CN101205166A - Adsorbent for low-concentration ethane separation and preparation thereof - Google Patents
Adsorbent for low-concentration ethane separation and preparation thereof Download PDFInfo
- Publication number
- CN101205166A CN101205166A CN 200610105323 CN200610105323A CN101205166A CN 101205166 A CN101205166 A CN 101205166A CN 200610105323 CN200610105323 CN 200610105323 CN 200610105323 A CN200610105323 A CN 200610105323A CN 101205166 A CN101205166 A CN 101205166A
- Authority
- CN
- China
- Prior art keywords
- sorbent material
- molecular sieve
- ethylene
- gas
- absorbent
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Abstract
The invention discloses an absorbent for ethylene efficiently separated from the gas with a light concentration of ethylene and a preparation method thereof. The absorbent is one or two metals supported on a molecular sieve and the composition of the absorbent is expressed by M-Z; Z symbolizes the molecular sieve and M is one or two selected from Ca, Ba, Sr, Ni, Co and Cu, and the weight percentage of M ranges from 10 per cent to 25 per cent; the absorbent possesses a high absorption capacity selectivity over the ethylene and the absorption capacity of the ethylene is higher than 3mmol/g under the suitable absorption conditions; the desorption temperature of the absorbent is low and the concentration of the ethylene in the desorption gas is high and the absorbent is suitable for the transformation absorption experiment equipment and is easy to be industrialized.
Description
Technical field
The present invention relates to a kind of from the gas that contains low-concentration ethane high efficiency separation go out sorbent material of ethene and preparation method thereof.
Background technology
Ethene is the most important industrial chemicals of petrochemical industry, the industrial method production of taking naphtha cracking usually.Along with constantly riseing of crude oil price, its manufacturing cost progressively increases, and the high efficiente callback utilization of low-concentration ethane becomes the problem that people pay close attention to.At present contain 5～20% ethene in the refinery catalytic cracked dry gas, because this part raw material small scale, dispersion, all act as a fuel gas basically and burn, cause the waste of resource.Though sophisticated low temperature or high pressure distillation isolation technique can obtain polymer grade ethylene, production energy consumption is higher, and scale of investment is big.Other separation method comprises absorption process, hydrate partition method, membrane separation process and absorption method.
The absorption extraction method mainly be utilize each component in the gas mixture in solvent different solubility and carry out isolating.According to fractionation by adsorption mechanism, be divided into two kinds of physical absorption method and chemical absorption methods.The physical absorption method has middle cold oil absorption technique (being solvent with C3, C4 and aromatic hydrocarbons generally) and Mehra technology (with C8-C10 aromatic hydrocarbons or to contain special mixtures such as polyoxyethylene glycol dialkyl ether, tetramethylene sulfone, N-Methyl pyrrolidone, propylene carbonate be solvent), and service temperature is usually at-20～-40 ℃.Chemical absorption method utilizes transition metal and alkene to form π-complex compound and alkene is separated.Main adopt the complex compound system that contains Cu or Ag arranged, as the CuAlCl of Tian Nake chemical company exploitation
4Aromatic solvent, yield of ethene is about 96%, and ethene purity can reach 99.5%, but such system is very responsive to raw material impurity, Cu
+Disproportionation reaction takes place easily.
The hydrate partition method is that the reaction of low-concentration ethane raw material and water is generated the hydrate that contains ethylene component, carries out fractionation through decompression or heating again and discharges ethene, and the ethylene concentration that obtains is lower, is generally 56%～81%.The membrane separation process separating ethene mainly contains planar film and hollow-fibre membrane, is in conceptual phase at present, and its efficient remains further to be improved.
Absorption method is comparatively favourable to separation and recovery lower concentration component, and its scale is to also comparatively suitable as FCC oil refinery dry gas separating ethene.Adsorption method of separation by component in the mixture on solid adsorbent preferentially adsorbed and carry out the separation of ethene.Difference according to adsorption mechanism has physical absorbent and chemosorbent, and is divided into transformation absorption (PSA) and alternating temperature absorption (TSA) according to the difference of sorbent material desorption conditions.Comparatively speaking, the pressure swing adsorption process energy consumption is lower, is used widely industrial.Obviously the core of adsorption method of separation is a sorbent material.In patent in the past, multiple sorbent material was once disclosed, as aluminum oxide, gac, the resin that contains AgCl or CuCl and molecular sieve etc.For loading capacity and the selectivity that improves ethene, select sorbent materials such as the aluminum oxide that is loaded with Cu (I) or Ag (I), molecular sieve usually for use, as the method for the disclosed alternating temperature transformation absorption of patent CN1048010C, U.S. Pat 6468329 disclosed pressure swing adsorption processs.Have problems such as the higher or loading capacity of ethene desorption temperature is lower in these methods, in addition, when containing Cu (I) in the sorbent material, make the adsorption selectivity of ethene and carbon monoxide obviously reduce, its range of application is restricted.Therefore the sorbent material of separating ethene still need improve loading capacity and optionally simultaneously from low-concentration ethane gas, the desorption temperature of reduction ethene or be easy to desorption.
Summary of the invention
One object of the present invention is to provide a kind of sorbent material, has higher ethylene absorption capacity and selectivity, can be from low-concentration ethane gas, and particularly efficient fractionation by adsorption goes out ethene in catalytic cracking oil refinery dry gas and the oxidative coupling of methane tail gas.
Another object of the present invention is to provide a kind of preparation of adsorbent method.
A kind of isolating sorbent material of low-concentration ethane that is used for, it is characterized in that: sorbent material is a kind of or two kinds of metals of load on the molecular sieve, the available M-Z of the composition of sorbent material represents, Z represents molecular sieve, M is selected from a kind of among Ca, Ba, Sr, Ni, Co, the Cu or two kinds, and the weight percentage of M is 10～25%.
In sorbent material of the present invention, molecular screening is from A type molecular sieve, X type molecular sieve or the Y zeolite of sodium, ammonium or Hydrogen.
Be used for the isolating preparation of adsorbent method of low-concentration ethane, may further comprise the steps:
1) molecular sieve is soaked in contains in the M metal salt solution;
2) under 40～100 ℃, stirring and refluxing 1～5 hour;
3) reduce to room temperature after, filter, use deionized water wash;
4) 100～150 ℃ of oven dry down;
5) 250～450 ℃ of following roastings 1～10 hour;
6) when needing second kind of metal of load in the sorbent material,, carry out ion-exchange with metallic solution with the above-mentioned method that contains the sorbent material of metal by above (1)～(5);
7) moulding through compressing tablet or bonding extruded moulding, obtains needed sorbent material.
In sorbent material preparation method of the present invention, the specific surface area of molecular sieve is 5～400m
2/ g.
The using method of sorbent material of the present invention:
(multitower) a certain amount of above-mentioned sorbent material of packing in adsorption tower is at exsiccant He or N
2Be warming up to 150～450 ℃ under the atmosphere, preferably 250～350 ℃, kept 1～6 hour, to remove moisture and the CO that adsorbs on the sorbent material
2Deng impurity.The unstripped gas such as catalytic cracking oil refinery dry gas or the oxidative coupling of methane tail gas that contain low-concentration ethane are at first through removing CO
2, sulfide, moisture and C
3 +Behind the preprocessing process such as hydro carbons, enter transformation absorption, adsorption temp is 0～100 ℃; Adsorptive pressure is 0.05～3.0MPa.Desorption pressure is 0.1～100kPa.Ethylene concentration is greater than 95% in the gas of desorption, and all the other components are ethane and carbon monoxide.
The present invention has following advantage and positively effect:
1, sorbent material is the modified molecular screen that contains metal, ethene is had high loading capacity and selectivity, and under suitable adsorption conditions, the ethylene absorption capacity is higher than 3mmol/g, the ratio of ethene and carbon monoxide adsorption selectivity is greater than 10, and the ratio of ethene and ethane adsorption selectivity is greater than 7;
2, the sorbent material desorption temperature is low, and ethylene concentration height in the desorption gas is selected suitable desorption conditions for use, and ethylene concentration can be higher than 95%;
3, sorbent material is applicable to pressure-swing absorption apparatus, is easy to industrialization.
Description of drawings
Fig. 1 is ethene, ethane and the carbon monoxide adsorption penetration curve on the Ba molecular sieve.Sorbent material loading amount 10g, it is methane 65.6% that unstripped gas is formed (V%), ethane 7.6%, ethene 21.7%, carbon monoxide 5.1%, gas flow 20ml/min, 40 ℃ of adsorption temps, pressure 0.01MPa.C among the figure
i/ C
0Ratio for component concentrations before adsorbing the back and adsorbing.
Fig. 2 is the method synoptic diagram that reclaims ethene from the low-concentration ethane unstripped gas.Pre-treatment mainly is carbonic acid gas, sulfide and the moisture etc. that remove in the gas; Gas separates ethene by the absorption of transformation on sorbent material of the present invention through pre-treatment.Gas composition before and after the absorption is by being connected in mass flow controller (MFC) gas chromatograph on-line analysis afterwards, and chromatographic column is that the 5A molecular sieve packed column separates packed column with a kind of lighter hydrocarbons, detects with TCD and FID respectively.The former can analyze O
2, N
2, CH
4And CO, the latter is the lower carbon number hydrocarbons dedicated analysis post of C1～C6.Under the condition of 80 ℃ of column temperatures, 150 ℃ of detectors, said components can obtain good analysis.
Embodiment
Following listed examples only is used for illustrating sorbent material composition of the present invention, preparation process and is used for low-concentration ethane fractionation by adsorption effect accordingly that obviously the present invention is not limited to the scope that embodiment describes.
Embodiment 1
With the 20g specific surface area is 15m
2The 4A molecular sieve of/g at room temperature joins the CaCl that 250ml contains 0.5mol/L
2In the aqueous solution, at 80 ℃ of stirring and refluxing 4h.Filter, with deionized water wash 3 times, obtain be deposited in 120 ℃ of oven dry 12h after, place retort furnace at 350 ℃ of roasting 3h.The Ca content of final sorbent material is 20%, and the XRD test analysis shows that its structure is a Ca-A type molecular sieve.After compressing tablet, screening, get 20～40 purpose sorbent material 10g, the gas with accompanying drawing 1 under normal pressure, room temperature adsorbs, and can obtain the ethylene absorption amount of 2.0mmol/g, the carbon monoxide adsorptive capacity of 0.2mmol/g.
With the 20g specific surface area is 410m
2The 13X molecular sieve of/g at room temperature joins the CaCl that 250ml contains 0.5mol/L
2In the aqueous solution, at 85 ℃ of stirring and refluxing 3h.Filter, with deionized water wash 3 times, obtain be deposited in 120 ℃ of oven dry 12h after, place retort furnace at 380 ℃ of roasting 3h.The Ca content of final sorbent material is 15%, after compressing tablet, screening, gets 20～40 purpose sorbent material 10g, and the gas with accompanying drawing 1 under normal pressure, room temperature adsorbs, and can obtain the ethylene absorption amount of 3.0mmol/g, the carbon monoxide adsorptive capacity of 0.4mmol/g.
Embodiment 3
With the 20g specific surface area is 330m
2The 4A molecular sieve of/g at room temperature joins the Ba (NO that 300ml contains 0.3mol/L
3)
2In the aqueous solution, at 90 ℃ of stirring and refluxing 2h.Filter, with deionized water wash 3 times, obtain be deposited in 120 ℃ of oven dry 12h after, place retort furnace at 400 ℃ of roasting 2h.The Ba content of final sorbent material is 15%, after compressing tablet, screening, gets 20～40 purpose sorbent material 10g, and the gas with accompanying drawing 1 under normal pressure, room temperature adsorbs, and can obtain the ethylene absorption amount of 2.8mmol/g, the carbon monoxide adsorptive capacity of 0.3mmol/g.
Embodiment 4
With the 20g specific surface area is 340m
2The NH of/g
4-Y molecular sieve at room temperature joins the Ca (NO that 350ml contains 0.5mol/L
3)
2In the aqueous solution, at 80 ℃ of stirring and refluxing 4h.Filter.With deionized water wash 3 times, obtain be deposited in 120 ℃ of oven dry 12h after, place retort furnace at 350 ℃ of roasting 3h.In an identical manner with the Sr (NO of calcareous Y molecular sieve with 0.05mol/L
3)
2Aqueous solution 300ml carries out ion-exchange, and the Ca content of final sorbent material is 15%, and Sr content is 5%.After compressing tablet, screening, get 20～40 purpose sorbent material 10g, the gas with accompanying drawing 1 under normal pressure, room temperature adsorbs, and can obtain the ethylene absorption amount of 2.1mmol/g, the carbon monoxide adsorptive capacity of 0.15mmol/g.
Embodiment 5
With the 20g specific surface area is 410m
2The 13X molecular sieve of/g at room temperature joins the Sr (NO that 300ml contains 0.5mol/L
3)
2In the aqueous solution, at 80 ℃ of stirring and refluxing 4h.Filter, with deionized water wash 3 times, obtain be deposited in 120 ℃ of oven dry 12h after, place retort furnace at 370 ℃ of roasting 2.5h.The Sr content of final sorbent material is 10%.After compressing tablet, screening, get 20～40 purpose sorbent material 10g, the gas with accompanying drawing 1 under normal pressure, room temperature adsorbs, and can obtain the ethylene absorption amount of 3.1mmol/g, the carbon monoxide adsorptive capacity of 0.28mmol/g.
Embodiment 6
With the 20g specific surface area is 410m
2The 10X molecular sieve of/g at room temperature joins the CaCl that 300ml contains 0.2mol/L
2In the aqueous solution, at 70 ℃ of stirring and refluxing 5h.Filter, use deionized water wash 3 times.Obtain be deposited in 120 ℃ the oven dry 12h after, place retort furnace at 400 ℃ of roasting 2h.In an identical manner with the NiCl of calcic molecular sieve with 0.1mol/L
2Aqueous solution 350ml carries out ion-exchange, the Ca content of final sorbent material is 12%, Ni content is 6%, after compressing tablet, screening, get 20～40 purpose sorbent material 10g, gas with accompanying drawing 1 under normal pressure, room temperature adsorbs, and can obtain the ethylene absorption amount of 3.5mmol/g, the carbon monoxide adsorptive capacity of 0.4mmol/g.
Embodiment 7
With the 20g specific surface area is 300m
2The Na-Y molecular sieve of/g at room temperature joins the Ba (NO that 300ml contains 0.3mol/L
3)
2In the aqueous solution, at 85 ℃ of stirring and refluxing 4.5h.Filter, with deionized water wash 3 times, obtain be deposited in 120 ℃ of oven dry 12h after, place retort furnace at 360 ℃ of roasting 3h.In an identical manner the Y molecular sieve of baric is used the Co (NO of 0.05mol/L
3)
2Aqueous solution 200ml carries out ion-exchange, and the Ba content of final sorbent material is 10%, Co content 5%.After compressing tablet, screening, get 20～40 purpose sorbent material 10g, the gas with accompanying drawing 1 under normal pressure, room temperature adsorbs, and can obtain the ethylene absorption amount of 3.1mmol/g, the carbon monoxide adsorptive capacity of 0.25mmol/g.
Embodiment 8
With the 20g specific surface area is 150m
2The 4A molecular sieve of/g at room temperature joins the CaCl that 300ml contains 0.2mol/L
2In the aqueous solution, at 80 ℃ of stirring and refluxing 4h.Filter, with deionized water wash 3 times, obtain be deposited in 120 ℃ of oven dry 12h after, place retort furnace at 350 ℃ of roasting 3h.In an identical manner with the CuCl of calcareous A molecular sieve with 0.1mol/L
2Aqueous solution 200ml carries out ion-exchange, and the Ca content of final sorbent material is 10%, Cu content 8%.After compressing tablet, screening, get 20～40 purpose sorbent material 10g, feeding flow at 250 ℃ is the 2%H of 30ml/min
2-He gas mixture 5h drops to room temperature in this atmosphere, under 0.3MPa pressure, adsorbs with the gas of accompanying drawing 1, can obtain the ethylene absorption amount of 3.5mmol/g, the carbon monoxide adsorptive capacity of 0.6mmol/g.
Embodiment 9
Adopt sorbent material and method among the embodiment 1, behind the adsorbents adsorb 120min, pressure is reduced to 30kPa desorption 30min, and then adsorb, after 5 times, the ethylene absorption amount is 2.1mmol/g so repeatedly, and the carbon monoxide adsorptive capacity is 0.23mmol/g.
Embodiment 10
Adopt sorbent material and method among the embodiment 7, behind the adsorbents adsorb 150min, pressure is reduced to 30kPa desorption 30min, and then adsorb, after 10 times, the ethylene absorption amount is 3.0mmol/g so repeatedly, and the carbon monoxide adsorptive capacity is 0.3mmol/g.
Embodiment 11
Adopt sorbent material and method among the embodiment 8, behind the adsorbents adsorb 150min, pressure is reduced to 30kPa desorption 30min, and then adsorb, after 10 times, the ethylene absorption amount is 3.3mmol/g so repeatedly, and the carbon monoxide adsorptive capacity is 0.5mmol/g.
Claims (4)
1. one kind is used for the isolating sorbent material of low-concentration ethane, it is characterized in that: sorbent material is a kind of or two kinds of metals of load on the molecular sieve, the composition of sorbent material is represented with M-Z, Z represents molecular sieve, M is selected from a kind of among Ca, Ba, Sr, Ni, Co, the Cu or two kinds, and the weight percentage of M is 10～25%.
2. sorbent material as claimed in claim 1 is characterized in that: molecular screening is from A type molecular sieve, X type molecular sieve or the Y zeolite of sodium, ammonium or Hydrogen.
3. preparation of adsorbent method according to claim 1, it is characterized in that: this may further comprise the steps:
1) molecular sieve is soaked in contains in the M metal salt solution;
2) under 40～100 ℃, stirring and refluxing 1～5 hour;
3) reduce to room temperature after, filter, use deionized water wash;
4) 100～150 ℃ of oven dry down;
5) 250～450 ℃ of following roastings 1～10 hour;
6) when needing second kind of metal of load in the sorbent material,, carry out ion-exchange with metallic solution with the above-mentioned method that contains the sorbent material of metal by above (1)～(5);
7) moulding through compressing tablet or bonding extruded moulding, obtains needed sorbent material.
4. method as claimed in claim 3 is characterized in that: the specific surface area of molecular sieve is 5～400m
2/ g.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200610105323 CN101205166A (en) | 2006-12-22 | 2006-12-22 | Adsorbent for low-concentration ethane separation and preparation thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200610105323 CN101205166A (en) | 2006-12-22 | 2006-12-22 | Adsorbent for low-concentration ethane separation and preparation thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101205166A true CN101205166A (en) | 2008-06-25 |
Family
ID=39565675
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200610105323 Pending CN101205166A (en) | 2006-12-22 | 2006-12-22 | Adsorbent for low-concentration ethane separation and preparation thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101205166A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103526021A (en) * | 2013-10-11 | 2014-01-22 | 南丹县吉朗铟业有限公司 | Cleansing and cobalt-removing method for zinc smelting leachate and scavenging agent used therein |
| CN103752266A (en) * | 2014-01-30 | 2014-04-30 | 中国石油大学(北京) | Bimetallic mineral spirit refining adsorbent and preparation method and application thereof |
| CN103772110A (en) * | 2013-12-20 | 2014-05-07 | 天津众智科技有限公司 | Application of zeolite molecular sieve as ethylene and propylene deeply drying adsorbent |
| CN105536695A (en) * | 2015-12-11 | 2016-05-04 | 中国海洋石油总公司 | Adsorbent for adsorbing and separating polycyclic aromatic hydrocarbons and preparation method thereof |
| CN109482136A (en) * | 2018-12-27 | 2019-03-19 | 青岛华世洁环保科技有限公司 | A kind of adsorbent and preparation method thereof |
| CN111302884A (en) * | 2020-02-13 | 2020-06-19 | 南京工业大学 | Method for recovering ethylene from ethane cracking gas |
| CN112774654A (en) * | 2020-12-31 | 2021-05-11 | 杭州谱育科技发展有限公司 | Preparation method of adsorbent for selectively adsorbing sulfur dioxide |
| CN113804535A (en) * | 2020-06-11 | 2021-12-17 | 中国石油大学(北京) | Wellhead dry gas C15-C32 molecular marker enrichment method and device |
-
2006
- 2006-12-22 CN CN 200610105323 patent/CN101205166A/en active Pending
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103526021A (en) * | 2013-10-11 | 2014-01-22 | 南丹县吉朗铟业有限公司 | Cleansing and cobalt-removing method for zinc smelting leachate and scavenging agent used therein |
| CN103526021B (en) * | 2013-10-11 | 2015-08-12 | 南丹县吉朗铟业有限公司 | A kind of zinc abstraction purification of leaching liquor is except cobalt method and scavenging agent used thereof |
| CN103772110A (en) * | 2013-12-20 | 2014-05-07 | 天津众智科技有限公司 | Application of zeolite molecular sieve as ethylene and propylene deeply drying adsorbent |
| CN103772110B (en) * | 2013-12-20 | 2015-10-28 | 天津众智科技有限公司 | A kind of zeolite molecular sieve is as the application of ethene, propylene depth drying sorbent material |
| CN103752266A (en) * | 2014-01-30 | 2014-04-30 | 中国石油大学(北京) | Bimetallic mineral spirit refining adsorbent and preparation method and application thereof |
| CN103752266B (en) * | 2014-01-30 | 2015-11-11 | 中国石油大学(北京) | A kind of bimetallic white spirit treating adsorbent and its preparation method and application |
| CN105536695A (en) * | 2015-12-11 | 2016-05-04 | 中国海洋石油总公司 | Adsorbent for adsorbing and separating polycyclic aromatic hydrocarbons and preparation method thereof |
| CN105536695B (en) * | 2015-12-11 | 2019-08-27 | 中国海洋石油集团有限公司 | A kind of adsorbent and preparation method of adsorbing separation polycyclic aromatic hydrocarbon |
| CN109482136A (en) * | 2018-12-27 | 2019-03-19 | 青岛华世洁环保科技有限公司 | A kind of adsorbent and preparation method thereof |
| CN111302884A (en) * | 2020-02-13 | 2020-06-19 | 南京工业大学 | Method for recovering ethylene from ethane cracking gas |
| CN113804535A (en) * | 2020-06-11 | 2021-12-17 | 中国石油大学(北京) | Wellhead dry gas C15-C32 molecular marker enrichment method and device |
| CN113804535B (en) * | 2020-06-11 | 2022-12-16 | 中国石油大学(北京) | Method and device for enriching C15-C32 molecular marker of wellhead dry gas |
| CN112774654A (en) * | 2020-12-31 | 2021-05-11 | 杭州谱育科技发展有限公司 | Preparation method of adsorbent for selectively adsorbing sulfur dioxide |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US10960343B2 (en) | Methods and systems for performing chemical separations | |
| US11001543B2 (en) | Separation methods and systems for oxidative coupling of methane | |
| CN101205166A (en) | Adsorbent for low-concentration ethane separation and preparation thereof | |
| CA2975743C (en) | Advanced oxidative coupling of methane | |
| KR101205078B1 (en) | Method for separating blast furnace gas | |
| CN101260017B (en) | Pressure-change absorption separation method for ethylene and hydrogen from refining plant dry gas | |
| KR20120083220A (en) | Methane recovering method and methane recovering apparatus | |
| CN202063710U (en) | Device for recovering hydrogen from refinery gas | |
| CN111683729A (en) | Pressure Swing Adsorption (PSA) device and pressure swing adsorption method | |
| CN107433107A (en) | C2+ two sections of points of concentration PSA methods are reclaimed from oil refinery dry gas | |
| WO2020167913A1 (en) | Processes for recovering lpg from a reforming-zone effluent | |
| CN202569906U (en) | Dry gas pressure swing adsorption (PSA) ethylene-and-hydrogen recycling device in oil refinery | |
| WO2015200075A1 (en) | Pressure swing adsorption processes and systems for recovery of hydrogen and c2+ hydrocarbons | |
| US20130053457A1 (en) | Method for naphthalene removal | |
| CN112374959B (en) | Method for separating ethylene and ethane in catalytic dry gas | |
| CN1465523A (en) | Method for refining mixed gas at least containing carbon monoxide, carbon dioxide, nitrogen and hydrogen | |
| KR20190071335A (en) | Carbon monoxide separation process and its system | |
| CN102898267A (en) | Method for purifying and recovering light hydrocarbon components of C3 and above C3 in polypropylene exhaust | |
| JPS58190801A (en) | Method for recovering high purity hydrogen from coke oven gas | |
| CN1093107C (en) | Gas-phase selective adsorption process for separating mixed dichlorobenzene | |
| CN1264786C (en) | Raw material gas purification method for propionaldehyde production | |
| CN1264787C (en) | Process for purifying ethylene from oil refinery dry gas | |
| CN112574784A (en) | Method for recovering hydrocarbon components with carbon number of 2 and carbon number of more than 2 in dry gas by adsorption absorption coupling process | |
| CN115716774A (en) | Method for separating ethane and ethylene | |
| CN112521245A (en) | Method for producing high-purity ethylene |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Open date: 20080625 |