CN102159298A - Process for removing gaseous contaminants from a feed gas stream comprising methane and gaseous contaminants - Google Patents
Process for removing gaseous contaminants from a feed gas stream comprising methane and gaseous contaminants Download PDFInfo
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- CN102159298A CN102159298A CN2009801369345A CN200980136934A CN102159298A CN 102159298 A CN102159298 A CN 102159298A CN 2009801369345 A CN2009801369345 A CN 2009801369345A CN 200980136934 A CN200980136934 A CN 200980136934A CN 102159298 A CN102159298 A CN 102159298A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/067—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
- F25J3/061—Natural gas or substitute natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/0635—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/304—Hydrogen sulfide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/06—Polluted air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Abstract
The invention provides a process for removing gaseous contaminants from a feed gas stream which comprises methane and gaseous contaminants, the process comprising: 1) providing the feed gas stream; 2) cooling the feed gas stream to a first temperature at which liquid phase contaminant is formed as well as a methane enriched gaseous phase; 3) separating the two phases obtained in step 2) by means of a first gas/liquid separator; 4) cooling the methane enriched gaseous phase obtained in step 3) at least party by means of an external refrigerant to a second temperature at which liquid phase contaminant is formed as well as a methane enriched gaseous phase; and 5) separating the two phases obtained in step 4) by means of a second gas/liquid separator. The invention further concerns a device for carrying out the present process, the purified gas stream, and a process for liquefying a feed gas stream.
Description
Technical field
The present invention relates to a kind of method that is used for removing gaseous contaminant, especially from natural gas, remove the method for gaseous contaminant, for example carbon dioxide and hydrogen sulfide from the inlet air flow that comprises methane and gaseous contaminant.
Background technology
The air-flow of producing from subsurface reservoir that comprises methane (especially natural gas, associated gas and coal bed methane) comprises a lot of pollutants, for example fragrant sulphur of carbon dioxide, hydrogen sulfide, carbon oxysulfide, mercaptan, sulfide and the synthetic that comprises different amounts usually.Great majority for these air-flows are used, and must remove pollutant, according to concrete pollutant and/or purposes, perhaps partly remove or almost entirely remove.Usually, must be removed to the ppm level to the sulphur synthetic, for carbon dioxide, must be removed to the ppm level in some cases, for example LNG uses, and perhaps reduces to 2 or 3 percents by volume, for example as heat production gas.Higher hydrocarbon may occur, according to purposes, this higher hydrocarbon can reclaim.
The technology that is used to remove carbon dioxide and sulphur synthetic is well known in the art.These technologies comprise uses for example absorption method of amine aqueous solution, perhaps uses for example absorption method of molecular sieve.These technologies be particularly useful for removing with low amount exist, for example pollutant of maximum several volumes percentage, especially carbon dioxide and hydrogen sulfide.
In WO 2006/087332, described a kind of being used for and removed the method for polluting gaseous component, for example carbon dioxide and hydrogen sulfide from natural gas flow.In this method, the contaminated natural gas flow of cooling in first expander, acquisition has the expanded gas flow of uniform temperature and pressure, under this temperature and pressure, can realize comprising the dew point state of the phase of most pollution components, for example carbon dioxide and/or hydrogen sulfide.Then expanded gas flow is supplied with to first whizzer, so that the liquid phase of enrichment pollutant and the gas phase of poor pollutant are separated.The gas phase of poor pollutant then enters second whizzer via recompression machine, intergrade cooler and second expander.The intergrade cooler and second expander are used for the gas phase of poor pollutant is cooled to such degree, promptly obtain the liquid phase of enrichment pollutant and the gas phase of poorer pollutant once more, by means of second whizzer they are separated subsequently.In the method, the energy that reclaims from first expansion step is used to compression step, and air, water and/or internal process stream are used to the intergrade cooler.
The defective of this known method is, between two whizzers, use recompression machine, intergrade cooler and expander, influenced the hydrocarbon efficient of separation process, described hydrocarbon efficient is the metering of hydrocarbon loss in fuel gas consumption and the liguid phase pollutant stream in this technical process.
Have been found that now, be used for from the integrated approach of air-flow removal gaseous contaminant, if the gas phase of poor pollutant is cooled off by means of external refrigerant at least in part between first and second gas-liquid separations, then can improve hydrocarbon efficient significantly, this allows to separate best gaseous contaminant, can avoid using expander between first and second gas-liquid separations.
Summary of the invention
Thereby, the present invention relates to a kind of method that is used for removing gaseous contaminant from the inlet air flow that comprises methane and gaseous contaminant, this method comprises:
1) provides inlet air flow;
2) inlet air flow is cooled to first temperature, under described first temperature, forms the gas phase of liguid phase pollutant and enrich methane;
3) by means of the first gas-liquid separator separates step 2) the middle two-phase that obtains;
4) at least in part by means of external refrigerant, the gas phase of the enrich methane that obtains in the step 3) is cooled to second temperature, under described second temperature, form the gas phase of liguid phase pollutant and enrich methane; With
5) by means of the two-phase that obtains in the second gas-liquid separator separates step 4).
Suitably, inlet air flow is a natural gas flow, and wherein gaseous contaminant is carbon dioxide and/or hydrogen sulfide.
Natural gas flow suitably comprises the carbon dioxide of 1～90% (volume ratio), preferably includes the carbon dioxide of 5～80% (volume ratios).
Natural gas flow suitably comprises the hydrogen sulfide of 0.1～60% (volume ratio), preferably includes the hydrogen sulfide of 20～40% (volume ratios).
The methane that comprises 20～80% (volume ratios) according to the inlet air flow of the present invention's use.
Suitably, the temperature of the inlet air flow in the step 1) is-20 ℃～150 ℃, is preferably-10 ℃～70 ℃, and its pressure is 10～150bara, is preferably 80～120bara.
Can carry out preliminary treatment to the raw material inlet air flow, partially or even wholly to remove water and some selected heavy hydrocarbons.This can for example carry out against external cooling circuit or cold internal process stream by pre-cooled circulation.Also can use molecular sieve, for example zeolite, or silica gel, or aluminium oxide, or other drier, for example ethylene glycol, PPG (MEG), diethylene glycol (DEG) (DEG) or tetraethylene glycol (TEG) or glycerine carry out preliminary treatment and remove water.The amount of water is less than 1% (volume ratio) suitably in the inlet air flow, preferably less than 0.1% (volume ratio), is more preferably less than 0.0001% (volume ratio).
Step 2) cooling to inlet air flow in can be undertaken by method as known in the art.For example, can cool off against the external refrigeration fluid.Under the sufficiently high situation of admission pressure, can realize cooling by the expansion of inlet air flow.
Also can make up.The suitable method of cooling inlet air flow can be undertaken by approximate constant entropy expansion, especially can be by means of expander, preferably by means of turbo-expander or Laval nozzle.Another suitable mode is by isenthalpic expansion cooling inlet air flow, is preferably the isenthalpic expansion through throttle orifice or valve, especially Joule-Thomson valve.
Preferably, expansion utilizes at least two expansion gears to carry out, and selects the running parameter of expansion gear, makes that the liquefied contaminants in the stream that cools off has certain droplets size distribution.By utilizing at least two expansion gears, allow the droplets size distribution of control condensed contaminants.
In a preferred embodiment, before expanding, carry out pre-cooled to inlet air flow.This can be by carrying out against external cooling circuit or against cold process flow, for example liquid pollutant.Preferably, air-flow was pre-cooled to 15 ℃～-35 ℃ temperature before expanding, preferably be cooled to 10 ℃～-20 ℃.Pre-cooled can carrying out against internal process stream.Especially when inlet air flow was compressed, the temperature of inlet air flow can be 100 ℃～150 ℃.In this case, can at first use air cooling or water-cooled to reduce temperature, optionally connected further cooling.
Another suitable cooling means is against cooling fluid medium, especially external refrigerant, for example propane cycles, ethane/propane cascade (cascade) or mix refrigerant circulation carrying out heat exchange, can select and the combination of internal process loop, suitably flow or flushing liquor for carbon dioxide stream (liquid or slurry stream), cold enrich methane in described internal process loop.
Inlet air flow is suitably in step 2) and 4) in be cooled to-30 ℃～-80 ℃ temperature, preferably be cooled to-40 ℃～-65 ℃ temperature.Under these temperature, will form liguid phase pollutant.
Suitably, applied pressure can be higher than step 2 in the step 4)) middle applied pressure.
Preferably, second temperature in the step 4) is lower than step 2) in first temperature.
Preferably, second temperature in the step 4) is than step 2) in low at the most 20 ℃ of first temperature.More preferably, second temperature is than step 2) in first temperature low 5 ℃～10 ℃.
Cooling in the step 4) also can be carried out by means of internal process stream, the liguid phase pollutant stream of for example separating from the gas phase of enrich methane in step 3).
According to the present invention, the cooling of the gas phase of enrich methane suitably can be undertaken by external refrigerant to small part in the step 4).
Preferably, the external refrigerant of using in step 4) has the molecular weight higher than the gas phase of enrich methane to be cooled.The example of this cooling medium that is fit to comprises ethane, propane and butane.Preferably, cooling medium comprises ethane and/or propane.
More preferably, employed external refrigerant comprises propane cycles, ethane/propane mix refrigerant or ethane/propane cascade.This ethane/propane cascade will be described hereinafter in further detail.
Cooling in the step 4) suitably can part be carried out by means of internal process stream by means of external refrigerant, part, and described internal process stream is the liguid phase pollutant stream for separating from the gas phase of enrich methane in step 3) for example.
Cooling in the step 4) is for example owing to use external refrigerant to carry out, so can change recompression machine, intergrade cooler and, improve the hydrocarbon efficient of separation process very attractively as the order of the WO 2006/087332 described expander that between two whizzers, uses.
In another embodiment of the present invention, before carrying out step 4), the gas phase of the enrich methane that obtains in the step 3) is recompressed in one or more compression step.
In another embodiment of the present invention, before the cooling of carrying out step 4), the gas phase of the enrich methane that obtains in the step 3) is at first by the cooling of intergrade cooler.
In another preferred embodiment of the present invention, the gas phase of the enrich methane that obtains in the step 3) is at first recompressed in one or more compression step, then by the cooling of intergrade cooler, cools off in step 4) subsequently.
Suitably, this intergrade cooler can be based on internal process stream and air cooling or water-cooled.
Suitably, under the situation of the inner formation of cooler liquid, this cooler is designed so that to remove liquid effectively from cooling device, and can not weaken heat transmission.
In described one or more compression step, suitably, can use step 2) the middle energy that reclaims.
In according to this technology of the present invention, step 3) and 5) can suitably use gas-liquid separator miscellaneous, for example rotating centrifugal device or cyclone.
Step 3) and 5) can use the gas-liquid separator of dissimilar or same type.Suitably, step 3) and 5) can use the gas-liquid separator of same type.
According to the present invention, the gas-liquid separator that be fit to use for example has been described among WO2008/082291, WO 2006/087332, WO 2005/118110, WO 97/44117, WO 2007/097621 and the WO 94/23823, and these files are hereby incorporated by.
Usually, because the drop that the homogeneous droplet nucleation produces after expanding lacks than the heterogeneous nucleation that is cooled off by external process stream in the heat exchanger, so the requirement of gas-liquid separator is stricter than the requirement in the step 5) in the step 3).
In a preferred embodiment of the invention, first and/or second gas-liquid separator comprises that the gas-liquid that is positioned at intermediate altitude enters the mouth, is arranged in the liquid outlet of gas-liquid inlet below and the gas vent that is arranged in gas-liquid inlet top, in this container, be provided with the coalescer that is generally horizontal above the gas-liquid inlet and on the entire cross section of container, and in this container, arranging a centrifugal liquid separator above the coalescer and on the entire cross section of container, this liquid separator comprises one or more swirling flow pipe.
When using vertical gas-liquid separator container, this technology only needs less zone.
According to preferred embodiment, the gas-liquid inlet comprises the input (admittance) that has horizontally extending supply allocation component in separator flask.In its simple form, inlet is a simple pipeline, has blind end and some equally distributed perforation on the length of pipeline.At random, pipeline also can have and phases down or conical shape.Also one or more cross pipeline can be set, form grid system, on the cross section of container, to distribute gas-liquid mixture more equably.Preferably, this assembly comprises a chamber, a vertical box structure for example, and it is connected in the gas access, and has the vertical side of at least one opening, and streamwise is seen, the grid of the guide vane that is provided with before and after the vertical side of described opening has.Supply with allocation component by means of this, the uniform distribution on the cross section of column casing (column) of the diversed blade of gas, this can additionally improve the fluid separation applications of coalescer/whizzer combination.Another advantage is, supplies with allocation component any liquid bolus that appears at suddenly in the air-flow is separated from gas, and this separation is subjected to the guide vane collision and in the influence of the fallen liquid in column casing inside.Suitably, box structure narrows down on flow direction.After being distributed on the column casing cross section by blade, gas flows upward to coalescer.
In a preferred embodiment, vertical cavity has two vertical sides of opening that have the guide vane grid.
The gas-liquid inlet that is fit to for example is described among GB 1119699, US 6942720, EP195464, US 6386520 and the US 6537458.The gas-liquid that can buy on the market inlet that is fit to is Schoepentoeter.
There are a lot of spendable horizontal coalescers in particular for vertical column casing.The well-known example of demister is the demist pad.All these more very thin (permeability is big), and have bigger unit (inside) surface area.Their operation is based on by the collision of drop and inner surface and collects drop, and drop increases on these surfaces then, removes the drop that increases at last by gas or by gravity.
Horizontal coalescer has many forms well known in the prior art, for example, can be by having multilayer gauze, especially metal gauze or nonmetal gauze, for example organic polymer gauze or base with one deck blade or layer of structured packing constitute.Also unsetting filler can be used, and also one or more pallet can be provided with.The coalescer of all these kinds all has the advantage that can buy on the market and can efficiently move in according to column casing of the present invention.Also can be referring to Perry ' s Chemical Engineers ' Handbook, sixth version, especially the 18th chapter.Also can be referring to EP 195464.
The centrifugal liquid separator of simple form can comprise level board and one or more vertical swirling flow pipe that extends from this level board downwards, and each swirling flow pipe all has one or more liquid outlet that is positioned at the level board below in the top.In another form, centrifugal liquid separator comprises one or more from the upwardly extending vertical swirling flow pipe of this level board, and each swirling flow pipe has one or more liquid outlet in the upper end.This level board is provided with downspout, is preferably the downspout of the lower end that extends to separator flask.
In a preferred embodiment of the present invention, centrifugal liquid separator comprises: two level trays, be extended with the vertical swirling flow pipe that has openend between two level trays, each swirling flow pipe extends to a distance of the coaxial openings below of top tray from the opening of following pallet; Be used for from the space drainage assist gas between the pallet of swirling flow tube outside and the device of liquid; And be arranged in the lower part of swirling flow pipe to give the device that rotatablely moves of gas-liquid around vertical axis.
Liquid separator also preferably is provided with vertical pipe fitting, and described vertical pipe fitting is projected into downwards the swirling flow pipe from the coaxial openings of top tray, and has the diameter littler than swirling flow pipe.This arrange improved separating between main gas and the liquid on the one hand, improved separating between assist gas and the liquid on the other hand, and this is because the opening from the swirling flow pipe to the top tray that is used for main gas can not be realized the latter.
According to preferred embodiment, be used for constituting by the vertical tubule that passes top tray, be used for constituting by one or more the vertical delivery pipe that extends to the column casing bottom from this space from the device of the space drainage liquid between the pallet from the device of the space drainage assist gas between the pallet.Thisly dispose following benefit, promptly, assist gas and pallet between described space in fluid separation applications after and then turn back to main gas, liquid is then at the liquid that joins the column casing bottom after coalescer comes out, like this, assist gas of removing in cyclone and liquid do not need independent processing.
In order further to improve the fluid separation applications in the cyclone, according to the present invention, preferably offer opening at the top of swirling flow pipe, be used for fluid discharge to the space between the pallet of swirling flow tube outside.The benefit of bringing like this is that less assist gas is sent in the space between the pallet.The cyclone that can buy on market that is fit to is Shell Swirltube deck.
In a preferred embodiment, separation container comprises that second on the entire cross section that is positioned at centrifugal formula separator top and is positioned at container is generally horizontal liquid coalescer.The benefit of bringing like this is that any drop that still is present in the air-flow can both be removed.Further describe referring to above.Preferably, second coalescer is to have for example base of organic polymer gauze of one deck or more multi-layered gauze, especially metal gauze or nonmetal gauze.In a further advantageous embodiment, second is generally horizontal liquid coalescer is positioned at assist gas outlet top, the mode described in EP83811, especially as shown in Figure 4.
In most preferred embodiment, the first and/or second used separator comprises:
A) shell, it comprises first, second and the 3rd separate sections that is used for from the mixture separating liquid, wherein second separate sections is arranged in the top of first separate sections below and the 3rd separate sections, and corresponding separate sections is communicated with each other, and second separate sections comprises the rotation coalescer element;
B) inlet device of arranged tangential is used for mixture is imported first separate sections;
C) be used for from the device of first separate sections removal liquid;
D) be used for from the device of the 3rd separate sections removal liquid; With
E) be used for from the device of the poor gaseous flow of the 3rd separate sections removal liquid.
In the present invention, first and/or second gas-liquid separator can suitably comprise cyclone, and described cyclone comprises a branch of parallel channels, and these parallel channels are arranged in one in coil, and parallel with the rotation from coil.
Suitably, in this technology, cyclone spins from coil by the swirling flow air-flow is imported.
Preferably, the cyclone that uses according to the present invention comprises shell, and described shell has: in the gas access that is used for dusty gas of container one end; Separate main body; The gas vent of the gas that is used to purify of the relative end of shell be in the pollutant outlet that separates the main body downstream or be in the pollutant outlet that separates the main body upstream and downstream, wherein separate main body and comprise a plurality of pipelines on the part of housing axis length, described pipeline is arranged around the pivot axis, in this equipment, separating main body is made of a plurality of perforated disc, wherein, the perforation of perforated disc forms pipeline.
Should be understood that these dishes can be easily by getting out or a plurality of perforation making of cutting on thin dish.By some dishes are attached together, these dish type compositions are from main body.By these perforation of aliging, form pipeline.
Also be very easy to now dish is attached together, make perforation not exclusively align.By changing quantity and the character that perforation does not line up, can make the pipeline of formation produce any desired shape.Under these circumstances, not only can obtain not exclusively to be parallel to the pipeline of pivot axis, and can obtain to form spiral-shaped pipeline around rotation.So realization so at an easy rate has the preferred embodiment of non-parallel pipeline.Therefore, preferably, the perforation of dish is arranged such that pipeline is not with the rotary middle spindle line parallel or form spiral-shaped around rotation.
Further be to be further appreciated that, increase or reduce penetration hole diameter and also be relatively easy to.Thereby those skilled in the art have simple mode and handle changing (fluid power) diameter of pipeline, thereby change Reynolds number, like this, can easily determine ductedly mobilely to be laminar flow or turbulent flow, and are desirable as it.By utilizing these dishes, can also make those skilled in the art change the diameter of pipeline along the axis of shell.Select different-diameter, make to be collected in not blocking pipe fully of the liquid state of being separated on the duct wall or solid pollutant, if blocking pipe can hinder the operation of equipment.
Those skilled in the art also can make the porosity maximum of separating main body at present.This simple construction of dish allows those skilled in the art that the dish of the perforation with as much desirable with it is provided carefully.And he also can select the shape of boring a hole.These perforation can have circular cross-section, but also can be square, pentagon, hexagon, octagon or elliptic cross-section.Therefore he also can minimize the wall thickness of separation main body and the wall thickness of pipeline.He can select the wall thickness and the shape of pipeline, makes the surface area minimum, and surface area is helpful to the cross section that separates main body.This means that the pressure drop that separates on the main body can minimize.
This equipment can have a small amount of or a large amount of pipelines.Explain that as existing equipment the scope of number of tubes is from 100 to 1000000 suitably, preferably from 500 to 500000.Also can change the diameter of cross-section of pipeline according to the amount of the amount of gas, pollutant and character for example droplets size distribution and desired pollutants removal rate.Suitably, diameter is 0.05mm～50mm, is preferably 0.1mm～20mm, more preferably 0.1mm～5mm.Under the situation of circular cross section, understand that all diameter is the twice of radius, perhaps under the situation of any other shape, diameter is a maximum diagonal.
According to the amount of gas to be processed, can change the size of equipment, especially separate the size of main body.Illustrated in EP-B 286 160, circle diameter is that 1m, axial length are that the separation main body of 1.5m is feasible.Can suitably have the radical length of scope from 0.1m to 5m according to separation main body of the present invention, the radical length of preferable range from 0.2m to 2m.The scope of axial length can be easily from 0.1m to 10m, preferably from 0.2m to 5m.
The quantity of dish also can be in wide variation very.Simple separation and/or can easily making when perforation can only have two dishes if desired.Other also can consider whether need parallelpiped or whether need homogeneous diameter.The right quantity of dish is 3～1000, is preferably 4～500, more preferably 4～40.If use more dish, those skilled in the art can find, change pipe diameter gradually and/or make up non-parallel pipeline to be more prone to.In addition, by the quantity of increase or minimizing dish, those skilled in the art also can change duct length.So when the state of gas or composition changed, those skilled in the art can easily change duct length and think that equipment of the present invention provides optimum state.The size of selective pan makes that radially radius suitably changes from 0.1m to 5m, preferably change from 0.2m to 2m.Also can wait the axial length that changes dish according to the expectation of the possibility of constructing, change shape etc.Suitably, the axial length range of each dish changes from 0.001m to 0.5m, preferably changes from 0.002m to 0.2m, more preferably changes from 0.005m to 0.1m.
Though dish can be by various materials, comprise that paper, cardboard and paper tinsel make, preferably by metal or ceramic making dish.Metal dish has easy perforation and is combined into the benefit of firm, firm separation main body.The material that can purify is as required selected suitable metal.Use for some, carbon steel is fit to, and for other application, especially when the sepatation etching material, possibility is stainless steel preferably.Pottery has can extrude into the benefit that desired form for example has the honeycomb of outstanding pipeline.
Usually, select the ceramic precursor material to form pottery fine and close or low-porosity.Thereby force solid pollutant or liquid pollutant to flow, rather than or the ceramic material by wall hardly along the wall of pipeline.The example of ceramic material is silica, alumina, zirconia, can select the conditioning agent of dissimilar and concentration so that its physics and/or chemical property adapt to gas and pollutant.
These dishes can be combined into one in various modes and separate main body.It will be understood by those skilled in the art that this can be depending on the material of manufacturing dish.Mode is that these dishes are attached on the axle that rotation is provided easily.The method that is fit to that makes up these dishes comprises these dishes is picked up, and still, also can bond them or weld together.As selection, these dishes can be stacked in the cylindrical sleeves.This sleeve also can replace axle at least in part.This may be convenient to extruding disk, because do not need to be used for the central opening of axle.Preferably has the metal dish that welds together.
In a preferred embodiment of the present invention, the gas phase of the enrich methane that obtains according to the present invention is further purified, for example by with chemical solvent for example amine aqueous solution, especially water-ethanol amine (for example diisopropanolamine (DIPA) (DIPA), dimethylamine (DMA), methyl diethanolamine (MDEA) etc.), perhaps for example cold methanol, DEPG, N-methyl pyrrolidone (NMP) or the like extract residual acidic components with physical solvent.
Contaminated air-flow is constantly supplied, cooling constantly, and constantly separate.
The invention still further relates to device (equipment) that is used to carry out said method and the purifying gas flow that obtains by this method.In addition, the invention still further relates to the method for the inlet air flow that is used to liquefy, it comprises by means of this method and purifies inlet air flow, then the inlet air flow that is purified by method liquefaction as known in the art.
The specific embodiment
To further specify the present invention by means of following accompanying drawing.
With reference to Fig. 1, natural gas via flows through expansion gear 2 by conduit 1, and acquisition comprises the stream of the gas phase of liguid phase pollutant and enrich methane thus.This is flowed through and flows into a gas-liquid separator 4 by a conduit 3, and here two-phase is separated from one another.Liguid phase pollutant reclaims via a conduit 5, and the gas phase of enrich methane then flows in the heat exchanger 7 via a conduit 6.Heat exchanger 7 uses ethane as external refrigerant, and ethane is cooled by means of ethane/propane cascade 8 thus, has described ethane/propane cascade 8 in Fig. 2 in further detail.The gas phase of enrich methane is cooled to a certain temperature in heat exchanger 7, form the gas phase of liguid phase pollutant and enrich methane thus.Comprise that then flowing through of this two-phase flowed in the gas-liquid separator 10 by a conduit 9, from this gas-liquid separator 10, further the gas phase of enrich methane reclaims via a conduit 11, and liguid phase pollutant reclaims via a conduit 12.
In Fig. 2, shown heat exchanger 7 has used ethane, and ethane cools off by means of ethane/propane cascade, and described ethane/propane cascade comprises ethane loop and propane loop.In the ethane loop, ethane stream flows into an expander 14 (for example turbine expander or Joule-Thomson valve) via a conduit 13, and the thus obtained ethane stream that is cooled is via in conduit 15 inflow heat exchangers 7.The ethane stream of temperature then flows into recompression machine 16 from heat exchanger 7 through a conduit 17, to increase the pressure of ethane stream.The ethane compressive flow that obtains from recompression machine 16 is then via in conduit 18 inflow heat exchangers 19, and in heat exchanger 19, ethane stream is cooled, and is condensed to small part.Ethane stream is recycled to expander 14 via conduit 13.In propane loop, propane stream flows into an expander 21 (for example turbine expander or Joule-Thomson valve) via a conduit 20, and the thus obtained propane stream that is cooled flows in the heat exchanger 19 in ethane loop via conduit 22.The propane stream of temperature then flows into recompression machine 24 from heat exchanger 19 through a conduit 23, to increase the pressure of propane stream.The propane compressive flow that obtains from recompression machine 24 is then via in conduit 25 inflow heat exchangers 26, and in heat exchanger 26, propane stream is cooled, and by means of water or air it is condensed to small part.Propane stream is recycled to expander 21 via conduit 20.
In Fig. 3, shown step 3) and 5 for this method) gas-liquid separator that is fit to that uses.Gas-liquid separator 4 shown in Figure 1 and 10 can be this type.The stream that comprises the gas phase of liguid phase pollutant and enrich methane flows into gas-liquid separator 4 (or gas-liquid separator 10) by conduit 3 (or conduit 9) and via supplying with allocation component 27.Most of liquid flows to the lower end of separator downwards, and leaves separator via liquid outlet 5.Comprise big and then flow upward to the top of separator flask, and leave separator flask via gas vent 6 via liquid coalescer 28, cyclone 29 and the second liquid coalescer 30 than the gaseous flow of droplet.
In Fig. 4, shown step 3) and 5 for this method) another gas-liquid separator that is fit to of using.Gas-liquid separator 4 shown in Figure 1 and 10 can be this type.The flowing through of gas phase that comprises liguid phase pollutant and enrich methane flow to the gas access 31 of the shell 32 of gas-liquid separator 4 (or gas-liquid separator 10) by conduit 3 (or conduit 9).Shell 32 comprises that also one separates main body 33, and this separation main body 33 has shown the pipeline of arranging around the axle 35 that rotation is provided in a large number 34.Separating main body 33 is made up of six dish 33a, 33b, 33c, 33d, 33e and 33f combining by welding or bonding.In the separation main body of rotation, the drop of carbon dioxide and/or hydrogen sulfide is separated from natural gas.The pollutant of separating is discharged from shell via pollutant outlet 36 and discharge pipe 5, and described pollutant outlet 36 is arranged in the downstream of separating main body 33.The natural gas via that purifies leaves shell 32 by the gas vent 6 of a relative end that is arranged in shell 32.
Claims (15)
1. one kind is used for from the method for the inlet air flow removal gaseous contaminant that comprises methane and gaseous contaminant, and this method comprises:
1) provides inlet air flow;
2) inlet air flow is cooled to first temperature,, forms the gas phase of liguid phase pollutant and enrich methane in described first temperature;
3) by means of the first gas-liquid separator separates step 2) the middle two-phase that obtains;
4) at least in part by means of external refrigerant, the gas phase of the enrich methane that obtains in the step 3) is cooled to second temperature, in described second temperature, form the gas phase of liguid phase pollutant and enrich methane; With
5) by means of the two-phase that obtains in the second gas-liquid separator separates step 4).
2. the method for claim 1, wherein first and/or second gas-liquid separator comprises cyclone, and described cyclone comprises a branch of parallel channels, and these parallel channels are arranged in one in coil, and parallel with the rotation from coil.
3. method as claimed in claim 1 or 2, wherein, first and/or second gas-liquid separator comprises shell, described shell has: in the gas access of the gas that is used to pollute of container one end; Separate main body; Gas vent at the gas that is used to purify of the relative end of this shell; Export with being in the pollutant outlet that separates the main body downstream or being in the pollutant that separates the main body upstream and downstream, wherein said separation main body comprises a plurality of pipelines on the part of housing axis length, described pipeline is arranged around the pivot axis, in this equipment, separating main body is made of a plurality of perforated disc, wherein, the perforation of perforated disc forms pipeline.
4. the method for claim 1, wherein first and/or second gas-liquid separator comprises:
A) shell, it comprises first, second and the 3rd separate sections that is used for from the mixture separating liquid, wherein second separate sections is arranged in the top of first separate sections below and the 3rd separate sections, and corresponding separate sections is communicated with each other, and second separate sections comprises the rotation coalescer element;
B) inlet device of arranged tangential is used for mixture is imported first separate sections;
C) be used for from the device of first separate sections removal liquid;
D) be used for from the device of the 3rd separate sections removal liquid; With
E) be used for from the device of the poor gaseous flow of the 3rd separate sections removal liquid.
5. the described method of arbitrary as described above claim, wherein, inlet air flow is a natural gas flow, gaseous contaminant is carbon dioxide and/or hydrogen sulfide.
6. method as claimed in claim 5, wherein, natural gas flow comprises that suitably volume ratio is 1～90% carbon dioxide, preferably includes volume ratio and be 5～80% carbon dioxide, and/or volume ratio is 0.1～60% hydrogen sulfide, preferably includes volume ratio and be 20～40% hydrogen sulfide.
7. the described method of arbitrary as described above claim, wherein, inlet air flow comprises that volume ratio is 20～80% methane.
8. the described method of arbitrary as described above claim, wherein, the temperature of the inlet air flow in the step 1) is-20 ℃～150 ℃, is preferably-10 ℃～70 ℃, its pressure is 10bara～150bara, is preferably 80bara～120bara.
9. the described method of arbitrary as described above claim, wherein, step 2) cooling is cooled off by isenthalpic expansion, be preferably isenthalpic expansion through throttle orifice or valve, especially Joule-Thomson valve, perhaps wherein by approximate constant entropy expansion, especially by means of expander, preferably carry out by means of turbine expansion device or Laval nozzle, preferred wherein inlet air flow was pre-cooled to 15 ℃～-35 ℃ temperature before expanding, preferably be cooled to 10 ℃～-20 ℃.
10. method as claimed in claim 9, wherein, expansion utilizes at least two expansion gears to carry out, and selects the running parameter of expansion gear, makes the acid pollution thing of liquefaction have certain droplets size distribution.
11. the described method of arbitrary as described above claim, wherein, inlet air flow is in step 2) and 4) in be cooled to-30 ℃～-80 ℃ temperature, preferably be cooled to-40 ℃～-65 ℃ temperature.
12. the described method of arbitrary as described above claim, wherein, applied pressure is higher than step 2 in the step 4)) middle applied pressure, perhaps wherein second temperature in the step 4) is lower than step 2) in first temperature, second temperature in the preferred wherein step 4) is than step 2) in low 20 ℃ at the most of first temperature.
13. the described method of arbitrary as described above claim, wherein, external refrigerant has the molecular weight higher than the gas phase of enrich methane to be cooled, and more preferably, wherein external refrigerant comprises propane cycles, ethane/propane mix refrigerant or ethane/propane cascade.
14. the described method of arbitrary as described above claim, wherein, first and/or second gas-liquid separator comprises that the gas-liquid that is positioned at intermediate altitude enters the mouth, is arranged in the liquid outlet of gas-liquid inlet below and the gas vent that is arranged in gas-liquid inlet top, in this container, be provided with the coalescer that is generally horizontal above the gas-liquid inlet and on the entire cross section of container, and in this container, arranging a centrifugal liquid separator above the coalescer and on the entire cross section of container, this liquid separator comprises one or more swirling flow pipe.
15. the air-flow of the purification that obtains according to the described method of aforementioned arbitrary claim.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP08164892 | 2008-09-23 | ||
| EP08164892.5 | 2008-09-23 | ||
| PCT/EP2009/061795 WO2010034627A1 (en) | 2008-09-23 | 2009-09-11 | Process for removing gaseous contaminants from a feed gas stream comprising methane and gaseous contaminants |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102159298A true CN102159298A (en) | 2011-08-17 |
Family
ID=40428001
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009801369345A Pending CN102159298A (en) | 2008-09-23 | 2009-09-11 | Process for removing gaseous contaminants from a feed gas stream comprising methane and gaseous contaminants |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US20110192190A1 (en) |
| CN (1) | CN102159298A (en) |
| CA (1) | CA2735919A1 (en) |
| EA (1) | EA201100522A1 (en) |
| WO (1) | WO2010034627A1 (en) |
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Also Published As
| Publication number | Publication date |
|---|---|
| CA2735919A1 (en) | 2010-04-01 |
| EA201100522A1 (en) | 2011-08-30 |
| WO2010034627A1 (en) | 2010-04-01 |
| US20110192190A1 (en) | 2011-08-11 |
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