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CN100473927C - Natural gas liquefaction method and device - Google Patents

Natural gas liquefaction method and device Download PDF

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Publication number
CN100473927C
CN100473927C CNB2004800428521A CN200480042852A CN100473927C CN 100473927 C CN100473927 C CN 100473927C CN B2004800428521 A CNB2004800428521 A CN B2004800428521A CN 200480042852 A CN200480042852 A CN 200480042852A CN 100473927 C CN100473927 C CN 100473927C
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China
Prior art keywords
flow
stream
residual gas
heat
condensation
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CNB2004800428521A
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Chinese (zh)
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CN1946979A (en
Inventor
约翰·D·威尔金森
汉克·M·哈德森
凯尔·T·奎利亚尔
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Ortloff Engineers Ltd
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Ortloff Engineers Ltd
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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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0214—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
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    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
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    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
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    • 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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Abstract

A process for liquefying natural gas in conjunction with producing a liquid stream containing predominantly hydrocarbons heavier than methane is disclosed. In the process, the natural gas stream to be liquefied is partially cooled, expanded to an intermediate pressure, and supplied to a distillation column. The bottom product from this distillation column preferentially contains the majority of any hydrocarbons heavier than methane that would otherwise reduce the purity of the liquefied natural gas. The residual gas stream from the distillation column is compressed to a higher intermediate pressure, cooled under pressure to condense it, and then expanded to low pressure to form the liquefied natural gas stream.

Description

The method of natural gas liquefaction and equipment thereof
Technical field
The present invention relates to a kind of method that is used for handling natural gas or other methane-rich gas stream, the liquid stream that has liquefied natural gas (LNG) stream of high methane purity and mainly comprise the hydro carbons heavier with generation than methane.
Background technology
Usually the well from pierce subsurface reservoir reclaims natural gas.It has the methane of main component usually, and namely for methane comprises the gas of at least 50 molar percentages.According to concrete subsurface reservoir, natural gas also comprise in a small amount than heavy hydrocarbons, as ethane, propane, butane, pentane or the like; And water, hydrogen, nitrogen, carbon dioxide, and other gas.
Most of natural gases are with handled in gaseous form.Being used for natural gas is the gases at high pressure conveyance conduits from the common unit that well head is transported to gas treatment factory and is transported to the natural gas client from here.Yet, under multiple situation, have been found that in order to transport or must and/or to wish liquefied natural gas in order to use.For example in remote location, usually do not allow easily transport natural gas to the pipeline foundation structure in market.Under these circumstances, by allowing to use freighter and haulage truck to carry LNG, the LNG specific volume much lower with respect to gaseous natural gas can reduce cost of transportation widely.
The another kind of situation of preference natural gas liquefaction is about its purposes as fuel for motor vehicle.In metropolitan area,, bus, taxi, car, and the truck caravan that can be supplied with power by LNG are arranged then if suitable economic LNG source is arranged.Such LNG for fuel vehicle when comparing, owing to natural gas clean burning characteristic produces remarkable less air pollution with the similar vehicles of supplying with power by the gasoline of burning higher molecular weight hydro carbons and Diesel engine.In addition, if LNG is highly purified (that is, having 95 molar percentages or higher methane purity), then since for other HC fuel of methane and all compare than low-carbon (LC): hydrogen ratio, the carbon dioxide of generation (" greenhouse gases ") amount is significantly less.
Summary of the invention
The present invention relates generally to the liquefaction of natural gas, simultaneously produce the liquid stream that mainly comprises the hydro carbons heavier, as comprise ethane, propane, butane, and the natural gas liquids of heavy hydrocarbons composition (NGL) more than methane as by-product stream; Comprise propane, butane, reach the more liquefied petroleum gas of heavy hydrocarbons composition (LPG); Or comprise butane, and the condensate of heavy hydrocarbons composition more.Produce byproduct liquid stream and have two important benefit: the LNG of generation has high methane purity, and byproduct liquid is the valuable product that can be used for multiple other purpose.Canonical analysis according to the pending natural gas flow of the present invention is 84.2% methane, 7.9% ethane and other C by approximate molar percentage 2Composition, 4.9% propane and other C 3Composition, 1.0% iso-butane, 1.1% normal butane, 0.8% pentane additives are formed remainder by nitrogen and carbon dioxide.Sulfurous gas also exists sometimes.
Be useful on the multiple known method of liquefied natural gas.For example, for Finn is seen in the investigation of multiple such process, Adrian J., Grant L.Johnson, and Terry R.Tomlinson " LNG Technology for Offshore and Mid-Scale Plants (the LNG technology that is used for offshore and medium-scale factory) ", Proceeding of the Seventy-Ninth AnnualConvention of the Gas Processors Association (the 79 annual meeting procceedings of gas treatment device association), pp.429-450, Atlanta, Georgia, March 13-15,2000 and Kikkawa, Yoshitsugi, Masaaki Ohishi, and Noriyoshi Nozawa " Optimize the Power System of Baseload LNG Plant (optimizing the dynamical system of base load LNG factory) ", Proceedings of the Eightieth AnnualConvention of the Gas Processors Association (the 80 annual meeting procceedings of gas treatment device association), San Antonio, Texas, March 12-14,2001.U.S. Patent No. 4,445,917; No.4,525,185; No.4,545,795; No.4,755,200; No.5,291,736; No.5,363,655; No.5,365,740; No.5,600,969; No.5,615,561; No.5,651,269; No.5,755,114; No.5,893,274; No.6,014,869; No.6,062,041; No.6,119,479; No.6,125,653; No.6,250,105 B1; No.6,269,655 B1; No.6,272,882 B1; No.6,308,531 B1; No.6,324,867 B1; No.6,347,532 B1; And be filed in our the U.S. Patent application No.10/161 common co-pending on June 4th, 2002,780 have also described correlated process.These methods generally comprise wherein and to purify (anhydrating and trouble compound such as carbon dioxide and sulphur compound by removing), cooling, condensation, and the step of expansion natural gas.The cooling of natural gas and condensation can be finished with multitude of different ways." tandem cooling " utilizes the heat exchange of natural gas and several cooling agents, and these several cooling agents have lower successively boiling point, as propane, ethane, and methane.As selecting example, this heat exchange can use single cooling agent to realize by evaporative cooling agent under several different pressures levels." multicomponent cooling " utilizes the heat exchange of natural gas and one or more coolant fluids, and this coolant fluid comprises several coolant compositions that replace a plurality of single component cooling agents.Expansion constant enthalpy ground of natural gas (for example, using Joule-Thomson to expand) and constant entropy ground (for example, use work-expansion turbine) are finished.
Regardless of being used for the method for liquefied natural gas stream, normally before the liquefaction methane-rich stream, require to remove the signal portion of the hydro carbons heavier than methane.The reason of removing step for this hydrocarbon is various, comprises the heat value of needs control LNG stream and as these values than the heavy hydrocarbons composition of product itself.Unfortunately, seldom notice being focused on hydro carbons so far removes on the efficient of step.
Have been found that according to the present invention hydro carbons is removed step to be integrated in the LNG liquefaction process carefully, use the energy that significantly lacks than the prior art process can produce LNG with separate than the heavy hydrocarbons fluid product.Although the present invention is suitable under lower pressure, when 400 to 1500psia[2,758 to 10, when handling feeding gas in 342kPa (a) or the higher scope, convenient especially.
Description of drawings
In order to understand the present invention better, with reference to following example and accompanying drawing.With reference to accompanying drawing:
Fig. 1 is the flow chart of natural gas liquefaction plant that is suitable for the byproduct of LPG according to the present invention;
Fig. 2 and 3 is figure of the fractionating system selected that can adopt in process of the present invention;
Fig. 4 is the pressure-enthalpy phase diagram that is used for methane, is used for illustrating that the present invention is better than the advantage of prior art process; And
Fig. 5,6,7,8,9, and 10 are the flow charts that to select natural gas liquefaction plant according to the pair production that the present invention is suitable for fluid stream.
In the description below of above accompanying drawing, the form of statistic flow is provided, be used for the calculating of exemplary process condition.Here in the form of Chu Xianing, the value (mole per hour) that is used for flow for convenience rounding to immediate integer value.The overall flow rate rate of representing in form comprises all non-hydrocarbons compositions, and therefore generally becomes the flow sum of shunting greater than hydro carbons.Temperature indicative is the approximation that rounding arrives the nearest number of degrees.Also should be noted that the process designing and calculating of carrying out for the purpose of the process described more in the accompanying drawings based on not from around to the hypothesis of the heat leakage of process (or from process to around).The quality of available insulating materials makes this become very reasonably hypothesis, and is a kind of hypothesis of being undertaken by those skilled in the art typical case.
For convenience's sake, procedure parameter is reported with traditional English unit with the unit of International System of Units (SI).The molar flow that in form, provides can be interpreted as the pound-mol per hour or kilogram mole per hour.Energy consumption be reported as horsepower (HP), and/or thousand British thermal unit (BTU)s per hour (MBTU/Hr) with corresponding with pound-mol's regulation molar flow hourly.Corresponding by kilowatt energy consumption of (kW) report with kilogram mole regulation molar flow hourly.By the pound per hour (Lb/Hr) report throughput rate corresponding with pound-mol's regulation molar flow hourly.Per hour the throughput rate of (kg/Hr) report is corresponding with kilogram mole regulation molar flow hourly by kilogram.
The specific embodiment
Referring now to Fig. 1, we begin explanation according to process of the present invention, wherein wish to produce the most of propane that is included in the natural gas feed flow and the LPG byproduct of heavier composition.In this simulation of the present invention, inlet gas is at 90 ℉ [32 ℃] and 1285psia[8,860kPa (a)] under 31 enter factory as stream.Prevent that product stream from satisfying the certain density carbon dioxide and/or the sulphur compound of specification if inlet gas comprises, then these compounds are removed by the suitable preliminary treatment (not showing) of feeding gas.In addition, feed flow dewaters usually, forms to prevent hydrate under cryogenic conditions (ice).Solid drier typically has been used for this purpose.
Feed flow 31 is cooled by the heat exchange with cooling agent under-14 ℉ [26 ℃] stream and dilatation separator liquid (flowing 40a) in heat exchanger 10.Note, in all cases, the heat exchanger 10 a plurality of single heat exchangers of representative or single repeatedly by heat exchanger or its any combination.(will depend on a plurality of factors for indicating the cooling service whether to use, include but not limited to inlet gas flow, heat exchanger size, stream temperature or the like more than the decision of a heat exchanger.) cool stream 31a is at 23 ℉ [5 ℃] and 1278psia[8,812kPa (a)] and under enter separator 11, wherein steam (stream 32) separates with condensed fluid (flowing 33).
Steam (stream 32) from separator 11 is divided into two streams 34 and 36, makes stream 34 comprise total steam of about 42%.Some situation may be had a preference for some part combination of stream 34 and condensed fluid (stream 39) forming stream 35, but in this simulation, does not flow in stream 39.Mix flow 35 causes flowing cooling and the condensation substantially of 35a to pass through heat exchanger 13 with the relation of cooling agent stream 71e heat exchange.The stream 35a of condensation passes through suitable expansion gear then substantially under-90 ℉ [68 ℃], as expansion valve 14, the operating pressure that dodging expands arrives a little higher than distillation column 19 (approximate 450psia[3,103kPa (a)].Between the phase of expansion, the part of stream is vaporized, and causes the cooling of total stream.In the process that shows in Fig. 1, the expansion flow 35b that leaves expansion valve 14 reaches the temperature of-123 ℉ [86 ℃].Because the cooling and the partial condensation of the steam distillation stream 37 that rises from the fractionation level of distillation column 19 are provided, and expansion flow 35b is heated to the temperature of-78 ℉ [61 ℃], and is further vaporized in heat exchanger 21.Add hot-fluid 35c and supply with mid point supplying position place, top in the deethanization section 19b of distillation column 19 then.
Residue 58% (stream 36) from the steam of separator 11 enters work expansion machine 15, wherein extracts mechanical energy from this part of high pressure feeding.Machine 15 steam substantially constant entropy ground from about 1278psia[8,812kPa (a)] pressure expansion to the tower operating pressure, expansion flow 36a is cooled to be similar to the temperature of-57 ℉ [49 ℃] by means of the expansion of doing work.Typical available decompressor can reclaim on the magnitude of the 80-85% of available merit in desirable constant entropy expansion in theory.The merit that reclaims usually is used for driving centrifugal compressor (as clauses and subclauses 16), and this centrifugal compressor for example can be used to compress again overhead gas (stream 49).Expansion and partial condensation stream 36a supply to distillation column 19 as feeding at intermediolateral column feeding point place, bottom.Stream 40, the remainder of separator liquid (stream 33) is flashed to the operating pressure of a little higher than deethanizer by expansion valve 12, before stream 40 provides cooling for the supply gas of coming in of previous description, it is cooled to the temperature of-14 ℉ [26 ℃] (stream 40a).Stream 40b under the temperature of 75 ℉ [24 ℃], enters deethanizer at intermediolateral column feed point place, second bottom now then.
Deethanizer in distillation column 19 is the conventional distillation column that comprises certain combination of a plurality of vertical isolation dishes, one or more packed bed or dish and filling.Situation in the natural gas processing factory that is everlasting as usual is such, and fractionating column can comprise two sections.Upper segment 19a is a separator, wherein the top feeding is divided into its corresponding steam and liquid part, and wherein the steam from bottom distillation or deethanization section 19b rising combines with the vapor portion (if there is) of top feeding, leaves the deethanizer overhead steam (stream 37) of top of tower with formation.Bottom, deethanization section 19b comprise dish and/or fill, and are provided at whereabouts liquid and contact with necessity between the rising steam.The deethanization section also comprises one or more reboilers (as reboiler 20), and the part of the liquid that heating of this reboiler and vaporization flow downward along post is to provide the stripped vapor that upwards flows along post.Liquid product flow 41 based in bottoms on mole foundation the ethane of 0.020:1 under 213 ℉ [101 ℃], leave the bottom of tower for the typical technology parameter of propane ratio.
Top distillation stream 37 leaves deethanizer with-73 ℉ [59 ℃], and as previous as described in reflux condenser 21, be cooled and partial condensation.Partial condensation stream 37a enters reflux drum 22 with-94 ℉ [70 ℃], and wherein condensed fluid (stream 44) separates with uncondensed vapor (stream 43).Condensed fluid (stream 44) is drawn onto top feeding point on deethanizer by pump 23 pumps, as reflow stream 44a.
When the part of the bottom of deethanization section formation fractionating column, reflux condenser 21 can be arranged in tower inside above distillation column 19, as shown in Figure 2.This eliminates the needs for reflux drum 22 and reflux pump 23, because distillation stream is cooled above the fractionation level of post in tower then and separates.Selectively, replace the use of the fractionator (as the fractionator in Fig. 3 21) of the reflux condenser 21 in Fig. 1 to eliminate reflux drum and reflux pump, and concurrent fractionation level also is provided, to replace those levels in the upper segment of deethanization post.If fractionator is positioned in the factory at classification height (grade level) and locates, then it is connected on the vapor/liquid separator, and is collected in the top that liquid in the separator is pumped in to distillation column.Also be to use the decision of fractionator to depend on factory's size and heat-exchanger surface requirement usually about reflux condenser being included in post inside.
In heat exchanger 24, be heated to 93 ℉ [34 ℃] from the uncondensed vapor of reflux drum 22 (stream 43), and a part (stream 48) withdraws from then with as the fuel gas that is used for factory.(amount of the fuel gas that must withdraw from is mainly by the gas compressor that drives in factory, as in this example refrigerant compressor 64,66, and 68, engine and/or the needed fuel of turbine determine.) remainder (stream 49) of heating steam is by compressor 16 compressions, this compressor 16 by expansion machine 15,61, and 63 drive.Be cooled to 100 ℉ [38 ℃] afterwards in drain cooler 25, stream 49b is further cooled to-83 ℉ [64 ℃] by the cross exchange with cold steam-stream 43 in heat exchanger 24.
Stream 49c enters heat exchanger 60 then, and further by cooling agent stream 71d be cooled to-255 ℉ [160 ℃] with condensation and sub-cooled it, this moment, it entered acting expansion machine 61, wherein extracted mechanical energy from stream.Machine 61 liquid stream 49d substantially constant entropy ground from about 593psia[4,085kPa (a)] pressure expansion to LNG store pressure (15.5psia[107kPa (a)], a little higher than atmospheric pressure.Acting is expanded and expansion flow 49e is expand into the temperature of approximate-256 ℉ [160 ℃], and this moment, it was drawn towards the LNG storage tank 62 (stream 50) that keeps the LNG product then.
All coolings for stream 35 and 49c are provided by the closed circulation cooling loop.The working fluid that is used for this circulation is the mixture of hydrocarbon and nitrogen, and the composition of mixture is regulated on demand so that the coolant temperature of requirement to be provided, and uses the cooling medium condensation under convenient pressure that is suitable for simultaneously.In this case, supposed and used cooling water condensation, thereby comprised nitrogen, methane, ethane, propane, and be used similarly than coolant mixture and Fig. 1 process of heavy hydrocarbons.The composition of stream by approximate molar percentage, is 8.7% nitrogen, 31.7% methane, 47.0% ethane, reaches 8.6% propane, and all the other are by forming than heavy hydrocarbons.
Cooling agent stream 71 is with 100 ℉ [38 ℃] and 607psia[4,185kPa (a)] pressure leave drain cooler 69.It enters heat exchanger 10, and is cooled to-34 ℉ [37 ℃] and partly condensation by part heats coolant stream 71f with by other cooling agent stream.For Fig. 1 situation, suppose that these other cooling agent streams are the commercial mass propane-cooled agent under three different temperatures and pressure stage.Partial condensation cooling agent stream 71a enters heat exchanger 13 then, partly adds thermal expansion cooling agent stream 71e with cause and further is cooled to-90 ℉ [68 ℃], further condensation cooling agent (stream 71b).Cooling agent flows the 71d condensation by the expansion cooling agent in heat exchanger 60, and sub-cooled arrives-255 ℉ [160 ℃] then.Sub-cooled liquid stream 71c enters acting expansion machine 63, wherein extracts mechanical energy from stream and since its substantially constant entropy ground from about 586psia[4,040kPa (a)] pressure expansion arrive about 34psia[234kPa (a)].Between the phase of expansion, the part of stream is vaporized, and causes total stream to be cooled to-264 ℉ [164 ℃] (stream 71d).Expansion flow 71d reenters heat exchanger 60,13, and 10 then, and wherein it is being vaporized when overheated, provides for stream 49c, stream 35, and the cooling of cooling agent ( stream 71,71a, and 71b).
Overheated coolant vapours (stream 71g) leaves heat exchanger 10 with 90 ℉ [32 ℃], and divides three grades to be compressed to 617psia[4,254kPa (a)].Each of three compression stages (compressor for cooling fluid 64,66, and 68) is by additional drive power source, and follows cooler ( drain cooler 65,67, reach 69) to remove the heat of compression.Compressive flow 71 from drain cooler 69 turns back to heat exchanger 10, to finish circulation.
Be used for narrating the stream flow and being summarised in the following form of energy consumption of the process that Fig. 1 shows:
Table I
(Fig. 1)
Flow summary-the pound of stream. mole/Hr[kg mole/Hr]
Stream Methane Ethane Propane Butane+ Amount to
31 40,977 3,861 2,408 1,404 48,656
32 40,93 3,667 2,171 1,087 47,123
33 784 194 237 317 1,533
34 16,680 1,522 901 451 19,556
36 23,513 2,145 1,270 636 27,567
37 44,813 7,065 120 0 52,035
40 784 194 237 317 1,533
41 0 48 2,385 1,404 3,837
43 40,977 3,813 23 0 44,819
44 3,866 3,252 97 0 7,216
48 2,527 235 1 0 2,765
50 38,450 3,578 22 0 42,054
The rate of recovery in LPG *
Propane 99.05%
Butane+100.00%
Productivity ratio197,031Lb/Hr [197,031kg/Hr]
The LNG product
Productivity ratio 725,522Lb/Hr [725,522kg/Hr]
Purity 91.43%
Low heat value 970.4 BTU/SCF [36.16MJ/m 3]
Power
Cooling agent compression 90,714HP [149,132kW]
Propane compression 36,493HP [59,994kW]
Total compression 127,207HP [209,126kW]
The facility heat
Deethanizer reboiler 58,003MBTU/Hr [37,470kW]
*(based on non-rounding flow)
" the specific power consumption " of the efficient instructions for use of LNG production process typically compares, and " specific power consumption " is the ratio of total refrigeration compression horsepower and total liquid production rate.The public information indication 0.168HP-Hr/Lb[0.276kW-Hr/kg that consumes about the specific power of the prior art process that is used for producing LNG] to 0.182HP-Hr/Lb[0.300kW-Hr/kg] scope, this believe be for LNG production plant based on annual 340 days the utilization of capacity (on-streamfactor).On this same basic, be 0.148HP-Hr/Lb[0.243kW-Hr/kg for the specific power consumption of Fig. 1 embodiment of the present invention], this provides the efficiency improvement of the 14-23% that is better than the prior art process.
Two principal elements that explanation improvement efficient of the present invention is arranged.By checking the thermodynamics of liquefaction process when being applied to high-pressure gas flow (as the gas stream of considering in this example), can understand first factor.Because the main composition of this stream is a methane, so the macroscopic property of methane can be used for respect to the purpose of the recycle ratio of using in the present invention than the liquefaction cycle that adopts in the prior art process.Fig. 4 comprises the pressure-enthalpy phasor that is used for methane.In the major part of prior art liquefaction cycle, stream under high pressure (in the path A-B), finish all coolings of gas stream, this moment stream (path B-C) the pressure (a little higher than atmospheric pressure) that expands then to the LNG storage container.This expansion step can adopt acting expansion machine, and this acting expansion machine typically can reclaim on the magnitude of the 75-80% of available merit in desirable constant entropy expansion in theory.For simplicity, for path B-C, constant entropy expansion is presented among Fig. 4 fully.Even like this, by this acting expand the enthalpy that provides reduce also very little because almost be vertical in the liquid regions of the line of constant enthalpy in phasor.
Now this and liquefaction cycle of the present invention are compared.After high pressure (path A-A ') lower part cooling, the acting of gas stream expand (path A '-A ") is to intermediate pressure.(same, for simplicity, show complete constant entropy expansion.) remainder of cooling finishes (path A " B '), and stream expands then, and (path B '-C) is to the pressure of LNG storage container under intermediate pressure.Because more slow in the Steam area of insentrope slope in phasor, thus by the first acting expansion step of the present invention (path A '-A ") provides significantly that bigger enthalpy reduces.Thereby, for total amount of cooling water of the presently claimed invention (path A-A ' and A " B ' sum) less than (path A-B) desired cooling reduces liquid gas and flows desired refrigeration (with therefore reducing the refrigeration compression) for the prior art process.
Second factor that improvement efficient of the present invention is described is in the superior function than hydro carbons Distallation systm under the low operating pressure.Hydrocarbon removal step is under high pressure carried out in the most prior art process, typically uses column scrubber, and this column scrubber flows cold hydrocarbon liquids as absorbing, to remove than heavy hydrocarbons from the gas stream of coming in.Under high pressure the operated wash post is not very efficient, because it causes the common absorption from the major part of the methane of gas stream and ethane, and must be after these methane and the ethane from absorbing the liquid stripping and being cooled to become the part of LNG product.In the present invention, carry out hydro carbons and remove step under intermediate pressure, wherein steam-fluid balance is more had a preference for, and causes wishing in byproduct liquid stream the very high efficiente callback than heavy hydrocarbons.
Other embodiment
Person of skill in the art will appreciate that the present invention can be suitable for using to allow the co-production of NGL stream, LPG stream or condensate flow, because be adapted at the needs of given factory location best for all types of LNG liquefaction plant.And, will recognize that the configuration of various processes can be used for the withdrawal liquid by-product stream.The present invention can be suitable for reclaiming and be included in the most of C that exists in the feeding gas 2The NGL stream of composition perhaps reclaims and only is included in the C that exists in the feeding gas 4The condensate flow of heavier composition, rather than as described in previous, produce the LPG byproduct.
Fig. 1 representative is used to indicate the preferred embodiments of the present invention of treatment conditions.Fig. 5 to 10 describes for the admissible embodiment of selection of the present invention of concrete purposes.According to amount and the feeding gas pressure in feeding gas than heavy hydrocarbons, the cooling feed flow 31a that leaves heat exchanger 10 may not comprise any liquid (because it is at it more than dew point, perhaps because it is higher than its critical condensation pressure), thereby the separator 11 of expression is unwanted in Fig. 1 and 6 to 10, and the cooling feed flow can flow directly to suitable expansion gear, as acting expansion machine 15.Inlet gas can adopt embodiments of the invention as shown in Figure 5 than under the rich situation described so far therein.Flow through heat exchanger 18 and by sub-cooled of condensate liquid stream 33 is divided into two parts then.First's (stream 40) expansion valve 12 of flowing through, it stands to be used for the expansion of flash distillation at this place, because pressure is reduced to the pressure of about distillation column 19.From the cold flow 40a of expansion valve 12 heat exchanger 18 of flowing through then, it is partly heated at this place, because as it is used for sub-cooled stream 33 as described in previous.Part adds hot-fluid 40b and is further heated in heat exchanger 10 then, and flows to the bottom mid point supplying position on distillation column 19.Second liquid part (stream 39), still under high pressure, (1) combines with part 34 from the vapor stream of separator 11, after this or supply at the distillation column 19 at mid point supplying position place, top or with expansion flow 35b and combine perhaps (2) and substantially condensate flow 35a combination, perhaps expand in expansion valve 17 and (3).Selectively, stream 39 part can be followed arbitrary of the flow path so far describing and describe or all in Fig. 5.
Be used for that the disposal of remaining air-flow can realize in many ways before condensation and the subcooled heat exchanger 60 supplying at it after the recovery of liquid by-product stream (at the stream 43 of Fig. 1 and 6 in 10).In the process of Fig. 1, stream is heated, and uses the energy of deriving from one or more acting expansion machines to be compressed to elevated pressures, and partly cooling in drain cooler is then by further cooling off with the cross exchange of primary flow.As shown in Figure 6, some purposes may be had a preference for auxiliary compressor that use drives by external power supply for example 59 stream is compressed to elevated pressures.As by in the dotted line equipment among Fig. 1 (heat exchanger 24 and drain cooler 25) expression like that, some situation may be had a preference for by reducing or eliminating the fund cost that compressive flow pre-cooled before it enters heat exchanger 60 reduce facility (is cost to be increased in cooling load and increase compressor for cooling fluid 64,66 on the heat exchanger 60, to reach 68 power consumption).Under these circumstances, the stream 49a that leaves compressor can flow directly to heat exchanger 24 as shown in Figure 7, perhaps flows directly to heat exchanger 60 as shown in Figure 8.If acting expansion machine is not used in the expansion of any part of high pressure feeding gas, then can use by the external power supply compressor driven, compressor 59 as shown in FIG. 9 replaces compressor 16.Other situation may not prove that any compression of stream is suitable, thereby stream flows directly to heat exchanger 60 as shown in Figure 10, and flows through dotted line equipment (heat exchanger 24, compressor 16, and drain cooler 25) in Fig. 1.If before factory's fuel gas (stream 48) withdraws from, do not comprise the heat exchanger 24 that adds hot-fluid, then may need auxiliary heater 58, flow with facility stream that use to supply with essential heat or another process and before fuel gas is consumed, to heat it, as shown in Fig. 8 to 10.Generally must estimate selection such as these for every kind of purposes, as such as gas composition, factory's size, wish that by-product stream reclaims the factor the level, and must all consider suitable device.
According to the present invention, the cooling of inlet gas stream and the feed flow produced section to LNG can be finished in many ways.In the process of Fig. 1 and 5 to 10, inlet gas stream 31 is by outside coolant flow and cooling of dilatation separator liquid and condensation.Yet cold process stream also can be used to some that cool off supplied to pressure coolant (stream 71a).And, can utilize any stream under the temperature colder than the stream that is cooled.Such as, extract and can withdraw from from the side of the steam of distillation column 19, and be used for cooling.For every kind of concrete purposes, must estimate to be used for the selection of using and distributing and be used for the concrete layout of inlet gas and the gas-cooled heat exchanger of feeding and be used for the process stream of particular thermal Exchange Service of the tower liquid and/or the steam of process heat exchanger.The selection of cooling source will be depended on a plurality of factors, include but not limited to feeding gas composition and condition, factory's size, heat exchanger size, may the cooling source temperature, or the like.Those skilled in the art also will recognize, can adopt any combination of above cooling source or method in combination, with the feed flow temperature that realizes wishing.
And, supply to inlet gas stream and the auxiliary external refrigeration of the feed flow produced section to LNG also can realize with multitude of different ways.In Fig. 1 and 6 to 10, supposed the single composition cooling agent of boiling for high-level external refrigeration, and supposed vaporization multicomponent cooling agent for low-level external refrigeration, make single composition cooling agent be used for pre-cooled multicomponent cooling agent stream.Selectively, high level cooling and low-level cooling can be used and have more lower boiling successively single composition cooling agent (that is, " cascade refrigeration ") or realizing hanging down a kind of single composition cooling agent under the evaporating pressure successively.Select example as another, high level cooling and low-level cooling can use multicomponent cooling agent stream to realize, the corresponding part of this multicomponent cooling agent stream is adjusted to provide essential chilling temperature.The selection that is used to provide the method for external refrigeration will be depended on a plurality of factors, include but not limited to feeding gas composition and condition, factory's size, compressor drive size, heat exchanger size, environment radiator temperature, or the like.Those skilled in the art will recognize that also any combination that is used to provide the method for external refrigeration described above can be adopted in combination, with the feed flow temperature that realizes wishing.
Leave the sub-cooled of the condensate liquid stream (the stream 49d in Fig. 1, the stream 49e in Fig. 6, the stream 49c in Fig. 7, the stream 49b in Fig. 8 and 9, and the stream 49a in Figure 10) of heat exchanger 60, reduce or eliminate the amount of issuable flash-off steam during stream expand into the operating pressure of LNG storage tank 62.This generally reduces the specific power consumption that is used for producing LNG by the needs of eliminating for the fast gas compression.Yet some situation may be had a preference for by the size that reduces heat exchanger 60 and use fast gas compression or other means to dispose issuable any flash gas, and reduces the fund cost of facility.
Describe in concrete expansion gear although individual flows expands, can adopt selectable expansion means in suitable occasion.For example, condition can guarantee that the acting of condensation feed flow (the stream 35a in Fig. 1 and 5 to 10) is expanded substantially.And, for the sub-cooled liquid stream that leaves heat exchanger 60 (the stream 49d in Fig. 1, the stream 49e in Fig. 6, in Fig. 7 stream 49c, in Fig. 8 and 9 stream 49b, and stream 49a in Figure 10), constant enthalpy dodges to expand and can be used for replacing acting to expand, but it is necessary will making the further sub-cooled in heat exchanger 60, to avoid in expansion, forming flash-off steam, perhaps also add other means that flash-off steam compresses or be used for disposing the flash-off steam of generation.Similarly, for the sub-cooled pressure coolant stream (the stream 71c in Fig. 1 and 6 to 10) that leaves heat exchanger 60, can use the constant enthalpy sudden strain of a muscle to expand replacing acting expansion, result is the increase that is used for the power consumption of the compression of cooling agent.
Believe it is the embodiment of the preferred embodiments of the present invention although described here, but person of skill in the art will appreciate that, can carry out other and further revise it, for example make the present invention adapt to various conditions, feeding type or other requirement, and do not break away from by the defined spirit of the present invention of following claims.

Claims (78)

1. one kind is used for liquefying and comprises methane and than the method for the natural gas flow of heavy hydrocarbons composition, wherein:
(a) described natural gas flow is cooled off under pressure, with its at least a portion of condensation and formation condensate flow; With
(b) described condensate flow is expand into lower pressure, to form described liquefied natural gas stream;
Improvement is, wherein
(1) described natural gas flow is handled in one or more cooling steps;
(2) natural gas flow with described cooling is divided at least one first air-flow and one second air-flow;
(3) with the cooling of described first air-flow, with it whole of cardinal principle condensation and after this expand into intermediate pressure;
(4) with first air-flow of the cardinal principle condensation of described expansion to become heat exchange relationship guiding and heating thus with more volatile steam distillation stream, this more volatile steam distillation stream rises from the fractionation level of distillation column;
(5) described intermediate pressure is arrived in described second flow expansion;
(6) add thermal expansion first air-flow and described expansion second air-flow is directed in the described distillation column with described, what wherein described stream is separated into described more volatile steam distillation stream and comprises described major part than the heavy hydrocarbons composition is difficult for volatile fraction;
(7) described more volatile steam distillation stream by described expansions substantially condensation first air-flow cool off fully with partial condensation it, and after this separate with formation comprise described methane and light composition major part volatile residual gas partly and reflow stream;
(8) described reflow stream is directed in the described distillation column, as top feeding to described distillation column; And
(9) described volatile residual gas part is cooled off under pressure, also formed described condensate flow thus with its at least a portion of condensation.
2. one kind is used for liquefying and comprises methane and than the method for the natural gas flow of heavy hydrocarbons composition, wherein
(a) described natural gas flow is cooled off under pressure, with its at least a portion of condensation and formation condensate flow; With
(b) described condensate flow is expand into lower pressure, to form described liquefied natural gas stream;
Improvement is, wherein:
(1) described natural gas flow is handled in one or more cooling steps, with condensation partly it;
(2) described partial condensation natural gas flow is separated, so that vapor stream and liquid stream to be provided thus;
(3) described vapor stream is divided at least one first air-flow and one second air-flow;
(4) with the cooling of described first air-flow, with it whole of cardinal principle condensation and after this expand into intermediate pressure;
(5) with first air-flow of the cardinal principle condensation of described expansion to become heat exchange relationship ground guiding and heating thus with more volatile steam distillation stream, this more volatile steam distillation stream rises from the fractionation level of distillation column;
(6) described intermediate pressure is arrived in described second flow expansion;
(7) described liquid stream is expand into described intermediate pressure;
(8) with described second air-flow that adds first air-flow of thermal expansion, described expansion, and the liquid stream of described expansion be directed in the described distillation column, what wherein said stream was separated into described more volatile steam distillation stream and comprised described major part than the heavy hydrocarbons composition is difficult for volatile fraction;
(9) with described more volatile steam distillation stream by described expansions substantially condensation first air-flow cool off fully with partial condensation it, and after this separate with formation comprise described methane and light composition major part volatile residual gas partly and reflow stream;
(10) described reflow stream is directed in the described distillation column, as top feeding to described distillation column; And
(11) described volatile residual gas part is cooled off under pressure, also formed described condensate flow thus with its at least a portion of condensation.
3. one kind is used for liquefying and comprises methane and than the method for the natural gas flow of heavy hydrocarbons composition, wherein
(a) described natural gas flow is cooled off under pressure, with its at least a portion of condensation and formation condensate flow; With
(b) described condensate flow is expand into lower pressure, to form described liquefied natural gas stream;
Improvement is, wherein
(1) described natural gas flow is handled in one or more cooling steps, with condensation partly it;
(2) described partial condensation natural gas flow is separated, vapor stream and liquid stream is provided thus;
(3) described vapor stream is divided at least one first air-flow and one second air-flow;
(4) at least a portion of described first air-flow and described liquid stream is combined, form mix flow thus;
(5) with the cooling of described mix flow with it whole of cardinal principle condensation, and after this expand into intermediate pressure;
(6) with the mix flow of the cardinal principle condensation of described expansion to become heat exchange relationship ground guiding and heating thus with more volatile steam distillation stream, this more volatile steam distillation stream rises from the fractionation level of distillation column;
(7) described intermediate pressure is arrived in described second flow expansion;
(8) any remainder with described liquid stream expand into described intermediate pressure;
(9) with described second air-flow that adds the mix flow of thermal expansion, described expansion, and the described expansion remainder of described liquid stream be directed in the described distillation column, what wherein said stream was separated into described more volatile steam distillation stream and comprised described major part than the heavy hydrocarbons composition is difficult for volatile fraction;
(10) with described more volatile steam distillation stream by the described mix flow that expands condensation substantially cool off fully with partial condensation it, and after this separate volatile residual gas part and the reflow stream that comprises the major part of described methane and light composition with formation;
(11) described reflow stream is directed in the described distillation column, as top feeding to described distillation column; And
(12) described volatile residual gas part is cooled off under pressure, also formed described condensate flow thus with its at least a portion of condensation.
4. one kind is used for liquefying and comprises methane and than the method for the natural gas flow of heavy hydrocarbons composition, wherein
(a) described natural gas flow is cooled off under pressure, with its at least a portion of condensation and formation condensate flow; With
(b) described condensate flow is expand into lower pressure, to form described liquefied natural gas stream;
Improvement is, wherein
(1) described natural gas flow is handled in one or more cooling steps, with condensation partly it;
(2) described partial condensation natural gas flow is separated, so that vapor stream and liquid stream to be provided thus;
(3) described vapor stream is divided at least one first air-flow and one second air-flow;
(4) with the cooling of described first air-flow with it whole of cardinal principle condensation, and after this expand into intermediate pressure;
(5) with first air-flow of the cardinal principle condensation of described expansion becoming heat exchange relationship ground guiding with more volatile steam distillation stream and to be heated thus, this more volatile steam distillation stream rises from the fractionation level of distillation column;
(6) described intermediate pressure is arrived in described second flow expansion;
(7), and after this be divided at least one first and a second portion with the cooling of described liquid stream;
(8) described first is expand into described intermediate pressure, and after this be heated;
(9) described second portion is expand into described intermediate pressure;
(10) with described second air-flow that adds first air-flow of thermal expansion, described expansion, the described first that adds thermal expansion, and the second portion of described expansion be directed in the described distillation column, what wherein said stream was separated into described more volatile steam distillation stream and comprised described major part than the heavy hydrocarbons composition is difficult for volatile fraction;
(11) with described more volatile steam distillation stream by described expansions substantially condensation first air-flow cool off fully with partial condensation it, and after this separate with formation comprise described methane and light composition major part volatile residual gas partly and reflow stream;
(12) described reflow stream is directed in the described distillation column, as top feeding to described distillation column; And
(13) described volatile residual gas part is cooled off under pressure, also formed described condensate flow thus with its at least a portion of condensation.
5. one kind is used for liquefying and comprises methane and than the method for the natural gas flow of heavy hydrocarbons composition, wherein
(a) described natural gas flow is cooled off under pressure, with its at least a portion of condensation and formation condensate flow; With
(b) described condensate flow is expand into lower pressure, to form described liquefied natural gas stream;
Improvement is, wherein
(1) described natural gas flow is handled in one or more cooling steps, with condensation partly it;
(2) described partial condensation natural gas flow is separated, so that vapor stream and liquid stream to be provided thus;
(3) described vapor stream is divided at least one first air-flow and one second air-flow;
(4) with the cooling of described first air-flow with it whole of cardinal principle condensation, and after this expand into intermediate pressure;
(5), and after this be divided at least one first and a second portion with the cooling of described liquid stream;
(6) described first is expand into described intermediate pressure, and after this be heated;
(7) with described second portion and the combination of described cardinal principle condensation first air-flow, form mix flow thus, by this described mix flow is expand into described intermediate pressure;
(8) mix flow with described expansion also heats thus to become heat exchange relationship ground guiding with more volatile steam distillation stream, and this more volatile steam distillation stream rises from the fractionation level of distillation column;
(9) described intermediate pressure is arrived in described second flow expansion;
(10) with described second air-flow that adds the mix flow of thermal expansion, described expansion, and the described first that adds thermal expansion be directed in the described distillation column, what wherein said stream was separated into described more volatile steam distillation stream and comprised described major part than the heavy hydrocarbons composition is difficult for volatile fraction;
(11) with described more volatile steam distillation stream by the mix flow of described expansion cool off fully with partial condensation it, and after this separate volatile residual gas part and the reflow stream that comprises the major part of described methane and light composition with formation;
(12) described reflow stream is directed in the described distillation column, as top feeding to described distillation column; And
(13) described volatile residual gas part is cooled off under pressure, also formed described condensate flow thus with its at least a portion of condensation.
6. according to claim 1 improving one's methods, wherein, described distillation column is the lower section of fractionating column, and wherein, with described more volatile steam distillation stream cool off fully with in the part of the described tower above described distillation column partly condensation it, and separate simultaneously to form described volatile residual gas part and described reflow stream, described by this reflow stream flows to the top fractionation level of described distillation column.
7. according to claim 2 improving one's methods, wherein, described distillation column is the lower section of fractionating column, and wherein, described more volatile steam distillation stream cooled off fully with in the part of the described tower above described distillation column partly condensation it, and simultaneously separated to form described volatile residual gas part and described reflow stream, described by this reflow stream flows to the top fractionation level of described distillation column.
8. according to claim 3 improving one's methods, wherein, described distillation column is the lower section of fractionating column, and wherein, described more volatile steam distillation stream cooled off fully with in the part of the described tower above described distillation column partly condensation it, and simultaneously separated to form described volatile residual gas part and described reflow stream, described by this reflow stream flows to the top fractionation level of described distillation column.
9. according to claim 4 improving one's methods, wherein, described distillation column is the lower section of fractionating column, and wherein, described more volatile steam distillation stream cooled off fully with in the part of the described tower above described distillation column partly condensation it, and simultaneously separated to form described volatile residual gas part and described reflow stream, described by this reflow stream flows to the top fractionation level of described distillation column.
10. according to claim 5 improving one's methods, wherein, described distillation column is the lower section of fractionating column, and wherein, described more volatile steam distillation stream cooled off fully with in the part of the described tower above described distillation column partly condensation it, and simultaneously separated to form described volatile residual gas part and described reflow stream, described by this reflow stream flows to the top fractionation level of described distillation column.
11. according to claim 1 improving one's methods, wherein, described more volatile steam distillation stream cooled off fully with in fractionator partly condensation it, and simultaneously separated to form described volatile residual gas part and described reflow stream, described by this reflow stream flows to the top fractionation level of described distillation column from fractionator.
12. according to claim 2 improving one's methods, wherein, described more volatile steam distillation stream cooled off fully with in fractionator partly condensation it, and simultaneously separated to form described volatile residual gas part and described reflow stream, described by this reflow stream flows to the top fractionation level of described distillation column from fractionator.
13. according to claim 3 improving one's methods, wherein, described more volatile steam distillation stream cooled off fully with in fractionator partly condensation it, and simultaneously separated to form described volatile residual gas part and described reflow stream, described by this reflow stream flows to the top fractionation level of described distillation column from fractionator.
14. according to claim 4 improving one's methods, wherein, described more volatile steam distillation stream cooled off fully with in fractionator partly condensation it, and simultaneously separated to form described volatile residual gas part and described reflow stream, described by this reflow stream flows to the top fractionation level of described distillation column from fractionator.
15. according to claim 5 improving one's methods, wherein, described more volatile steam distillation stream cooled off fully with in fractionator partly condensation it, and simultaneously separated to form described volatile residual gas part and described reflow stream, described by this reflow stream flows to the top fractionation level of described distillation column from fractionator.
16. according to claim 1,2,3,4,5,6,7,8,9,10,11,12,13,14 or 15 described improving one's methods, wherein, described volatile residual gas is partly compressed and after this cools off under pressure, also form described condensate flow thus with its at least a portion of condensation.
17. according to claim 1,2,3,4,5,6,7,8,9,10,11,12,13,14 or 15 described improving one's methods, wherein, described volatile residual gas is partly heated, compresses and after this cools off under pressure, also form described condensate flow thus with its at least a portion of condensation.
18. according to claim 1,2,3,4,5,6,7,8,9,10,11,12,13,14 or 15 described improving one's methods, wherein, described volatile residual gas partly comprises described methane, light composition, reaches C 2The major part of composition.
19. according to claim 16 improving one's methods, wherein, described volatile residual gas partly comprises described methane, light composition, reaches C 2The major part of composition.
20. according to claim 17 improving one's methods, wherein, described volatile residual gas partly comprises described methane, light composition, reaches C 2The major part of composition.
21. according to claim 1,2,3,4,5,6,7,8,9,10,11,12,13,14 or 15 described improving one's methods, wherein, described volatile residual gas partly comprises described methane, light composition, C 2Composition, and C 3The major part of composition.
22. according to claim 16 improving one's methods, wherein, described volatile residual gas partly comprises described methane, light composition, C 2Composition, and C 3The major part of composition.
23. according to claim 17 improving one's methods, wherein, described volatile residual gas partly comprises described methane, light composition, C 2Composition, and C 3The major part of composition.
24. one kind is used for liquefying and comprises methane and than the equipment of the natural gas flow of heavy hydrocarbons composition, it comprises
(1) one or more first heat-exchange devices receive described natural gas flow and cool off it under pressure;
(2) classification apparatus is connected on described first heat-exchange device, to receive described cooled natural gas stream and it is divided at least one first air-flow and one second air-flow;
(3) second heat-exchange devices are connected on the described classification apparatus, receiving described first air-flow, and with it cool off fully with the cardinal principle condensation it;
(4) first expansion gears are connected on described second heat-exchange device, to receive described cardinal principle condensation first air-flow and it is expand into intermediate pressure;
(5) the 3rd heat-exchange devices, be connected on described first expansion gear, to receive described expansion cardinal principle condensation first air-flow and to heat it, described the 3rd heat-exchange device is also connected on the distillation column, with receive the more volatile steam distillation stream that rises from the fractionation level of described distillation column and it cool off fully with partial condensation it;
(6) second expansion gears are connected on the described classification apparatus, to receive described second air-flow and it is expand into described intermediate pressure;
(7) described distillation column is also connected on described the 3rd heat-exchange device and described second expansion gear, to receive described thermal expansion first air-flow and described expansion second air-flow of adding, make described distillation column be suitable for that described stream is separated into described more volatile steam distillation stream and comprise described major part than the heavy hydrocarbons composition be difficult for volatile fraction;
(8) separator, be connected on described the 3rd heat-exchange device, to receive described cooling segment condensation distillation stream, and it is separated into the volatile residual gas part and the reflow stream of the major part that comprises described methane and light composition, described separator is also connected on the described distillation column, so that described reflow stream is directed in the described distillation column, as top feeding to described distillation column;
(9) the 4th heat-exchange devices, be connected on the described separator, to receive described volatile residual gas part, make described the 4th heat-exchange device be suitable for the described volatile residual gas part of cooling under pressure, also form condensate flow thus with its at least a portion of condensation;
(10) the 3rd expansion gears are connected on described the 4th heat-exchange device, to receive described condensate flow and it is expand into lower pressure, to form described liquefied natural gas stream; And
(11) control device is suitable for being adjusted to the amount and the temperature of the described feed flow of described distillation column, so that the head temperature of described distillation column is kept at a certain temperature, is difficult for reclaiming in the volatile fraction described major part than the heavy hydrocarbons composition described whereby.
25. one kind is used for liquefying and comprises methane and than the equipment of the natural gas flow of heavy hydrocarbons composition, it comprises
(1) one or more first heat-exchange devices, receive described natural gas flow and under pressure it cool off fully with partial condensation it;
(2) first separators are connected on described first heat-exchange device, to receive described partial condensation natural gas flow and it is separated into vapor stream and liquid stream;
(3) classification apparatus is connected on described first separator, to receive described vapor stream and it is divided at least one first air-flow and one second air-flow;
(4) second heat-exchange devices are connected on the described classification apparatus, receiving described first air-flow, and it cool off fully with the cardinal principle condensation it;
(5) first expansion gears are connected on described second heat-exchange device, to receive described cardinal principle condensation first air-flow and it is expand into intermediate pressure;
(6) the 3rd heat-exchange devices, be connected on described first expansion gear, to receive described expansion cardinal principle condensation first air-flow and to heat it, described the 3rd heat-exchange device is also connected on the distillation column, with receive the more volatile steam distillation stream that rises from the fractionation level of described distillation column and it cool off fully with partial condensation it;
(7) second expansion gears are connected on the described classification apparatus, to receive described second air-flow and it is expand into described intermediate pressure;
(8) the 3rd expansion gears are connected on described first separator, to receive described liquid stream and it is expand into described intermediate pressure;
(9) described distillation column is also connected to described the 3rd heat-exchange device, described second expansion gear, reaches on described the 3rd expansion gear, to receive described thermal expansion first air-flow, described expansion second air-flow, and the described expanding liquid stream of adding, make described distillation column be suitable for described stream be separated into described more volatile steam distillation flow and comprise described major part than the heavy hydrocarbons composition be difficult for volatile fraction;
(10) second separators, be connected on described the 3rd heat-exchange device, to receive described cooling segment condensation distillation stream, and it is separated into the volatile residual gas part and the reflow stream of the major part that comprises described methane and light composition, described second separator is also connected on the described distillation column, so that described reflow stream is directed in the described distillation column, as top feeding to described distillation column;
(11) the 4th heat-exchange devices, be connected on described second separator, to receive described volatile residual gas part, make described the 4th heat-exchange device be suitable for the described volatile residual gas part of cooling under pressure, also form condensate flow thus with its at least a portion of condensation;
(12) the 4th expansion gears are connected on described the 4th heat-exchange device, to receive described condensate flow and it is expand into lower pressure, to form described liquefied natural gas stream; And
(13) control device is suitable for being adjusted to the amount and the temperature of the described feed flow of described distillation column, so that the head temperature of described distillation column is kept at a certain temperature, is difficult for reclaiming in the volatile fraction described major part than the heavy hydrocarbons composition described whereby.
26. one kind is used for liquefying and comprises methane and than the equipment of the natural gas flow of heavy hydrocarbons composition, it comprises
(1) one or more first heat-exchange devices, receive described natural gas flow and under pressure it cool off fully with partial condensation it;
(2) first separators are connected on described first heat-exchange device, to receive described partial condensation natural gas flow and it is separated into vapor stream and liquid stream;
(3) classification apparatus is connected on described first separator, to receive described vapor stream and it is divided at least one first air-flow and one second air-flow;
(4) composite set is connected on the described classification apparatus and is connected on described first separator, with at least a portion of receiving described first air-flow and described liquid stream and form mix flow thus,
(5) second heat-exchange devices are connected on the described composite set, receiving described mix flow, and it cool off fully with the cardinal principle condensation it;
(6) first expansion gears are connected on described second heat-exchange device, expand into intermediate pressure with the mix flow that receives described cardinal principle condensation and it;
(7) the 3rd heat-exchange devices, be connected on described first expansion gear, with the mix flow that receives the described condensation substantially of expanding and heat it, described the 3rd heat-exchange device is also connected on the distillation column, with receive the more volatile steam distillation stream that rises from the fractionation level of described distillation column and it cool off fully with partial condensation it;
(8) second expansion gears are connected on the described classification apparatus, to receive described second air-flow and it is expand into described intermediate pressure;
(9) the 3rd expansion gears are connected on described first separator, expand into described intermediate pressure with any remainder of receiving described liquid stream and it;
(10) described distillation column is also connected to described the 3rd heat-exchange device, described second expansion gear, reaches on described the 3rd expansion gear, to receive the described mix flow of thermal expansion, described expansion second air-flow, and the described expansion remainder of described liquid stream of adding, make described distillation column be suitable for described stream be separated into described more volatile steam distillation flow and comprise described major part than the heavy hydrocarbons composition be difficult for volatile fraction;
(11) second separators, be connected on described the 3rd heat-exchange device, distillation stream with the partial condensation that receives described cooling, and it is separated into the volatile residual gas part and the reflow stream of the major part that comprises described methane and light composition, described second separator is also connected on the described distillation column, so that described reflow stream is directed in the described distillation column, as top feeding to described distillation column;
(12) the 4th heat-exchange devices, be connected on described second separator, to receive described volatile residual gas part, make described the 4th heat-exchange device be suitable for the described volatile residual gas part of cooling under pressure, also form condensate flow thus with its at least a portion of condensation;
(13) the 4th expansion gears are connected on described the 4th heat-exchange device, to receive described condensate flow and it is expand into lower pressure, to form the natural gas flow of described liquefaction; And
(14) control device is suitable for being adjusted to the amount and the temperature of the described feed flow of described distillation column, so that the head temperature of described distillation column is kept at a certain temperature, is difficult for reclaiming in the volatile fraction described major part than the heavy hydrocarbons composition described whereby.
27. one kind is used for liquefying and comprises methane and than the equipment of the natural gas flow of heavy hydrocarbons composition, it comprises
(1) one or more first heat-exchange devices, receive described natural gas flow and under pressure it cool off fully with partial condensation it;
(2) first separators are connected on described first heat-exchange device, are separated into vapor stream and liquid stream with the natural gas flow that receives described partial condensation and it;
(3) second heat-exchange devices are connected on described first separator, to receive described liquid stream and to cool off it;
(4) first classification apparatus are connected on described second heat-exchange device, are divided at least one first and a second portion with the liquid stream that receives described cooling and it;
(5) first expansion gears, be connected on described first classification apparatus, to receive described first and it expand into intermediate pressure, described first expansion gear also connects into described expansion first is supplied to described second heat-exchange device, heats described expansion first thus in the described liquid stream of cooling;
(6) second classification apparatus are connected on described first separator, to receive described vapor stream and it is divided at least one first air-flow and one second air-flow;
(7) the 3rd heat-exchange devices are connected on described second classification apparatus, receiving described first air-flow, and it cool off fully with the cardinal principle condensation it;
(8) second expansion gears are connected on described the 3rd heat-exchange device, expand into described intermediate pressure with first air-flow that receives described cardinal principle condensation and it;
(9) the 3rd expansion gears are connected on described second classification apparatus, to receive described second air-flow and it is expand into described intermediate pressure;
(10) the 4th expansion gears are connected on described first classification apparatus, to receive described second portion and it is expand into described intermediate pressure;
(11) the 4th heat-exchange devices, be connected on described second expansion gear, with first air-flow of the cardinal principle condensation that receives described expansion and heat it, described the 4th heat-exchange device is also connected on the distillation column, with receive the more volatile steam distillation stream that rises from the fractionation level of described distillation column and it cool off fully with condensation partly it;
(12) described distillation column is also connected to described the 4th heat-exchange device, described the 3rd expansion gear, described the 4th expansion gear, reaches on described second heat-exchange device, to receive described thermal expansion first air-flow, described expansion second air-flow, described expansion second portion, and the described thermal expansion first that adds of adding, make described distillation column be suitable for described stream be separated into described more volatile steam distillation flow and comprise described major part than the heavy hydrocarbons composition be difficult for volatile fraction;
(13) second separators, be connected on described the 4th heat-exchange device, distillation stream with the partial condensation that receives described cooling, and it is separated into the volatile residual gas part and the reflow stream of the major part that comprises described methane and light composition, described second separator is also connected on the described distillation column, so that described reflow stream is directed in the described distillation column, as top feeding to described distillation column;
(14) the 5th heat-exchange devices, be connected on described second separator, to receive described volatile residual gas part, make described the 5th heat-exchange device be suitable for the described volatile residual gas part of cooling under pressure, also form condensate flow thus with its at least a portion of condensation;
(15) the 5th expansion gears are connected on described the 5th heat-exchange device, to receive described condensate flow and it is expand into lower pressure, to form described liquefied natural gas stream; And
(16) control device is suitable for being adjusted to the amount and the temperature of the described feed flow of described distillation column, so that the head temperature of described distillation column is kept at a certain temperature, is difficult for reclaiming in the volatile fraction described major part than the heavy hydrocarbons composition described whereby.
28. one kind is used for liquefying and comprises methane and than the equipment of the natural gas flow of heavy hydrocarbons composition, it comprises
(1) one or more first heat-exchange devices, receive described natural gas flow and under pressure it cool off fully with partial condensation it;
(2) first separators are connected on described first heat-exchange device, are separated into vapor stream and liquid stream with the natural gas flow that receives described partial condensation and it;
(3) second heat-exchange devices are connected on described first separator, to receive described liquid stream and to cool off it;
(4) first classification apparatus are connected on described second heat-exchange device, to receive described cooled liquid stream and it is divided at least one first and a second portion;
(5) first expansion gears, be connected on described first classification apparatus, to receive described first and it expand into intermediate pressure, described first expansion gear also connects into described expansion first is supplied to described second heat-exchange device, heats described expansion first thus in the described liquid stream of cooling;
(6) second classification apparatus are connected on described first separator, to receive described vapor stream and it is divided at least one first air-flow and one second air-flow;
(7) the 3rd heat-exchange devices are connected on described second classification apparatus, receiving described first air-flow, and it cool off fully with the cardinal principle condensation it;
(8) composite set is connected on described the 3rd heat-exchange device and is connected on described first classification apparatus, with first air-flow and the described second portion that receives described cardinal principle condensation, and forms mix flow thus;
(9) second expansion gears are connected on the described composite set, to receive described mix flow and it is expand into described intermediate pressure;
(10) the 3rd expansion gears are connected on described second classification apparatus, to receive described second air-flow and it is expand into described intermediate pressure;
(11) the 4th heat-exchange devices, be connected on described second expansion gear, with the mix flow that receives described expansion and heat it, described the 4th heat-exchange device is also connected on the distillation column, with receive the more volatile steam distillation stream that rises from the fractionation level of described distillation column and it cool off fully with condensation partly it;
(12) described distillation column is also connected to described the 4th heat-exchange device, described the 3rd expansion gear, reaches on described second heat-exchange device, to receive described second air-flow that adds the mix flow of thermal expansion, described expansion, and the described first that adds thermal expansion, make described distillation column be suitable for described stream be separated into described more volatile steam distillation flow and comprise described major part than the heavy hydrocarbons composition be difficult for volatile fraction;
(13) second separators, be connected on described the 4th heat-exchange device, distillation stream with the partial condensation that receives described cooling, and it is separated into the volatile residual gas part and the reflow stream of the major part that comprises described methane and light composition, described second separator is also connected on the described distillation column, so that described reflow stream is directed in the described distillation column, as top feeding to described distillation column;
(14) the 5th heat-exchange devices, be connected on described second separator, to receive described volatile residual gas part, make described the 5th heat-exchange device be suitable for the described volatile residual gas part of cooling under pressure, also form condensate flow thus with its at least a portion of condensation;
(15) the 5th expansion gears are connected on described the 5th heat-exchange device, to receive described condensate flow and it is expand into lower pressure, to form described liquefied natural gas stream; And
(16) control device is suitable for being adjusted to the amount and the temperature of the described feed flow of described distillation column, so that the head temperature of described distillation column is kept at a certain temperature, is difficult for reclaiming in the volatile fraction described major part than the heavy hydrocarbons composition described whereby.
29. equipment according to claim 24, wherein
(1) described distillation column is the lower section of fractionating column, and wherein, described more volatile steam distillation stream cooled off fully with in the section of the described fractionating column above described distillation column partly condensation it, and simultaneously separated to form described volatile residual gas part and described reflow stream, described by this reflow stream flows to the top fractionation level of described distillation column; And
(2) described the 4th heat-exchange device is connected on the described fractionating column to receive described volatile residual gas part, make described the 4th heat-exchange device be suitable for the described volatile residual gas part of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
30. equipment according to claim 25, wherein
(1) described distillation column is the lower section of fractionating column, and wherein, described more volatile steam distillation stream cooled off fully with in the section of the described fractionating column above described distillation column partly condensation it, and simultaneously separated to form described volatile residual gas part and described reflow stream, described by this reflow stream flows to the top fractionation level of described distillation column; And
(2) described the 4th heat-exchange device is connected on the described fractionating column to receive described volatile residual gas part, make described the 4th heat-exchange device be suitable for the described volatile residual gas part of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
31. equipment according to claim 26, wherein
(1) described distillation column is the lower section of fractionating column, and wherein, described more volatile steam distillation stream cooled off fully with in the section of the described fractionating column above described distillation column partly condensation it, and simultaneously separated to form described volatile residual gas part and described reflow stream, described by this reflow stream flows to the top fractionation level of described distillation column; And
(2) described the 4th heat-exchange device is connected on the described fractionating column to receive described volatile residual gas part, make described the 4th heat-exchange device be suitable for the described volatile residual gas part of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
32. equipment according to claim 27, wherein
(1) described distillation column is the lower section of fractionating column, and wherein, described more volatile steam distillation stream cooled off fully with in the section of the described fractionating column above described distillation column partly condensation it, and simultaneously separated to form described volatile residual gas part and described reflow stream, described by this reflow stream flows to the top fractionation level of described distillation column; And
(2) described the 5th heat-exchange device is connected on the described fractionating column to receive described volatile residual gas part, make described the 5th heat-exchange device be suitable for the described volatile residual gas part of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
33. equipment according to claim 28, wherein
(1) described distillation column is the lower section of fractionating column, and wherein, described more volatile steam distillation stream cooled off fully with in the section of the described fractionating column above described distillation column partly condensation it, and simultaneously separated to form described volatile residual gas part and described reflow stream, described by this reflow stream flows to the top fractionation level of described distillation column; And
(2) described the 5th heat-exchange device is connected on the described fractionating column to receive described volatile residual gas part, make described the 5th heat-exchange device be suitable for the described volatile residual gas part of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
34. equipment according to claim 24, wherein, described equipment comprises
(1) fractionator, be connected on described first expansion gear, with first air-flow of the cardinal principle condensation that receives described expansion and heat it, described fractionator is also connected on the described distillation column, with receive described more volatile steam distillation stream and it cool off fully with condensation partly it, and simultaneously it is separated to form described volatile residual gas part and described reflow stream, described fractionator is also connected on the described distillation column, to supply with described first air-flow of thermal expansion that adds as the feeding to described distillation column, with the top feeding of described reflow stream conduct to described distillation column; With
(2) described the 4th heat-exchange device, be connected on the described fractionator to receive described volatile residual gas part, make described the 4th heat-exchange device be suitable for the described volatile residual gas part of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
35. equipment according to claim 25, wherein, described equipment comprises
(1) fractionator, be connected on described first expansion gear, to receive described expansion cardinal principle condensation first air-flow and to heat it, described fractionator is also connected on the described distillation column, with receive described more volatile steam distillation stream and it cool off fully with condensation partly it, and simultaneously it is separated to form described volatile residual gas part and described reflow stream, described fractionator is also connected on the described distillation column, to supply with described first air-flow of thermal expansion that adds as the feeding to described distillation column, with the top feeding of described reflow stream conduct to described distillation column; With
(2) described the 4th heat-exchange device, be connected on the described fractionator to receive described volatile residual gas part, make described the 4th heat-exchange device be suitable for the described volatile residual gas part of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
36. equipment according to claim 26, wherein, described equipment comprises
(1) fractionator, be connected on described first expansion gear, to receive described expansion cardinal principle condensation first air-flow and to heat it, described fractionator is also connected on the described distillation column, with receive described more volatile steam distillation stream and it cool off fully with condensation partly it, and simultaneously it is separated to form described volatile residual gas part and described reflow stream, described fractionator is also connected on the described distillation column, to supply with the described mix flow of thermal expansion that adds as the feeding to described distillation column, with the top feeding of described reflow stream conduct to described distillation column; With
(2) described the 4th heat-exchange device, be connected on the described fractionator to receive described volatile residual gas part, make described the 4th heat-exchange device be suitable for the described volatile residual gas part of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
37. equipment according to claim 27, wherein, described equipment comprises
(1) fractionator, be connected on described second expansion gear, to receive described expansion cardinal principle condensation first air-flow and to heat it, described fractionator is also connected on the described distillation column, with receive described more volatile steam distillation stream and it cool off fully with condensation partly it, and simultaneously it is separated to form described volatile residual gas part and described reflow stream, described fractionator is also connected on the described distillation column, to supply with described first air-flow of thermal expansion that adds as the feeding to described distillation column, with the top feeding of described reflow stream conduct to described distillation column; With
(2) described the 5th heat-exchange device, be connected on the described fractionator to receive described volatile residual gas part, make described the 5th heat-exchange device be suitable for the described volatile residual gas part of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
38. equipment according to claim 28, wherein, described equipment comprises
(1) fractionator, be connected on described second expansion gear, to receive described expansion cardinal principle condensation first air-flow and to heat it, described fractionator is also connected on the described distillation column, with receive described more volatile steam distillation stream and it cool off fully with condensation partly it, and simultaneously it is separated to form described volatile residual gas part and described reflow stream, described fractionator is also connected on the described distillation column, to supply with the described mix flow of thermal expansion that adds as the feeding to described distillation column, with the top feeding of described reflow stream conduct to described distillation column; With
(2) described the 5th heat-exchange device, be connected on the described fractionator to receive described volatile residual gas part, make described the 5th heat-exchange device be suitable for the described volatile residual gas part of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
39. equipment according to claim 24, wherein, described equipment comprises
(1) compression set is connected on the described separator, to receive described volatile residual gas part and to compress it; With
(2) described the 4th heat-exchange device, be connected on the described compression set to receive the volatile residual gas part of described compression, make described the 4th heat-exchange device be suitable for the volatile residual gas part of the described compression of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
40. according to claim 25 or 26 described equipment, wherein, described equipment comprises
(1) compression set is connected on described second separator, to receive described volatile residual gas part and to compress it; With
(2) described the 4th heat-exchange device, be connected on the described compression set to receive the volatile residual gas part of described compression, make described the 4th heat-exchange device be suitable for the volatile residual gas part of the described compression of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
41. according to claim 27 or 28 described equipment, wherein, described equipment comprises
(1) compression set is connected on described second separator, to receive described volatile residual gas part and to compress it; With
(2) described the 5th heat-exchange device, be connected on the described compression set to receive the volatile residual gas part of described compression, make described the 5th heat-exchange device be suitable for the volatile residual gas part of the described compression of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
42. according to claim 29,30 or 31 described equipment, wherein, described equipment comprises
(1) compression set is connected on the described fractionating column, to receive described volatile residual gas part and to compress it; With
(2) described the 4th heat-exchange device, be connected on the described compression set to receive the volatile residual gas part of described compression, make described the 4th heat-exchange device be suitable for the volatile residual gas part of the described compression of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
43. according to claim 32 or 33 described equipment, wherein, described equipment comprises
(1) compression set is connected on the described fractionating column, to receive described volatile residual gas part and to compress it; With
(2) described the 5th heat-exchange device, be connected on the described compression set to receive the volatile residual gas part of described compression, make described the 5th heat-exchange device be suitable for the volatile residual gas part of the described compression of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
44. according to claim 34,35 or 36 described equipment, wherein, described equipment comprises
(1) compression set is connected on the described fractionator, to receive described volatile residual gas part and to compress it; With
(2) described the 4th heat-exchange device, be connected on the described compression set to receive the volatile residual gas part of described compression, make described the 4th heat-exchange device be suitable for the volatile residual gas part of the described compression of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
45. according to claim 37 or 38 described equipment, wherein, described equipment comprises
(1) compression set is connected on the described fractionator, to receive described volatile residual gas part and to compress it; With
(2) described the 5th heat-exchange device, be connected on the described compression set to receive the volatile residual gas part of described compression, make described the 5th heat-exchange device be suitable for the volatile residual gas part of the described compression of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
46. equipment according to claim 24, wherein, described equipment comprises
(1) heater is connected on the described separator, to receive described volatile residual gas part and to heat it;
(2) compression set is connected on the described heater, with the volatile residual gas part that receives described heating and compress it; And
(3) described the 4th heat-exchange device, be connected on the described compression set volatile residual gas part with the heating that receives described compression, make described the 4th heat-exchange device be suitable for the volatile residual gas part of the heating of the described compression of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
47. according to claim 25 or 26 described equipment, wherein, described equipment comprises
(1) heater is connected on described second separator, to receive described volatile residual gas part and to heat it;
(2) compression set is connected on the described heater, with the volatile residual gas part that receives described heating and compress it; And
(3) described the 4th heat-exchange device, be connected on the described compression set volatile residual gas part with the heating that receives described compression, make described the 4th heat-exchange device be suitable for the volatile residual gas part of the heating of the described compression of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
48. according to claim 27 or 28 described equipment, wherein, described equipment comprises
(1) heater is connected on described second separator, to receive described volatile residual gas part and to heat it;
(2) compression set is connected on the described heater, with the volatile residual gas part that receives described heating and compress it; And
(3) described the 5th heat-exchange device, be connected on the described compression set volatile residual gas part with the heating that receives described compression, make described the 5th heat-exchange device be suitable for the volatile residual gas part of the heating of the described compression of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
49. according to claim 29,30 or 31 described equipment, wherein, described equipment comprises
(1) heater is connected on the described fractionating column, to receive described volatile residual gas part and to heat it;
(2) compression set is connected on the described heater, with the volatile residual gas part that receives described heating and compress it; And
(3) described the 4th heat-exchange device, be connected on the described compression set volatile residual gas part with the heating that receives described compression, make described the 4th heat-exchange device be suitable for the volatile residual gas part of the heating of the described compression of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
50. according to claim 32 or 33 described equipment, wherein, described equipment comprises
(1) heater is connected on the described fractionating column, to receive described volatile residual gas part and to heat it;
(2) compression set is connected on the described heater, with the volatile residual gas part that receives described heating and compress it; And
(3) described the 5th heat-exchange device, be connected on the described compression set volatile residual gas part with the heating that receives described compression, make described the 5th heat-exchange device be suitable for the volatile residual gas part of the heating of the described compression of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
51. according to claim 34,35 or 36 described equipment, wherein, described equipment comprises
(1) heater is connected on the described fractionator, to receive described volatile residual gas part and to heat it;
(2) compression set is connected on the described heater, with the volatile residual gas part that receives described heating and compress it; And
(3) described the 4th heat-exchange device, be connected on the described compression set volatile residual gas part with the heating that receives described compression, make described the 4th heat-exchange device be suitable for the volatile residual gas part of the heating of the described compression of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
52. according to claim 37 or 38 described equipment, wherein, described equipment comprises
(1) heater is connected on the described fractionator, to receive described volatile residual gas part and to heat it;
(2) compression set is connected on the described heater, with the volatile residual gas part that receives described heating and compress it; And
(3) described the 5th heat-exchange device, be connected on the described compression set volatile residual gas part with the heating that receives described compression, make described the 5th heat-exchange device be suitable for the volatile residual gas part of the heating of the described compression of cooling under pressure, also form described condensate flow thus with its at least a portion of condensation.
53. according to claim 24,25,26,27,28,29,30,31,32,33,34,35,36,37,38,39 or 46 described equipment, wherein, described volatile residual gas partly comprises described methane, light composition, reaches C 2The major part of composition.
54. according to the described equipment of claim 40, wherein, described volatile residual gas partly comprises described methane, light composition, reaches C 2The major part of composition.
55. according to the described equipment of claim 41, wherein, described volatile residual gas partly comprises described methane, light composition, reaches C 2The major part of composition.
56. according to the described equipment of claim 42, wherein, described volatile residual gas partly comprises described methane, light composition, reaches C 2The major part of composition.
57. according to the described equipment of claim 43, wherein, described volatile residual gas partly comprises described methane, light composition, reaches C 2The major part of composition.
58. according to the described equipment of claim 44, wherein, described volatile residual gas partly comprises described methane, light composition, reaches C 2The major part of composition.
59. according to the described equipment of claim 45, wherein, described volatile residual gas partly comprises described methane, light composition, reaches C 2The major part of composition.
60. according to the described equipment of claim 47, wherein, described volatile residual gas partly comprises described methane, light composition, reaches C 2The major part of composition.
61. according to the described equipment of claim 48, wherein, described volatile residual gas partly comprises described methane, light composition, reaches C 2The major part of composition.
62. according to the described equipment of claim 49, wherein, described volatile residual gas partly comprises described methane, light composition, reaches C 2The major part of composition.
63. according to the described equipment of claim 50, wherein, described volatile residual gas partly comprises described methane, light composition, reaches C 2The major part of composition.
64. according to the described equipment of claim 51, wherein, described volatile residual gas partly comprises described methane, light composition, reaches C 2The major part of composition.
65. according to the described equipment of claim 52, wherein, described volatile residual gas partly comprises described methane, light composition, reaches C 2The major part of composition.
66. according to claim 24,25,26,27,28,29,30,31,32,33,34,35,36,37,38,39 or 46 described equipment, wherein, described volatile residual gas partly comprises described methane, light composition, C 2Composition, and C 3The major part of composition.
67. according to the described equipment of claim 40, wherein, described volatile residual gas partly comprises described methane, light composition, C 2Composition, and C 3The major part of composition.
68. according to the described equipment of claim 41, wherein, described volatile residual gas partly comprises described methane, light composition, C 2Composition, and C 3The major part of composition.
69. according to the described equipment of claim 42, wherein, described volatile residual gas partly comprises described methane, light composition, C 2Composition, and C 3The major part of composition.
70. according to the described equipment of claim 43, wherein, described volatile residual gas partly comprises described methane, light composition, C 2Composition, and C 3The major part of composition.
71. according to the described equipment of claim 44, wherein, described volatile residual gas partly comprises described methane, light composition, C 2Composition, and C 3The major part of composition.
72. according to the described equipment of claim 45, wherein, described volatile residual gas partly comprises described methane, light composition, C 2Composition, and C 3The major part of composition.
73. according to the described equipment of claim 47, wherein, described volatile residual gas partly comprises described methane, light composition, C 2Composition, and C 3The major part of composition.
74. according to the described equipment of claim 48, wherein, described volatile residual gas partly comprises described methane, light composition, C 2Composition, and C 3The major part of composition.
75. according to the described equipment of claim 49, wherein, described volatile residual gas partly comprises described methane, light composition, C 2Composition, and C 3The major part of composition.
76. according to the described equipment of claim 50, wherein, described volatile residual gas partly comprises described methane, light composition, C 2Composition, and C 3The major part of composition.
77. according to the described equipment of claim 51, wherein, described volatile residual gas partly comprises described methane, light composition, C 2Composition, and C 3The major part of composition.
78. according to the described equipment of claim 52, wherein, described volatile residual gas partly comprises described methane, light composition, C 2Composition, and C 3The major part of composition.
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