SA05260083B1 - Natural Gas Liquefaction - Google Patents

Abstract

Abstract: This invention relates to a process for liquefying natural gas while simultaneously producing a liquid stream containing mostly hydrocarbons heavier than methane. In the process, the natural gas stream to be liquefied is partially cooled. The first stream is cooled down again to condensate it all to a great extent, expanded to medium pressure and then passed to the distillation column at a first feed position in the center of the column. The second stream will also be extended to medium pressure and then passed to the shaft at a second feed position in the center of the shaft. The distillation stream is drawn from the column below the feed point of the second stream and cooled to condense at least part of it to form a reflux stream. At least part of the reflux stream is directed to the distillation column as its top feed. The bottom product from this distillation column contains, as detailed, most any hydrocarbons heavier than methane which otherwise could reduce the purity of the liquefied natural gas. The remaining gas stream from the distillation column is compressed to a higher intermediate pressure, cooled under pressure to condense and then expanded to a lower pressure to form the LNG stream.

Description

Y

Natural gas liquefaction

Natural Gas Liquefaction Full Description Background of the Invention Natural Gas Rich Stream Natural Gas This invention relates to a process for processing other liquefied natural gas (LNG) natural gas to produce a methane liquefied natural gas stream .methane Predominant heavier than methane hydrocarbons High purity and stream containing hydrocarbons Natural gas is usually extracted from wells drilled in reservoirs. It usually contains gas that contains a large percentage of methane. any methane containing 100 pmol per cent gas and depending on the particular aquifer; Natural gas also contains relatively smaller amounts of propane and ethane, which is the heaviest hydrocarbons of hydrocarbons and the like. In addition to water, hydrogen, pentanes, pentanes, butanes, butanes, carbon dioxide, carbon dioxide, nitrogen, and other natural hydrogen gases in gaseous form. Most of the ways are gases, and most of the gases are dealt with to the gas processing plants and then to the IDL from the natural gas nozzle, which is common to transport natural gas to natural gas consumers through high-pressure gas transmission pipelines. And in a number of 1 circumstances; In any case ; It is found necessary and/or desirable to liquefy natural gas, either for transportation or use. and in remote locations; For example ; There is usually no natural gas infrastructure to market. And in such cases; The DL Pipelines allow for transport and even

. The lower specific volume of LNG related to natural gas in the gaseous state greatly reduces transportation costs by allowing LNG to be transported using freighters or tankers. There is another case that favors the liquefaction of natural gas, which is to be used as fuel for cars. In d large metropolitan areas there are fleets of buses, vans and trucks that can run on liquefied natural gas (LNG) if there is an economical source of LNG available. These vehicles powered by liquefied natural gas (LNG) cause less air pollution than gasoline and Allg diesel engines burn hydrocarbons of higher molecular weight 0. in addition to ; If the liquefied natural gas (LNG) is of high purity (i.e. with a methane purity of 90 mol per cent or higher); The amount of carbon dioxide ("heating gas") produced is reasonably less due to the ratio of carbon:_hydrogen to methane compared to all other hydrocarbon fuels. Vo General Description of the Invention The present invention generally relates to the liquefaction of natural gas which is produced as an associated product; a liquid stream consisting primarily of JB hydrocarbons of methane; LNG natural gas consisting of ethane, propane, butanes and heavier hydrocarbon components and liquefied petroleum gas (LNG) consisting of propane, butanes and heavier hydrocarbon components; or the condensate consisting of butane and heavier hydrocarbon components; The liquid stream production of the Calas product has two important benefits: Liquefied Natural Gas (LNG) has calle methane purity and the associated liquid Yo product is a valuable product that can be used for many other purposes. that analysis

¢ Conventional natural gas stream produced according to this invention will be at an approximate fractional rate; It consists of 784.7 methane, 77.9 ethane butane and other © ingredients and £9.9 propane and ye components and 71001 iso-butane 70110 yiso-butane Z+. Nitrogen© and carbon dioxide. Sometimes there are gases containing sulfur. There are many known ways to liquefy natural gas. For example, ¢ See Finn, Adrian J., Grant L.

Johnson and Terry R.

Tomlinson "LNG Technology for Offshore and Mid-Scale Plants" Proceedings of the Seventy — Ninth Annual Conventions of the Gas Processors Associations pp. p. the Gas Processors Association, San Antonio, Texas, — MARCH 4, 7000 - To estimate and check the number of these processes: US Patents Nos. 44,059,117, 5751/85, fofoVao, 47000.., 41951777, 5 011780: 76 Md. 1747097 31 and US Patent Pending Application No. 119770150 filed at; Jun 70607; Relevant processes Jain this dale way also describes the steps by which natural gas is purified (by removing 0 0 (water and unwanted components Jie carbon dioxide and sulfur components) and cooled The cooling and condensing of natural gas can be accomplished in many different ways, and the process of “cascade cooling” in which the heat exchange of natural gas is used with

Different refrigerants with successive degrees of decrease, such as propane, ethane, and methane. Alternatively, this heat exchange can be accomplished by using a single gas refrigerant by evaporating the refrigerant at several different pressures. and the 'multi-component refrigeration' process in which the heat exchange of natural gas is used with one or more

else 0 cooling; It consists of multiple refrigerant components rather than single, multi-component refrigerants. Natural gas expansion can be accomplished by both isenthalpically isothermal enthalpy (using Johle-Thomson expansion for example; and by isentropically isothermal (using an operational expansion turbine). ; For example .

01 Regardless of the method used to liquefy the natural gas stream; It is common for a portion of the hydrocarbons heavier than methane to be removed before the methane-rich stream is liquefied. There are many reasons for removing hydrocarbons, including the need to control the heating value of the natural gas (LNG) stream and the value of these heavier hydrocarbon components as products in their own right. Unfortunately, it has not yet been focused and paid enough attention

1 for the effectiveness of the hydrocarbon removal step.

And according to the invention, Jal; It was found that careful integration of the carbon removal step into the LNG liquefaction process could produce both LNG and separate heavier liquid hydrocarbons using less energy than previous processes in the field. the present invention; Although applicable and usable

at lower pressures; However, it is particularly useful when treating feed gases in the range from 0 to 0501 psia [YVOA] to 01747 [kPa(a) or higher. Brief description of the drawings

00

For a better understanding of the invention, Jad, it is possible to refer to the following examples and drawings, and by reference to the drawings: Figure -1 shows a flow diagram of a natural gas liquefaction unit prepared for the co-production of liquefied petroleum gas (LPG) according to the present invention. > Figures 1 and “- show diagrams of alternative fractional distillation systems that may be used in the process of the present invention. Fig.- a graphical representation of the pressure enthalpy phase of methane which is used to illustrate the advantages of the present invention over previous processes in the same field; f © shapes; cA YT and 01 show flow diagrams of alternative 0 natural gas liquefaction units intended for liquid-liquid co-production according to the present invention. The following interpretations of the above figures; The figures and tables are presented to summarize flow rates calculated for representative process conditions. And in the tables shown here; The values of flow rates (molecular weights per hour) have been rounded to the nearest integer for suitability. The total current flow rates shown in the tables include all non-Vo hydrocarbon components, and therefore it is greater than Ae gana current flow rates for the hydrocarbon components. The temperatures shown are approximate values rounded to the nearest degree. It should be noted that the process design calculations prepared for the purpose of comparing the processes shown in the figures are based on the assumption that there is no heat leakage from (or to) the environment surrounding (or from) the process. The quality of commercially available insulation materials makes this a very reasonable assumption which has traditionally been made by those experts in the same field. For AD, the parameters of the process variables were set in both traditional British units and SI units. The particle flow rates shown in the tables (Say) can be interpreted either in moles (pound moles per hour) or in moles (kilograms) Yiv.

Vv

per hour. The energy consumptions stated in horsepower (HP) and/or British thermal units in thousands per hour (MBTU / Hr) are equivalent to the molecular weight flow rates stated in pounds moles per hour. The incoming energy consumption in kilowatts (kW) is identical to the particle weight flow rates stated in kilogram moles in

0 o'clock. incoming production rates. Pounds per hour is the same as the molecular weight flow rates stated in pounds moles per hour. The reported production rates in kilograms per hour are the same as the molecular flow rates stated in moles per hour.

0 Detailed description

With reference to Figure 1; We start by clarifying the process according to the present invention as he desires

Associated NGL ite production contains the majority of the propane and heavier components in the natural gas feed stream. and in this calendar of the present invention; The gas entering the unit, Jay, is at a temperature of 8 FY [degrees Celsius] and a pressure of 185 psi [8860 kPa(2)].

carbon dioxide and if the incoming gas contains a concentration of carbon dioxide. ©1 as stream 1 Sulfur compounds prevent product streams from meeting specifications; These Sf components are eliminated by appropriate pretreatment of the feed gas (not shown). In addition ; The feed stream is usually dried to prevent the formation of water (ice) under low temperature conditions. A solid desiccant was usually used for this purpose

Yes and the feed stream YY in the heat exchanger 01 is cooled by heat exchange with the coolant and flash separator fluid streams at [YU] YE (stream 40 A). It is noted that in all cases; The heat exchanger 01 is representative of either several individual heat exchangers or a single multi-role heat exchanger; or any direction thereof. (The decision to use more than one heat exchanger for the refrigeration services described depends on a number of factors

Yo include; But it is not limited to; Inlet gas flow rate and heat exchanger volume

A

-DAM YY at 11 A YY disconnect device and current temperatures; etc). The refrigerant stream enters from the liquid (YY) the vapor is separated (Cus kPa(a) AMY psi VYVA stream and condensate (TY) pressure and the vapor (YY stream) is separated from the separator 11 into two streams WE;YO with the YE stream 0 containing about 715 total vapor.In some circumstances it is preferable to combine the YE stream with part of the condensed liquid (VA stream) to form a combined stream. TO; but in this view there is no flow in the current FA. The combined current Fo passes through the heat exchanger 1" in a heat exchange relationship with the refrigerant stream VY e and the liquid distillation stream 50 which produces die Substantial cooling and condensation of the current © A. A flash expansion of the condensed current much fre at (YA-) Gam 0 through a masked expansion device such as expansion valve 06 is made to rise slightly above operating pressure (approximately 0 psi square) YY VY kPa(a)] ] of the fractional distillation tower 19. Part of the stream is evaporated during expansion resulting in cooling of the total stream. In the process shown in Figure 1, the expanding stream Fo b which Allows expansion valve VE up to -?11 F sy (a AY) heating of expanded stream fe to -78” F (aM) and further evaporates in heat exchanger 1 _ jie Cus YY Partial cooling and condensation of the YV steam distillation stream ascending from the fractional distillation stages of the fractional distillation tower 19 . The Land stream 75c is passed at an upper intermediate feed position in the ethane removal section 1b of the NA fractional distillation tower and the remaining 7880 percent of steam from separator 11 (stream FV) enters into A operational expansion 11 in which the mechanical energy is extracted from this portion of high pressure Aa 0. Machine 15 expands the steam entropically greatly from a pressure of about 74 psi [7 kPa(a) AM to operating pressure for the tower with the working expansion cooling of the expanding stream “A to a temperature of approximately 0Y=F (9£m). and conventional extensions

.

The commercially available ones are capable of extracting Av - 788 percent of the theoretically available yield in perfect isoentropic expansion. The extracted product is usually used to power the centrifugal hel a (eg item (V1) which can be used to recompress the tower head gas Ss (£9) for example). The expanded and partially condensed stream is passed “©a” as feed to the distillation column © 19 at a lower feed point in the middle of the shaft. A flash expansion of the stream fe, which is the remaining part of the separator fluid (VF) slightly above the operating pressure of the dethanizer 09, is carried out by expansion valve VY as stream 0 cools. ? to GE (2°77) (60 bar) before giving cooling to the inlet feed gas as previously described. By entering a 0b stream now at TY (7”m) then into a 14 LAY remover ) at a second lower feed point in the middle

.1? Column 0 is a conventional distillation column containing 19 and the deethane in a molecular distillation tower a set of trays spaced vertically apart; and one or more supportive cradles or some combination trays and support fillings. As is usually the case in natural gas processing units; The molecular distillation tower may consist of two parts. Upper section 119 is a natural gas apparatus _modern chapter divides the upper feed into its corresponding parts of steam and liquid; Whereas, 1 the rising steam from the lower distillation section or the ethane removal section 401b combines with the FV part of the steam (if any) from the upper feed to form the upper evaporator steam (tower stream). It contains the lower part, which is the removal section 4 ab On the Ad which exits the trays and/or the support gaskets and provides the necessary contact between the downward liquids and the upward rising vapors It also includes a de-ethane section and one or more of the 30 re-stages which heats and vaporizes a portion of the flowing liquids downward 01) Boiling (such as re-boiling phases which flow up the column. The liquid product stream Juan) exits the column to introduce vapors

1; from the bottom of the tower at 7 F (01 (27) based on the conventional specification of the ratio of ethane to propane which is equal to 1 : 0.0710 based on the molecular weight of the bottom product. The upper distillation stream 17 VA de-ethane at (p08) YF and is partially cooled and condensed in a reflux condenser 71 as previously described. The compressed current We 7©a enters the reflux cylinder YY at AE (-70 um) where it separates the liquid Co Sal (stream ;;) of non-condensed vapor (stream 6) and the compressed liquid (stream £5) is pumped by the YY pump to the upper feed point of the deethanizer 11 as a reflux stream 4a. From the fractional distillation tower, the reflux condenser 71 can be placed inside the tower above column VA as shown in Figure 0. Thus, there is no need for reflux cylinder YY and reflux pump YY because the distillation stream then cools It is condensed on top of the tower above the column fractional distillation stages.Alternatively, the use of a fractional condenser (such as fractional condenser 71 in fig. ”) instead of reflux condenser 71 in fig.1 excludes the reflux cylinder and reflux pump and also provides synchronized fractional distillation stages To replace those stages at the top of column 1 is methane removal. And if the fractional capacitor is placed separately on a graduated level; It is connected to the steam/liquid separating device, and the liquid collected in the separating device is filtered to the distillation column. The decision whether a reflux condenser can be placed within the column or a fractional condenser used usually depends on the unit size and surface requirements of the heat exchanger. The non-condensed steam (Stream 61) from the reflux cylinder is heated to 99 F © (4,7 C) in Thermal Jobe YE and a portion (Stream 44) is then withdrawn to act as fuel gas for the unit. which must be drawn to a large extent according to the fuel required for the engines and/or turbines that operate the gas pistons in the unit; die

liquid pistons to cool CTT CTE 18 in this example). The remaining part of the superheated steam (stream 449;) is compressed by piston 11 which is actuated by expansion machines CTV “+”; b) to a greater degree GAY (-14m) in Vesa 0 exchanger by transverse exchange with cold steam; AY stream then Jay stream 9; c in Te heat exchanger and cooled again by stream Refrigerant 1d to Yoon degree (-100m) to condensate and further cool it, and so on Ja 71 work expansion machine where mechanical energy is extracted from the stream The +1 machine expands the liquid stream 4d; Further isobaric expansion from 0 pressure measured at ~5497 psi [4085 [kPa(a) to storage pressure — LNG V0.0) psi [107 [kPa@] ); higher From the atmospheric pressure at a slight rate, the expanded workpiece extends the stream 4 e approximately to a temperature of 755 F (-11 C), and is then directed to the TY LNG storage tank containing the (e + LL) LNG product Vo, and all the cooling is obtained for the streams, Ye and 9; c, by means of a closed loop refrigeration circuit.The operating system for this boiler consists of a mixture of hydrocarbons and nitrogen ¢ with the mixing composition modified as needed to obtain a temperature refrigeration required; Lay Condensation is done at a reasonable pressure using the available refrigerant medium. In this case, the occurrence of 0 condensation using chilled water was assumed; Thus, the cryogenic mixture consisting of 0 nitrogen, methane, ethane, propane, and fewer hydrocarbons is used in simulating the process in Figure (1).

VY

is 72.7 nitrogen 7018 nitrogen methane and 7.0; ethane and 8.76 propane; The remainder are heavier hydrocarbons. The refrigerant stream VY exits the vacuum cooler 4 at YA (Yee) (01 psi [4.185 kPa(a)) pressure. Then it enters the heat exchanger 01 and cools down to 0 degrees. (VS) GFE m) and it is partially condensed by the partially cooled expansion stream (Gad) VY and by other cooled streams. and to simulate 1 Jal; These other refrigerant streams were assumed to be commercial quality propane refrigerants at three different levels of pressure and temperature. Then the partially condensed cooled stream 17a enters the 1” heat exchanger to be further cooled to -40°F (A) by a partially expanded cooled YS stream VY e to further condensate the cooled stream (stream 1/ 1 b). The refrigerant is sealed and then further cooled to Yoo F-01 (m) in the heat exchanger by means of an expanding refrigerant stream of 1 Lad. The cooled liquid stream enters additional cooling (Aisle) operating expansion 17 whereby mechanical energy is extracted from the stream as it expands abundantly and isotropiically from a pressure of about 583 psi [4040 [kPa(a)] to about 4040 [kPa(a). VE pounds per square inch [234 [kPa(a) . A proportion of the current evaporates during the expansion; As a result, the alah current is cooled to (VY tal) (pV VES) Yes; Then the expanded al VY d enters again into heat exchangers 10, VY and 01 where it provides cooling for stream 44c, current V, current EY and coolant streams VY) 17a and 1lab ) as it evaporated and was heated above the heating temperature YL. The coolant stream steam (GY) heated above the preheating point exits heat exchanger 01 at 90°F (YY) m) and is compressed in three stages to TY psi

VY

squared]4254 [kPa(a) . JS runs one stage of the ADA Jax all (4+, +1 and TA refrigeration compressors) by an auxiliary power supply followed by a cooler (Vacuum Refrigerants 510 7+ and 19) to remove the compression heat. The compressed stream returns VY from the vacuum cooler 9 to the heat exchanger 01 to complete the cycle.° A summary of the current flow rates and power consumption for the process shown in Figure 1 is shown in the following table: Table “1” 0 Summary of current flow lb / mol/hour (kilograms/mol/hour) Cer Can [ee ee |e a Cen |r ear [ ew | | Con | [wee [rn |e | en | | bright | two | ov fre |e q | Coe | |v ren

Ve

NGL recovered from 8m propane

Yeon + Butanes (kg/hr) 1997.071 lb/hr 097.071 Production Rate

LNG Product lb/hr (775.577 kg/hr) VYo.0YY Production Rate 74 * Purity (MJ /m® 10) (84 BTU/SCF) Lower Heating Value Power ( KW 64 HP (44.771 0) Refrigerant Pressure 01 (KW 04.44¢) HP ¥1.£4Y Propane Pressure (KW 1 kg) Total Pressure 4 m1 Heat Used (KW 3.49760) h /MBTU 0007 De-Methane Reboiler (dependent on incomplete flow rates) 0 Typically compared using the required “LNG Consumption The Specific Energy Production Process Efficiency” which is: Ratio of Total Cooling Pressure Power to

Dla The total rate of liquid production and the preparation of published information on the extent of a SING specific energy in favor of technical processes prior to the production of ; Which 0.182 HP-Hr/Lb [0.300 KW-Hr/Kg] to 0.168 HP-Hr [0.276 KW-Hr/Kg] 0 days per year of unit production VE for lal duration is believed to depend on a factor Validity and on the same basis; The specific consumption of energy to embody . Industrial LNG from

Fig. 1 The subject matter of the present invention presented is 0.148HP-Hr Lb [0.243 KW-Hr/Kg] which gives an estimated yield improvement of 4 -1 777 over previous technical processes. There are two main factors due to the improved efficiency of this invention. The first factor can be understood by selecting the thermodynamics of the liquefaction process when it is applied to a high-pressure gas stream, such as the one studied in this example. And since the main component of this Lal is methane; (Sad) The use of the thermodynamic properties of methane for purposes of comparing the liquefaction cycle that is employed in the previous technical processes against the cycle used in this invention. The figure contains a diagram of the enthalpy phase of methane pressure. The cooling of the gas stream while the stream is at high pressure (path A - B) and so the stream then expands (path B - C) to the pressure of the ING storage vessel (slightly greater than atmospheric pressure). It employs a work-expansion machine, which can recover VO = 786 of theoretically available work in an ideal isentropic expansion of 1880808. For the sake of simplicity, the complete isentropic expansion (for path B-C) is shown in Figure 4. Although 1 Therefore, the enthalpy reduction obtained by work expansion is very small, because the lines of constant temperature equivalence are nearly vertical in the liquid region of the phase diagram.This is now compared to the liquefaction cycle of the present invention after partial cooling at a pressure of l (path A - A); the gas stream is expanded by operation (path A - A) to medium 0 pressure. (Again, a full isoentropic expansion is shown for simplicity) – The remainder of the cooling process is completed at medium pressure (path A-B); Then the current expands (path b" - c) to the pressure of the ING storage vessel and since the lines of the degree of the shelf

V1: the constant thermoneutral is less strongly inclined in the vapor region of the phase diagram; Lala we get a much lower enthalpy overall; By the first step of operating expansion (A-A path) in the present invention. Thus the amount of total cooling required of the present invention (sum of paths A = T and a - b) is less than the 0 cooling (and therefore cooling pressure) required to liquefy the gas stream.

Ld The second factor illustrating the improved efficiency of the present invention is the higher performance of hydrocarbon distillation systems at lower operating pressures and the hydrocarbon removal step is performed in most prior art processes. When pressing add je usually with a washing column a cold hydrocarbon liquid is used as an absorbent stream to remove the lesser hydrocarbons

0 .of the inlet gas stream. and operating the scrubber at high pressure is not efficient enough; As it results in the accompanying absorption of a large part of methane and ethane from the gas stream; Which must be removed later from the absorbent liquid and cooled to become part of the LNG product. The hydrocarbon removal step in the present invention takes place at medium pressure; where the vapor-liquid equilibrium is more appropriate; It results in a very efficient recovery

1 for the heavier hydrocarbons required for the liquid stream produced at the same time. Other incarnations

Those skilled in the art will understand that the present invention can be adapted to all types of ING liquid units to allow the production of a co-stream of .1101 and an LPG or condenser stream simultaneously; According to what best suits the needs in a specific location of the industrial unit. as

© He will also understand that a variety of process forms can be used to recover the common fluid stream produced at the same time. The present invention can also be adapted to recover an NGL stream containing a large portion of the :© components present in the enrichment gas; or

: l

To recover a compressed stream containing only gas and heavier components present in the feed gas;

You was co-produced by LPG at the same time as described above. Figure 1 is the preferred embodiment of the present invention for the described operating conditions. Figures illustrate © to 01 alternative embodiments of the present invention 'Ally' that may be considered for a particular use. Depending on the amount of heavier hydrocarbons in the feed gas and the pressure of the feed gas; the refrigerant feed stream 1?a leaving heat exchanger 01; It may not contain any liquid (because it is above its dew point; or because it is higher than its cricoundentbar) and so that separator 11 shown in Figures 1 and Figures + to 01 is not required; The cooled feed stream can flow directly into a suitable expansion device; Like the stretching machine 115. In cases where the input gas is more saturated than that described hereto, an embodiment of the present invention as shown in Figure 0 may be used. The TY CES liquid stream flows through the VA heat exchanger and is further cooled; Then it is divided into two parts. The first section (stream 00;) flows through a VY expansion valve where it undergoes flash evaporation expansion as the pressure is reduced to approximately No from the distillation pressure 19 . The cold stream FEe from expansion valve 11 then flows through the heat exchanger VA; Where it is partially heated, as it is used to cool the current © for additional cooling, as previously explained. Stream 0 kb is further warmed molecularly in thermal jalal 01 and flows to a mid-low point feed site on split shaft 19 . As for the second part of the liquid (stream (YR) which is still at high pressure, it (1) 0 merges with the section YE of the vapor stream leaving separator 11 or (7) ay with the stream YO already condensed; or (VF) is expanded at its expansion valve VY and thereafter either passes to fracturing column 198 at an overhead intermediate point feed site or merges with the GVO stream

‎YAY.

Ha

Alternatively, stream 9 segments can follow any or all of the validation paths

Described or shown so far in (Fig. *). The process of draining the remaining gas stream after recovery of the co-produced liquid stream (EY stream in Figs. 1 and 1 to 01) before feeding it to the exchanger 01 for condensation and vacuum cooling can be done in many ways. In the process shown in Figure 1 col is heated and compressed at high pressure using the energy extracted from one or more stretching machines; and partially cooled in a vacuum cooler; Then it is further cooled by transversal exchange with the original stream. As shown in Figure +; Some applications can help compress the stream to a higher pressure by using an auxiliary compressor 09 powered by an external power supply 0 eg . As shown by the additive equipment (Ye heat exchanger and YO vacuum cooler (Fig. At the cost of increasing the cooling load on the To heat exchanger and increasing the power consumption of the refrigeration compressors 14, 16 and TA. In such cases the current 169 leaving the compressor can flow directly to the heat exchanger YE as shown in the figure” or flows directly into the heat exchanger Te shown in the figure + If not using stretching machines to stretch any of the parts of the high-pressure feed Sle ¢ a compressor driven by an external power source can be used - such as a compressor 08 shown in Fig. 4 instead of the compressor 11. In some cases no current pressure 0 may be justified at all, so the current flows directly into the heat exchanger 01 as shown in Fig. 01 and by means of the equipment additive (heat exchanger 010 as shown in Fig. 0 and by means of additive equipment (heat exchanger 7; compressor 16; vacuum cooler

01

(Yo) in Figure 1. If the heat exchanger YE is not incorporated to heat the stream before the industrial unit fuel gas (stream 8A) is withdrawn, we may need an additional heating device OA to heat the fuel gas before it is consumed; therefore, by using a stream of Utility or other process stream to provide the necessary heat, as shown in Figures © to 01. These options must generally be evaluated for each application because all factors such as gas composition, unit size, and level of desired co-current recovery produced at the same time must be considered. time -

and equipment available. According to the present invention; The cooling of the inlet gas stream and the feed stream to the LNG fusion section can be done in many ways in the processes shown in Figures 1 and # to 01 . ys The incoming gas stream VY is cooled and condensed by external cooling streams and separator flash liquids. However ; Process cold streams can also be used to provide some cooling for the high pressure coolant (IVY stream). In addition, any temperature stream colder than the cooled streams can be used. For example Gor, a bypass can be made For steam from cracking tower 19 to be used for cooling 1. The use and distribution of tower fluids and/or vapors for process heat exchange and the particular arrangement of heat exchangers for inlet gas cooling and feed gas cooling must be evaluated for each particular Gada; as well as the selection of process streams For special heat exchange services, the selection of a refrigerant source will depend on several factors including, but not limited to, the composition and conditions of the feed gas, the size of the industrial unit, the size of the heat exchanger and the possible temperature of the refrigerant source...etc. Any combination of the aforementioned refrigeration sources or refrigeration methods

palanquin

Y.

To be used together in a group to obtain the required temperature (or temperatures) lal feeding.

Furthermore ; the external supplemental refrigerant added to the inlet gas stream and forms +” to 01 single-component refrigerant continued boiling for high external cooling

Level and evaporative multi-component refrigerant for low level outdoor cooling; that with oo

Use single content refrigerant for pre-cooling of multi-content refrigerant stream. Alternatively; Both high-level cooling and low-level cooling can be done using single-content refrigerants with successively low boiling points (eg cascade cooling) or a single-content refrigerant at successive low pressures.

01 and as another alternative; Both high-level cooling and low-level cooling can be done by using multi-content refrigerant streams with the adjustment of their relative compositions to obtain the necessary cooling temperatures. The selection of the means of providing external cooling depends on a number of factors, including; without limitation; feed gas conditions sc and unit volume; compressor actuator size; and the size of the heat exchanger; The ambient discharge temperature...

_ etc. It will become clear to those skilled in this field, Lind, that any combination or combination of the means of providing external cooling described above can be used together to reach the degree or temperature required for the feed stream.

that further cooling of the condensed liquid stream leaving heat exchanger 01 (stream 4 in Fig. 1, stream 4e in Fig. To, stream 4c in Fig. eV, and stream 4b in

2 cA Figs 4 and stream 9;a in Fig. 01) reduces or eliminates the amount of flash vapor that can be generated during expansion of the stream up to the operating pressure of reservoir 67 for LNG storage. This generally reduces the energy consumption for LNG production by removing and eliminating the screen

1d for the flash gas pressure however; Certain circumstances can help reduce the capital cost of the method by reducing the size of the heat exchanger 01 and using a flash gas pressure or other means to eliminate any flash gas that may be generated. Although single current expansion has been demonstrated in special expansion devices; However, an alternative dilation method can be used when appropriate. and for example ; Conditions can include that an already capacitive feed stream has an operating dilation (current “a in Figs. 1 and © to 01) . In addition ; The even-containing flash expansion Yay can extend from the operating expansion of the further cooled liquid stream which leaves the heat exchanger To (stream 4;d in Fig. 1; stream 4;e in Jal and stream 49;c in Fig. CV 0 and stream 4b in Figs 4cA and stream 44a in Fig. 01) but either more additional cooling in heat exchanger 01 will be necessary to avoid gas formation and flash upon expansion; or the addition of flash vapor pressure or other means to remove the resulting flash vapor. Equally enthalpy iso flash expansion can be used in place of the operating expansion of the additionally cooled high pressure refrigerant stream which leaves the heat exchanger 0 01 (alg stream in figures 1 and 1 to 01) with the resulting increase in power consumption for refrigerant pressure. While preferred embodiments of the invention have been described; It will become clear to those skilled in this field that other modifications and additions can be made; For example, adapting the invention according to the many different Cag Bll ¢ and various feeding patterns; or other requirements without deviating from the spirit of the present invention as described in the following claims:

Claims (1)

YY | protection_elements -1 1 in dle to liquefy a natural gas stream containing methane (lise) and heavier hydrocarbon Y components in which: The aforementioned condensed under pressure in order for natural gas to condensate. The natural gas stream (00 v) is cooled; at least part of it is he, forming a stream of 4 M - (b) said condensate stream is set to a pressure OF of said LNG stream 1 formation; v improvement in which: (1 A) Said natural gas stream is treated in one or more cooling steps q; (Y) 1 The said refrigerated natural gas stream is divided or subdivided into a first gaseous stream at least 11 second gaseous; (V) VY The aforementioned first gas is cooled so that all condense essentially condenses and then returns to yy medium pressure. Ve (4) The aforementioned condensed and extended first gaseous stream is directed in a heat exchange relationship with yo a more volatile steam distillation stream which rises from cracking stages of a distillation column and ym is heated thus  VY (©) is expanded Said second gaseous stream to said medium pressure; YA (7) said first gaseous stream 5:88 expanded warm and said second gaseous 14 gaseous stream said expanded to said Jala distillation column where the streams are separated 0 said to said more volatile steam distillation stream and a relatively less volatile fraction containing YY a large portion of said heavier hydrocarbon constituents. YY (VY) YY Said more volatile steam distillation stream is cooled by the gaseous stream OY vy essentially expanded said condensed sufficiently to partially condense and then separated to form vg a volatile residual gas fraction containing a large portion of said methane and lighter components and stream Yo flashback ¢ (A) Said reflux stream is directed into said distillation column as yy top feed charge; And The remaining cay of the aforementioned pilot is under pressure so that part of the aforementioned (9) v4 gas is cooled. Condensed from it at least, thus forming a condensate stream oy, 1 “- in a process to liquefy a natural gas stream containing methane 0060806 and heavier hydrocarbon Y components and in which: Said Ca Sy under pressure so that the natural gas natural gas stream (0 v) is cooled; FX at least 4% fraction forming a condense ¢ stream ° (b) said condensate stream is limited to a lower pressure to form said LNG Stream 4; 7 improvement in it: (1) A Said natural gas stream is treated in one or more cooling steps in order to partially condense; 1 (7) said partly condensed natural gas stream is separated so as to produce a yy steam stream or liquid stream; VY (1) said vapor stream is split into at least a first stream and a second stream; Vy (?) said first gaseous is cooled so that basically all condense and then returns to yg medium pressure. Humiliation Y¢ The said first condensed and expanded gaseous stream is directed into a heat exchange (0) relationship with a more volatile steam distillation stream which rises from cracking stages from a 1% distillation column and is subsequently heated. yy The second gaseous stream is expanded said to said medium pressure; (1) VA said liquid stream is diluted to said medium pressure; (V) 5 said first dilute gaseous stream and said dilute gaseous stream are directed to (A) 02 within said distillation column Where the aforementioned streams are separated into the more volatile vy steam distillation stream and a relatively less volatile part that contains a large part of the aforementioned heavier hydrocarbon yy components. Hydrocarbon yy The mentioned more volatile steam distillation stream is cooled by the gaseous stream (9) The aforementioned first expanded Ys basically condensed to a degree sufficient to partially condense it and then separated to form vo a volatile residual gas fraction containing a large portion of said methane and lighter components and a vy stream reflux; vy said reflux stream is directed into the said distillation column As a top feed charge (01) YA; and vq, the part of the aforementioned volatile residual gas is cooled under pressure in order to condensate from it at least the aforementioned (11) ro. Natural gas containing methane 0060806 and hydrocarbon components -* 1 in which: the aforementioned Js hydrocarbon 0 is under pressure so that part of it condenses natural gas the natural gas stream is cooled (00 v and ¢ condensed stream the least component leg Yo (b) said condensate stream is reduced to a lower pressure to form said °LNG stream; 1 improvement in which: 7 Cy said natural gas stream is treated in one or more cooling steps so as to (1) ( A partly; At least a second; (©) yy (?) The aforementioned first gaseous stream is combined with at least part of the aforementioned liquid stream 7 in order to form a combined stream; That is extended to (0) vo medium pressure; yn said second gas stream is extended to said medium pressure; (1) vy said liquid stream is extended to said medium pressure; (V) YA is extended Any residual portion of said liquid stream to medium pressure; (A)/4 said combined warm stream expanded; said second gaseous stream expanded (4) YX. and said residual expanded portion of said liquid stream is directed into the distillation column yy _ mentioned where the mentioned streams are separated into the more volatile steam distillation stream vy mentioned and a relatively less volatile part that contains a large part of the mentioned heavier hydrocarbon components yy hydrocarbon ys The said more volatile steam distillation stream is cooled by the spooled stream (01) ve the aforementioned diluted essentially condensed to a degree sufficient to partially condense it and then separate to form a gas fraction, lighter components, and a return stream Sal; volatile residue containing a large portion of methane vy a (VY) YA Said reflux current is directed into the distillation column Hs Sha as a feed charge 4? overhead; and condense The aforementioned volatile residue is under pressure to condense gas The part of the gas (VY) v. At least, and thus the aforementioned condensate current is formed.‎ 4a yy 1 ?4- In a process to liquefy a natural gas stream containing methane and hydrocarbon components Ji Y, in which: v 0 The aforementioned natural gas stream is cooled under pressure so that part of it condenses; Je is the least condensed current component; And 8 (b) said condensate stream is extended to a lower pressure to form said LNG Stream 4; 7 improvement in it: (1) A said natural gas stream is treated in one or more cooling steps in order 4 to partially condense; 1 (7) The said partly condensed natural gas stream is separated so as to produce 1 vapor stream and a liquid stream; VY (3) said vapor stream is split into at least a first gas stream and a second gas stream; oy (8) The aforementioned first gaseous is cooled so that all of it condenses essentially and then returns to a medium pressure yg ¢ yo (0) The mentioned first condense and expanded gaseous stream is directed in relation to JB 1% thermal With a more volatile steam distillation stream which rises from cracking stages of yy phi column and is thus warmed, VA (7) said second gas stream is extended to said medium pressure; ‎YAY. Yv said vapor stream is partitioned into at least a first gas stream and a second gas stream; (V) 5 said first portion is expanded to said intermediate pressure and thereafter warmed; (A) 5 said second portion is expanded to said pressure said medium; (9) vy the said first expanded expanded gaseous stream and said second expanded gaseous stream (01) vv are directed into said distillation column where said streams are separated into said ++ more volatile steam distillation stream and part comparatively less volatile containing a large fraction yg ; Sad of heavier hydrocarbon constituents ys Said more volatile steam distillation stream is cooled by said essentially expanded collector stream (11)b condensed above said enough to partially condense and thereafter Separates to form a gas fraction Yv, lighter components, and a reflux stream; 5s Saal residual methane major YA Such reflux stream is directed into said distillation column as feed charge (VY) 1 top; and Part of the aforementioned volatile residual gas is cooled under pressure so that part of it condenses on the aforementioned (VY) vy condensed at least, thus forming condensate stream vy containing methane 0601806 and components of natural gas ALLY natural gas stream in a process -© 1 is heavier and in which: hydrocarbon 0 (a) the said natural gas stream is cooled under pressure so that at least part of it condenses 'and ¢ condensed FE forming stream 1 (b) Said condensate stream is limited to a lower pressure to form said 0 LNG stream; + improvement in which: 7 oe. Said natural gas stream is processed in one or more cooling steps; (V) 0 Ya (Y) 9 Said refrigerated natural gas stream is divided or subdivided into a second first gaseous stream at least, yy; 'y (©) The first mentioned gas is cooled so that it all condenses mainly and then returns to the pressure of huge yy ¢ - (8) The aforementioned first gaseous stream is cooled so that it actually condenses entirely; (0) The said liquid stream is cooled and then divided into a first part and a second part at least yo; 1 (1) The first part mentioned shall be determined to medium pressure and then warmed; (V) vy The said second part is combined with the said first gaseous stream actually condensed so that 01- a combined stream is thus formed and said combined stream is thus extended to said medium pressure; (A) 14 Said expanding stream is extended in a heat exchange relationship with a more volatile vapor distillation stream which rises from the cracking stages of a distillation column and is thus warmed; (9) YY said second gaseous stream is expanded to said medium pressure; (01) YY said first expanded gaseous stream (aad) and said second expanded gaseous stream (vy) are expanded; And the aforementioned extended heated first part into the aforementioned distillation column, where vg. Separation of the aforementioned streams into the aforementioned more volatile steam distillation stream and a relatively less volatile fraction Yo containing a large part of the hydrocarbon components JY hydrocarbon yy mentioned ¢ by (VY) Said more volatile steam distillation stream is cooled by the combined stream, ya - said diluted sufficiently to be partially condensed and then separated to form a volatile residual gas fraction va containing a large portion of said methane, lighter components and a reflux stream; (VY) 7 Said reflux stream is directed into said distillation column as top wy feed charge; and YAV. Ya part of it on ES The part of the aforementioned volatile residual gas is cooled under pressure so that (VY) vy is the least, and thus the aforementioned condensate stream is formed. The cracking tower, and where the aforementioned most volatile steam distillation stream is cooled to a degree oe sufficient to condense it in a part of the aforementioned tower located at the top of the aforementioned distillation column, preferably at - + at the same time to form the aforementioned volatile residual gas part and the rejected reflux stream - 1 m Thus said reflux stream flows to the upper cracking stage of said distillation column. Optimization according to element ¥ « where said distillation column is a lower section of 17 \ cracking and where said more volatile steam distillation stream is cooled enough zy to condense it In a part of the said tower above the said distillation column, preferably in the same y; - the time for the formation of the said volatile residual gas fraction and the denounced reflux stream; And so. The ameliorated reflux stream flows to the upper crushing stage of the ameliorated distillation column © is a lower section Saal where the distillation column is “Y optimization according to element =A 3” from the cracking tower and where the more volatile steam distillation stream is cooled The aforementioned degree of the aforementioned distillation column, preferably in ef sufficient to condense it in a part of the aforementioned tower located yp; - the same time for formation of said volatile residual gas fraction and said reflux stream ; e | Thus, the said reflux stream flows to the upper crushing stage of the said distillation column. Optimization according to the element; ; Where the said distillation column is a lower section of the 4-1 cracking tower and where the most volatile steam distillation stream is cooled, degraded at 0 degrees. YAY. ve. Sufficient to condense it in a part of the aforementioned tower located above the aforementioned distillation column, preferably in - »; - the same time for the formation of the said volatile residual gas fraction and the denounced reflux stream; Thus, said reflux stream flows to the upper cracking stage of said distillation column. » The mentioned distillation column lef to a degree sufficient to condense it in a part of the said existing tower - » It is preferable at the same time to form the aforementioned volatile residual gas part and the aforementioned reflux stream; Thus, the mentioned reflux stream flows to the upper crushing stage of the distillation column. denounced 4; wherein said more volatile steam distillation stream 1 improvement according to item 11-0 is sufficiently cooled to be condensed in a desiccant preferably at the same time to form the residual gas portion - said volatile and said reflux stream; Then the denounced feedback stream flows from + ; - decooler to the upper crushing stage of said distillation column. Optimization according to item 7; Wherein the aforementioned more volatile steam distillation stream 1-1"-1 is sufficiently cooled to be condensed in a desiccant preferably at the same time to form the gas fraction - » the said pilot and the said reflux stream; then the said reflux stream flows Badly ; From the decooler to the upper crushing stage of said distillation column. Optimization according to element ©; Whereas the more volatile steam distillation stream VY said is sufficiently cooled to be condensed in a desiccant preferably at the same time to form the gas fraction 0 A the said pilot residual and the mentioned reflux stream ' and then the denounced reflux stream (¥ oS) decooler flows to the upper crushing stage of the distillation column eg ny | The vapor distillation stream Cus ¢ improvement according to item 4-1 the aforementioned volatilities are cooled sufficiently to be condensed in a desiccant preferably at the same time Y and then the Sad flows to form the said volatile residual gas fraction and the reflux stream v ; Said backflow stream from the decooler to the upper cracking stage of the distillation column m mentioned. Optimization according to element ©; Where the stream of the most volatile steam distillation -1 #© 1 mentioned above is cooled enough to condense it in a decooler and preferably at the same time to form the gas part - 0 the aforementioned volatile residual and the aforementioned reflux stream » and then the denounced reflux stream flows v the decooler to the upper crushing stage in the aforementioned distillation column. 11609 0 ci Aa) that is under pressure to condense at least part of it, and a current is formed, yp . ; - Al-Madhkur 1 Tech Mek for Naf Net (oY), ala optimization according to VY, where the aforementioned volatile residual gas part is heated and pressurized, then 0 or 05617” is then cooled under pressure to condense at least part of it and form With that accommodating current - + . Al-Madhkur - + vy GAY ON) ede cde AY Refinement according to the separator bit Nmk -18“. Cp said methane and lighter components and components + residual pilot gas The gas fraction contains Cum; The remainder of the said pilot is gas; Where the part of gas contains 17 improvement according to the element 01-0 Cy mentioned and lighter components and methane components contain a large part of methane CAT in cq ACY improvement according to the storm PYNM-71 where the gas part contains Said volatile residue contains a significant portion of Vo or 140 170 CC m said methane and lighter components and components of said residual volatile gas The gas fraction contains Cus; and lighter components and components of methane a large part of the remaining methane dey is volatile gas; Where the gas fraction VY improvement according to the element YY Cy mentioned and lighter components and methane components contain a large portion of methane Y and methane components contain methane natural gas natural gas stream Alay device —VE \ g is heavier « which includes: hydrocarbn + VY. vy (1) 1 one or more primary heat exchange means for receiving the said natural gas stream; at least a second gaseous; (©) a second means of heat exchange connected to said splitting means to receive said first gaseous stream A and cooled sufficiently to actually condense it; q (?) a first extension means connected to said second heat exchange means to receive aly, The aforementioned first actually condensed gaseous stream and its extension to a medium pressure. Distillation to receive a steam distillation stream Sl 4 highly volatilized from the crushing stages of said column and cooled sufficiently to condense it; (V)” said distillation column which shall also be connected to said third heat exchange device yA and said second expansion device to receive said first heated gaseous stream 1 said expanded and second expanded stream Saal) so that said distillation column © . intended to separate the said streams into the said more volatile steam distillation streams and a proportionally less volatile x fraction containing a large portion of the said JB vy hydrocarbine components; for (A) a separator by said third heat exchange method for receiving the vg stream of the cooled distillation Ch AS partially pelletized and separating it into a volatile residual gas fraction Yo containing a large portion of said mechanization, lighter components and a reflux stream; 1 Ye where the aforementioned separation means is also connected to the aforementioned distillation column vy to direct the aforementioned reflux stream into the aforementioned distillation column as a feed charge vy top; ya a fourth heat exchange means connected to the aforementioned separation means to receive part (9) Yq said pilot residual gas; So that the mentioned fourth heat exchange method is prepared - ©. At least part of it cai to cool the said volatile residual gas part under pressure ry, thus forming a condensate stream; © a third expansion means connected to the said fourth heat exchange means (01) er the said condensing stream and extending it to a lower pressure To form the said LNG stream JY vg; and vo a control means prepared to regulate and adjust the quantities and temperatures (VY) a of the said feed currents to the said distillation column to maintain the top temperature py of the said distillation column at a temperature It is then possible to recover a large part wa the heavier mentioned in the relatively less volatile hydrocarbon part of the aforementioned v4 hydrocarbon components. Comprising: J hydrocarbon J hydrocarbon 7 natural gas One or more first heat exchangers to receive the natural gas stream Aly (V) and - said and cool it under pressure sufficient to partially condense it; A first separation means connected to a means The aforementioned first heat exchange (Y) 5 to Al aig partially mentioned condensed natural gas to receive the condensed natural gas stream 4 vapor stream and liquid stream; YAV. Wm A (?) a partitioning device connected to said first separation device for receiving said vapor stream a and partitioning it into at least a first gaseous stream and a second gaseous stream; Aly (£) 1 second heat exchange connected by said fractionation to receive said first gaseous stream and cool it sufficiently to actually condense it; ay (*) a first extension means connected to said second heat exchange means to receive said yy the first actually condensed gaseous stream and extend it to medium pressure; (1) 4: A third heat exchange means connected to the denied first expansion means to receive the aforementioned first actually condensed expanded SY 1 stream, whereby the said third heat exchange means 41 is also connected to the distillation column to receive a more volatile vapor distillation stream yy high from the crushing stages of the aforementioned distillation column and cooled to a sufficient degree of condensation yA; (V) 0 A second expanding means connected to said splitting means to receive said second gaseous stream, vy, and extend it to said medium pressure; Ali (A) 71 A third extension connected to said first separation means to receive said vy liquid stream and extend it to said medium pressure; vr (9) said column of distillation which is also connected to said third heat exchange device vg, said second expansion device and said third expansion device to receive said expanded first gaseous ve stream and said second expanding stream; so that said distillation column © intended for separating said streams into the more volatile steam distillation streams mentioned _yy and a comparatively less volatile fraction containing a large portion of the said heavier hydrocarbon + - constituents; (01) ve a second separator connected to said third heat exchange method to receive the distillation stream The aforementioned partially condensed refrigerant and separated into a volatile residual gas fraction containing part aaa Larger than aforementioned mechine, lighter components, and reflux current; Where the said Jill ry means is also connected to the distillation column ys Shall to direct the said reflux stream into the said distillation column py as top feed charge; (VY) Ye a fourth heat exchange means connected to said second separation means to receive ve the portion of said volatile residual gas; So that the fourth heat exchange Al © - mentioned is prepared to cool the aforementioned volatile residual gas part under pressure to condense part of it vy at least, thus forming a condensed stream ¢ (VY) A fourth expansion medium connected to the heat exchange method the fortunate fourth to receive the aforementioned condensate stream va to be extended to a lower pressure to form the aforementioned LNG stream; And (VY) 'a control means designed to regulate and control the amounts and temperatures of the mentioned feed streams 0 to the said distillation column to maintain the upper temperature of the mentioned distillation column $Y at a temperature at which the bulk of the hydrocarbon components is recovered gy the heavier mentioned in the relatively less volatile fractions mentioned. 1-1 Apparatus for liquefaction of a natural gas stream containing methane 211806 and heavier hydrocarbon 7 components 0 comprising: (1) v one or more primary heat exchange means for receiving the natural gas stream natural; - said gas and cooling it under pressure to a degree sufficient to partially condense it; (Y) 5 a first separation means connected to the said first heat exchange means to receive the aforementioned partially condensed natural gas stream and separate it into a steam stream and a liquid stream; 7 (? ) a fractionation method connected to the aforementioned first separation method, Juin the aforementioned +-_ vapor stream, and partitioning it into a first gaseous stream and a second gaseous stream of at least 4; YAY. vv (8) A collecting means connected to the aforementioned fragmentation means and the aforementioned first separation means 1 to receive the first mentioned gaseous stream and at least part of the said liquid stream yy and thus a combined stream is formed; VY (©) a second heat exchange device connected to said collector to receive said collector current yg and cool it sufficiently to condense it; vo (1) a first extending means connected to said splitting means to receive said second current 4 and extend it to said medium pressure; (V) vy a third expansion medium connected to the aforementioned second heat exchange method to receive the current yA _ the first expanded gas actually condensed se Sal and heat it; Where the mentioned third heat exchange vg is also connected to the distillation column to receive a more volatile steam distillation stream from the cracking stages of the aforementioned distillation column and to cool it sufficiently to condense it; (A) YY a second expanding means connected to said splitting means to receive said second yy gaseous stream and extend it to said medium pressure; ~ (9) extension device A310 connected to said first separation means to receive any residual portion ev of said liquid stream and extend it to said medium pressure; (01) vo said distillation column also connected to said third heat exchange medium; said second pial yy and said third expanding medium to receive said expanded collector Jl 4 -_ said heated + and said first expanded second gaseous stream; and the expanded residual part The aforementioned A prepared to separate the aforementioned streams into a more volatile steam distillation stream aforementioned ve and a relatively volatile fraction OF containing a large part of the aforementioned JZ + hydrocarbon components; M (11) A separation method connected to the mentioned third heat exchange method to receive the distillation stream © _ the partially condensed refrigerant Js Sa and separate it into a volatile residual gas part over a large part of the aaa YA said methane and lighter components and reflux current; Where said separator is connected vy to said distillation column to direct said reflux into said Lal ve distillation column as top feed charge; vo Juin fourth heat exchange means connected to said second separator (VY) vi gas fraction remaining said pilot; Where the aforementioned fourth heat exchange method is prepared vy part of the aforementioned volatile residual gas is under pressure to condense at least part of it and anal ra “condensed stream” is formed by that condensed stream vq a fourth extension means connected to the said fourth heat exchange method to receive (VY 2) said condensate stream and its extension to a lower pressure to form said LNG stream; gy and &Y a controlling means of regulating the quantities and temperatures of said feed streams to (1£); - Said distillation column to maintain the upper temperature of said distillation column at a temperature at which the bulk of the heavier hydrocarbon components mentioned in the aforementioned relatively less volatile go fraction can be recovered. Apparatus for liquefaction — YV 1 heavier » comprising: hydrocarbon Y natural gas and one or more primary heat exchange means for receiving the natural gas stream (1) 3; - the aforementioned and cooling it under pressure sufficient to partially condense it; Jus a first separation means connected by said first heat exchange (Y) ee said partially condensed natural gas stream and separated into a vapor stream and a liquid stream; > a second heat exchange means connected to said first separation means to receive the liquid stream ( V) 7 oe Ya first partitioning means connected to said second heat exchange means to receive current (£) 9 said refrigerated liquid and partition it into at least a first and second part; first all first spreading means connected to said first partitioning means to receive (0) The aforementioned 1 is also connected to the means of feeding the first rounded expanded part to the aforementioned second heat exchange method yy; The said first expanding part is thus heated with the cooling of said liquid stream gy; yg a partitioning device connected to the first separation device to receive said vapor stream and partition it (7) yo into at least a first gaseous stream and a second gaseous stream; ay a means A third heat exchange connected to said second splitting means to receive the said first gaseous stream (V) vy and to cool it sufficiently to actually condense it; and extending it to said medium pressure; _ ©. an extension device connected to said second partitioning means to receive the second (9) 1 said gaseous stream and extending it to said medium pressure; yy a fourth extension device connected to said first partitioning means to receive the part ) (01) Yr said second expansion and its expansion to said medium pressure; xg a fourth heat exchange medium connected to said second expansion device to receive (VY) Yo the said first expanded gaseous actually condensed and heated; wherein the exchange device SL vy is connected to a distillation column to receive more steam distillation stream Lad thermic 4th said vy volatilized upward from the crushing stages of said distillation column and cooled sufficiently to condensate ya in part 4 said distillation column and said fourth expansion medium; and heat exchange medium (VY) 7 0 second said to receive said first expanded heated gaseous stream and gaseous stream py 0 py is the second expanded mentioned; And the second extended part mentioned alge the first extended muskhan »+ mentioned; Where the aforementioned distillation column (Liga) is used to separate the aforementioned streams into a more volatile steam distillation ve stream and a relatively less volatile fraction containing a large part of the mentioned heavier ve hydrocarbon components. m (VY) a second separation means connected to said fourth heat exchange means to receive the partially condensed cryogenic distillation stream © decondensed and separated into a volatile residual gas fraction containing vA .containing a large portion of said methane, lighter components and a return stream; wherein said separator v4 is also connected to said distillation column to direct said reflux stream 0 to said distillation column Jala as top feed charge; 0 (£ 1) a fifth connected heat exchange means, Ale gy of the said second chapter, to receive, gx, the aforementioned volatile residual gas portion; so that the aforementioned fifth Jalal heat exchange means, shee gv, to cool the aforementioned residual gas portion under pressure to condense part At least from it and so that ;; a condensed stream (V0) {0) is thus formed, a fifth expansion means connected to the mentioned fifth heat exchange method to receive the mentioned condensed stream gn and extend it to a lower pressure to form the normal (Sal) liquefied stream B the aforementioned liquefied natural conch; And (V1) 2 a control means designed to regulate and control the amounts and temperatures of the aforementioned 4 feed streams to the aforementioned distillation column to maintain the upper temperature of the aforementioned distillation column - at a temperature baie can recover a large part of the aforementioned heavier hydrocarbon components 0e in The relatively less volatile parts mentioned. 1 78- ALY device Natural gas stream containing methane 60806 and hydrocarbon components Jz hydrocarbon Y ¢ includes: ry. 1 natural gas One or more primary heat exchange means for receiving the natural gas stream (1) v ; - the aforementioned and cooled under pressure sufficient to partially condense it; (“”) a primary separation means connected by means of said first heat exchange to receive the said natural gas condensate stream, Lie, and separate it into a vapor stream and a liquid stream; (V) v a second heat exchange means connected to said first separating means for receiving and cooling said liquid stream A; q (£) a first partitioning means connected to said second heat exchange means of receiving said refrigerated liquid stream and partitioning it into a first part and a second part at least 111; VY (©) a first expanding means connected to said first fragmentation means to receive and extend said first yy part to medium pressure; where said first expansion means yg is also connected to said first expanded part feeding means to said second heat exchange medium yo; Thus, the aforementioned expanded first part is heated with the cooling of the aforementioned liquid stream; VY (1) a partitioning device connected to the first separation device to receive said vapor stream aa and partition it into a first gaseous stream and a second gaseous stream on the first; (V) 4 a third heat exchange device connected to said second partitioning device to receive the first gaseous stream 7 aforementioned and to cool it sufficiently to condense it (Jail (A) 0 collector connected to said third heat exchange means and said first vy part gypsum to receive said first gaseous stream actually condensed and said second part yy and consequently form a collector stream; 7 (9) a second extension means connected to said collector to receive said collector current vo and extend it to said medium pressure; aaa Ly to receive stream 55s Sha a third extending means connected to the second splitting means (01) Y1 ¢ said second gaseous and extended to said medium pressure vy a fourth heat exchange means connected to said second expanding means (VY) YA receiving stream The aforementioned expanded gaseous collector and its heating, where the exchange medium is 4 with a distillation column to receive a more steam distillation stream. said distillation connected also to said fourth heat exchange medium (VY) - said and said second heat exchange medium A AEN; said expanding medium vg to receive said said expanding heated collector stream and said second gaseous stream vo and said heated expanded part one Where the distillation column -© _ mentioned is prepared to separate the mentioned streams into a more volatile steam distillation stream denied SEY hydrocarbon Slip Se and a relatively less volatile fraction containing a large part of the aforementioned va. vq A second separation method connected to said fourth heat exchange facility to receive (VT) 2 said partially condensed cooled distillation stream and separate it into a volatile residual gas fraction containing gy a large portion of said methane and lighter components and a reflux stream; Where said gy separator is also connected to said distillation column to direct said reflux stream to gy within said distillation column as top feed charge; gg a fifth heat exchange means connected to said second separator to receive (V£)m the aforementioned remaining volatile gaseous fraction; So that the aforementioned fifth heat exchange method is prepared to cool the part of the aforementioned volatile residual gas under pressure to condense at least part of it, gy, and to form a condensate stream, ga; YAV. (V0) 4 a fourth extension means connected to said fifth heat exchange means to receive 6 said condensate stream and extend it to a lower pressure to form said LNG stream; 1E and (V1) oY is a control means designed to regulate the quantities and temperatures of the aforementioned feed streams oy to the said distillation column to maintain the upper temperature of the said distillation column of at a temperature at which the bulk of the hydrocarbon components can be recovered Heavier hydrocarbon J mentioned in the heavier volatile fractions mentioned. 1 79- An apparatus according to claim YE in which: (1) Y the said distillation column is a lower section of the cracking tower in which the said more volatile steam distillation stream y is cooled sufficiently to condense it Ls In; a section of said cracking tower above said distillation column preferably at the same time 0 to form the said residual volatile gas fraction and said reflux stream; then said reflux stream flows to the top of the cracking stage of said distillation column; and 7 (7) heat exchange medium The aforementioned fourth that is connected to the cracking tower to receive A the aforementioned volatile residual gas part, whereby the aforementioned fourth heat exchange method 4 is prepared to cool the aforementioned volatile residual gas part under pressure to condensate part of it at least 0 and to form a condensed stream <a said Saal; >71 > 1 apparatus according to claim Yo in which: (1) Y said distillation column is a lower section of the cracking tower in which + the said more volatile steam distillation stream is cooled sufficiently to condense it Partially in; a section of the said crushing tower above the said distillation column and preferably at the same time but rather 0 to form said residual volatile gas fraction and said return stream; Thereupon said reflux stream flows to the top of the crushing stage of said distillation column; and (vii) said fourth heat exchange facility which connects to the cracker tower to receive + said volatile residual gas fraction; Where the aforementioned fourth heat exchange method 4 is prepared to cool the part of the aforementioned volatile residual gas under pressure to condense at least part of it and to form the aforementioned condensing stream; -©1 1 apparatus ly of protection element YY in which: (V) Y said distillation column is a lower section of the cracking tower in which is named » -cooling of said more volatile steam distillation stream sufficiently to partially condense it in ; A section of the aforementioned cracking tower above the aforementioned distillation column, preferably at the same time, to form the aforementioned residual volatile gas fraction and the aforementioned reflux stream; Thereupon said reflux flows to the top of the crushing stage of said distillation column; And v (“”) the aforementioned fourth heat exchange method that is connected to the cracking tower to receive A part of the aforementioned volatile residual gas, where the aforementioned fourth heat exchange means gq Lea is to cool the aforementioned volatile residual gas part under pressure to condense part of it At least and in order to form the said condensate stream, FY, a device ly of protection element YY in which: (1) Y the said distillation column is a lower section of the crushing tower in which © the more volatile steam distillation stream is cooled The aforementioned to a degree sufficient to condense it Wis 4 in a section of the aforementioned cracking tower above the aforementioned distillation column and preferably at the same time to form the aforementioned residual volatile gas part and the backflow stream F with > - mentioned; Then the aforementioned reflux stream flows to the top of the crushing stage of the distillation column » - mentioned; and (Y) A said fifth heat exchange facility which is connected to the cracker tower to receive q the portion of said volatile residual gas; Where the aforementioned Adal 0 heat exchange method is prepared to cool the aforementioned volatile residual gas part under pressure to condense at least part of it yy and to form the aforementioned condensate stream; 10**- A device according to claim YA in which: (1) The said distillation column is a lower section of the cracking tower in which the most volatile steam distillation stream of condensed © is cooled sufficiently to be partially condensed in the ; section from the said cracking tower above the said distillation column and preferably at the same time 0 to form the said residual volatile gas fraction and said reflux stream; then said reflux stream will flow to the top of the cracking stage of said distillation column; and ( ) said 5th heat exchange medium Which is connected to the cracking tower to receive A the aforementioned volatile residual gas fraction, whereby the aforementioned 5th heat exchange method 4 is prepared to cool the aforementioned volatile residual gas fraction under pressure to condensate at least part of it and to form the aforementioned condensate stream; YE Device Gy For the element of protection YE wherein this device comprises: (V) Y a degelator connected to the aforementioned first dilation device to receive and heat the first expanding gaseous y stream condensed by the aforementioned act; where the degelator is connected; - also to the said distillation column to receive The aforementioned most volatile steam distillation stream is sufficiently cooled to partially condense and separate at the same time from the residual volatile gas fraction. Av. said + and said return stream 0 where said degelator is also connected y to said distillation column to feed said first heated gaseous stream said expanded as charge + auto feed and said back stream as auto top feed charge; And (Y) said fourth heat exchange means which is connected to the degelator 0 receiving said volatile residual gas fraction; Where the aforementioned fourth heat exchange method, yy, is prepared to cool the part of the volatile residual gas, sp Sha, under pressure, to condense at least 0 part of it, and to form the aforementioned condensate stream; To 0 device according to protection Yo; Cus this device includes: (1) y a degelator connected to said first dilation device to receive © the first dilated gaseous stream condensed with said action and heat it ¢ wherein the degelator 4 connected to said distillation column to receive said M steam distillation stream more volatile and cooled sufficiently to partially condense And separating it at the same time from the part 0 of the mentioned volatile residual gas 0 and the mentioned reflux stream, whereby the said de-gels remover is also connected to the said distillation column to feed the mentioned expanded heated first gaseous stream A as a mechanical feed charge and the said reflux stream as a charge automatic q top feed; f (Y) Ve said 4th heat exchange means which is connected to the de-gel remover 1 receiving said volatile residual gas fraction; Where the means of heat exchange 1 is the fourth mentioned bee to cool the part of the aforementioned volatile residual gas under pressure to condense at least 1# part of it and to form the aforementioned condensate stream; ole This device includes Cum; YT device according to claim -*1 1 a LV (1) A gel remover connected to the aforementioned first dilation method to receive the stream + the expanded collector condensed by the aforementioned action and heat it, where the gel material remover is also connected to the aforementioned distillation column to receive the aforementioned more volatile steam distillation stream and cool it sufficiently to partially condense it and separate it at the same time For said volatile residual gas fraction + and said backflow stream; said cum remover of gels is also connected y to said distillation column to feed said expanding combined stream as auto-feed charge and said +- backflow stream as mechanical top-feed charge; and a (7) said fourth heat exchange means which is in contact with the gel remover 0 receiving the said volatile residual gas fraction; Where the aforementioned yy fourth heat exchange method is prepared to cool the said volatile residual gas part under pressure to condense at least 1 part thereof and to form the said condensate stream; F = device according to claim YY ; Cum This device includes: (1) Y a degelator connected to said second dilatation device to receive the stream » - the first dilatant gaseous condensed in said act and heated ¢ as the degelator is connected; also to said distillation column to receive said more volatile steam distillation stream M | and cooled sufficiently to condense it partly and separating it at the same time from said volatile residual gas fraction + said and reflux stream LSA whereby said gel remover is also connected to said distillation column to feed said first heated gas stream said expanded as charge + auto enrich and said dia SC auto top feed; And q (7) said fifth heat-exchanging means which is connected to the degelator to receive said volatile residual gas fraction; Wherein said fifth heat exchange means yy is prepared to cool said volatile residual gas fraction churning B yy under pressure to condensate at least part of it and to form the aforementioned recombinant lal el Wy #1 ; TA is a device according to the YA claim; Where this device includes: (1) A gel remover connected to the aforementioned second expansion method to receive the stream - the expanding accumulator condensed in the aforementioned action and heat it, as the gel removal agent is also connected to the aforementioned distillation column to receive the aforementioned more volatile steam distillation stream and cool it sufficiently to partially condense it and separate it at the same time. time for said volatile residual gas fraction > and said reflux stream wherein said de-gels remover is also connected “- to said distillation column to feed said expanded heated collector JL as auto feed charge A and said reflux stream as auto top feed charge; and 9 (7) said fifth heat exchange means which is connected to the gel remover 0 receiving the said volatile residual gas fraction; Where the aforementioned fifth yy heat exchange method is prepared to cool the part of the remaining volatile gas yp SAN under pressure to condense at least yy part of it and to form the aforementioned condensate stream; >10 ly device of protection YE; Where this device includes: (1) Y a pressure device connected to said separation device to receive and compress the said + volatile residual gas portion; f (7) said fourth heat exchange means connected to said pressure medium to receive the portion of said compressed volatile residual gas; Where the means of exchange > - the fourth heat mentioned bee is to cool the part of the aforementioned compressed volatile residual gas yy under pressure to condense at least part of it and to form the aforementioned condensing stream; z mE is a device of claim Yo or 77; Whereas this device comprises: (1) 1 compression device connected to said second separation device for receiving and compressing the residual gas portion + said pilot and 1 (7) said fourth heat exchange device connected to said pressure_m to receive said compressed pilot residual gas portion Where the aforementioned fourth heat exchange method is > -Lea to cool the aforementioned compressed volatile residual gas part cad pressure to condense at least part of it and to form the aforementioned condensing current; or YA; where the apparatus comprises: (1) 0 compression device connected to said second separation device to receive the residual gas portion + said pilot and pressurize it; and ¢ (7) said fifth heat exchange device connected to said compression device 6 to receive the gas portion The aforementioned compressed volatile residual gas, where the aforementioned fifth heat exchange method 1 - the fifth heat is prepared to cool the part of the aforementioned compressed volatile residual gas y under pressure to condense at least part of it and to form the aforementioned condensing stream; 1?;- a device according to the elements Protection 74 1 © or FY where the apparatus comprises: (1) a Y pressure device attached to said cracking tower to receive and compress said 0 | residual gas portion; and 1 (7) said fourth heat exchange means connected to said pressure medium receiving said compressed volatile residual gas portion; Where Ay is the fourth heat exchange + - mentioned bee to cool the part of the aforementioned compressed volatile residual gas under pressure to condense at least part of it and to form the aforementioned condensate stream; a 1 9;- a device pursuant to Clause 7© or PY where such device includes: (1) Y A pressure device connected to the aforementioned cracking tower to receive the remaining volatile gas fraction » - mentioned and its pressure; And ¢ (7) Said fifth heat exchange device connected to said pressure device © Receiver Part of said compressed pilot residual gas; Where is the medium of exchange + - The aforementioned fifth thermocouple prepared to cool the aforementioned compressed volatile residual gas y under pressure to condense at least part of it and to form the aforementioned condensate stream; 1 0 4 ;;- A device according to the protection elements FU YO FE, where this device includes: (1) 0 A pressure device connected to the aforementioned material remover to receive the remaining volatile gas part + mentioned and pressed; And ¢ (7) Said fourth heat exchange device connected to said pressure device Receiving part of the aforementioned compressed volatile residual gas; Where is the medium of exchange + The aforementioned fourth heat, bee, to cool the aforementioned compressed volatile residual gas » Under pressure to condense at least part of it and to form the aforementioned condensate stream; 0©?;- a device according to protection element “©” or “PA” where such device includes: (1) Y A pressure device connected to said gel remover to receive the residual gas portion + the aforementioned pilot and his pressure; And ¢ (7) Said fifth heat exchange device connected to said pressure device They are the receiver part of the aforementioned compressed pilot residual gas; Where is the medium of exchange > - The aforementioned fifth thermal lee to cool the aforementioned compressed volatile residual gas » Under pressure to condense at least part of it and to form the aforementioned condensate stream; o\ :; Where this device comprises a YE device according to Clause 1 -; 1 heating device connected to said separation device for receiving and heating the residual volatile gas fraction LLYS_(1); Sly a pressure device connected to said device for receiving the gas part Residual (Y) ¢ m said pilot and its heating. Said 4th heat exchange medium connected to said pressure medium (Y) 1 Said compressed heated pilot; Adapted to cool the said heated + volatile residual gas portion under pressure to condense at least part of it and form the said unearthed current 4. - 0 : or 776 where such device comprises YO 7;- device according to the element of protection 1 heating device connected to said second separation device for receiving and heating the residual gas portion (1) 1 said pilot; said fourth heat exchange medium connected to said pressure medium (Y)., where HSA all is for receiving the compressed heated residual gas fraction 7 said fourth heat exchange medium is conditioned to cool part of the residual gas portion A of it on the least and thus the formation of the aforementioned heated condensate ci BSG under pressure 4. - 0: ; Where such device comprises YA or YY 8;- device of protection 1 oY heating device connected to said second separation device for receiving and heating the residual gas portion (1) 0 said pilot; oy pressure device connected By the said heating means for receiving the said residual gas portion (Y) ¢ the said pilot and heating it; and by pressing Al gy the mentioned fifth heat exchange means connected (( 1 Erne) for receiving the said residual gas portion heated pilot_compressed shall be a means The aforementioned fifth heat exchange is provided to cool the said residual gas portion A of the said heated volatile under pressure to condense at least part of it and thus form the said condensing stream 4. Protection 79 © 0 or 1 heating device connected to said cracking tower to receive and heat said (1) residual volatile gas portion of said Y; and 0 : said fourth heat exchange medium connected to said pressure medium (V) “ said pressurized heated pilot residual; Where the receiving Lad is part of the aforementioned 4th means of heat exchange prepared to cool the aforementioned heated remaining volatile gas part A under pressure to condense at least part of it and thus form the aforementioned condensing stream 4. yy: on lead where This includes TY or FY device according to claim mor 1 oY heating mill connected to said cracking tower to receive and heat said Ay (V) Y residual volatile gas portion; said fifth heat exchange means connected to pressure device (Y) 1 to receive said compressed heated pilot residual gas portion; at least part of it and thus the formation of the said condensate 4 stream. a : or 76 where this device includes a YO 4 device according to the protection elements 1 -© 1 heating device connected to the said gel remover to receive the volatile gas part (V) said Y and its heating; Eady a pressure device connected to said heater to receive the residual gas portion (7) ¢ said pilot and to compress it; and 0 said fourth heat exchange means connected to said pressure (©) + Receiving the aforementioned compressed heated volatile residual gas, whereby the aforementioned fourth heat exchange method is prepared to cool the heated volatile residual gas A fraction under pressure to condense at least part of it and thus form the aforementioned condensate stream 4. - 0: a device of claim 7” or 78; Where this apparatus comprises 1 m0 ot a heater connected to said gel remover to receive and heat said (V) Y volatile gas fraction; said pilot and its pressure ¢ and Jan all said fifth heat exchange medium connected to said (7) 1 means of said; Where bg all mentioned to receive the heated pilot residual gas part 7 the aforementioned fifth heat exchange method is prepared to cool the mentioned heated residual gas part 4 under pressure to condense at least part of it and thus form the aforementioned condensing stream 4. CFF ALL LLA OYA Apparatus according to Claims 76 76 15 LAT mo + where the residual good gas fraction £T or 24 CFA CTY 231 278 (YE mentioned and components of methane contains a large part of methane volatile residue gas v Cy; - lighter and components of volatile residue gas A device according to claim 46 where the residual volatile gas fraction - 4 1 The aforementioned Cy and lighter components and components of methane contains a large portion of methane - 0 volatile residue gas Where volatile residue gas fraction of claim 41 Apparatus according to claim —o0 1 Cy mentioned lighter components and methane components containing a large portion of methane 0 volatile residue gas of claim 47 Where volatile residue gas fraction of claim 47 The remaining a Olea on \ Cp mentioned and lighter components and methane components contain a large part of methane Y Mt—1 oV device a of protection element £F; Where the volatile residue gas fraction " - contains a large portion of the said methane and lighter components and Cy components 1 - device according to the element of protection £6; Gus the residual volatile gas fraction volatile residue gas Y contains a large part of the aforementioned methane and lighter components and components of Cp 1 4- Device according to the protection element ©, where the remaining volatile gas part 7 contains a large part of methane Said methane, lighter components, and components Cy 1 = device a for EV protection; Cus fraction of volatile residue gas Y contains a significant portion of said methane and lighter components And the components of Cy -7 + 1 1 device according to the element of protection EA, where the residual volatile gas part volatile residue gas y contains a large part of the said methane and lighter components and components Cp - +1 1 device to claim £9 wherein the volatile residue gas portion of the residual volatile gas contains a large portion of said methane and lighter components and Cy 1 components +- device to claim 86 Cua The residual volatile gas fraction Y contains a large portion of said methane and lighter components and Cy components 1 4- Apparatus according to claim) 0; Where the volatile residue gas fraction ¥ contains a large portion of said methane, lighter components, and Cp components 1 5- A device according to the element of protection (OF); Cua Residual volatile gas fraction Volatile residue gas Y contains a large portion of the said methane and lighter components and Cy components —1T 0 Apparatus according to protections 76 768 5 OYA YY CFF solution CTY CF) CF (Ye Y m 1 FA CFA PY or £7; wherein the volatile residue gas fraction volatile residue gas v contains a significant portion of said methane and components; lighter and Cp components and the components of Cy Olea YY 1 according to claim 56, where the remaining volatile gas fraction, volatile residue gas ¥ contains a large portion of the said methane, lighter components, Cp components 7, and Cs components = TA 1 device according to Clause 41, wherein the remaining volatile gas fraction, volatile residue gas y, contains a large portion of the said methane, lighter components, Cr Y components, and 1 Cs components. 4- A device according to Clause 7, where the part of the volatile residue gas Y contains a large part of the aforementioned methane and lighter components and components with Y and components of Cs —Ve 1 device According to the element of protection £1, where the remaining volatile gas fraction, volatile residue gas Y, contains a large portion of the said methane, lighter components, M7 components, and Cs components. ov volatile residue gas Device to claim £8; Where the residual volatile gas fraction = 1 Cy mentioned and lighter components and methane components contain a large part of methane vy . Cs and components of y volatile residue gas device according to claim 0; where the residual volatile gas fraction —VY 1 0 the said lighter components and methane components contain a significant portion of methane 7 . Cs and components of 7 volatile residue gas apparatus of claim 47; where the residual volatile gas fraction is -1/ 1 C, the aforementioned and lighter components and methane components contain a large portion of methane 7 Cs and components y volatile residue gas residual volatile JL all device according to claim 48; Where part -1; where residual volatile gas fraction —Ve 1© containing a significant portion of said methane, lighter components, vy Cs components, and y volatile residue gas components Apparatus according to claim 560; where residual volatile gas fraction —VA 1 and lighter components and components and 0 methane contains a significant portion of said methane 7 . Cs and components 7 Yiv. oA volatile residue gas of the protector) 0; where residual volatile gas fraction a device —VY 1 0 mentioned lighter components and methane components containing a significant portion of methane 7 . Cs and components of 7 volatile residue gas; Where the fraction of residual volatile gas OF a device according to the element of protection — VA 0 Cp mentioned, lighter components and methane components containing a significant fraction of methane 0 . 0 and Y components