CN1713949A - Membrane separation process - Google Patents
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- CN1713949A CN1713949A CN 200380103765 CN200380103765A CN1713949A CN 1713949 A CN1713949 A CN 1713949A CN 200380103765 CN200380103765 CN 200380103765 CN 200380103765 A CN200380103765 A CN 200380103765A CN 1713949 A CN1713949 A CN 1713949A
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Abstract
A high purity stream of methane can be obtained from crude natural gas, especially exhaust gas from waste landfills, by a process that includes first removing moisture (4), then feeding the dried crude gas mixture to a gas-liquid contact absorber (10) to strip heavy hydrocarbon compounds in a primarily carbon dioxide by product stream. Methane enriched gas from the absorber (10) is separated in a membrane separation unit (20) which provides permeates enriched in carbon dioxide that is recycled to the absorber and a purified product stream of methane.
Description
Technical field
The present invention relates to a kind of membrane separating method that is used for refined natural gas.More specifically, the present invention relates to a kind of being included in and utilize membrane separation unit operation, remove the method for heavy hydrocarbon contaminants by absorbing the thick gas raw material of processing with before carbon dioxide and the methane separation.
Background technology
For application such as exotic fuels that are used for chemical production processes and raw material, refined natural gas, just typically about 97 moles of % methane, about 3 moles of % carbon dioxide and trace water steam are a kind of important commercial products.Raw gas just is mixed with the methane of pollutant, can obtain from various sources such as missile silo.Waste gas from the solid refuse landfill yard also becomes a kind of value-added gradually thick methane source.The thick gas of this class typically contains the methane of the carbon dioxide of 10～50 moles of %, 50～80 moles of % and comprises the small amounts of contamination of heavy hydrocarbon.Carbon dioxide can be used for food processing and other purposes.Therefore natural gas mixtures can provide two kinds of valuable industrial materials, namely for methane and carbon dioxide.
The film separation is a kind of very effective method with carbon dioxide and methane separation.But the separating property of selective gas permeable membrane is subjected to the adverse effect of the pollutant, the particularly heavy hydrocarbon that exist in the thick admixture of gas usually.Therefore for feasible methane film separates, need remove heavy hydrocarbon.In addition, the natural gas that contains heavy hydrocarbon contaminants is for for the transmission of originating between the consumer, and is industrial and infeasible.So the what is called " pipeline specifications " that is used for refined natural gas has low concentration limits to heavy hydrocarbon.Former thereby speech to this, it also is desirable removing heavy hydrocarbon from carbon dioxide and methane.
Thereby some is used for making the film of methane and carbon dioxide separate the method that can carry out subsequently from the raw gas strip, hydrocarbons and has adopted unit operations such as dew point control (" DPC "), alternating temperature absorption (" TSA ") and transformation to adsorb (" PSA ") major part as the methane concentration technology.According to the qualification of broad sense, DPC, TSA and PSA need cooling, steam and the clean gas of a great deal of with effective operation separately.These auxiliary equipment costlinesses, and therefore significantly increased product cost.
Film separates maximal efficiency ground operation when raw material is compressed usually.The expense of compression can reduce these class methods reasonability economically.In addition, in order to obtain desirable pure methane product design, film separate generally include series connection multistage, just more than the film separation unit of one-level.Multistagely can produce potential waste byproduct streams, this has further reduced film and has separated attraction to refine methane.Mainly for these reasons, do not find that so far membrane separating method is for the big benefit of commercially producing methane from landfill yard waste gas.
A kind of attractive method that is used for concentrating and reclaim from landfill gas methane and carbon dioxide is disclosed in the US5 that assigns to Acrion Technologies, in 681,360.Should " Acrion " method comprise, in one or two container, absorb the pollutant that exists usually in the solid waste gas with the relatively small amount carbon-dioxide absorbent that exists in the gas.The method produces a logistics and a logistics that is rich in carbon dioxide that is rich in methane.This logistics amount that is rich in methane but accounts for the carbon dioxide that can not ignore part less, and this carbon dioxide is waited until separation so that refining methane product to be provided.This logistics that is rich in carbon dioxide contains the methane that slatterns, and may need the processing to promote to be undertaken by burning of the methane that adds.
It is desirable to a kind of method of comprehensive and expense and energy efficient, this method produces the methane component that highly concentrates from raw gas, and the methane that has minimizing in discarded object loses.
Summary of the invention
Had been found that a kind of very effective method and system that is used for from the raw gas refine methane.This new method and system are characterised in that with a kind of carbon-dioxide absorbent pre-absorption heavy hydrocarbon compounds, then the absorption product that is rich in methane are carried out film and separate.It should be noted that the infiltration gas that makes from the main membrane separation unit operation in downstream returns, think that the absorption operation of upstream provides absorbent.Separate in the embodiment at a preferred multistage film, from second and the infiltration gas recirculation of optionally more senior film level get back in the raw material of absorptive unit, thereby raw material recovery efficiently is provided.
Therefore, the invention provides a kind of being used for from the method for the thick admixture of gas separation of methane that contains methane, carbon dioxide and heavy hydrocarbon compounds, this method comprises: absorb heavy hydrocarbon compounds with a kind of composition that is rich in carbon dioxide from this thick admixture of gas, thereby a kind of medium-gas mixture that is substantially free of heavy hydrocarbon compounds is provided; Separate this medium-gas mixture with a selective gas permeable membrane, to form the composition that (a) is rich in the product mixture of methane and (b) is rich in carbon dioxide; With, the composition that is rich in carbon dioxide that is obtained is used for absorbing heavy hydrocarbon compounds from thick admixture of gas.
The present invention also provides a kind of and is used for from the method for the crude mixture separation of methane that contains methane, carbon dioxide and hydrocarbon compound, and this method comprises the steps:
(A) compression this thick admixture of gas, and therefrom except that anhydrating contains the dehydration unstrpped gas of methane, carbon dioxide and heavy hydrocarbon compounds with generation,
(B) make this unstrpped gas in an absorber unit, contact the liquid-absorbant of the first order permeate gas mixture of the self-contained most of carbon dioxide of a kind of condensation, described heavy hydrocarbon compounds is absorbed fully basically and enters in the absorbent, to form the liquid by-product of carbonated and heavy hydrocarbon compounds
(C) shift out this liquid by-product and medium-gas mixture respectively from this absorber unit, this medium-gas mixture contains methane and carbon dioxide, is substantially free of heavy hydrocarbon compounds,
(D) this medium-gas mixture is contacted than the methane feed side of first film of permeable for carbon dioxide more preferably in first order film separation unit, make this medium-gas mixture selectively penetrating cross this film, with film see through side form described first order permeate gas mixture and
(E) shift out the first order that more is rich in methane than medium-gas mixture from the feed side of first order film separation unit and ooze residual air body mixture.
The present invention further provides a kind of being used for from the system of the crude mixture production refine methane that contains methane, carbon dioxide and VOC, this system comprises:
(a) drier, its running is anhydrated to remove from crude mixture; And compressor, its running increases to the pressure that is suitable for absorbing heavy hydrocarbon with the pressure with crude mixture,
(b) the adverse current gas-liquid directly contacts absorber, it is positioned at drier and compressor downstream, be suitable for from crude mixture heavy hydrocarbon compounds absorbed basically fully and enter in the liquid CO 2 absorbent, and be suitable in one way, producing the medium-gas mixture that is substantially free of heavy hydrocarbon compounds
(c) first order film separation unit, its have than methane more preferably permeable for carbon dioxide first film, be positioned at the permeate chamber that film and medium-gas mixture fluid are communicated with the feed chamber of side and are positioned at the relative side with feed chamber of this first film, this permeate chamber is suitable for receiving the first order infiltration gas of medium-gas mixture selectively penetrating by first film
(d) condenser, its running with liquefy this first order infiltration gas and
(e) recirculation transfer line, fluid is communicated with between the permeate chamber of this pipeline and the absorber and first film separation unit, turns round to send first order infiltration gas to absorber.
Description of drawings
Fig. 1 is schematic flow diagram of an embodiment of the present invention.
The specific embodiment
With reference to Fig. 1, as can be seen in an embodiment of the invention, raw gas logistics 1 is processed, to produce refine methane logistics 32.This raw gas comprises a large amount of methane and carbon dioxide, and comprises a spot of all contaminations such as oxygen, nitrogen, hydrogen sulfide, water and the hydrocarbon except that methane.This thick gas is pretreated to anhydrate to remove.This passes through this gas of compression in compressor 2, and carries out at drier 4 inner dryings.This drier is an any type dehumidifier well known in the art, as the cooling coil coalescing filter.Typically, water shifts out in condensed liquid stream 3.
The thick gas stream 5 that has dewatered is removed with the absorption that is suitable for heavy hydrocarbon compounds by conditioning subsequently.This conditioning is carried out in compressor 6 and heat exchanger 8, and they increase to the value that is suitable for removing dealkylation with the pressure and temperature of absorber feed gas 9 respectively.
The poor overhead product 12 that contains heavy hydrocarbon enters in the first order film separation unit 20.An optional compressor (not shown) can be used to convey this stream into this separative element 20.This medium-gas mixture is substantially free of heavy hydrocarbon compounds, otherwise this compound will be harmful to film, or influences membrane separating property unfriendly.Term " basically " and " substantially fully " are used in this context and other place, are not fully or fully to exist though mean associated performance, are to exist in large quantities.For example, " being substantially free of heavy hydrocarbon compounds " means that this admixture of gas has considerably lacked these hydrocarbon, but is not contain this hydrocarbon fully.
Can adopt membrane separator known in the art.The separative element that is used for this invention is characterised in that to have a selective gas permeable membrane 21, and this film is than methane permeable for carbon dioxide more preferably.That is, carbon dioxide penetrates this film quickly than methane.Film 21 has both sides, will divide the separation unit into a feed chamber 25 and a permeate chamber 23.The medium-gas mixture 12 that enters and contact with film 21 penetrates into permeate chamber.In this permeate chamber, it is removed, and returns the absorption tower as first order permeate gas mixture 26.This first order permeate gas mixture is rich in carbon dioxide, therefore can serve as absorbent fluid ideally in the absorption tower.
The residual air body mixture that oozes in film 21 feed chamber one side has been got rid of carbon dioxide by the effect of membrane separating method, and therefore is rich in methane.Some product is used, and the methane concentration that the first order is oozed in the residual air body mixture may be satisfactory.In this case, the first order is oozed residual air body mixture and can be stored or be directly used in the subsequent technique unit operations.Usually, being used for refine methane that exotic fuels use should have than single stage membrane separation obtainable higher methane concentration of institute and pollutant still less.For this purpose, carrying out second level film separates.
The first order is oozed residual air body mixture 22 and can be admitted in the feed chamber 35 of a second level film separation unit 30.This second level permeate chamber 33 is positioned at the opposite side of second film 31, and this second film also is than methane permeable for carbon dioxide more preferably.Because the first order is oozed contacting of residual air body mixture and second film, gas-selectively ground permeates, and is rich in the second level permeate gas mixture 36 of carbon dioxide with formation, and provides the second level of highly being rich in methane to ooze residual air body mixture 32.This admixture of gas that highly is rich in methane has sufficiently high methane concentration usually, is enough to as exotic fuels, and therefore can be discharged in the storage facilities from the film separation unit of the second level, perhaps directly is discharged in the burning process, to change into heat energy.
Second level permeate gas mixture 36 has significantly concentrated carbon dioxide, and contains a small amount of methane of infiltration by second film.In order to reclaim methane, film separation unit is passed through in these second level infiltration gas 36 recirculation.This second level infiltration gas is usually under low-down pressure, so that can not directly add in the absorber together with first order infiltration gas 26.When second level penetrant can recycle when getting back to coarse raw materials gas 1, this penetrant is drying.Therefore, second level penetrant preferably turns back in the dried crude gas mixture 5 of compressor 6 upstreams, as shown in Figure 1.
The thick gas raw material composition of process for refining changes, and depends on the source of raw gas.For example, thick admixture of gas typically contains the carbon dioxide of the 30 volume % that have an appointment, and the methane of 60 volume % and about 10 volume % comprise other pollutant of hydrogen sulfide, water, oxygen, nitrogen and the hydrocarbon except that methane.This other hydrocarbon can be divided into " light hydrocarbon compounds " or " heavy hydrocarbon compounds ".As used herein, term " heavy hydrocarbon compounds " only is meant and formed by hydrogen and carbon, and contains the compound more than 6 carbon atoms.Heavy hydrocarbon enters and stops up the hole of selective gas permeable membrane usually, and this promptly is called a kind of phenomenon of " plasticizing " often.Plasticizing has adverse influence to membrane separating property, the membrane separating property that the has influence on assembly usually actual infeasible stage that becomes.
In an exemplary embodiment of this invention, thick admixture of gas is compressed to about 2.1MPa (300psi), and dry in a coalesces water filter, to remove whole basically water.This dry thick admixture of gas is compressed to about 6.0MPa (870psi), and is heated to about 35 ℃ in a finned tube exchanger, and half that introduce packed absorber then highly located.This absorber is usually in about 5.5～7.6MPa (800～1100psi) times operations.This pressure limit makes this novel method be used for ideally from the thick gas refine methane from raw gas source (well that just natural subsurface geology forms).These sources typically provide be not far below the high pressure of absorber operating pressure under thick gas.Therefore, by this fact, just only need the less energy input so that thick gas is compressed to operating pressure, efficient of the present invention is increased.This new absorption process can be made with extra care the thick gas from discarded refuse landfill, and still, these sources produce the very thick gas of low-pressure.Landfill yard waste gas is increased to the absorber operating pressure needs the lot of energy input usually.This makes this new method more not be preferred for disposal of refuse landfill yard waste gas.
Thick admixture of gas is in absorber and be rich in the absorbent counter current contacting of carbon dioxide, a kind of overhead stream is provided, and this overhead stream contains the pollutant that about 45 volume % methane, 50 volume % carbon dioxide and about 5 volume % comprise hydrogen sulfide, oxygen, nitrogen and light hydrocarbon compounds.By absorbent is cooled to-5 ℃ as the top of tower that liquid begins to descend by tower, make the absorbent condensation.Than other adverse current fractionation process, the absorption that heavy hydrocarbon enters absorbent much is an one-pass operation.That is to say that thick gas upwards flows from the point that enters absorber, absorbent flows downward from inlet point.When two kinds of logistics contacted with each other, heavy hydrocarbon stripping from thick gas comes out and absorbent leaves from the bottom together.This bottoms is a kind of liquid stream, contains have an appointment 97 volume % carbon dioxide and about 3 volume % heavy hydrocarbon compounds.Basically whole heavy hydrocarbon compounds all is exhausted in the absorber bottom product.
Along with thick gas upwards passes through absorber, it contains heavy hydrocarbon less and less.At the top, gas is substantially free of heavy hydrocarbon compounds, and discharges this absorber as overhead gas.Enter the feed end of first hollow fiber film assembly from the overhead gas on absorption tower.Permeate gas mixture has about 90 volume % carbon dioxide, about 10 volume % methane and comprises the composition of the pollutant of light hydrocarbon compounds.This admixture of gas is compressed, cools off and turns back to the top on absorption tower from first membrane module, there the gas that upwards flows of contact.
A favorable characteristics of this new method is derived from high pressure, and promptly usually above 5.5MPa (800psi), the absorption of heavy hydrocarbon compounds in absorber occurs under this pressure.When first order infiltration gas be compressed to one allow to get back to the suitable high pressure of absorber after, can utilize a kind ofly only first order infiltration gas to be condensed to liquid condition for the medium of gentle chilling temperature.For example, temperature can be used to make co 2 liquefaction under the high pressure for-5 ℃ approximately～about 20 ℃ salt solution or water.By comparison, the reflux condensation mode that the fractionation of hydrocarbon-carbon dioxide usually need be under unusual low temperature under the low pressure, this reflux condensation mode needs more expensive and unworkable low-temperature cooling media, and the temperature of cooling agent is lower than-50 ℃ approximately.
Contact after the feed side of first film, gas shifts out from first order film separation unit.This first order is oozed the composition that residual air body mixture has about 60 volume % methane, about 30 volume % carbon dioxide and comprises the surplus of light hydrocarbon, water, oxygen and nitrogen except that methane.
The first order is oozed residual air body mixture and is added in the gas separation membrane unit, the second level, thereby a side of permeable membrane is selected in its contact second.It is the carbon dioxide of about 62 volume % and the methane of about 35 volume % that this second level permeate gas mixture is formed.Although the amount of methane is few in the penetrant, be worth holding back.Therefore, permeate gas mixture recirculation in the second level is got back in the dry thick gas.The composition that residual air body mixture has about 98 volume % methane, light hydrocarbon compounds and about 2 volume % carbon dioxide that oozes from second level separative element.This mixture is suitable for commercial Application, is mainly used in by the burning that acts as a fuel and produces calorific value.
The film separation unit that can be used for this invention is known in the art.The primary clustering of this type of film separation unit is a selective gas permeable membrane.Typically, this film has the polymer composition.
The polymeric material of wide region has desirable gas permeability, and can be used as film of the present invention.Representational material comprises polyamide, polyimides, polyester, Merlon, the ester of Copolycarbonate, polyethers, polyether-ketone, PEI, polyether sulfone, polysulfones, fluorine substituted ethylene polymer and copolymer such as polyvinylidene fluoride, tetrafluoroethene, the copolymer of tetrafluoroethene and perfluoroalkyl vinyl ether or perfluoro dioxole, polybenzimidazoles, polybenzoxazole, polyacrylonitrile, cellulose derivative, poly-azo aromatics, poly-(2,6-dimethyl phenylene oxygen), polyphenylene oxide, polyureas, polyurethane, polyhydrazide, poly methylene imine, polyacetals, cellulose acetate, celluloid, ethyl cellulose, SAN, bromination is gathered (xylene oxygen), and sulfonation gathers (xylene oxygen), and four halogens replace Merlon, four halogens replace polyester, four halogens replace the ester of Merlon, polyquinoxaline, polyamide-imides, polyesteramide, their mixture, copolymer, replace material and analog.Other similarly suitable gas separating layer membrane material comprises polysiloxanes, polyacetylene, polyphosphazenes, polyethylene, poly-(4-methylpentene), poly-(trimethyl silyl propine), poly-(trialkylsilkl acetylene), polyureas, polyurethane, their mixture, copolymer, replacement material and analog.Further expectation is, polymerizable material, and the material of just curable formation polymer may be the suitable gas separating layer of multicomponent gas diffusion barrier of the present invention as sulfuration siloxanes and analog.The preferred material that is used for the dense gas separating layer comprises the composition of aromatic polyamides and aromatic polyimide.
Film can have a lot of shapes, as plain film, pleat sheet, rolling, tubular type, band shape and hollow fiber, can list a lot.Film can place the gas supply that is suitable for supplying raw materials, permeate and ooze any general type housing or container that the residual air body shifts out.This container also provides a high-pressure side (be used for raw material and ooze the residual air body) and a low-pressure side (being used for infiltration gas) of film.For example, flat sheet membrane can be stacked in the plate-and-frame module, or is wrapped in the screw assembly.A large amount of hollow-fibre membranes can be assembled into a branch of membrane module, and this membrane module typically is packaged with thermosetting resin in cylindrical housings, and have by this fibre bundle and flow configuration.Consider that hollow-fiber module provides big film surface in small size, so hollow-fiber module is generally preferred.Final film separation unit comprises one or more membrane modules, and this assembly is contained in separately in the pressure vessel, and perhaps a plurality of elements place in the seal casinghousing of suitable diameter and length together.
For improved performance, hollow-fibre membrane generally includes an extremely thin selection layer, and this layer formed the part than thick structure.This can be whole asymmetric membrane for example, and it comprises and forms a fine and close epidermis district and micropore Support of selecting floor.Such film is described in for example US5 of Ekiner, in 015,270.As a further and preferred example, hollow-fibre membrane can be so-called " composite membrane " type, the film that just has multilayer.Composite membrane typically comprises a porous but the support membrane of non-selectivity, and this support membrane provides mechanical strength, has applied the thin of responsible separating property above it and has had optionally another kind of material layer.Multiple polymers can both be used as matrix.Typical support membrane material comprises polysulfones, polyether sulfone, PEI, the composition of polyimides and polyamide, their mixture, copolymer, replacement material and analog.Typically, such composite membrane is that the solution coating is selected layer and made in separating step then by solution-cast (perhaps, being spinning under the situation of doughnut) support membrane.Hollow fiber composite membrane can also be made by matrix material and the two coextrusion spin processes simultaneously of separating layer, and as the US5 of Ekiner, 085,676 is described.Therefore whole disclosures of aforementioned patent are included in herein.Being used for film separation unit of the present invention can be from Air Liquide, S.A., and Houston, the MEDAL unit of Texas obtains.
Although in order to describe concrete form of the present invention fully, sufficiently to those of ordinary skills, select these concrete forms of the present invention with concrete wording in front, but, should be appreciated that generation is of equal value basically or be dominant the result and/or the various replacements and the modification of performance all are considered to fall into by in appended claims institute's restricted portion and the spirit.
Claims (12)
1, a kind of being used for from the method for the thick admixture of gas separation of methane that contains methane, carbon dioxide and heavy hydrocarbon compounds, this method comprises: absorb heavy hydrocarbon compounds with a kind of composition that is rich in carbon dioxide from this thick admixture of gas, thereby a kind of medium-gas mixture that is substantially free of heavy hydrocarbon compounds is provided; Separate this medium-gas mixture with a selective gas permeable membrane, to form the composition that (a) is rich in the product mixture of methane and (b) is rich in carbon dioxide; With, the composition that is rich in carbon dioxide that is obtained is used for absorbing heavy hydrocarbon compounds from thick admixture of gas.
2, a kind of being used for from the method for the crude mixture separation of methane that contains methane, carbon dioxide and hydrocarbon compound, this method comprises the steps:
(A) compression this thick admixture of gas, and therefrom except that anhydrating contains the dehydration unstrpped gas of methane, carbon dioxide and heavy hydrocarbon compounds with generation,
(B) make this unstrpped gas in an absorber unit, contact the liquid-absorbant of the first order permeate gas mixture of the self-contained most of carbon dioxide of a kind of condensation, described heavy hydrocarbon compounds is absorbed fully basically and enters in the absorbent, to form the liquid by-product of carbonated and heavy hydrocarbon compounds
(C) shift out this liquid by-product and medium-gas mixture respectively from this absorber unit, this medium-gas mixture contains methane and carbon dioxide, is substantially free of heavy hydrocarbon compounds,
(D) this medium-gas mixture is contacted than the methane feed side of first film of permeable for carbon dioxide more preferably in first order film separation unit, make this medium-gas mixture selectively penetrating cross this film, with film see through side form described first order permeate gas mixture and
(E) shift out the first order that more is rich in methane than medium-gas mixture from the feed side of first order film separation unit and ooze residual air body mixture.
3, the described method of claim 2, wherein heavy hydrocarbon compounds is absorbed in the process of one way by this absorptive unit and enters absorbent.
4, the described method of claim 2, wherein the heavy hydrocarbon compounds absorption that enters absorbent occurs in greater than under about 5.5MPa (800psi).
5, the described method of claim 2 further comprises:
(F) make the first order ooze residual air body mixture and in the film separation unit of the second level, contact, make first to ooze residual air body mixture selective permeation second film than the methane feed side of second film of permeable for carbon dioxide more preferably, with form second level permeate gas mixture and
(G) from the film separation unit of the second level, shift out and ooze the second level that residual air body mixture more is rich in methane than the first order and ooze residual air body mixture.
6, the described method of claim 5 further comprises this second level permeate gas mixture is added in the dehydration unstrpped gas.
7, the described method of claim 2, wherein contact and absorption step comprise:
(B-1) unstrpped gas of will dewatering is introduced this absorption tower from the feed points of a vertical counter current contacting Gas-Liquid Absorption tower of placing,
(B-2) the most of carbon dioxide in the permeate gas mixture of the condensation first order at least, with formation liquid CO 2 absorbent,
(B-3) the liquid CO 2 absorbent is added from feed points top this absorption tower and
(B-4) discharge byproduct from this absorption tower.
8, the described method of claim 7, wherein being condensate in this absorption tower of carbon dioxide carried out.
9, the described method of claim 7, wherein feed points is positioned at this top, bottom, absorption tower and is lower than half position highly.
10, the described method of claim 2 further comprises with temperature being higher than-5 ℃ cooling medium condensation first order permeate gas mixture approximately.
11, a kind of being used for from the system of the crude mixture production refine methane that contains methane, carbon dioxide and VOC, this system comprises:
(a) drier, its running is anhydrated to remove from crude mixture; And compressor, its running increases to the pressure that is suitable for absorbing heavy hydrocarbon with the pressure with crude mixture,
(b) the adverse current gas-liquid directly contacts absorber, it is positioned at drier and compressor downstream, be suitable for from crude mixture heavy hydrocarbon compounds absorbed basically fully and enter in the liquid CO 2 absorbent, and be suitable in one way, producing the medium-gas mixture that is substantially free of heavy hydrocarbon compounds
(c) first order film separation unit, its have than methane more preferably permeable for carbon dioxide first film, be positioned at the permeate chamber that film and medium-gas mixture fluid are communicated with the feed chamber of side and are positioned at the relative side with feed chamber of this first film, this permeate chamber is suitable for receiving the first order infiltration gas of medium-gas mixture selectively penetrating by first film
(d) condenser, its running with liquefy this first order infiltration gas and
(e) recirculation transfer line, fluid is communicated with between the permeate chamber of this pipeline and the absorber and first film separation unit, turns round to send first order infiltration gas to absorber.
12, the described system of claim 11, wherein feed chamber is suitable for receiving the first order and oozes the residual air body, and this system further comprises:
(f) second level film separation unit, its have than methane more preferably permeable for carbon dioxide second film, be positioned at this second film and the first order and ooze the permeate chamber that residual air body fluid is communicated with the feed chamber of side and is positioned at the relative side with feed chamber of this second film, this permeate chamber be suitable for receiving the first order ooze residual air body mixture selectively penetrating by second film second level infiltration gas and
(g) echo-plex pipeline, fluid is communicated with between the permeate chamber of this pipeline and second level film separation unit and the crude mixture of absorbent upstream, and running is to add second level infiltration gas in the crude mixture that has compressed and dewatered.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
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| US42804702P | 2002-11-21 | 2002-11-21 | |
| US60/428,047 | 2002-11-21 | ||
| US10/712,752 | 2003-11-13 |
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| CN1713949A true CN1713949A (en) | 2005-12-28 |
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