KR100220576B1 - Low pressure ethanol psa drying device using carbon dioxide - Google Patents

Low pressure ethanol psa drying device using carbon dioxide Download PDF

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KR100220576B1
KR100220576B1 KR1019970005142A KR19970005142A KR100220576B1 KR 100220576 B1 KR100220576 B1 KR 100220576B1 KR 1019970005142 A KR1019970005142 A KR 1019970005142A KR 19970005142 A KR19970005142 A KR 19970005142A KR 100220576 B1 KR100220576 B1 KR 100220576B1
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ethanol
carbon dioxide
low pressure
pressure
adsorption
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KR1019970005142A
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KR19980068513A (en
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현건호
주창업
박융호
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양인모
삼성엔지니어링주식회사
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/02Separation 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
    • B01D53/04Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047Pressure swing adsorption
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/26Drying gases or vapours
    • B01D53/261Drying gases or vapours by adsorption

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Abstract

본 발명은 연료용 알코올로 사용되는 고순도 알코올(99.5

Figure kpo00001
이상)을 얻기 위해 증류탑에서 얻어지는 에탄올과 공비혼합물(92-95
Figure kpo00002
)로부터 선택적 흡착방법에 의해 물을 추가적으로 제거시키기 위하여 제올라이트(Zeolite)흡착제를 이용하여 압력스윙 흡착방식으로 에탄올을 탈수시키는 공정에서, 저압에서 물의 탈착을 돕기 위해 이미 건조된 에탄올의 일부를 다시 흡착층(Adsorption Bed)으로 흘러 보내서 퍼지(Purge)시키는데, 이러한 퍼지용 에탄올을 이산화탄소로 대체하며 수율의 감소를 방지하고 공정의 경제성을 향상시킨 이산화탄소를 이용한 저압식 에탄올 압력스윙흡착 탈수장치에 관한 것으로, 원료기체흐름(1)에 이산화탄소 재순환흐름(2)을 더하여 흡착층(5)에서 흡착시키고 건조된 이산화탄소를 재생과정의 흡착층(10)에 보내 퍼지를 돕도록 하며, 퍼지된 기체흐름에서 묽은 에탄올 용액을 응축제거한 후 얻어진 이산화탄소를 진공펌프(14)와 송풍기(16)를 거쳐 압축시킨 후 다시 원료기체와 혼합시키는 것이다.The present invention is a high purity alcohol (99.5) used as a fuel alcohol
Figure kpo00001
Ethanol and azeotrope (92-95)
Figure kpo00002
In the process of dehydrating ethanol by pressure swing adsorption using a zeolite adsorbent to further remove water by the selective adsorption method, a portion of the already dried ethanol is re-adsorbed to assist the desorption of water at low pressure. The present invention relates to a low pressure ethanol pressure swing adsorption dehydration device using carbon dioxide, which replaces the purge ethanol with carbon dioxide and prevents a decrease in yield and improves the economics of the process. The carbon dioxide recycle stream (2) is added to the gas stream (1) to adsorb in the adsorption layer (5) and to send the dried carbon dioxide to the adsorption layer (10) during the regeneration process to assist purge, and dilute ethanol solution in the purged gas stream. After condensation removal, the obtained carbon dioxide is compressed through a vacuum pump (14) and a blower (16), and then again. It is to mix with the gas exit.

Description

이산화탄소를 이용한 저압식 에탄올 압력스윙 흡착 탈수장치Low Pressure Ethanol Pressure Swing Adsorption Dewatering System Using Carbon Dioxide

본 발명은 연료용 알코올로 사용되는 고순도 알코올(99.5

Figure kpo00004
이상)을 얻기 위해, 증류탑에서 얻어지는 에탄올과 공비혼합물(92-95
Figure kpo00005
)로부터 선택적 흡착방법에 의해 물을 추가적으로 제거시키기 위하여 제올라이트(Zeolite)흡착제를 이용하여 압력스윙 흡착방식으로 에탄올을 탈수시키는 공정에서, 저압에서 물의 탈착을 돕기 위해 이미 건조된 에탄올의 일부를 다시 흡착층(Adsorption Bed)으로 흘려 보내서 퍼지(Purge)시키는데, 이러한 퍼지용 에탄올을 이산화탄소로 대체하며 수율의 감소를 방지하고 공정의 경제성을 향상시킨 이산화탄소를 이용한 저압식 에탄올 압력스윙 흡착 탈수장치에 관한 것이다.The present invention is a high purity alcohol (99.5) used as a fuel alcohol
Figure kpo00004
To obtain an azeotrope (92-95)
Figure kpo00005
In the process of dehydrating ethanol by pressure swing adsorption using a zeolite adsorbent to further remove water by the selective adsorption method, a portion of the already dried ethanol is re-adsorbed to assist the desorption of water at low pressure. The present invention relates to a low pressure ethanol pressure swing adsorption dehydration apparatus using carbon dioxide which replaces the purge ethanol with carbon dioxide and prevents a decrease in yield and improves the economics of the process.

종래의 미국 특허(US 4,407,662) 에탄올 흡착 탈수장치는 에탄올 용액을 가열하여 과열증기로 만든 다음 이를 결정형 3A 제올라이트로 구성된 흡착층을 통과시켜 건조시키며 흡착에 사용된 흡착층은 다시 물을 탈착 재생시켜 사용하게 되는데, 흡착층의 재생시에는 흡착층의 압력을 저하시키고 나아가 물 이외의 다른성분 즉 건조된 에탄올을 흡착층으로 다시 흘려 보내 주므로써 흡착층 내 물의 분압을 낮추어 주게된다.Conventional US patent (US 4,407,662) ethanol adsorption dehydrator is heated by heating the ethanol solution to make a superheated steam and then dried by passing through the adsorption layer consisting of crystalline 3A zeolite, the adsorption layer used for adsorption is used to desorb and regenerate water again At the time of regeneration of the adsorption layer, the pressure of the adsorption layer is lowered, and further, other components other than water, ie, dried ethanol, are flowed back into the adsorption layer to lower the partial pressure of water in the adsorption layer.

상기한 흡착층 재생과정 중에 원료용액 중의 30

Figure kpo00006
이상에 해당하는 에탄올이 손실되는 것이 종래 공정의 경제성을 저하시키는 요인이 되고 있다.30 in the raw material solution during the adsorption layer regeneration process
Figure kpo00006
The loss of ethanol corresponding to the above is a factor that lowers the economics of the conventional process.

흡착층 재생과정에 퍼지용 물질로서 건조된 에탄올 증기 대신 다른 대체물질을 사용한다면 퍼지과정중의 에탄올 손실을 막을수 있을 것이나 아직 저압 에탄올 흡착 탈수공정에는 이러한 일이 아직 실행된 바가 없다.The use of other substitutes instead of dried ethanol vapor as the purge material in the adsorption bed regeneration process will prevent ethanol loss during the purge process, but this has not yet been done in the low pressure ethanol adsorption dehydration process.

에탄올 흡착 탈수공정에서 퍼지 대체물질로서 이산화탄소가 사용된 것으로 미국특허(US 4,273,621)가 있으나 공정은 3기압 이상 7기압 정도의 고압에서 수행되는 흡착공정으로 고압의 증류공정에 연결되어 운전되는데 고압의 증류공정에 따르는 장치비, 고압의 에탄올 과열증기를 만드는데 소요되는 연료비, 이산화탄소를 다시 고압으로 압축시키는 데 사용되는 압축기의 장치비 및 운전비 등의 부수적인 문제점이 있으며, 이러한 공정은 75

Figure kpo00007
농도의 에탄올 용액을 농축시켜 90
Figure kpo00008
정도의 용액을 만드는 것으로서 99.5
Figure kpo00009
의 연료용 알코올을 생산하는데는 적합하지 못한 것으로 판단된다.Carbon dioxide is used as a purge substitute in the ethanol adsorption dehydration process, and there is a US patent (US 4,273,621). However, the process is an adsorption process performed at high pressure of 3 to 7 atm. There are additional problems such as the equipment cost according to the process, the fuel cost for making high-pressure ethanol superheated steam, the equipment cost of the compressor used to compress carbon dioxide back to high pressure, and the operating cost.
Figure kpo00007
Concentrate the ethanol solution at 90
Figure kpo00008
99.5 by making a solution
Figure kpo00009
It is not suitable to produce alcohol for fuel.

그리고 상기한 특허 공정에서는 이산화탄소와 에탄올 증기혼합물중 이산화탄소가 80

Figure kpo00010
나 차지하므로서 흡착층을 지나는 기체의 선속도가 과다하게 높아지고 결과적으로 흡착층의 흡착능(Adsorption Capacity)이 크게 저하되므로 장치의 크기가 커지게 되는 문제점을 안고 있다.In the above patented process, carbon dioxide in the carbon dioxide and ethanol vapor mixture is 80
Figure kpo00010
As a result, the linear velocity of the gas passing through the adsorption layer is excessively increased, and as a result, the adsorption capacity of the adsorption layer is greatly reduced, thereby increasing the size of the device.

따라서 본 발명은 상기한 종래의 문제점을 개선하기 위한 목적으로 창출된 것으로, 흡착시 저압을 유지하여 고압운전에 따르는 문제점을 피하면서도 흡착상의 퍼지과정에 사용되는 에탄올 증기를 이산화탄소로 대치하여 그 손실을 막는 생산방법을 제공하기 위한 것이다.Therefore, the present invention was created for the purpose of improving the above-mentioned conventional problems, while maintaining the low pressure during the adsorption, avoiding the problems caused by high pressure operation, while replacing the ethanol vapor used in the purge process of the adsorption phase with carbon dioxide to reduce the loss. The membrane is to provide a production method.

상기한 장치를 제공하기 위한 수단으로 종래의 저압식 흡착탈수 공정내에 소량의 이산화탄소를 주입하여 흡착층의 퍼지에 사용하고 사용된 이산화탄소를 다시 물과 에탄올 용액으로부터 분리하고 건조한 후 흡착층의 재생에 순환적으로 사용할 수 있는 공정을 제공하는 것이다.As a means for providing the above apparatus, a small amount of carbon dioxide is injected into a conventional low pressure adsorption dehydration process to purge the adsorption layer, and the used carbon dioxide is separated from the water and ethanol solution, dried and circulated for regeneration of the adsorption layer. It is to provide a process that can be used as an alternative.

제1도는 본 발명의 공정장치를 나타낸 흐름도.1 is a flow chart showing a process apparatus of the present invention.

* 도면의 주요부분에 대한 부호의 설명* Explanation of symbols for main parts of the drawings

1 : 원료흐름 2 : 이산화탄소 재순환흐름1: material flow 2: carbon dioxide recycle flow

3,6,9,11,17,18,19,20 : 개폐변3,6,9,11,17,18,19,20: opening and closing side

5,10 : 흡착층 7,12 : 냉각기5,10: adsorption layer 7,12: cooler

8,13,15 : 기액분리기 14 : 진공펌프8, 13, 15: gas-liquid separator 14: vacuum pump

16 : 송풍기16: blower

이하 발명의 요지를 첨부된 도면에 연계시켜 그 구성과 작용을 상세히 설명하면 다음과 같다.Hereinafter, the configuration and operation of the present invention will be described in detail with reference to the accompanying drawings.

제1도에서 원료 에탄올 기체흐름(1)은 에탄올 발효공정에서 생성되어 증류공정에서 92-95

Figure kpo00011
로 정제된 에탄올을 과열기(Superheater)에서 가열하여 얻어지는 것으로서 1.2-2기압의 압력과 100-140
Figure kpo00012
의 온도를 가지고 있으며 재생분리된 이산화탄소 흐름(2)과 합쳐져서 개폐변(3)과 인입관(4)을 통과하여 흡착층(5)으로 유입되며 흡착층(5)에서 흐름중의 물이 흡착됨에 따라 건조된 에탄올증기와 이산화탄소는 개폐변(6)과 냉각기(7)에서 냉각된 후 기액분리기(8)에서 에탄올 용액과 이산화탄소 기체로 분리되며 이산화탄소 기체는 개폐변(9)을 통과하여 흡착층(10)의 퍼지과정에 사용되게 된다.In Figure 1, the raw ethanol gas stream (1) is produced in the ethanol fermentation process and is 92-95 in the distillation process.
Figure kpo00011
Obtained by heating the purified ethanol in a superheater, and the pressure of 1.2-2 atm and 100-140
Figure kpo00012
It is combined with the regenerated separated carbon dioxide stream (2) and passes through the opening / closing valve (3) and the inlet pipe (4) to enter the adsorption layer (5). The ethanol vapor and carbon dioxide dried according to the present invention are cooled in the open / close valve 6 and the cooler 7, and then separated into an ethanol solution and a carbon dioxide gas in the gas-liquid separator 8, and the carbon dioxide gas passes through the open / close valve 9 and the adsorption layer 10) to be used in the purge process.

상기한 퍼지과정 중에는 흡착층(10)으로부터 물의 탈착을 돕기 위하여 0.1-0.4기압의 낮은 기압을 유지하게 되며 흡착층(10)으로부터 나온 이산화탄소, 물, 에탄올은 개폐변(11)을 거쳐 냉각기(12)에서 냉각된 후 기액분리기(13)로 들어가 에탄올용액과 이산화탄소가 주성분인 기체로 분리되게 된다.During the purge process, a low pressure of 0.1 to 0.4 atm is maintained to assist the desorption of water from the adsorption layer 10. The carbon dioxide, water, and ethanol from the adsorption layer 10 pass through the opening and closing side 11 to cool the cooler 12 After cooling in the) into the gas-liquid separator (13) is separated into a gas ethanol solution and carbon dioxide as the main component.

기체흐름은 공정내 압력을 저압으로 만들기 위한 진공펌프(14)를 거쳐 기액분리기(15)로 다시 들어가 기체흐름 중에 포함되었던 일부 물과 에탄올 성분을 용액으로 제거시키고 송풍기(16)를 거치면서 2기압 정도의 압력을 얻게된다.The gas flow enters the gas-liquid separator 15 through a vacuum pump 14 for lowering the in-process pressure to a low pressure, removes some water and ethanol contained in the gas stream as a solution, and passes through a blower 16 at 2 atmospheres. You get a degree of pressure.

여기서 필요한 경우 이산화탄소를 추가적으로 공급할 수 있으며 이때 이산화탄소는 앞서 에탄올 발효과정에서 얻어진 것을 활용할 수 있다.In this case, carbon dioxide may be additionally supplied if necessary, and carbon dioxide may be used in the ethanol fermentation process.

송풍기(16)에서 나온 기체흐름은 주로 이산화탄소로 구성되어 있으며 원료에탄올 기체와 함게 다시 흡착공정으로 들어가 건조된 후 흡착층의 탈착 재생에 퍼지물질로서 활용하게 된다.The gas flow from the blower 16 is mainly composed of carbon dioxide, which is dried together with the raw ethanol gas to be adsorbed and dried, and then used as a purge material for desorption and regeneration of the adsorption layer.

그리고 사용되지 않았던 개폐변(17)(18)(19)(20)들은 흡착층의 순환주기가 바뀌면 앞서 개폐변(3)(6)(9)(11)들이 수행하였던 역할을 맡으면서 흐름이 반전되게 된다.And the opening and closing valves 17, 18, 19, and 20 that are not used have the role that the opening and closing valves 3, 6, 9, and 11 previously performed when the circulation cycle of the adsorption layer was changed. Will be reversed.

본 발명에서는 이산화탄소의 순환적 사용에 의해 흡착층의 퍼지물질로 사용되던 에탄올 증기를 절약하여 결과적으로 공정수율을 향상시킬 뿐만아니라 종래 상용공정들과 같이 저압에서 운전되므로 공정비율을 절감시킬수 있는 효과가 있는 것이다.In the present invention, by reducing the ethanol vapor used as the purge material of the adsorption layer by the cyclic use of carbon dioxide to improve the process yield, as well as operating at low pressure as in conventional commercial processes, the effect of reducing the process ratio It is.

Claims (5)

증류탑에서 얻어지는 92-95
Figure kpo00013
의 에탄올을 탈수시켜 99.5
Figure kpo00014
이상의 연료용 알코올을 생산하기 위한 공정에 있어서, 저압에서 에탄올 증기를 결정형 3A 제올라이트로 구성된 흡착층을 통과시켜 건조시키며, 이산화탄소를 퍼지용 흡착물질로 사용하여 에탄올 회수율을 향상시킬수 있는 것을 특징으로 하는 이산화탄소를 이용한 저압식 에탄올 압력스윙 흡착 탈수장치.
92-95 from distillation column
Figure kpo00013
Dehydrate ethanol 99.5
Figure kpo00014
In the process for producing the above alcohol for fuel, ethanol vapor at low pressure passing through the adsorption layer consisting of crystalline 3A zeolite and dried, carbon dioxide, characterized in that to improve the ethanol recovery by using carbon dioxide as the adsorption material for purge Low pressure ethanol pressure swing adsorption dehydration device using.
제1항에 있어서 저압은 0.1-2기압의 압력을 스윙하면서 운전하는 것을 특징으로 하는 이산화탄소를 이용한 저압식 에탄올 압력스윙 흡착 탈수장치.The low pressure ethanol pressure swing adsorption dewatering device using carbon dioxide according to claim 1, wherein the low pressure is operated while swinging a pressure of 0.1-2 atmospheres. 제1항에 있어서 흡착층을 통과한 에탄올을 일부 퍼지시키는 대신, 기액분리기에서 에탄올을 분리시켜 낸 후 얻어지는 기상의 이산화탄소를 흡착층으로 보내 퍼지에 사용하는 것을 특징으로 하는 이산화탄소를 이용한 저압식 에탄올 압력스윙 흡착 탈수장치.The low pressure ethanol pressure using carbon dioxide according to claim 1, wherein instead of purging a portion of the ethanol that has passed through the adsorption layer, the gaseous phase separator separates the ethanol and sends gaseous carbon dioxide to the adsorption layer for purging. Swing adsorption dehydrator. 제3항에 있어서 저압을 얻기위해 진공펌프를 설치하고 회수된 이산화탄소를 송풍기를 이용하여 1-2기압으로 밀어 보내며 필요시 에탄올 발효공정에서 얻어진 이산화탄소를 보충시켜 원하는 압력을 얻을수 있게한 것을 특징으로 하는 이산화탄소를 이용한 저압식 에탄올 압력스윙 흡착 탈수장치.The method of claim 3, wherein a vacuum pump is installed to obtain low pressure, and the recovered carbon dioxide is pushed to 1-2 atm using a blower, and if necessary, the carbon dioxide obtained in the ethanol fermentation process is supplemented to obtain a desired pressure. Low pressure ethanol pressure swing adsorption dehydration device using carbon dioxide. 탈착된 흐름에서 에탄올과 물을 냉각 응축시켜 다시 증류탑에 보내 처리하도록 하고 기상으로 얻어지는 이산화탄소는 다시 한 번 응축단계를 거쳐 건조회수된 후 원료에탄올 기체와 혼합시켜 흡착층으로 들어가게 한 것을 특징으로 하는 이산화탄소를 이용한 저압식 에탄올 압력스윙 흡착 탈수장치.Carbon dioxide obtained by cooling and condensing the ethanol and water in the desorbed stream to be returned to the distillation column for treatment, and the carbon dioxide obtained in the gaseous phase is once again recovered through a condensation step and dried and mixed with raw ethanol gas to enter the adsorption layer. Low pressure ethanol pressure swing adsorption dehydration device using.
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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100415803B1 (en) * 2001-01-08 2004-01-24 한국에너지기술연구원 Microwave Applied Adsorptive Ethanol Drying Apparatus and Its Operation Method
KR101478344B1 (en) * 2013-01-28 2014-12-31 주식회사 창해에탄올 Method of preparing fuel-grade bioethanol
KR20170007571A (en) 2015-07-08 2017-01-19 (주)파인텍 The ethanol dehydration system
US10603626B2 (en) 2016-09-01 2020-03-31 Exxonmobil Upstream Research Company Swing adsorption processes using zeolite structures
US11433346B2 (en) 2019-10-16 2022-09-06 Exxonmobil Upstream Research Company Dehydration processes utilizing cationic zeolite RHO

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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
WO2010077439A2 (en) * 2008-12-17 2010-07-08 Uop Llc Temperature controlled adsorption for dehydration of water rich streams

Citations (1)

* Cited by examiner, † Cited by third party
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JPH05337323A (en) * 1992-06-05 1993-12-21 Mitsubishi Heavy Ind Ltd Method for recovering solvent

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Publication number Priority date Publication date Assignee Title
JPH05337323A (en) * 1992-06-05 1993-12-21 Mitsubishi Heavy Ind Ltd Method for recovering solvent

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100415803B1 (en) * 2001-01-08 2004-01-24 한국에너지기술연구원 Microwave Applied Adsorptive Ethanol Drying Apparatus and Its Operation Method
KR101478344B1 (en) * 2013-01-28 2014-12-31 주식회사 창해에탄올 Method of preparing fuel-grade bioethanol
KR20170007571A (en) 2015-07-08 2017-01-19 (주)파인텍 The ethanol dehydration system
US10603626B2 (en) 2016-09-01 2020-03-31 Exxonmobil Upstream Research Company Swing adsorption processes using zeolite structures
US11318413B2 (en) 2016-09-01 2022-05-03 Exxonmobil Upstream Research Company Swing adsorption processes using zeolite structures
US11433346B2 (en) 2019-10-16 2022-09-06 Exxonmobil Upstream Research Company Dehydration processes utilizing cationic zeolite RHO

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