Π内之壓力降至既定壓力時,流 量調整閥17a開始打開,以既定之流量流向第一吸附解吸塔 11之方式控制流量調整閥17a的開度。根據定時器等,第 再生製程結束時,吸氣泵13或加壓泵14停止,而流量調 整閥17a變成關閉之狀態,二路閥12a變成關閉之狀態。然 後,第一凝結裝置1 〇之冷卻開始,第二凝結裝置丨〇内部之 溫度達到設定值時’第二吸附解吸塔16的再生開始。二路 閥12a打開’而且吸氣泵13及加壓泵14進行運轉時,由第 二吸附解吸塔16將汽油蒸氣加以解吸,按照第一凝結裝置 9、第一凝結裝置10、及第一吸附解吸塔π之順序通過後 向大軋排出。此時,藉由吸氣泵13之運轉而第二吸附解吸 塔16内之壓力降至既定壓力時,流量調整閥i7b開始打開, 以既定之流量流向第二吸附解吸塔16之方式控制流量調整 2118-8326-PF 23 1327164 閥17b的開度。在固定時間,再生處理結束時,第二凝結裝 置10之冷卻停止’而且吸氣泵13或加壓泵14停止,二路 閥12a、12b變成全閉狀態,流量調整閥17a、17b變成關閉 之狀態。依以上之方式,回收裝置重複進行運轉。 最後,說明使用加壓泵14及壓力控制器19,提高第 二凝結裝置15及第二吸附解吸塔16之内部壓力的效果。第 . 5圖係表示第三凝結裝置15及第二吸附解吸塔16之内部壓 力和充填於第二吸附解吸塔16的吸附劑之關係圖。如此, _得知藉由提高内部壓力,而可使矽膠之充填量變少^可是, 得知即使變成高於〇 4MPa,矽膠充填量亦幾乎不減少。另 一方面’提高壓力時’因為需要提高第三凝結裝置15及第 二吸附解吸塔16之耐壓性,裝置變得昂貴。因此,可確認 將第三凝結裝置15及第二吸附解吸塔16之内部壓力設為 〇·2~0·3ΜΡα的作法係高效率。此外,第6圖係表示未包括 加壓系14和壓力控制器19之氣體狀碳氫的處理、回收裝置 之流程的整體構造圖。藉此,可減少構成裝置之元件數。可 疋’因為第二吸附解吸塔16所使用之矽膠量變成2倍以上, 所以第二吸附解吸塔16變大,得知裝置費用不太降低。 由以上之事項’設置加壓泵14和壓力控制器19,提 尚第三凝結裝置15及第二吸附解吸塔16之内部壓力,亦藉 由提兩至0.4]\^3,最好為〇.2〜〇.31^?&,而具有可提供便宜 之回收裝置的效果。 第2實施形態 第7圖係表示本發明之第2實施形態的氣體狀碳氫之 處理、回收裝置的流程之整體構造圖。 2118-8326'ρρ 24 1327164 本第2實施形態和該第1實施形態之差異在於未使用 二通換向閥3a。在本第2實施形態,如第7圖所示,不需 . 要三通換向閥3a,而新包括閥21。作成這種構造,藉由使 , 在回收裝置之壓力損失比調壓閥4的設定值小,而一般在汽 油蒸氣流向回收裝置’並在回收裝置發生氣體阻塞等之不良 的情況,可自動地經由調壓閥4將汽油蒸氣向大氣排出。此 . 外,本第2實施形態之回收裝置藉由具有2個溫度帶的凝 結’而可使吸附劑之使用量變成很少,因為可將回收裝置之 'Φ 壓力損失降至極限,而可實現這種裝置。 因而,在回收裝置發生氣體阻塞等,回收裝置及汽油 儲存槽1内之壓力亦不會高於調壓閥4的設定值,具有可提 高安全的回收裝置之效果。 第3實施形態 第8圖係表示本發明之第3實施形態的氣體狀碳氫之 處理、回收裝置的流程之整體構造圖。 在該第1實施形態,雖然連續地設置吸氣泵13和加 鲁壓泵14,但是在本第3實施形態,藉由將具有岐容積之 壓力緩衝容器31及壓力量測器32設置於吸氣泵13和加壓 栗14之間,以監視吸氣系η和加壓泵14之間的壓力,而 可檢測吸氣泵13和加壓泵14之運轉的誤動作,可預防危險 •之運轉。即,在吸氣泵13和加壓泵14之間的壓力變成負壓 之情況可防止加壓泵14的性能降低,而在吸氣泵13和加壓 泵14之間的壓力變成正壓之情況可防止吸氣泵^的性能降 低。又,藉由在吸氣泵13和加壓泵14之間包括固定容積的 空間,可緩和激烈之壓力變動,並可實現具有餘裕之運轉異 2118-8326-PF 25 丄 w/164 常檢測。 藉此在回收裝置内之來自吸附解吸塔11、的解吸 .製程,可檢測吸氣泵13或加壓泵14之不良,而且可防止不 :良之急速地擴大,具有可提供安全的回收裝置之效果。 ' 第4實施形態 第9圖係表不本發明之第4實施形態的氣體狀碳氫之 . 處理、回收裝置的流程之整體構造圖。 本第4實施形態和該第1實施形態之差異為在第一吸 •附解吸塔11的再生時之氣體處理的流程相異,即第ι實施 形態所示之第二再生製程相異。而且,在本第4實施形態, 如第9圖所示,二通換向閥3c不是位於吸氣泵丨3和加壓泵 14之間,而設置於第三凝結裝置15和第二吸附解吸塔16 之間。又,和調整第二吸附解吸塔16内之壓力的壓力控制 器19a另外地設置調整第三凝結裝置15内之壓力的壓力控 制器19b。 在第1實施形態’將由第二吸附解吸塔16利用吸氣 ® 栗13已解吸之汽油蒸氣供給第一凝結裝置9,並通過第二 凝結裝置10及第一吸附解吸塔11後向大氣排出。可是,在 本第4實施形態,由第二吸附解吸塔16利用吸氣栗13已解 吸之A油蒸氣,利用加壓系14加壓後,供給第三凝結裝置 ' 15。然後’通過第三凝結裝置15之汽油蒸氣,再通過第二 凝結裝置10及第一吸附解吸塔11後向大氣排出。藉由作成 這種流程,而可有效地利用加壓泵14,並可高效率地回收 通過第三凝結裝置15之汽油蒸氣。此外,在無法降低冷束 機5之冷媒的蒸發溫度的情況,利用這種流程係有效,具有 2118-8326-PP 26 可高效率地回收汽油之效果。 第5實施形態 帛10圖係表示本發明之第5實施形態的氣體狀碳氣 外理、回收裝置的流程之整體構造圖。 本第5實施形態和該第i實施形態之差異為在第一吸 附解吸塔11的再生時之氣體處理的流程相異,即第工實施 形態所示之第一再生製程相異。在第i實施形態,如第工 =所不’將第二吸附解吸塔16設置於第三凝結裝置i5之後 匕,而,在本第5實施形態,如第1〇圖所示,在第三凝結 穿置15之後段包括氣體儲存容器41。又,42係設置於氣體 :存容器41和三通換向閥3 b之間的作為主流量控制器之流 量調整閥,43係設置於氣體儲存容器41和第三凝結裝置15 之間的斷流閥。 在第1實施形態,由第一吸附解吸塔丨丨利用吸氣泵 13已解吸之汽油蒸氣,利用加壓泵14加壓後,供給第三凝 結裝置15。通過第三凝結裝置15之汽油蒸氣,再通過第二 吸附解吸塔16後向大氣排出。可是’在第5實施形態,由 第一吸附解吸塔11利用吸氣泵13已解吸之汽油蒸氣,利用 加壓泵14加壓後,供給第三凝結裝置15。雖然至此為止和 第1實施形態相同,但是之後,通過第三凝結裝置〗5之汽 油祭氣直接被氣體儲存容器41冷卻並以加壓壓縮之狀態被 封入。氣體儲存容器41之壓力達到既定壓力時,第一再生 製程結束。然後’氣體儲存容器41所儲存之汽油蒸氣經由 流量調整閥42供給第一吸附解吸塔i丨,並利用第一吸附解 吸塔11内之吸附劑除去汽油蒸氣後向大氣排出。藉由作成 2118-8326-PF 27 1327164 廷種構造及處理流程,而可簡化系統構造,並可降低裝置之 費用。又,可減少吸氣泵13及加壓泵14之運轉時間,並可 節省能源。 由以上之事項,藉由包括替代第二吸附解吸塔16之 虱體儲存容器41,而具有能以低費用提供省能源的回收裝 置之效果》 第6實施形態 第11圖係表示本發明之第6實施形態的氣體狀碳氫之 '·處理、回收裝置的流程之整體構造圖。 本第6實施形態和該第丨實施形態之差異為在第一吸 附解吸塔11的再生時之氣體處理的流程相異,即第丨實施 形態所示之第一再生製程相異及無第二再生製程。又,在構 成機器上,在第1實施形態,如第丨圖所示,利用溫度媒質 將第三凝結裝置15之内部冷卻至〇〜rc,但是在本第6實 施形態,如第11圖所示,包括作成由冷凍機5利用冷媒可 直接冷卻之第四凝結裝置51,且不需要第二吸附解吸塔16。 ® 在第1實施形態,由第一吸附解吸塔11利用吸氣泵 13已解吸之汽油蒸氣,利用加壓泵14加壓後,供給第三凝 結裝置15。通過第三凝結裝置15之汽油蒸氣,再通過第二 吸附解吸塔16後向大氣排出。可是,在第6實施形態,由 第一吸附解吸塔11利用吸氣泵13已解吸之汽油蒸氣,利用 加壓泵14加壓後’供給第四凝結裝置51。利用冷束機5所 冷卻之冷媒直接冷卻第四凝結裝置51的内部,而變成約一 3〇°C。在壓力0_3MPa、冷卻溫度—3(rc之條件,汽油蒸氣 濃度變成約lvol%。因此,直接向大氣排出。藉此,可簡化 2118-8326-PF 28 1327164 費用。又,可不需要第二再生製 泵14之運轉時間,並可節省能 系統構造,並可降低裝置之 程’可減少吸氣泵13及加壓 源。 由以上之事項 第四凝結裝置51, 置之效果。 第7實施形態 ’藉由包括替代第第三凝結裝置15之 而具有能以低費用提供省能源的回收裝The cooling temperature of the apparatus 10 is such that the amount of the yttrium filled in the first adsorption desorption column i 1 is changed. However, it was found that even if it was cooled to a 30. (The following amount of silicone is also a few.) Salty. For the results of experimental investigations on various gasolines, it is known that the composition of gasoline vapor 2118-8326-PP 15 1327164 is irrelevant, even if the cooling temperature becomes below 30 °C, gasoline vapor The fact that the saturation concentration is hardly lowered is also due to the decrease in the amount of reduction of the silicone rubber. Therefore, in consideration of the input energy, it is not high efficiency to set the cooling temperature of the second condensation device 10 to _30 乞 or less. The cooling temperature of the second condensation-device 10 is set to a 30T: preferably. 'Next' describes the regeneration process of the first adsorption-desorption column 11, that is, the desorption process of the gasoline. Vapor. The regeneration of the first adsorption-desorption column π The process includes: a first regeneration process 'desorbing gasoline from the first adsorption desorption column 11 and discharging it to the atmosphere via the second condensation device 15 and the second adsorption desorption column 16; and a second regeneration process, desorbing by the second adsorption The tower 16 desorbs the gasoline and discharges it to the atmosphere via the first condensing device 9, the second condensing device 10, and the first adsorption desorption column 11. First, the first regeneration process will be described. In the case where the adsorbed gasoline is desorbed, the gas is sucked by the first adsorption/desorption column 11 through the three-way switching valve 3b by the getter pump 13 and the gasoline is desorbed by the adsorbent. At this time, the two-way wide 12a is closed. When the pressure in the adsorption desorption column 11 is reduced to a predetermined pressure, the flow regulating valve is opened. 17a 'The fixed flow of air flows from the atmosphere into the first adsorption desorption column U, and the pressure inside the first adsorption desorption column u becomes a substantially constant value. Although the first adsorption desorption column operates at an atmospheric pressure of 〇1 MPa during adsorption, since it is depressurized to below atmospheric pressure by the getter pump 13 during desorption, the gasoline adsorbed by the adsorbent is concentrated by the pressure difference. In the case of a high concentration of the state solution and in this case, although it is related to the gas flow rate of the gasoline vapor or the adsorption at the time of adsorption, the pressure in the first adsorption desorption column U is controlled to be 〇·〇2~〇. 〇4MPa' and the gasoline vapor concentration can be changed to 2〇~4〇v〇1%. The desorbed gasoline vapor is led to the pressure pump via the three-way selector valve 3c to the pump 2118-8326-PF 16 1327164 14 ° Pump 14 will The oil vapor is pressurized to about 0.3 MPa and supplied to the second condensing device 15. That is, the gasoline concentration of 30 vol%, the pressure 〇3 MPa, and the pressurized gasoline vapor are supplied to the third condensing device 15. By using the liquid. 8 is supplied to the temperature medium cooled by the refrigerator 5 to indirectly cool the third condensation device 15. Generally, the third condensation device 15 is internally held in a portion of the gasoline vapor from 〇r ' to about 5. The moisture is condensed, and is separated into a gas (gasoline vapor) and a liquid (gasoline) by a gas-liquid separator (not shown) or the like, and is stored in the lower side of the third condensing device 15, and is sent back via the gasoline_pipe 18. To the petrol storage tank 1. Further, as shown in Fig. 1, by introducing gasoline vapor from above the second condensing device 丨5 and flowing downward, the liquefied gasoline or water flows efficiently downward by gravity and airflow, and these liquefied materials are liquefied. The recycling becomes easy. On the other hand, the pressure of the operating conditions of the third condensing device 15 is 0.3 MPa and the cooling temperature is 5. . Under the condition, the gasoline vapor concentration at the outlet becomes about 8 vol%. In addition, from the saturation concentration curve of gasoline vapor, the saturated gasoline vapor concentration is about 8v〇1% at a pressure of 0.3MPa and a temperature of 5°C. In this article, the π oil vapor concentration is theoretically not lower than 8v〇1%. X, by lowering the temperature, the concentration of gasoline vapor at the outlet of the third condensing device 15 can be lowered. However, when the set temperature is set to be below the freezing point, the water contained in the gas is frozen in the third condensation device 15, because the pressure loss inside the third condensation device 15 is increased, so the second condensation device 15 The set temperature is preferably set from ot to about rc. Further, in the second coagulation device 15, since it is pressurized to about 3 MPa, a cylindrical structure is employed. By adopting the cylindrical structure, the pressure acting on the wall surface can be changed to a uniform sentence 'even if the third condensing device i...the pressure becomes about 0.3 MPa', the safety can be high, that is, the second deformation does not occur, etc., 2118-8326 - PF 17 1327164 Three condensation device 15. Then, about 8 vol% of the vapor vapor which cannot be treated by the third condensing device 15 is sent to the second adsorption/desorption column 16 and processed. Fig. 1 shows a case where the second adsorption/desorption column 16 operates as an adsorption column. Therefore, the two-way valve 12b is opened (blackened), and the flow regulating valve 17b is in a closed (blank) state. The adsorption tower is used as a desorption column after being subjected to adsorption treatment at an arbitrary timing. In this case, the two-way valve 12b is closed and the flow regulating valve i7b is in an open state. The second adsorption-desorption column 16 is also sealed with an adsorbent for adsorbing gasoline vapor, which is the same as the first adsorption-desorption column 11. The gasoline vapor is passed through the adsorbent to adsorb and remove the gasoline component, and becomes clean air having a vapor concentration lower than 丨v〇1%, and is discharged to the atmosphere via the two-way valve 12b. Further, the first adsorption/desorption column 16 is also cooled to a fixed temperature by the temperature medium supplied from the liquid circulation pump 8 regardless of the function of adsorption and desorption of the gasoline vapor. That is, it is always kept 〇~5 like the first adsorption desorption column U. The operation mode is controlled by the method of 〇. Further, the second adsorption/desorption column 16 is subjected to pressure by a pressure of about 0.02 MPa in the gas inside the adsorption column when the adsorption pressure is about 0.3 MPa. Therefore, a cylindrical structure is employed. By adopting the cylindrical structure, the pressure acting on the wall surface can be made uniform, and even if the pressure in the first adsorption/desorption column 16 is varied from 〇〇3 to about M3 Mpa, safety can be achieved, that is, the shape does not occur. a second adsorption desorption column 16 such as a deformation. Further, regarding the internal structure, the same configuration as that of the first adsorption desorption column is preferable. According to the above, in the first regeneration process, the gasoline vapor discharged from the first adsorption desorption column can be efficiently liquefied and recovered by performing the cold portion and adsorption in a pressurized state. Further, at the time of desorption, although the temperature inside the first adsorption desorption column u is raised by raising 2118-8326-PF 18 1327164, the desorption rate can be increased, or the a-oil vapor concentration can be increased, but the temperature is varied and consumed. The energy is increased, so the temperature is not increased during desorption, and the same temperature as that at the time of adsorption is used to solve the problem, which is effective for energy saving. 'Secondary' illustrates the second regeneration process in which the gasoline is desorbed by the second adsorption/desorption column 16, and is discharged to the atmosphere by the first condensation device 9, the second condensation device 1, and the first adsorption desorption column 11. In the case where the gasoline adsorbed by the adsorbent in the second adsorption desorption column 16 is desorbed, the gas is sucked from the second adsorption desorption column 16 by the getter pump 13 via the 'φ three-way switching valve 3b and is adsorbed by the adsorbent. Gasoline is desorbed. At this time, the two-way valve 12b is closed. Further, when the pressure in the second adsorption/desorption column 16 is lowered to a predetermined pressure, the flow rate adjusting valve i7b is opened, and the air of the fixed flow rate flows from the atmosphere into the second adsorption/desorption column 16, and the pressure inside the second adsorption/desorption column 16 becomes Approximate setting. Although the second adsorption/desorption column 16 operates at an atmospheric pressure of 0.3 MPa during adsorption, since it is depressurized to below atmospheric pressure by the getter pump 13 during desorption, the gasoline adsorbed by the adsorbent is concentrated to a high level by the pressure difference. The state of concentration is desorbed. In this case, although it is related to the gas flow rate of the gasoline vapor or the adsorption amount at the time of adsorption, 'but by controlling the pressure in the second adsorption desorption column 16 to 0. 〇 2 to 0.04 MPa, the gasoline vapor can be made. Degree becomes 2〇~4〇vol%. • The desorbed gasoline vapor is led to the first condensation device 9 via the three-way selector valve 3c. That is, a gasoline concentration of 30 vol%, a high concentration of pressure 〇1 MPa, and gasoline vapor are supplied to the first condensing device 9, and as described above, the inside of the first condensing device 9 is maintained at from 0 ° C to about 5 ° C. One part of the gasoline vapor and the moisture contained in the gas are condensed, and are separated into a gas (gasoline vapor) and a liquid (gasoline) by a gas-liquid separator (not shown) or the like. Next, the first coagulation device 9 cannot supply about 20 vol% of gasoline vapor at 2118-8326-PF, and the second coagulation device 10 is supplied in the same manner as the time. Here, the liquefaction enthalpy is further carried out - ^" only about 8% of the gasoline vapor-adsorption desorption column u which cannot be treated by the second coagulation device 10, by the gasoline second-adsorption desorption column U. The gasoline component is adsorbed and removed by the adsorbent, and the clean air having a low gasoline concentration of 1% is obtained, and is discharged to the atmosphere via the two-way valve 12a. As described above, by performing the adsorption process, The first regeneration process, and the first regeneration process, and the series of operations are completed, each time the oil storage tank i is supplied with oil, the series of operations are repeated. With this action, only a maximum of 1 v is discharged to the atmosphere. 〇i% of gasoline vapor is a treatment and recovery device for gaseous hydrocarbons with a small environmental load. Moreover, because only the most gasoline vapor is discharged, it can recover 40% of the gasoline vapor of 40v〇1%, and the recovery efficiency It is 97.5%, which is a highly efficient recovery device. Moreover, since the adsorption operation is performed after the condensation operation in one temperature zone, the first adsorption/desorption column 11 can be greatly miniaturized, and the device can be made small overall. Chemical Further, 'the discharge port of the gasoline vapor from the first adsorption desorption column u and the second adsorption desorption column 16 at the time of desorption is formed, and the gasoline of the first adsorption desorption column 11 and the second adsorption desorption column 16 disposed at the time of adsorption is formed. The supply port of the vapor concentration is in the same portion. Since the adsorption desorption columns U and 16 are used in such a manner that the concentration of the gasoline vapor at the outlet of the adsorption desorption columns u and 16 becomes less than 1 vol%, they become gasoline in the adsorption desorption columns ii, 16 at the time of adsorption. In the vicinity of the vapor inlet, the gasoline vapor is densely adsorbed, and the gasoline vapor is less adsorbed in the vicinity of the gasoline vapor discharge port of the adsorption/desorption columns 11 and 16. In order to efficiently collect the adsorption/desorption column 11 by coagulation during desorption, 16 discharged gasoline vapors 'requires as much as possible to increase the concentration of gasoline vapor. Therefore, because high-density absorption of 2118-8326-PF 20 1327164 ::: can be discharged from gasoline vapor can discharge high concentrations of gasoline vapor, so the density is south. The part that adsorbs the gasoline vapor, that is, in the vicinity of the adsorption desorption and extraction, and the oil vapor suction port, and in the desorption, the exhaust steam is only relied on the pressure of _W 13 The desorption method is effective because it is not used to flush the gas system from the outside, and in this embodiment, it is also replaced by a gas which is inhaled and used with a flushing gas from the adsorption desorption columns 11, 16. The gasoline vapor is desorbed. In the present embodiment, the air is sent to the atmosphere of the flushing gas system of the adsorption desorption columns 11 and 16. Since the air contains a certain amount of water, the flushing gas supplied to the adsorption desorption columns u and 16 is required. As described above, as shown above, when the pressure in the adsorption/desorption columns 11, 16 is lowered to a predetermined pressure after a certain period of desorption, the flow rate adjusting valves m, 17b are opened, and the air of a fixed flow flows in from the atmosphere. The adsorption/desorption columns u and 16 are desorbed so that the pressure inside the adsorption desorption columns u and 16 becomes a substantially constant value. The figure is a diagram for explaining a method of controlling the amount of gas for flushing. By this means, it is possible to prevent the amount of the inhaled gas from decreasing as time passes, and the desorption operation of the gasoline vapor can be stably performed. As a timing of introduction of the rinsing gas, there is a method of introducing a rinsing gas after a fixed time from the desorption by a timer or the like (timer method), and introducing the rinsing when the internal pressure of the adsorption/desorption columns 11 and 16 reaches a set value. The method of the gas (pressure measurement method) and the method of introducing the gas for flushing (gas amount measurement method) when the gas amount of the gasoline vapor discharged from the adsorption desorption columns u and |6 reaches a set value. Although the timer method is most advantageous in terms of initial cost, the timing of introducing the flushing gas is shifted according to the amount of gasoline adsorbed by the adsorption desorption columns 1^, 16 and may reduce the effective introduction of the flushing gas 2118-8326-PF. 21 ^27164 : If the amount of adsorption is large, the amount of gas in the gasoline vapor will be reduced in the adsorption desorption "I. If the amount of adsorption is small, the amount of gasoline discharged from the /6 is less in the mountains, and the adsorption desorption tower 11 is 16 The time zone in which the amount of gasoline vapor gas is reduced is increased, and the amount of gasoline desorption tower is reduced by the amount of the adsorption desorption tower. The method of gas pumping and gas efficiency is as follows: 1. The problem of the above-mentioned timer mode is determined, and In addition, in this gasoline recovery unit, in terms of safety, it is indispensable to install a pressure gauge system for the ^= flow piping system. Therefore, the :::= test method can be combined with (four) pressure gauges, so in three types In the middle of the system, the oil supply to the gasoline storage tank of the gas station is regularly carried out, and the oil vapor in the production line is limited to the fixed time of the day. Point of view in producing gasoline When the vapor is to be subjected to the adsorption operation, and the regeneration of the desorption columns U and 16 is carried out in the time zone when the gasoline vapor is not generated, this is effective. Secondly, the number of gasolines which are reduced by the amount of gas and long-time operation is used. Therefore, it is known that the recovery rate is lowered by reducing the amount of gas. It is also known that when the gas flow rate becomes 40 L/min or more, the recovery rate does not increase. This is because the flow rate is increased when the flow rate of the wide body is increased. The amount of air flowing into the regulating valve 17a is increased: = the oil vapor concentration is diluted by the air and lowered in the gasoline condensation of the third condensing device 15. Therefore, it is known that the steam is removed by the first adsorption desorption tower In the case of vapor desorption, it is preferable that the gas flow rate is at most 4 〇L/min, and it is possible to efficiently recover the first adsorption/desorption column U by a long time at a low flow rate. The method of controlling the hydrocarbon-like hydrocarbon and the recovery device 2118-8326-PF 22 1327164. When the recovery device is stopped, the suction pump 13A pressurizes the pump 14 to stop. The two-way valves 12a and 12b are fully closed. And traffic ^ The adjustment valve is deuterated and 17b is in a closed state. The first adsorption desorption column U and the second and desorbing column 16 are cooled by the temperature medium cooled by the refrigerator 5. When t/fly/the storage tank 1 starts to supply oil The three-way switching valve 3a is switched 'and the -way valve 12a is opened, and the cooling of the second condensing device 10 is started. The second condensate<- sigh,, σ 裒 is set to 1 〇 when the internal temperature reaches the set value, the gasoline The recovery of the steam begins. At the end of the supply of the gasoline storage tank i and the generation of the gasoline vapor, the three-way selector valve 3a is switched, and the second passage 12 a is closed, the second condensation device is stopped! 0 the cooling is stopped. Then, two When the gate valve 2 b is opened and the getter pump 13 and the pressurizing pump 14 are operated, the gasoline vapor is desorbed by the first adsorption desorption column 11 and passed through the third coagulation device 15 and the second adsorption desorption column 16 The atmosphere is discharged. At this time, when the pressure in the first adsorption desorption column is reduced to a predetermined pressure by the operation of the getter pump 13, the flow rate adjusting valve 17a starts to open, and the flow rate adjustment is controlled in such a manner that the flow rate flows to the first adsorption desorption column 11 at a predetermined flow rate. The opening degree of the valve 17a. At the end of the first regeneration process, the intake pump 13 or the pressure pump 14 is stopped, and the flow rate adjustment valve 17a is turned off, and the two-way valve 12a is turned off. Then, the cooling of the first condensing device 1 is started, and when the temperature inside the second condensing device 达到 reaches the set value, the regeneration of the second adsorption/desorption column 16 is started. When the two-way valve 12a is opened and the suction pump 13 and the pressure pump 14 are operated, the gasoline vapor is desorbed by the second adsorption/desorption column 16, according to the first condensation device 9, the first condensation device 10, and the first adsorption. The order of the desorption column π is discharged through the backward large rolling. At this time, when the pressure in the second adsorption/desorption column 16 is reduced to a predetermined pressure by the operation of the getter pump 13, the flow rate adjusting valve i7b starts to open, and the flow rate adjustment is controlled in such a manner that a predetermined flow rate flows to the second adsorption/desorption column 16. 2118-8326-PF 23 1327164 Opening of valve 17b. At the fixed time, when the regeneration process is completed, the cooling of the second coagulation device 10 is stopped and the intake pump 13 or the pressurizing pump 14 is stopped, the two-way valves 12a and 12b are fully closed, and the flow rate adjusting valves 17a and 17b are closed. status. In the above manner, the recovery device is repeatedly operated. Finally, the effect of increasing the internal pressure of the second coagulation device 15 and the second adsorption desorption column 16 by using the pressurizing pump 14 and the pressure controller 19 will be described. Fig. 5 is a view showing the relationship between the internal pressure of the third condensing device 15 and the second adsorption/desorption column 16 and the adsorbent charged in the second adsorption/desorption column 16. Thus, it is known that the amount of the silicone filler can be reduced by increasing the internal pressure. However, it is found that even if it becomes higher than 〇 4 MPa, the amount of the silicone filler is hardly reduced. On the other hand, when the pressure is increased, the pressure of the third condensing device 15 and the second adsorption/desorption column 16 needs to be increased, and the device becomes expensive. Therefore, it was confirmed that the internal pressures of the third condensing device 15 and the second adsorptive desorption column 16 were set to 〇·2~0·3ΜΡα. Further, Fig. 6 is a view showing an overall configuration of a flow of a treatment and recovery apparatus that does not include gaseous hydrocarbons of the pressurizing system 14 and the pressure controller 19. Thereby, the number of components constituting the device can be reduced. Since the amount of the silicone used in the second adsorption/desorption column 16 is twice or more, the second adsorption/desorption column 16 becomes large, and the device cost is not lowered. From the above matters, 'the pressure pump 14 and the pressure controller 19 are provided, and the internal pressures of the third condensing device 15 and the second sorption desorbing tower 16 are raised, and by two to 0.4]\^3, preferably 〇 .2~〇.31^?&, and has the effect of providing an inexpensive recycling device. (Second Embodiment) Fig. 7 is a view showing an overall configuration of a flow of a gaseous hydrocarbon processing and recovery apparatus according to a second embodiment of the present invention. 2118-8326'ρρ 24 1327164 The difference between the second embodiment and the first embodiment is that the two-way switching valve 3a is not used. In the second embodiment, as shown in Fig. 7, the three-way switching valve 3a is not required, and the valve 21 is newly included. In such a configuration, the pressure loss in the recovery device is smaller than the set value of the pressure regulating valve 4, and generally, in the case where the gasoline vapor flows to the recovery device and the gas is blocked in the recovery device, etc., it is automatically The gasoline vapor is discharged to the atmosphere via the pressure regulating valve 4. In addition, the recovery apparatus of the second embodiment can reduce the amount of adsorbent used by the condensation of two temperature zones, because the pressure loss of the recovery device can be reduced to the limit. Implement this device. Therefore, the gas in the recovery device and the gas storage tank 1 are not higher than the set value of the pressure regulating valve 4, and the safety recovery device can be improved. (Embodiment 3) FIG. 8 is a view showing an overall configuration of a flow of a gaseous hydrocarbon processing and recovery apparatus according to a third embodiment of the present invention. In the first embodiment, the air suction pump 13 and the squeezing pump 14 are continuously provided. However, in the third embodiment, the pressure buffer container 31 and the pressure measuring device 32 having the 岐 volume are provided in the suction. Between the air pump 13 and the pressurized pump 14, the pressure between the intake system η and the pressure pump 14 is monitored, and the malfunction of the operation of the air suction pump 13 and the pressure pump 14 can be detected, and the operation of the danger can be prevented. . That is, the pressure between the getter pump 13 and the pressurizing pump 14 becomes a negative pressure to prevent the performance of the pressurizing pump 14 from deteriorating, and the pressure between the getter pump 13 and the pressurizing pump 14 becomes a positive pressure. The situation can prevent the performance of the getter pump from degrading. Further, by including a space of a fixed volume between the getter pump 13 and the pressurizing pump 14, the intense pressure fluctuation can be alleviated, and the running difference 2118-8326-PF 25 丄 w/164 can be detected. Thereby, the desorption process from the adsorption/desorption column 11 in the recovery device can detect the malfunction of the getter pump 13 or the pressurizing pump 14, and can prevent the rapid expansion without a rapid increase, and can provide a safe recovery device. effect. [Fourth Embodiment] Fig. 9 is a view showing an overall configuration of a flow of a treatment and recovery apparatus in a gaseous hydrocarbon gas according to a fourth embodiment of the present invention. The difference between the fourth embodiment and the first embodiment is that the flow of the gas treatment at the time of regeneration of the first absorption/desorption column 11 is different, that is, the second regeneration process shown in the first embodiment is different. Further, in the fourth embodiment, as shown in Fig. 9, the two-way switching valve 3c is not disposed between the air suction pump 丨3 and the pressure pump 14, but is disposed in the third condensing device 15 and the second adsorption desorption Between towers 16. Further, the pressure controller 19a for adjusting the pressure in the second adsorption/desorption column 16 is additionally provided with a pressure controller 19b for adjusting the pressure in the third coagulation device 15. In the first embodiment, the gasoline vapor desorbed by the second adsorption/desorption column 16 by the intake pump 13 is supplied to the first condensing device 9, and is discharged to the atmosphere through the second condensing device 10 and the first adsorption/desorption column 11. However, in the fourth embodiment, the second adsorption/desorption column 16 is pressurized by the pressurized system 14 by the A oil vapor desorbed by the intake pump 13, and then supplied to the third condensation device '15. Then, the gasoline vapor passing through the third condensing device 15 passes through the second condensing device 10 and the first adsorption/desorption column 11 and is discharged to the atmosphere. By making such a flow, the pressurizing pump 14 can be effectively utilized, and the gasoline vapor passing through the third coagulation device 15 can be efficiently recovered. Further, in the case where the evaporation temperature of the refrigerant of the cold beam machine 5 cannot be lowered, it is effective to use such a flow, and the effect of efficiently recovering gasoline with 2118-8326-PP 26 can be obtained. (fifth embodiment) FIG. 10 is a view showing an overall configuration of a gas-like carbon gas external treatment and recovery apparatus according to a fifth embodiment of the present invention. The difference between the fifth embodiment and the i-th embodiment is that the flow of the gas treatment at the time of regeneration of the first adsorption/desorption column 11 is different, that is, the first regeneration process shown in the first embodiment is different. In the i-th embodiment, the second adsorption/desorption column 16 is disposed after the third condensation device i5 as in the first embodiment, and in the fifth embodiment, as shown in the first figure, in the third embodiment. The subsequent section of the coagulation through 15 includes a gas storage container 41. Further, 42 is a flow rate adjusting valve provided as a main flow controller between the gas storage container 41 and the three-way switching valve 3b, and 43 is disposed between the gas storage container 41 and the third condensing device 15 Flow valve. In the first embodiment, the gasoline vapor desorbed by the air suction pump 13 by the first adsorption/desorption tower is pressurized by the pressure pump 14, and then supplied to the third condensation device 15. The gasoline vapor passing through the third condensing device 15 is passed through the second adsorption/desorption column 16 and then discharged to the atmosphere. However, in the fifth embodiment, the gasoline vapor desorbed by the air suction pump 13 by the first adsorption/desorption column 11 is pressurized by the pressure pump 14, and then supplied to the third condensation device 15. Although it is the same as the first embodiment, the gasoline atmosphere by the third condensing device 5-1 is directly cooled by the gas storage container 41 and sealed in a state of pressure compression. When the pressure of the gas storage container 41 reaches a predetermined pressure, the first regeneration process ends. Then, the gasoline vapor stored in the gas storage container 41 is supplied to the first adsorption/desorption column i via the flow rate adjusting valve 42, and the gasoline vapor is removed by the adsorbent in the first adsorption/desorption column 11 and then discharged to the atmosphere. By constructing the 2118-8326-PF 27 1327164 configuration and processing flow, the system configuration can be simplified and the cost of the device can be reduced. Further, the operation time of the getter pump 13 and the pressurizing pump 14 can be reduced, and energy can be saved. According to the above, the effect of providing the energy-saving recovery device at a low cost by including the cartridge storage container 41 in place of the second adsorption/desorption column 16 is described. FIG. 11 is a view showing the first aspect of the present invention. (6) Overall structural diagram of the flow of the gas-like hydrocarbon in the embodiment and the processing and recovery device. The difference between the sixth embodiment and the second embodiment is that the flow of the gas treatment during the regeneration of the first adsorption/desorption column 11 is different, that is, the first regeneration process shown in the second embodiment is different and there is no second. Recycling process. Further, in the first embodiment, as shown in the first embodiment, the inside of the third condensing device 15 is cooled to 〇 rc by the temperature medium. However, in the sixth embodiment, as shown in FIG. It is shown that the fourth condensing device 51 which is directly cooled by the refrigerator 5 by the refrigerant is formed, and the second adsorption/desorption column 16 is not required. In the first embodiment, the gasoline vapor desorbed by the air suction pump 13 by the first adsorption/desorption column 11 is pressurized by the pressure pump 14, and then supplied to the third condensation device 15. The gasoline vapor passing through the third condensing device 15 is passed through the second adsorption/desorption column 16 and then discharged to the atmosphere. However, in the sixth embodiment, the gasoline vapor desorbed by the air suction pump 13 by the first adsorption/desorption column 11 is pressurized by the pressure pump 14 and supplied to the fourth condensation device 51. The inside of the fourth condensing device 51 is directly cooled by the refrigerant cooled by the cold beam machine 5 to become about 3 〇 ° C. At a pressure of 0_3 MPa and a cooling temperature of -3 (the condition of rc, the gasoline vapor concentration becomes about 1 vol%. Therefore, it is directly discharged to the atmosphere. Thereby, the cost of 2118-8326-PF 28 1327164 can be simplified. Further, the second regeneration system is not required. The operation time of the pump 14 can save the energy system structure and reduce the number of devices. The air suction pump 13 and the pressure source can be reduced. The fourth condensation device 51 has the above effect. The seventh embodiment Recycling equipment capable of providing energy saving at a low cost by including an alternative to the third condensing device 15
第12圖係表示本發明之第7實施形態的氣體狀碳氣 之處理、回收裝置的流程之整體構造圖。 本第7實施形態和該第1實施形態之差異為,作成並 列地包括性旎、大小和第一吸附解吸塔i i同等之第三吸附 解吸塔61,且不需要第二吸附解吸塔16。即,在作成在第 一吸附解吸塔11吸附由第二凝結裝置1〇所排出之汽油蒸 氣,同時將由第三吸附解吸塔61所吸附的汽油蒸氣加以解 析上相異。 在第12圖,61係規格和第一吸附解吸塔u 一樣,且 籲和第一吸附解吸塔11並列地包括之第三吸附解吸塔,62a、 62b係用以將由第二凝結裝置i 〇所排出之汽油蒸氣引至第 一吸附解吸塔11或第二吸附解吸塔16的吸附用閥,63a、 63b係在由第一吸附解吸塔u或吸氣泵13將汽油蒸氣加以 解吸時使用之解吸用閥’ 64a、64b係用以將由第一吸附解 吸塔11或第三吸附解吸塔61已處理之汽油蒸氣向大氣排出 的排氣閥’ 65a、65b係在由第一吸附解吸塔π或第三吸附 解吸塔61將汽油蒸氣加以解吸時,用以向第一吸附解吸塔 11或第二吸附解吸塔61引入空氣的氣體流量調整閥。 2118'8326-PF 29 1327164 其次’說明動作。本第7實施形態所示之裝置, —般按照吸附製程、再生製 明㈣ 步驟進行。首先,說明 二附製程°在開始供油時,三通換向間3a切換至回收裝置 :卜二通換向閥3a切換後,由油罐車等經由汽油配管2向 ::儲存槽1開始供油時,汽油儲存槽i所充滿之汽油蒸氣 /飞油儲存槽1排出。此時之汽油蒸氣濃度在常溫係約 30〜杨。1%。由汽油儲存槽1所排出之汽油蒸氣,經由三通 換向闕3a’向第-凝結裝置9送氣。第—凝結裝置9藉由 利用液體循環栗8供給冷;東機5所冷卻之溫度媒質,而被間 接地冷卻。一般,第一凝結裝置9内部保持於至約, 汽油蒸氣之一部分及氣體中所含的水分凝結,並利用氣液分 離器(未圖不)等分離成氣體(汽油蒸氣)和液體(汽油)^液體 積存於第一凝結裝置9的下側,並經由汽油配管18被送至 Ά油健存槽1。 接著,將在第一凝結裝置9無法處理之約20v〇1%的汽 油蒸氣供給第二凝結裝置1 〇。第二凝結裝置1 〇藉由將冷凍 機5已冷卻之冷媒供給第二凝結裝置1〇,而被直接地冷卻。 一般’第二凝結裝置10之内部保持在由—2〇〇c至約_ 1(rc, 汽油蒸氣之一部分凝結,而分離成氣體(汽油蒸氣)和液體 (汽油)’僅排出未凝結的汽油蒸氣β液體積存於第一凝結裝 置9的下側,並經由汽油配管18被送至汽油儲存槽1。此 外’在第1實施形態,在吸附由汽油儲存槽1所排出之汽油 蒸氣時’因為未進行解吸操作,所以吸附操作結束時,停止 第二凝結裝置10之冷卻。可是,在第7實施形態,在吸附 由汽油儲存槽1所排出之汽油蒸氣時,亦由另一方之吸附解 2118-8326-PF 30 1327164 吸塔進行汽油蒸氣的解吸操作,所以在進行回收時,不會停 止第二凝結裝置1 〇之冷卻。 . 接著,將在第二凝結裝置1 〇無法處理之約8vol%的汽 /由蒸氣送至吸附解吸塔1卜61加以處理。在第12圖,表示 11作為吸附塔、61作為解吸塔動作的情況。因此,吸附用 閥62a打開(塗黑),62b處於關閉(空白)之狀態。作為吸附 塔在任意的時間進行吸附處理後,用作解吸塔。在此情況, 吸附用閥62a在關閉、62b在打開之狀態使用。又在汽油之 •解吸結束的時刻’再用作吸附塔,在時間上重複地使用該動 作。吸附、解吸之切換如上述所示,係藉由吸附用閥62a、 62b之切換而控制^在吸附解吸塔u、61封入吸附汽油蒸 氣的吸附劑。藉由汽油蒸氣通過該吸附劑中,而除去汽油成 分,變成低於lvol%之汽油濃度的清淨空氣,並經由排氣閥 64a向大氣排出。吸附解吸塔n、61和汽油蒸氣之吸附解 吸的功能無關,總是利用液體循環泵8所供給之溫度媒質冷 卻至固定溫度《即,對第一凝結裝置9及吸附解吸塔丨i、 ® 61之冷卻系統以總是保持係設定溫度的0〜5°C之方式進行 運轉控制。 其次,說明汽油蒸氣之解吸處理。在將吸附劑所吸附 之》飞油解吸的情況’利用吸氣泵13由吸附解吸塔61吸入氣 體,並由吸附劑將汽油加以解吸。此時,預先將解吸用閥 63b打開’將63a關閉。雖然在吸附時吸附塔在〇 1]y[pa之 大氣壓狀態動作’但是在解吸時因為利用吸氣泵13降壓至 大氣壓以下,所以利用該壓力差將吸附劑所吸附之汽油加以 解吸。解吸後之汽油蒸氣,利用加壓泵14加壓後,供給第 2118-8326-PF 31 1327164 三凝結裝i 15。制壓力控制器19將第三凝結裝置Μ内 部之壓力保持於0.3MPa之高壓狀態,對汽油蒸氣高效率地 進灯液化回收。由壓力控制器19所排出之汽油蒸氣回到第 二凝結M 1G,對汽油成分再度進行凝結㈣後,再回到 吸附解,塔11。在重複此操作之期間,在凝結裝置9、⑺、 15對全量之汽油進行凝結回收。 僅靠利用吸氣泵13之壓力差的解吸方法,因為其效 率不太南’所以由外部引人沖洗用氣體係有效。在本第7 實施形態’將經由氣體流量調整_咖由第一吸附解吸技 U向向大氣所排出之清淨氣體的-部分送至解吸塔61,^ 中先用氣體。在此情況,氣體流量調整閥6讣在打開狀 〜係規疋1之軋體可流通的狀態,氣體流量調整閥“a 變成關閉,而氣體不流動。 助此外,在本第7實施形態,因為 在前段之第-凝結裝置9使氣體中的含办充分低,所以沖 洗用氣體所含之水分對第三吸附解吸塔Η内之吸 無不良影響。 對加油站之汽油料^十— 绪存槽的供油一般定期地進行固定 時間。因而,產生诗、.占兮友、 'U氣這件事僅限於一天中之固定時 _ /站在>提回裝置之運轉率的觀點,本實施形態因為 同時進灯吸附操作和解吸操作所以和串列地進行吸附操作 和解吸操作,:可延長解析時間之第ι實施形態相比,可說 運轉率低可疋因為同時進行吸附操作和解吸操作,在未 =施吸附操作或解吸操作時,即在不回收汽油蒸氣的情況可 停止冷卻’而可使冷卻所 便·用之能量變少,可說是省能源機 器0Fig. 12 is a view showing the overall configuration of a flow of a process and a recovery apparatus for a gaseous carbon gas according to a seventh embodiment of the present invention. The difference between the seventh embodiment and the first embodiment is that the third adsorption/desorption column 61 having the same size and size as the first adsorption/desorption column i i is formed in parallel, and the second adsorption/desorption column 16 is not required. Namely, the gasoline vapor discharged from the second condensation device 1 is adsorbed in the first adsorption/desorption column 11, and the gasoline vapor adsorbed by the third adsorption/desorption column 61 is analyzed to be different. In Fig. 12, the 61 series specification is the same as the first adsorption desorption column u, and the third adsorption desorption column, 62a, 62b, is included in parallel with the first adsorption desorption column 11, and is used to be used by the second condensation device i. The discharged gasoline vapor is introduced to the adsorption valve of the first adsorption/desorption column 11 or the second adsorption/desorption column 16, and 63a, 63b are desorbed when the gasoline vapor is desorbed by the first adsorption/desorption column u or the getter pump 13 The valves '64a, 64b are used to discharge the gasoline vapors processed by the first adsorption desorption column 11 or the third adsorption desorption column 61 to the atmosphere, and the exhaust valves '65a, 65b are connected to the first adsorption desorption column π or When the three adsorption/desorption column 61 desorbs the gasoline vapor, a gas flow rate adjustment valve for introducing air into the first adsorption/desorption column 11 or the second adsorption/desorption column 61 is introduced. 2118'8326-PF 29 1327164 Next 'Description of action. The apparatus shown in the seventh embodiment is generally carried out in accordance with the steps of the adsorption process and the regeneration process (four). First, the second attachment process is described. When the fuel supply is started, the three-way reversing chamber 3a is switched to the recovery device: after the switching of the two-way switching valve 3a, the tanker or the like starts to the storage tank 1 via the gasoline piping 2 When the oil is supplied, the gasoline vapor/flying oil storage tank 1 filled with the gasoline storage tank i is discharged. At this time, the gasoline vapor concentration is about 30 to yang at room temperature. 1%. The gasoline vapor discharged from the gasoline storage tank 1 is supplied to the first condensing device 9 via the three-way switching enthalpy 3a'. The first condensing device 9 is cooled by the liquid circulating medium 8 to be cooled by the liquid circulating pump 8 and cooled by the ground. Generally, the inside of the first condensing device 9 is kept at about, and a part of the gasoline vapor and the moisture contained in the gas are condensed, and separated into a gas (gasoline vapor) and a liquid (gasoline) by using a gas-liquid separator (not shown) or the like. The liquid volume is stored on the lower side of the first condensing device 9, and is sent to the sputum storage tank 1 via the gasoline pipe 18. Next, about 20 v 〇 1% of the steam vapor which cannot be processed by the first condensing device 9 is supplied to the second condensing device 1 〇. The second condensing device 1 is directly cooled by supplying the refrigerant cooled by the refrigerator 5 to the second condensing device 1 。. Generally, the inside of the second condensing device 10 is maintained from -2 〇〇 c to about _ 1 (rc, part of the gasoline vapor is condensed, and separated into gas (gasoline vapor) and liquid (gasoline)' to discharge only uncondensed gasoline. The volume of the vapor β liquid is stored in the lower side of the first condensing device 9 and is sent to the gasoline storage tank 1 via the gasoline piping 18. Further, in the first embodiment, when the gasoline vapor discharged from the gasoline storage tank 1 is adsorbed, Since the desorption operation is not performed, the second coagulation device 10 is stopped at the end of the adsorption operation. However, in the seventh embodiment, when the gasoline vapor discharged from the gasoline storage tank 1 is adsorbed, the other adsorption solution 2118 is also used. -8326-PF 30 1327164 The suction tower performs the desorption operation of the gasoline vapor, so the cooling of the second condensing unit 1 is not stopped when the recovery is performed. Next, about 8 vol% which cannot be processed in the second condensing unit 1 The steam is sent to the adsorption desorption column 1 to be treated by steam. In Fig. 12, 11 is shown as the adsorption column and 61 is operated as a desorption column. Therefore, the adsorption valve 62a is opened (blackened), 62b. In the state of being closed (blank), it is used as a desorption column after being adsorbed at an arbitrary time as an adsorption tower. In this case, the adsorption valve 62a is closed and 62b is opened, and the desorption of gasoline is completed. The time is 're-used as an adsorption tower, and the operation is repeatedly used in time. The switching of adsorption and desorption is controlled by the switching of the adsorption valves 62a and 62b, and is sealed in the adsorption/desorption columns u and 61. An adsorbent that adsorbs gasoline vapor. The gasoline vapor passes through the adsorbent to remove the gasoline component, and becomes clean air having a gasoline concentration lower than 1 vol%, and is discharged to the atmosphere via the exhaust valve 64a. The adsorption desorption tower n, 61 Regardless of the function of adsorption and desorption of gasoline vapor, the temperature medium supplied by the liquid circulation pump 8 is always used to cool to a fixed temperature. That is, the cooling system for the first condensation device 9 and the adsorption desorption column 丨i, ® 61 is always The operation control is performed in such a manner that the temperature of the system is set to 0 to 5 ° C. Next, the desorption treatment of the gasoline vapor will be described. In the case of desorbing the fly oil adsorbed by the adsorbent, The getter pump 13 draws in gas from the adsorption/desorption column 61, and desorbs the gasoline by the adsorbent. At this time, the desorbing valve 63b is opened in advance to close 63a. Although the adsorption tower is in the 〇1]y [pa In the atmospheric pressure state, the gasoline adsorbed by the adsorbent is desorbed by the pressure difference due to the pressure drop to the atmospheric pressure or lower during the desorption. The desorbed gasoline vapor is pressurized by the pressurizing pump 14, Supply 2118-8326-PF 31 1327164 Three-condensing device i 15. The pressure controller 19 maintains the pressure inside the third condensing device 于 at a high pressure of 0.3 MPa, and efficiently liquefies the gasoline vapor into the lamp. The gasoline vapor discharged from the pressure controller 19 is returned to the second condensation M 1G, and the gasoline component is again coagulated (4), and then returned to the adsorption solution, the column 11. During the repetition of this operation, the coagulation device 9, (7), and 15 are coagulated and recovered for the entire amount of gasoline. The desorption method using the pressure difference of the getter pump 13 is effective because it is not too south in efficiency. In the seventh embodiment, the portion of the clean gas discharged to the atmosphere is sent to the desorption column 61 via the gas flow rate adjustment method, and the first gas is used. In this case, the gas flow rate adjusting valve 6 is in a state in which the rolling body of the opening type to the gauge 1 can flow, and the gas flow rate adjusting valve "a is closed, and the gas does not flow. Further, in the seventh embodiment, Since the first-coagulation device 9 in the preceding stage sufficiently lowers the content in the gas, the moisture contained in the flushing gas has no adverse effect on the suction in the third adsorption desorption column. The oil supply to the storage tank is generally fixed for a fixed period of time. Therefore, the production of poetry, the occupation of friends, and the 'U gas are limited to the fixed time of the day _ / standing > In the present embodiment, since the adsorption operation and the desorption operation are simultaneously performed, and the adsorption operation and the desorption operation are performed in series, the first operation example in which the analysis time can be extended can be said to have a low operation rate because the adsorption operation is performed at the same time. The desorption operation can be stopped when the adsorption operation or the desorption operation is not performed, that is, the cooling can be stopped without recovering the gasoline vapor, and the energy used for cooling can be reduced, which can be said to be an energy-saving machine.
2118-8326-PF 32 1327164 由以上之事項,藉由一面同時進行吸附操作和解吸操 作一面進行運轉’而可進行省能源、且高效率之汽油回收。 其次,說明吸附解吸塔11、61之切換。在本第7實施 形態’說明使用定時器進行吸附解吸塔11、61的切換的情 況。如上述所示,藉由汽油蒸氣通過第一吸附解吸塔丨i而 吸附並除去汽油成分,變成低於1 vol%之汽油濃度的清淨空 氣,並經由排氣閥64a向大氣排出。可是,隨著供給第—吸 附解吸塔11之汽油蒸氣量增大,而第一吸附解吸塔11的吸 •附性忐逐漸降低。此狀態持續,而在第一吸附解吸塔^ 1出 口之汽油濃度接近lv〇l%時,需要切換吸附解吸塔U、6ι。 在加油站’因為對汽油儲存槽1的供油定期地進行固定時 間,所以在開始回收後單純地根據固定時間進行切換者成為 最簡單的控制。因此,吸附解吸塔i i、61之切換,在三通 換向閥3a已切換的情況,或以回收裝置動作時為起始時間 按照固定時間切換下去係有效。又,在實際之切換動作上, 以不會產生吸附用閥62a、62b同時關閉之狀態,且汽油蒸 鲁氣總是流動之方式,實施切換的方式較佳。即,在以第一吸 附解吸塔11進行吸附、以第三吸附解吸塔61進行解吸的情 況,以將關閉之吸附用閥62b、解吸用閥63a、及排氣閥64b 設為打開狀態,接著原本打開之吸附用閥62a、解吸用閥 63b、及排氣閥64a設為關閉狀態之方式實施切換較佳。藉 此,可提供一種安全之汽油回收裝置,不會不供給吸附解吸 塔11、61汽油蒸氣,亦不會發生對汽油儲存槽1之供油速 度變慢,或汽油儲存槽i内的壓力變高。 最後,說明本第7實施形態之氣體狀碳氫的處理、回 2118-8326-PF 33 13271642118-8326-PF 32 1327164 From the above, it is possible to perform energy-saving and high-efficiency gasoline recovery by performing the operation while performing the adsorption operation and the desorption operation simultaneously. Next, the switching of the adsorption/desorption columns 11, 61 will be described. In the seventh embodiment, the case where the adsorption/desorption columns 11 and 61 are switched using a timer will be described. As described above, the gasoline vapor is adsorbed and removed by the first adsorption desorption column 丨i, and becomes a clean air having a gasoline concentration of less than 1 vol%, and is discharged to the atmosphere via the exhaust valve 64a. However, as the amount of gasoline vapor supplied to the first adsorption/desorption column 11 increases, the adsorption enthalpy of the first adsorption/desorption column 11 gradually decreases. This state continues, and when the gasoline concentration at the outlet of the first adsorption desorption column 1 is close to lv〇l%, it is necessary to switch the adsorption desorption columns U, 6ι. Since the gas station's oil supply to the gasoline storage tank 1 is regularly fixed for a fixed period of time, it is the simplest control to simply switch to a fixed time after starting the recovery. Therefore, the switching between the adsorption/desorption columns i i and 61 is effective when the three-way switching valve 3a has been switched or when the recovery device is operated as the starting time. Further, in the actual switching operation, the mode in which the suction valves 62a and 62b are not closed at the same time and the gasoline vapor is always flowing, and the switching is preferably performed. In other words, when the adsorption is performed by the first adsorption/desorption column 11 and the third adsorption/desorption column 61 is desorbed, the closed adsorption valve 62b, the desorption valve 63a, and the exhaust valve 64b are opened, and then Switching is preferably performed such that the suction valve 62a, the desorption valve 63b, and the exhaust valve 64a that are originally opened are in a closed state. Thereby, a safe gasoline recovery device can be provided, which does not supply the gasoline desorption tower 11, 61 gasoline vapor, nor does the oil supply speed to the gasoline storage tank 1 slow down, or the pressure in the gasoline storage tank i changes. high. Finally, the treatment of gaseous hydrocarbons in the seventh embodiment will be described, and the return 2118-8326-PF 33 1327164
收裝置之控制方法。回收裝置停止時,吸氣泵13或加壓果 Μ停止,吸附用閥62a、62b、解吸用閥心、631)、及排氣 閥料…處於全閉狀態,而氣體流量調整閥65a、65b處 於關閉狀態。三通換向閥3a切換,而開始供油時,收到運 轉信號,例如,收到三通換向閥3a之切換信號,吸附用閥 62a解吸用閥63b、及排氣間㈣變成打開狀態,^ & 儲存槽1開始供油,而汽油蒸氣流人第—凝結農置9、第二 凝結裝置ίο、及第一吸附解吸塔u。吸氣泉13及加壓泵 14和吸附操作之開始同時地運轉。藉由吸氣栗13之運轉, 而第三吸附解料61之壓力降至既定壓力時,氣體流量調 整閥⑽開始打開’以既定之流量流向第三吸附解吸塔Μ 之方式控制氣體流量調整閥65b的開度。 “ 依以上之方式,繼續供油固定時間後,實施吸附解吸 :61之切換。由定時器等收到切換信號時,如上述所 示’關閉之吸附用閥62b、解吸用閥63a、及排氣閥_變 成打開狀態’氣體流量調整閥65b變成關閉狀態。接著,吸 附用闊仏、解吸用閱63b、及排氣閥64a變成打開狀態, 第三吸附解吸塔61變成吸附操作,而第-錢解吸塔U 變成解吸操作。藉由吸氣泵13之運轉,而第三吸附解吸塔 61之壓力降至既疋壓力時’氣體流量調整閥開始打開, 以既定之流量流向第三吸附解吸塔61之方式控制氣體流量 調整閥65b的開度。按照這種步驟重複進行切換運轉,對汽 油儲存槽1之供油機停止時,三通換向㈤3“刀換,收到停 止信號後’吸氣泵13或加壓泵14停止,氣體流量調整閥 65b變成關閉狀態’而吸附用閥62&、解吸用閥㈣、及排The control method of the receiving device. When the recovery device is stopped, the intake pump 13 or the pressurized fruit juice is stopped, the adsorption valves 62a and 62b, the desorption valve core, 631), and the exhaust valve material are in a fully closed state, and the gas flow rate adjustment valves 65a and 65b are closed. Is off. When the three-way switching valve 3a is switched, an operation signal is received, for example, a switching signal of the three-way switching valve 3a is received, and the suction valve 62a desorbing valve 63b and the exhaust gas (four) are turned on. , ^ & storage tank 1 starts to supply oil, and gasoline vapor flow first - condensing farm 9, second condensing device ίο, and first adsorption desorption tower u. The suction spring 13 and the pressure pump 14 are operated simultaneously with the start of the adsorption operation. By the operation of the suction pump 13, and the pressure of the third adsorption solution 61 is lowered to a predetermined pressure, the gas flow adjustment valve (10) starts to open to control the gas flow adjustment valve by a predetermined flow rate to the third adsorption desorption column. The opening of 65b. "According to the above method, after the fuel supply is fixed for a fixed period of time, the adsorption desorption: 61 is switched. When the switching signal is received by the timer or the like, the closed adsorption valve 62b, the desorption valve 63a, and the row are closed as described above. The gas valve _ is in an open state, and the gas flow rate adjustment valve 65b is in a closed state. Then, the adsorption bleeder, the desorption reading 63b, and the exhaust valve 64a are turned on, and the third adsorption/desorption column 61 becomes an adsorption operation, and the first - The money desorption column U becomes a desorption operation. By the operation of the getter pump 13, and the pressure of the third adsorption desorption column 61 is reduced to the same pressure, the gas flow regulating valve starts to open, and flows to the third adsorption desorption column at a predetermined flow rate. In the manner of 61, the opening degree of the gas flow regulating valve 65b is controlled. According to this step, the switching operation is repeated, and when the fuel supply of the gasoline storage tank 1 is stopped, the three-way reversing (five) 3 "knife change, after receiving the stop signal" sucks The air pump 13 or the pressure pump 14 is stopped, the gas flow rate adjustment valve 65b is turned off, and the adsorption valve 62 & the desorption valve (four), and the row
2118-8326-PF 34 氣閥64a變成關閉狀態。 如以上所示’本第7實施形態之氣體狀碳氫的處理、 回收裝置’因為由2個溫度帶之凝結裝置9、1〇和吸附解吸 塔11、61組合而成’排出最多亦僅lv〇1%之汽油蒸氣,係 環境負載很小的氣體狀碳氫之處理、回收裝置。又,因為排 出最多亦僅lvol%之汽油蒸氣,可回收4〇ν〇ι%的汽油蒸氣 之中的39%,回收效率為97 5% ’係效率很高的回收裝置。 又’因為作成進行凝結操作後進行吸附操作,所以可使吸附 解吸塔11、61變成小型,亦具有可使裝置整體小型化之效 果。此外,因為同時進行吸附操作和解吸操作,所以可減少 無益之運轉,可降低運轉費用。 第8實施形態 第13圖係表示本發明之第8實施形態的氣體狀碳氫 之處理、回收裝置的流程之整體構造圖。 本第8實施形態和該第7實施形態之差異為在第一吸 附解吸塔11的再生時之氣體處理的流程相異。又,在構成 機器上’在第8實施形態’如第13圖所示,未包括在第u 圖之加壓泵14、第三凝結裝置15、及壓力控制器19。 在第7實施形態’由第三吸附解吸塔61利用吸氣泵 13解吸後的汽油蒸氣,利用加壓泵14加壓後,供給第三凝 結裝置15。通過第三凝結裝置15之汽油蒸氣,通過第二凝 結裝置10及第一吸附解吸塔11後向大氣排出。可是,在第 8實施形態,由第一吸附解吸塔u利用吸氣泵13解吸後的 汽油蒸氣,供給第一凝結裝置9。在第一凝結裝置9,和由 汽油儲存槽1所排出之汽油蒸氣合流,並通過第一凝結装置 2118-8326-PF 35 1327164 9及第-吸附解吸塔U後向大氣排出。藉此,可簡化系統 構造,並降低裝置之費用。 • 由以上之事項,藉由刪除加壓泵14、第三凝結裝置 15、及壓力㈣胃19,而具有可提供低費用且省能源的回 ' 收裝置。 ' 第9實施形態 . 第14圖係表示本發明之第9實施形態的氣體狀碳氫 之處理、回收裝置的流程之整體構造圖。 本第9實施形態和該第7實施形態之差異為在第一吸 附解吸塔11的再生時之氣體處理的流程相異。又,在構成 機器上,在第7實施形態,如第12圖所示,利用溫度媒質 將第三凝結裝置15之内部冷卻至〇〜5。〇,但是在本第9實 施形態,如第14圖所示,包括作成由冷凍機5利用冷媒可 直接冷卻之第四凝結裝置51。 在第7實施形態’由第一吸附解吸塔u利用吸氣泵 13已解吸之Ά油蒸氣’利用加壓泵14加壓後’供給第三凝 •結裝置15。通過第三凝結裝置15之汽油蒸氣,再通過第二 凝結裝置10及第一吸附解吸塔U後向大氣排出。可是,在 第9實施形態,由第一吸附解吸塔丨丨利用吸氣泵13已解吸 之汽油蒸氣’利用加壓泵14加壓後,供給第四凝結裝置51。 利用冷凍機5所冷卻之冷媒直接冷卻第四凝結裝置51的内 部,而變成約一30°C。在壓力〇_3MPa、冷卻溫度一30°C之 條件,汽油蒸氣濃度變成約lv〇l%,並供給第一吸附解吸塔 11。藉此’可減少第一吸附解吸塔丨i所吸附並除去之汽油 蒸氣量,並可增長吸附解吸塔11、61之切換時間,而可延 2118-8326-PF 36 1327164 長間之奇命。又,m认 人因為可減少闊之切換次數,可實現更安 的運轉。 由以上之事項,藉由包括替代第三凝結裝置15之第 四凝結裝置5 1,a a 具有可提供低費用、可靠性高的回收裝置。 【圖式簡單說明】 第1圖係表示本發明之第1實施形態的氣體狀碳氫之 處理、回收震置的流程之整體構造圖。2118-8326-PF 34 The air valve 64a is turned off. As described above, the treatment and recovery device for gaseous hydrocarbons in the seventh embodiment is a combination of two condensation devices 9 and 1 in the temperature zone and the adsorption/desorption columns 11 and 61. 〇 1% of gasoline vapor is a treatment and recovery device for gaseous hydrocarbons with little environmental load. In addition, since only up to 1 vol% of gasoline vapor is discharged, 39% of the 4 ν ν% of gasoline vapor can be recovered, and the recovery efficiency is 97 5%, which is a highly efficient recovery device. Further, since the adsorption operation is performed after the coagulation operation is performed, the adsorption/desorption columns 11 and 61 can be made small, and the entire device can be miniaturized. In addition, since the adsorption operation and the desorption operation are simultaneously performed, the unhelpful operation can be reduced, and the running cost can be reduced. (Embodiment 8) FIG. 13 is a view showing an overall configuration of a flow of a gaseous hydrocarbon processing and recovery apparatus according to an eighth embodiment of the present invention. The difference between the eighth embodiment and the seventh embodiment is that the flow of the gas treatment at the time of regeneration of the first adsorption/desorption column 11 is different. Further, in the configuration of the eighth embodiment, as shown in Fig. 13, the pressure pump 14, the third condensing device 15, and the pressure controller 19 are not included in the drawing. In the seventh embodiment, the gasoline vapor desorbed by the air suction pump 13 by the third adsorption/desorption column 61 is pressurized by the pressure pump 14, and then supplied to the third condensation device 15. The gasoline vapor passing through the third condensing device 15 is discharged to the atmosphere through the second condensing device 10 and the first adsorption/desorption column 11. However, in the eighth embodiment, the gasoline vapor desorbed by the air suction pump 13 by the first adsorption/desorption column u is supplied to the first condensation device 9. The first coagulation device 9 merges with the gasoline vapor discharged from the gasoline storage tank 1, and is discharged to the atmosphere through the first coagulation device 2118-8326-PF 35 1327164 9 and the first adsorption desorption column U. This simplifies system construction and reduces the cost of the unit. • From the above, by removing the pressurizing pump 14, the third condensing device 15, and the pressure (four) stomach 19, there is a low-cost and energy-saving returning device. [Embodiment 9] Fig. 14 is a view showing an overall configuration of a flow of a gaseous hydrocarbon processing and recovery apparatus according to a ninth embodiment of the present invention. The difference between the ninth embodiment and the seventh embodiment is that the flow of the gas treatment at the time of regeneration of the first adsorption/desorption column 11 is different. Further, in the configuration of the seventh embodiment, as shown in Fig. 12, the inside of the third condensing device 15 is cooled to 〇5 by the temperature medium. In the ninth embodiment, as shown in Fig. 14, the fourth condensing device 51 which is directly cooled by the refrigerator 5 by the refrigerant is formed. In the seventh embodiment, the sputum oil vapor desorbed by the air suction pump 13 by the first adsorption/desorption column u is pressurized by the pressurizing pump 14, and then supplied to the third condensing device 15. The gasoline vapor passing through the third condensing device 15 is discharged to the atmosphere through the second condensing device 10 and the first adsorption/desorption column U. However, in the ninth embodiment, the gasoline vapor desorbed by the air suction pump 13 by the first adsorption/desorption tower is pressurized by the pressure pump 14, and then supplied to the fourth condensation device 51. The inside of the fourth condensing device 51 is directly cooled by the refrigerant cooled by the refrigerator 5 to become about 30 °C. The gasoline vapor concentration becomes about lv 〇 1% under the conditions of a pressure of 〇 3 MPa and a cooling temperature of 30 ° C, and is supplied to the first adsorption/desorption column 11 . Thereby, the amount of gasoline vapor adsorbed and removed by the first adsorption desorption column 丨i can be reduced, and the switching time of the adsorption desorption columns 11, 61 can be increased, and the long life of 2118-8326-PF 36 1327164 can be extended. In addition, m recognizes that it can achieve a safer operation because it can reduce the number of switching times. From the above, the fourth condensing device 5 1, a a including the third condensing device 15 is provided with a recovery device which can provide low cost and high reliability. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 is a view showing an overall configuration of a process for treating and recovering a gaseous hydrocarbon according to a first embodiment of the present invention.
第2圖係表示冷卻溫度和矽膠充填量之關係的特性 圖。 第3圖係用以說明沖洗用氣體量之控制方法的特性 圖。 第4圖係表示處理氣體流量和回收率之關係的特性 圖。 第5圖係表示内部壓力和矽膠充填量之關係的特性 圖。 第6圖係表示本發明之第1實施形態的氣體狀碳氫之 處理、回收裝置的流程之整體構造圖。 第7圖係表示本發明之第2實施形態的氣體狀碳氫之 處理、回收裝置的流程之整體構造圖。 第8圖係表示本發明之第3實施形態的氣體狀碳氫之 處理、回收裝置的流程之整體構造圖。 第9圖係表示本發明之第*實施形態的氣體狀碳氩之 處理、回收裝置的流程之整體構造圖。 第1〇圖係表示本發明之第5實施形態的氣體狀碳氫 2118-8326-PF 37 LU^f 之處理、回收裝置的流程之整體構造圖。 第U圖係表不本發明之第6實施形態的氣體狀碳氫之 處理、回收裝置的流程之整體構造圖。 第12圖係表示本發明之第7實施形態的氣體狀碳氫 之處理、回收裝置的流程之整體構造圖。 第13圖係表示本發明之第8實施形態的氣體狀碳氫 之處理、回收裝置的流程之整體構造圖。 第14圖係表示本發明之第9實施形態的氣體狀碳氫 之處理、回收裝置的流程之整體構造圖。 【主要元件符號說明】 1 汽油儲存槽 2 供油管 3 二通換向閥 4 調壓閥 5 冷凍機 6 熱交換器 7 溫度媒質槽 8 液體循環系· 9 第一凝結裝置 10 第二凝結裝置 11 第一吸附解吸塔 12 二路閥 13 吸氣泵 14 加壓果 15 第三凝結裝置 16 第二吸附解吸塔 17 流量調整閥 18 汽油配管 19 壓力控制器 21 閥 31 壓力緩衝容器 32 壓力量測器 41 氣體儲存容器 42 主流量控制器 43 斷流閥 51 第四凝結裝置 61 第三吸附解吸塔 62 吸附用閥 63 65 解吸用閥 氣體流量調整閥 64排氣閥 2118-8326-PF 38Fig. 2 is a characteristic diagram showing the relationship between the cooling temperature and the amount of silicone filling. Fig. 3 is a characteristic diagram for explaining a method of controlling the amount of gas for flushing. Fig. 4 is a characteristic diagram showing the relationship between the flow rate of the treatment gas and the recovery rate. Fig. 5 is a characteristic diagram showing the relationship between the internal pressure and the amount of silicone filling. Fig. 6 is a view showing the overall configuration of the flow of the gaseous hydrocarbon processing and recovery apparatus according to the first embodiment of the present invention. Fig. 7 is a view showing the overall configuration of the flow of the gaseous hydrocarbon processing and recovery apparatus according to the second embodiment of the present invention. Fig. 8 is a view showing the overall configuration of the flow of the gaseous hydrocarbon processing and recovery apparatus according to the third embodiment of the present invention. Fig. 9 is a view showing the overall configuration of a flow of a gaseous carbon argon treatment and recovery apparatus according to a fourth embodiment of the present invention. Fig. 1 is a view showing the overall structure of a process for treating and recovering gaseous hydrocarbons 2118-8326-PF 37 LU^f according to the fifth embodiment of the present invention. Fig. U is a view showing the overall configuration of the flow of the gaseous hydrocarbon processing and recovery apparatus according to the sixth embodiment of the present invention. Fig. 12 is a view showing the overall configuration of the flow of the gaseous hydrocarbon processing and recovery apparatus according to the seventh embodiment of the present invention. Fig. 13 is a view showing the overall configuration of the flow of the gaseous hydrocarbon processing and recovery apparatus according to the eighth embodiment of the present invention. Fig. 14 is a view showing the overall configuration of the flow of the gaseous hydrocarbon processing and recovery apparatus according to the ninth embodiment of the present invention. [Main component symbol description] 1 Gasoline storage tank 2 Oil supply pipe 3 Two-way switching valve 4 Pressure regulating valve 5 Freezer 6 Heat exchanger 7 Temperature medium tank 8 Liquid circulation system · 9 First condensation device 10 Second condensation device 11 First adsorption desorption tower 12 Two-way valve 13 Suction pump 14 Pressurized fruit 15 Third condensation device 16 Second adsorption desorption tower 17 Flow adjustment valve 18 Gasoline piping 19 Pressure controller 21 Valve 31 Pressure buffer container 32 Pressure measurement 41 gas storage container 42 main flow controller 43 shut-off valve 51 fourth coagulation device 61 third adsorption desorption column 62 adsorption valve 63 65 desorption valve gas flow adjustment valve 64 exhaust valve 2118-8326-PF 38
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KR101215211B1 (en) * | 2008-03-28 | 2012-12-24 | 가부시키가이샤 다쯔노 | Gaseous hydrocarbon treating/recovering apparatus and method |
JP2008238171A (en) * | 2008-06-06 | 2008-10-09 | Mitsubishi Electric Corp | Method for treating/recovering gaseous hydrocarbon |
JP2009028723A (en) * | 2008-09-08 | 2009-02-12 | Mitsubishi Electric Corp | Method for treating and recovering gaseous hydrocarbon |
JP5693448B2 (en) * | 2009-03-31 | 2015-04-01 | 三菱電機株式会社 | Gaseous hydrocarbon recovery apparatus and method |
CN102441310A (en) * | 2010-10-12 | 2012-05-09 | 中国石油化工股份有限公司 | Method for recovering oil gas and device |
CN103952173A (en) * | 2014-05-22 | 2014-07-30 | 青岛科技大学 | Oil gas recovery device |
CN103965943A (en) * | 2014-05-22 | 2014-08-06 | 青岛科技大学 | Oil gas recovering method |
CN105031962A (en) * | 2015-08-31 | 2015-11-11 | 常州大学 | Novel methyl alcohol waste gas recovery system adopting condensation and adsorption integration technology |
JP6337921B2 (en) * | 2016-06-15 | 2018-06-06 | 株式会社タツノ | Vapor collection device |
WO2018014221A1 (en) * | 2016-07-19 | 2018-01-25 | 深圳市尚佳能源网络有限责任公司 | Low-temperature condensation oil vapor recovery system |
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TW460314B (en) * | 1997-09-10 | 2001-10-21 | System Eng Service Co Ltd | Process for processing waste gases containing gaseous hydrocarbons and recovering the hydrocarbons as liquid |
KR100228536B1 (en) * | 1997-12-30 | 1999-11-01 | 윤명조 | Volatile organic vapour recovery system |
KR100287321B1 (en) * | 1998-09-01 | 2001-06-01 | 윤명조 | Volatile organic vapor prevention and recovery device |
US20050109207A1 (en) * | 2003-11-24 | 2005-05-26 | Olander W. K. | Method and apparatus for the recovery of volatile organic compounds and concentration thereof |
JP4671772B2 (en) * | 2004-12-22 | 2011-04-20 | 三菱電機株式会社 | Apparatus and method for treating and recovering gaseous hydrocarbons |
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KR20070104193A (en) | 2007-10-25 |
TWI381879B (en) | 2013-01-11 |
TW200916182A (en) | 2009-04-16 |
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