CN101460597A - Membrane process for LPG recovery - Google Patents
Membrane process for LPG recovery Download PDFInfo
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- CN101460597A CN101460597A CNA2007800206426A CN200780020642A CN101460597A CN 101460597 A CN101460597 A CN 101460597A CN A2007800206426 A CNA2007800206426 A CN A2007800206426A CN 200780020642 A CN200780020642 A CN 200780020642A CN 101460597 A CN101460597 A CN 101460597A
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Abstract
Liquefied Petroleum Gas (LPG) can be recovered from various streams using a multiple membrane recovery process producing hydrogen stream at high yield and high purity and a C3<+> LPG stream at high yield with low energy expenditure.
Description
Invention field
[0001] the present invention relates to from the multiple C of containing
3 +Reclaim liquefied petroleum gas (LPG) in the logistics source of hydrocarbon.
Background technology
[0002] liquefied petroleum gas (LPG) (LPG) is defined as from containing C
3 +Different hydrocarbon streams source in the C that reclaims
3 +Part, for example refinery gas, particularly fuel gas stream.C
3 +But part constitutes this logistics only accounts for sub-fraction.Low molecular weight stream from these sources contains hydrogen, methane, ethane/ethylene, contains heteroatoms (S, O, light gas N) (for example mercaptan), and as the C of LPG
3 +Part.At present, owing to be difficult to from these feed streams, further low molecular weight stream is divided into C
3 +LPG part and C
2 -The lighting end part, isolating large quantities of gaseous, low molecular weight logistics are generally used for the fuel as the fuel source on the spot of refining and lighting end device from multiple refinery gas, and need not further separate.
[0003] nearest, membrane sepn has been found to be handles thick LPG with from the partially recycled C of lighting end
3 +LPG part, manufacturing have the cost effective means of the LPG of commercial value, but still can only make single logistics (being the LPG logistics) with any true value.Byproduct stream from these methods contains mixture of ingredients, wherein lacks purity and secondarily purified expensively makes them can only utilize its fuel value economically in refining and lighting end device
[0004] typically, according to Fig. 1, in implementing membrane separating method, will send into compressor (2) with boil down to logistics (3) from the thick LPG logistics (logistics 1) of the steam form in any source.This logistics is delivered to separating tank (4) (mainly being C from removing any spissated hydrocarbon as the bottoms of liquid (5)
3 +), steam reclaims as vapor overhead overhead product (6) simultaneously.With this hydrogen, the C of containing
1, C
2And number of C
3 +The vapor overhead overhead product of material is delivered to film separation unit (7), wherein C
3 +The LPG material passes through rubbery polymer membranes (9) selective permeation (8), simultaneously H in batches
2, C
1, C
2And number of C
3 +Logistics goes out film unit to material as poor LPG product (10).Rich LPG product in pipeline (8) is circulated to feeding line (1), is used at feeding separating tank (4) before in compressor (2) and fresh feed recompression, wherein by pipeline 5 recyclable LPG products.
[0005] in such system a lot of energy expenditures in all thick LPG logistics of compression with from the circulation C of film unit
3 +In the logistics, wherein film unit causes the final LPG product stream of preparation from separating tank.Purity and function from the poor LPG product of the retentate of film unit stream are insecure, and act as a fuel in a refining unit and gas fractionation plant usually and burn.In addition, owing to use high hydrogen to be worth purified hydrogen is reclaimed in refining (for example hydrogen treatment, desulfurization-hydrogenation, hydrocracking) from poor LPG product stream high commercial cost, this valuable hydrogen product stream that gas is used for obtaining that acts as a fuel, wherein it has only low-down value as heating fuel.
[0006] has the steam that is lower than about 70 to 80mol% hydrogen and can not be used for high hydrogen value refining, for example hydrogen treatment, desulfurization-hydrogenation, hydrocracking usually economically.Because it is obvious that the low value hydrogen purity is offset the capacity trend of these processes that consume hydrogen, and because do not cause this process to select the obvious reduction that transforms owing to do not wish low hydrogen dividing potential drop, the preferred hydrogen purity of 90mol% at least of 80mol% is applied in these processes that consume hydrogen usually at least.In addition, in these processes, form the more high-molecular weight pollutent meeting cracking of logistics remainder to low value products.
[0007] preferably uses the logistics of 80mol% hydrogen purity at least, and have suitable purity so that it can mix with high purity (95+mol% hydrogen), be used for the refining hydrotreatment and use at least about the logistics of 70 to 90mol% hydrogen purities.But the logistics that is less than the 70mol% hydrogen purity is too low usually for these processes, and sends into fuel gas system usually.
Therefore [0008] needing a kind of method, all is efficient from the thick LPG in any source wherein and cost is divided into high-purity C effectively
3 +Logistics, and obtain the another kind of logistics that contains high-purity hydrogen, it has enough purity and is worth refining process to be used for high hydrogen.
Summary of the invention
[0009] the present invention is a kind of from hydrogen and C
1, C
2And C
3 +Reclaim rich C in the hydrocarbon-containing feedstock logistics that hydrocarbon is formed
3 +The multiple membrane method of LPG logistics.
[0010] in a preferred implementation, the present invention is a kind of being used for from hydrogen and C
1, C
2And C
3 +Reclaim rich C in the hydrocarbon-containing feedstock logistics that hydrocarbon is formed
3 +The method of LPG logistics and high-purity hydrogen logistics comprises:
(a) the hydrocarbon-containing feedstock logistics is joined first film separation unit, wherein first side contacts of hydrocarbon-containing feedstock logistics and at least one first rubbery polymer membranes;
(b) return first from first side-draw of first rubbery polymer membranes and ooze surplus product stream, it has than hydrocarbon-containing feedstock logistics and has higher hydrogen mol%, and return the first infiltration product stream from second side-draw of first rubbery polymer membranes, it has the C higher than hydrocarbon-containing feedstock logistics
3 +Mol%;
(c) the first infiltration product stream is joined in the compressor, wherein to the first infiltration product stream pressurization;
(d) more first of the high pressure infiltration product stream joins in the separating tank;
(e) from separating tank, fetch liquid rich C
3 +LPG product stream, wherein rich C
3 +LPG product stream has than the higher C of the first infiltration product stream
3 +Mol%.
(f) from separating tank, fetch the rich C of steam
2 -Logistics, wherein rich C
2 -Logistics has the C higher than first penetrant
2 -Mol%.
(g) with rich C
2 -Logistics joins second film separation unit, wherein rich C
2 -First side contacts of thing and at least one second rubbery polymer membranes;
(h) return second from first side-draw of second rubbery polymer membranes and ooze surplus product stream, it has than rich C
2 -The C that logistics is higher
2 -Mol%, and return the second infiltration product stream from second side-draw of second rubbery polymer membranes, it has than rich C
2 -The C that logistics is higher
3 +Mol%, and
(i) at least a portion second infiltration product stream of naming a person for a particular job in the upstream of compressor flows with the first infiltration product and mixes.
[0011] in another preferred implementation, the present invention is a kind of being used for from hydrogen and C
1, C
2And C
3 +Reclaim rich C in the hydrocarbon-containing feedstock logistics that hydrocarbon is formed
3 +The method of LPG logistics and high-purity hydrogen logistics comprises:
(a) hydrocarbon feed stream is joined first film separation unit, wherein first side contacts of hydrocarbon-containing feedstock logistics and at least one first rubbery polymer membranes;
(b) return first from first side-draw of first rubbery polymer membranes and ooze surplus product stream, it has than hydrocarbon-containing feedstock logistics and has higher hydrogen mol%, and return the first infiltration product stream from second side-draw of first rubbery polymer membranes, it has the C higher than hydrocarbon-containing feedstock logistics
3 +Mol%;
(c) the first infiltration product stream is joined in the separating tank;
(d) from separating tank, fetch liquid rich C
3 +LPG product stream, wherein rich C
3 +LPG product stream has than the higher C of the first infiltration product stream
3 +Mol%.
(e) from separating tank, fetch the rich C of steam
2 -Logistics, wherein rich C
2 -Logistics has the C higher than first penetrant
2 -Mol%.
(f) with rich C
2 -Logistics joins second film separation unit, wherein rich C
2 -First side contacts of thing and at least one second rubbery polymer membranes;
(g) return second from first side-draw of second rubbery polymer membranes and ooze surplus product stream, it has than rich C
2The C that product stream is higher
2 -Mol%, and return the second infiltration product stream from second side-draw of second rubbery polymer membranes, it has than rich C
2 -The C that logistics is higher
3 +Mol%,
(h) at least a portion second infiltration product stream is joined in the compressor, wherein to the second infiltration product stream pressurization;
(i) the highly compressed second infiltration product stream of naming a person for a particular job in the upstream of separating tank flows with the first infiltration product and mixes.
Description of drawings
[0012] Fig. 1 is to use the monofilm separating unit to make the typical LPG removal process synoptic diagram of single valuable logistics.
[0013] Fig. 2 is the synoptic diagram of the preferred implementation of the improved LPG removal process of the present invention, has wherein used incorporate two film separation units to make three kinds of logistics: high purity LPG logistics, high-purity hydrogen logistics and poor H
2/ rich C
2 -Logistics.
Detailed Description Of The Invention
[0014] the present invention is a kind of high by using two film separation units to reclaim from thick LPG logistics Purity LPG reclaims the method for high-purity hydrogen-rich stream simultaneously, and described thick LPG logistics can be any next The source, for example refining coal gas, particularly fuel gas flow, and it contains hydrogen, methane, ethane/ethylene, contains The light gas that hetero atom (sulphur, oxygen, nitrogen, for example mercaptan) is arranged. In the present invention, first film separates The unit is positioned at before the first optional compressor and the knockout drum, and second film separation unit is positioned at knockout drum Afterwards, knockout drum has the rich C from second film separation unit3 +The logistics circulation is so that thick LPG is more logical Cross knockout drum. The present invention causes making from knockout drum and reclaiming high-purity LPG, and from first film Upper manufacturing and recovery high-purity hydrogen retentate. This high-purity hydrogen that obtains from first film unit has Sufficiently high purity is to be used for the hydrogen stream composition as refining hydrotreatment process. Oozing of second film unit Excess mainly comprises other lighter hydrocarbon, for example C1And C2, i.e. rich C2 -/ poor LPG logistics, it is logical The gas that often acts as a fuel uses.
[0015] under for example 50 to 1000psi the pressure that is subjected to by its source, first film separation unit (not carrying out the precommpression step) is at first sent in most thick LPG logistics, and feed stream is divided into poor H2With rich C3 +LPG permeate stream and rich H2Retentate stream. Owing to remove H2And number of C2 -Permeate stream under the volume of retentate stream and the pressure that reduces and minimizing so can add Enter to knockout drum, or can before sending into knockout drum, in first compressor of choosing wantonly, recompress. By In the volume of the minimizing of this logistics, if need compressor in this process, with respect to not dividing Before the compression step of the upstream of tank, remove and to use a littler compressor the hydrogen. This leads Cause lower cost of investment and lower energy consumption.
[0016] as shown in Figure 2, in an embodiment of the inventive method, be subjected to by its source To any pressure (being generally 50 to 1000psi) under, by pipeline (1) will be from any source new The LPG raw material joins in first film unit (2), and wherein it contacts with rubbery polymer membranes (3). New LPG Raw material is divided into retentate stream (4) and the rich C of Fu Qing by this film3 +LPG hydrocarbon and than feed stream Hydrogen concentration low lower/reduce the permeate stream (5) of pressure. Rich C3 +LPG but still the permeate stream that contains the lower pressure of some hydrogen (although having reduced concentration) flows through optional valve (6) to optional compressor (7a) by pipeline 5, wherein its pressure can be increased to the pressure of getting back at least thick LPG, for example 50 to 1000psi, and pass through subsequently pipeline (8) to knockout drum (9), wherein high-purity C3 +LPG is by liquid Change and pass through pipeline (10) and reclaim as product, vapor phase is returned as overhead by pipeline (11) Receive, and it is sent into second film unit (12), wherein it contacts with rubbery polymer membranes (13). In two film units (12), be divided into from the vapor overhead distillate flow of knockout drum (9) and be rich in C1And C2With reduction C3 +The retentate stream of LPG content (14) and rich C3 +The permeate stream of the reduction pressure of LPG (15). Optional compressor shown in need not (7a) by pipeline (15), permeate stream joins compressor The point of the upstream of 7 (a), at this it with merge from the permeate stream of first film separation unit.
[0017] in another embodiment, if the pressure of permeate stream is enough big in pipeline (5), Then can omit compressor (7). In the embodiment of this replacement, penetrant adds by pipeline (5a) Enter in knockout drum (9). In second film unit (12), the vapor overhead distillate flow point of knockout drum (9) For being rich in C1And C2With reduction C3 +The retentate stream of LPG content (14) and rich C3 +LPG falls The permeate stream of low-pressure (15). By pipeline (15) permeate stream is joined in this embodiment In the compressor (7b) that uses. Be recycled in the pipeline (5a) by the permeate stream of pipeline (15b) with compression, With the penetrant at this and pipeline (5) merge to introduce/be incorporated into again in the knockout drum (9).
[0018] although that compressor 7 (a) and 7 (b) are defined as is optional, or needs one or in addition One so that the logistics that reclaims under the pressure that reduces is pressurizeed again, and this logistics is as by the first film branch The penetrant of (2) from the unit, logistics (5) or the penetrant by second film separation unit (12), logistics (15), thus promote processing and/or the circulation of these logistics in the pipeloop. Lead by each film unit Caused and reclaimed penetrant than joining under the film unit low-pressure. If penetrant reduces in the pipeline (5) Pressure is still enough high to provide effective separation in knockout drum (9) film unit (12) pipeline, then can Omit compressor (7a). If not, the again compression in compressor (7a) is necessary so. If the pressure for the passing through of knockout drum (9) and film unit (12) in the pipeline (5) need to be in compression Compression is just enough high again in the machine (7a), so in pipeline (5) from the penetrant of film unit (12) recovery still So be in lower pressure (being lower than pipeline 5/5a's), then in order to be recycled to this penetrant of knockout drum (9) Need again to pressurize by compressor (7b).
[0019] in this film separation unit, the gas branch that usually under pressure, (is generally applied pressure) Son absorbs (namely absorbing or absorption) to as the reinforced side on the thin polymer film of film. This being absorbed in Produced the molecular concentration gradient from a reinforced side to penetrant one side on the film film. In concentration difference The lower gas molecule of impact spreads the material that absorbs simultaneously from a reinforced side direction penetrant one side by the film film Material is discharged into low-pressure permeability thing one side of film separation unit from penetrant one side of film film. This pressure Difference may be owing to be higher than penetrant one side and/or the infiltration of film at a reinforced side applied pressure of film Thing one side can be to make necessary pressure differential under vacuum partially or completely.
[0020] film that great majority use in gas separates is glassy polymers, for example acetate fiber The combination of element, polysulfones, polyamide, polyimides etc. and these polymer. At glassy polymers In, polymer molecule strictly is filled in the film film, and therefore diffusion is restricted, and diffusion speed Rate has been controlled separation. Bigger molecule has slower diffusion rate. Like this, glassy polymer membranes Can be used for from for example methane (kinetic diameter 3.8) and propane (kinetic diameter 4.3) big molecule in separate for example hydrogen (kinetic diameter 2.89) little molecule, but since diffusion rate reduce, because of This dispersion rate is also very slow.
[0021] in the recovery of LPG, be for example poly-silicon of rubber polymer as what use among the application Oxygen alkane, polybutadiene etc. In this rubbery state, the polymer molecule of film film is filled relatively Loose, this causes the high flexibility of rubber polymer film and consists of between the different polymer strands of film Flexible. Like this, the difference of diffusion velocity is not obvious between little molecule and the big molecule. At this, selective Separate the different driving of main except for molecular dimension, but since film in the adding material certain Plant the affinity of component. In the LPG that uses this rubbery polymer membranes reclaims, a reinforced side Absorb the big C of tendency3Molecule rather than littler hydrogen, C1Or C2Molecule.
[0022] because C3 +The absorbability that molecule is higher, more C3 +Molecule absorption causes more C to a reinforced side3 +Molecule is penetrated into penetrant one side by film, causes in adding material from hydrogen, C1Or C2Isolate C in the molecule3 +Molecule. In a preferred embodiment, method of the present invention will Make rich C3 +Product stream, the C that it has3 +Purity is 70mol% at least, more preferably 80mol% at least. One preferred embodiment in, method of the present invention will be made rich C3 +Product stream, rich C wherein3 +Product stream in C3 +The % by weight of component is C in the hydrocarbon-containing feedstock logistics that adds this process at least380 % by weight of+component. More preferably, method of the present invention will be made rich C3 +Product stream, rich C wherein3 +Product stream in C3 +The % by weight of component is C in the hydrocarbon-containing feedstock logistics that adds this process at least3 +90 % by weight of component.
[0023] similarly, such as the rubbery polymer membranes of polysiloxanes, polybutadiene etc. can be used for first film separation unit with the hydrogen-rich stream of making lower molecular weight as the retentate high-purity (greater than 70mol%) under, and make the rich C that can be further purified for the LPG recovery2 +Permeate stream. In a preferred embodiment, method of the present invention is rich in the product stream of hydrogen with manufacturing, and it goes to have Hydrogen purity 70mol% at least, more preferably 80mol% at least. One preferred embodiment in, Method of the present invention is rich in the product stream of hydrogen with manufacturing, wherein is rich in the weight of hydrogen component in the product stream of hydrogen Amount % is 40 % by weight of hydrogen component in the hydrocarbon-containing feedstock logistics that adds this process at least. More preferably Ground, method of the present invention is rich in the product stream of hydrogen with manufacturing, wherein is rich in hydrogen component in the product stream of hydrogen % by weight be 50 % by weight of hydrogen component in the hydrocarbon-containing feedstock logistics that adds this process at least, and Even more preferably be 60 % by weight of hydrogen component in the hydrocarbon-containing feedstock logistics that adds this process at least.
[0024] being used for the preferred rubbery polymer membranes of this method is that glass transition temperature is lower than 20 ℃ Those, namely (about 20 ℃ or higher) is rubber under room temperature or higher temperature. Separate single at each film Can use identical or different rubbery polymer membranes in the unit.
Embodiment A
[0025] in embodiment A, uses raw material as shown in table 1.Raw material consists of:
Table 1: take off isohexane agent tail gas and form
Flow 49.11316 lb mol/ hours
Pressure 136 psia
H
249.845 mole %
C
19.961 mole %
C
216.442 mole %
C
38.5309 mole %
IC
42.9003 mole %
C
47.0507 mole %
IC
52.3802 mole %
C
51.9602 mole %
C
6 +0.93009 mole %
C
3 +, 75.53414 moles of % of bpd
[0026] raw material carries out membrane sepn under following condition:
Feed pressure to film unit: 135.7psia
Retentate pressure 120.7pisa
Permeate pressure 56.7psia.
The result who obtains is as shown in table 2 below:
Table 2
Component (mole %) retentate penetrant
H
2 55.5 29.5
Methane 10.5 8.6
Ethane 14.6 21.8
Propane 7 13.3
Trimethylmethane 2.3 4.8
Normal butane 5.5 11.8
Iso-pentane 1.8 4.2
Skellysolve A 1.5 3.5
C
6 + 0.7 1.8
Amount to 99.4 99.3
Design the computer simulation of Comparative Examples and embodiment with these information, the pressure condition that its hypothesis is as follows.
The assumed stress condition that is used for the ratio 1-3 and the embodiment 1-7 of computer simulation: reinforced to first film unit under 135psia
Retentate is 133.6 (to be rich in H
2Logistics)
The penetrant that leaves first film unit is 20psia
100 ℉ lower compression machine ejectas are 250psia and 100 ℉
From film 2 unitary retentates is 238.7psia
[0027] by the unrestriced information shown in the table 3 use of the present invention is described.
[0028] film that is used to produce embodiment A (it is the embodiment of real rather than computer simulation) basic data is from " membrane technique and research (MTR) " acquisition, and is the rubbery polymer membranes that is defined as " PDMS film ".The True Data that the Comparative Examples 1-3 of computer simulation produces based on embodiment A is if but if having provided the surface-area that uses the compressor and first film unit increases (if perhaps used extra unit (Comparative Examples 1,2 and 3) if or the calculation result when using second film separation unit after separating together in embodiment 1-7.
[0029] Comparative Examples 1,2 and 3 is the comparative examples that carry out according to scheme shown in Figure 1 in table 3, but has omitted compressor, and raw material is processed under 135.7psia, need not extra compression and can obtain this pressure.In the Comparative Examples 1,2 and 3 of computer simulation, the film surface-area is made as about 202,358 and 693 square feet respectively, is representing the film unit that uses different size or parallel a plurality of film units.
[0030] compares mutually, the embodiment 1-7 of computer simulation is embodiments of the invention, wherein film separation unit is applied on every kind of raw material, and (i.e. " second film separation unit ") before the separating tank left in (i.e. " first film separation unit ") and steam logistics before separating tank.
[0031] according to Fig. 3, in these embodiment 1-7, can think that the raw material in pipeline 1 is 135.7psia, retentate in pipeline 4 returns to 133.6psia, penetrant in pipeline 5 is 20psia, compressor is forced into 250psia under 100 ℉ (pipeline 8) again to penetrant in pipeline 5, and is identical among all conditions and the embodiment 1.In computer simulation, can think that the raw material that is added to film unit (12) in 100 ℉ underground pipelines 11 is 245psia, be 20psia and the retentate in the pipeline 14 is a penetrant in 238.7psia and the pipeline 15.
[0032] obviously as seen, calculate from a hydrogen purity of three (Comparative Examples) and to be preferably 68.7%, with 693 square feet film and 83.47% C
3 +LPG purity, in the present invention, under identical film surface-area (embodiment 5), hydrogen purity is calculated as under 58.56% the rate of recovery may reach 80.6%, and C
3 +LPG purity is calculated as up to 82.8% under 92.7% the rate of recovery.The surface-area that calculating first film unit (unit 2 of Fig. 2) increases may cause hydrogen purity further to increase and rate of recovery reduction, and C
3 +LPG purity increases and rate of recovery reduction.
Therefore [0033], can calculate and not only can reclaim and the monofilm separating unit method C of same purity and yield in fact by the enforcement of the present invention's pair film separation unit methods
3 +The LPG logistics also can reclaim the H that hydrogen purity obviously increases when using less compressor
2Logistics, the power that needs with respect to monofilm element method multimembrane element method of the present invention obviously hangs down and can prove.
[0034] explanation of above-mentioned preferred implementation is meant and implements optimal way of the present invention.Those skilled in the art will recognize that in order to implement spirit of the present invention and can design other equivalent way.
Claims (14)
1. one kind is used for from by hydrogen and C
1, C
2And C
3 +Reclaim rich C in the hydrocarbon-containing feedstock logistics that hydrocarbon is formed
3 +The method of LPG logistics and high-purity hydrogen logistics comprises:
(a) the hydrocarbon-containing feedstock logistics is joined first film separation unit, wherein first side contacts of hydrocarbon-containing feedstock logistics and at least one first rubbery polymer membranes;
(b) return first from first side-draw of first rubbery polymer membranes and ooze surplus product stream, it has the hydrogen mol% higher than hydrocarbon-containing feedstock logistics, and returns the first infiltration product stream from second side-draw of first rubbery polymer membranes, and it has the C higher than hydrocarbon-containing feedstock logistics
3 +Mol%;
(c) the first infiltration product stream is joined in the compressor, wherein to the first infiltration product stream pressurization;
(d) more first of the high pressure infiltration product stream joins in the separating tank;
(e) from separating tank, fetch liquid rich C
3 +LPG product stream, wherein rich C
3 +LPG product stream has than the higher C of the first infiltration product stream
3 +Mol%.
(f) from separating tank, fetch the rich C of steam
2 -Logistics, wherein rich C
2 -Logistics has than the higher C of the first infiltration product stream
2 -Mol%.
(g) with rich C
2 -Logistics joins second film separation unit, wherein rich C
2 -First side contacts of logistics and at least one second rubbery polymer membranes;
(h) return second from first side-draw of second rubbery polymer membranes and ooze surplus product stream, it has than rich C
2 -The C that logistics is higher
2 -Mol%, and return the second infiltration product stream from second side-draw of second rubbery polymer membranes, it has than rich C
2 -The C that logistics is higher
3 +Mol%, and
(i) at least a portion second infiltration product stream of naming a person for a particular job in the upstream of compressor flows with the first infiltration product and mixes.
2. the process of claim 1 wherein that the hydrogen purity that the first infiltration product stream has is at least 70mol%.
3. the method for claim 2, wherein the weight % of hydrogen component is at least 40 weight % of hydrogen component in the hydrocarbon-containing feedstock logistics in the first infiltration product stream
4. the method for claim 3, wherein rich C
3 +The C that LPG product stream has
3 +Purity is at least 70mol%.
5. the method for claim 4, wherein rich C
3 +C in the product stream
3 +The weight % of component is at least C in the hydrocarbon-containing feedstock logistics
3 +80 weight % of component.
6. the method for claim 5, wherein the second-order transition temperature of rubbery polymer membranes is lower than 20 ℃.
7. the method for claim 6, wherein at least one rubbery polymer membranes is made up of the material that is selected from polysiloxane and polyhutadiene.
8. one kind is used for from by hydrogen and C
1, C
2And C
3 +Reclaim rich C in the hydrocarbon-containing feedstock logistics that hydrocarbon is formed
3 +The method of LPG logistics and high-purity hydrogen logistics comprises:
(a) the hydrocarbon-containing feedstock logistics is joined first film separation unit, wherein first side contacts of hydrocarbon-containing feedstock logistics and at least one first rubbery polymer membranes;
(b) return first from first side-draw of first rubbery polymer membranes and ooze surplus product stream, it has than hydrocarbon-containing feedstock logistics and has higher hydrogen mol%, and return the first infiltration product stream from second side-draw of first rubbery polymer membranes, it has the C higher than hydrocarbon-containing feedstock logistics
3 +Mol%;
(c) the first infiltration product stream is joined in the separating tank;
(d) from separating tank, fetch liquid rich C
3 +LPG product stream, wherein rich C
3 +LPG product stream has than the higher C of the first infiltration product stream
3 +Mol%.
(e) from separating tank, fetch the rich C of steam
2 -Logistics, wherein rich C
2 -Logistics has the C higher than first penetrant
2 -Mol%.
(f) with rich C
2 -Logistics joins second film separation unit, wherein rich C
2 -First side contacts of logistics and at least one second rubbery polymer membranes;
(g) return second from first side-draw of second rubbery polymer membranes and ooze surplus product stream, it has than rich C
2 -The C that logistics is higher
2 -Mol%, and return the second infiltration product stream from second side-draw of second rubbery polymer membranes, it has than rich C
2 -The C that logistics is higher
3 +Mol%,
(h) at least a portion second infiltration product stream is joined in the compressor, wherein to the second infiltration product stream pressurization;
(i) the highly compressed second infiltration product stream of naming a person for a particular job in the upstream of separating tank flows with the first infiltration product and mixes.
9. the method for claim 8, wherein the hydrogen purity of the first infiltration product stream is at least 70mol%.
10. the method for claim 9, wherein the weight % of hydrogen component is at least 40 weight % of hydrogen component in the hydrocarbon-containing feedstock logistics in the first infiltration product stream
11. the method for claim 10, wherein rich C
3 +The C of LPG product stream
3 +Purity is at least 70mol%.
12. the method for claim 11, wherein rich C
3 +C in the product stream
3 +The weight % of component is at least C in the hydrocarbon-containing feedstock logistics
3 +80 weight % of component.
13. the method for claim 12, wherein the second-order transition temperature that has of rubbery polymer membranes is lower than 20 ℃.
14. the method for claim 13, wherein at least a rubbery polymer membranes is made up of the material that is selected from polysiloxane and polyhutadiene.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US78948906P | 2006-04-04 | 2006-04-04 | |
| US60/789,489 | 2006-04-04 | ||
| US11/731,871 | 2007-03-30 |
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| Publication Number | Publication Date |
|---|---|
| CN101460597A true CN101460597A (en) | 2009-06-17 |
Family
ID=40770642
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|---|---|---|---|
| CNA2007800206426A Pending CN101460597A (en) | 2006-04-04 | 2007-04-03 | Membrane process for LPG recovery |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102556967A (en) * | 2010-10-05 | 2012-07-11 | 林德股份公司 | Removal of hydrogen |
| CN111321022A (en) * | 2018-12-14 | 2020-06-23 | 乔治洛德方法研究和开发液化空气有限公司 | Apparatus and method for osmotically treating a gas stream through a membrane with an adjusted suction pressure of a second permeate |
-
2007
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102556967A (en) * | 2010-10-05 | 2012-07-11 | 林德股份公司 | Removal of hydrogen |
| CN111321022A (en) * | 2018-12-14 | 2020-06-23 | 乔治洛德方法研究和开发液化空气有限公司 | Apparatus and method for osmotically treating a gas stream through a membrane with an adjusted suction pressure of a second permeate |
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Application publication date: 20090617 |