TW426665B - Aromatics and/or heavies removal from a methane-based feed by condensation and stripping - Google Patents

Abstract

A process for removing and concentrating the higher molecular weight hydrocarbon species from a methane-based gas stream comprising the steps of: (a) condensing a minor portion of the methane-based gas stream thereby producing a two-phase stream; (b) feeding said two-phase stream into the upper section of a column; (c) removing from the upper section of said column a heavies-depleted gas stream; (d) removing from the lower section of said column a heavies-rich liquid stream; (e) contacting via indirect heat exchange the heavies-rich liquid stream with a methane-rich stripping gas stream thereby producing a warmed heavies-rich stream and a cooled methane-rich stripping gas stream; (f) feeding said cooled methane-rich stripping gas stream to the lower section of the column; and (g) contacting the two-phase stream and the cooled methane-rich stripping gas stream in said column thereby producing the heavies-depleted gas stream and the heavies-rich liquid stream. A process for removing benzene and other aromatics from a methane-based gas stream comprising the steps of: (a) condensing a minor portion of the methane-based gas stream thereby producing a two-phase stream; (b) feeding said two-phase stream into the upper section of a column; (c) removing from the upper section of said column a benzene/aromatic-depleted gas stream; (d) removing from the lower section of said column a benzene/aromatic-rich liquid stream; (e) contacting via indirect heat exchange the benzene/aromatic-rich liquid stream with a methane-rich stripping gas stream thereby producing a warmed benzene/aromatic-rich stream and a cooled methane-rich stripping gas stream; (f) feeding said cooled methane-rich stripping gas stream to the lower section of the column; and (g) contacting the two-phase stream and the cooled methane-rich stripping gas stream in said column thereby producing the benzene/aromatic-depleted gas stream and the benzene/aromatic-rich liquid stream. An apparatus for removing and concentrating the high molecular weight hydrocarbon species from a methane-based gas stream comprising: (a) a condenser; (b) a column for stripping out the lighter components of the liquid phase of a two phase liquid gas methane stream using a cooled methane rich stripping gas; (c) a heat exchanger providing for indirect heat exchange between two fluids; (d) a conduit between said condenser and the upper section of the column for flow of a two-phase stream to the column; (e) a second conduit connected to the upper section of the column for the removal of a vapor stream from the column; (f) a conduit between said column and heat exchanger for flow of a cooled gas stream from the heat exchanger; (g) a conduit between said column and said heat exchanger for flow of a liquid stream from the column; (h) a conduit connected to the heat exchanger for flow of a warmed liquid stream form the heat exchanger; and (i) a conduit connect to the heat exchanger for flow of a gas stream to the heat exchange. An apparatus for providing heat exchanger controls separation column comprising: (a) a cryogenic separation column for partially condensing a feed gas stream in an LNG recovery process; (b) means for withdrawing a liquid condensate stream from said cryogenic separation column; (c) a heat exchanger associated with said cryogenic separation column; (d) means for passing a warm dry gas stream through said heat exchanger and thereafter to said cryogenic separation column, wherein said warm dry gas stream is cooled by indirect heat exchange with said liquid condensate stream in said heat exchanger, (f) a bypass conduit having a first control valve operably located therein for bypassing said warm dry gas stream around said heat exchanger; (g) means for establishing a first signal representative of the actual temperature of said warm dry gas stream exiting said heat exchanger; (h) means for establishing a second signal representative of the actual temperature of said liquid condensate stream entering said heat exchanger; (i) means for dividing said first signal by said second signal to establish a third signal representative of the ratio of said first signal and said second signal; (j) means for establishing a fourth signal representative of a desired value for the ratio represented by said third signal; (k) means for comparing said third signal and said fourth signal and establishing a fifth signal which is responsive to the difference of said third signal and said fourth signal, wherein said fifth signal is scaled to be representative of the position of said first control valve required to maintain the actual ratio represented by said third signal substantially equal to the desired ratio represented by said fourth signal; and (m) means for manipulating said first control valve in said bypass conduit in response to said fifth signal. A method for controlling temperature in a heat exchanger equipped with a bypass conduit having a first control valve operatively connected therein, said heat exchanger being associated with a cryogenic separation column that removes a benzene contaminant from a feed stream in and LNG recovery process, said method comprising: withdrawing a liquid condensate stream at a cryogenic temperature from said cryogenic separation column; passing said liquid condensate stream through said heat exchanger; passing a warm dry gas stream through said heat exchanger and thereafter introducing said warm dry gas stream into said cryogenic separation column, wherein said warm dry gas stream is cooled by indirect heat exchange with said liquid condensate stream in said heat exchanger, establishing a first signal representative of the actual temperature of said warm dry gas stream exiting said heat exchanger; establishing a second signal representative of the actual temperature of said liquid condensate stream entering said heat exchanger; dividing said first signal by said second signal to establish a third signal representative of the ratio of said first signal and said second signal; establishing a fourth signal representative of a desired value for said third signal; comparing said third signal and said fourth signal and establishing a fifth signal which is responsive to the difference between said third signal and said fourth signal, wherein said fifth signal is scaled to be representative of the position of said first control valve required to maintain the actual ratio represented by said third signal substantially equal to the desired ratio represented by said fourth signal; and manipulating said first control valve in said bypass conduit in response to said fifth signal.

Description

426665 Printed by the Central Standards Bureau of the Ministry of Economic Affairs and Consumer Cooperatives A7 B7 V. Description of the Invention (1) — The present invention discloses the removal of stupid gas from a methane-based gas stream through a single concentration or stripping process. Other aromatic systems And / or methods of heavier hydrocarbon components and combined devices. BACKGROUND OF THE INVENTION The freezing and liquefaction of general gaseous materials is used for the purpose of component separation, purification, storage 'and to transport the component in a more economical and convenient form. Most of these liquefaction systems usually have many operations, regardless of the gas contained Why, and because of the code, have many of the same questions. One of the problems commonly encountered in liquefaction processes (especially when containing aromatics) is the precipitation and subsequent solidification of these species in the process equipment, resulting in reduced process efficiency and credibility. Another general problem is the removal of a small amount of a relatively cheaper ' higher molecular weight chemical from the gas stream before the major part of the gas stream is liquefied. According to this, the present invention will make special reference to the description of natural gas processing, but can be used to process gas in other systems that need to overcome similar problems. The ordinary operation of natural gas processing in the technology is to freeze the gas and separate the molecular weight of natural gas from methane Hydrocarbons, thus producing better than methane t-line gas; and C2 + streams for other purposes. Usually, the stream will be separated into separate component streams, for example, C2, c3, C4 & C5 +. Freezing natural gas to liquefy it for general transportation and storage. The main reason for liquefied natural gas is that liquefaction leads to a reduction in volume to about 1/600, which makes it possible to transport this liquefied gas in a more economical and operationally designed container. For example, when gas flooding is transported from a supply source to a long-distance market, the pipeline is expected to operate with a certain and high load factor in quality. Usually, the transportation capacity or capacity will be required for operation, but -4 (please read the precautions on the back before filling this page). The paper size of the paper is applicable to the Chinese National Standard (cns). A7 printed by the Bureau's Consumer Cooperatives ------------- B7 V. Description of Invention (2)-At other times, the transportation capacity of the pipeline may be required. In order to clear the demand beyond the supply peak, when the supply exceeds the demand, excess gas needs to be stored in a transportable way, so that the peak of future demand can be consistent with the stored material. This is done-the actual device is to convert the gas into a storable liquefied state 'and then vaporize the liquid as required. When the source is far from the market and the pipeline is not used or unusable, it is possible to transport it from the supply source to the market, so it is more important to know the liquefaction of natural gas. This is particularly necessary when it is necessary to ship by sea. Shipping in a gaseous state is often impractical. • Since pressurization is required to significantly reduce the specific volume of gas, more expensive storage containers are required. In order to store and transport natural gas in a liquid state, the natural gas is preferably cooled to -24 F to -260 T, at which time it contains a vapor pressure of near atmospheric pressure. Natural gas liquefaction Most systems exist in the pre-scientific technology. The gas system sequentially passes the gas through many cooling stages under high pressure. At this time, the gas is cooled to a lower temperature until the liquefaction temperature is reached. Cooling is usually accomplished by heat exchange with one or more coolants, such as propane, propylene, ethane, ethylene, and methane, or a combination of one or more of the foregoing. In the art, coolants are often arranged in a stepwise manner, and each coolant is used in a closed cooling cycle. Further cooling of the liquid may occur by expanding the liquefied natural gas to atmospheric pressure in one or more expansion stages. In each stage, the liquefied gas is flashed to a lower pressure, so a two-phase gas-liquid mixture is produced at significantly lower temperatures. The liquid is recovered and can be flashed again. In this way, the liquefied gas is further cooled to near-atmospheric pressure, subject to the storage or transport pressure of the liquefied gas storage. Expansion to near atmospheric pressure flashes an additional volume of liquefied gas. Flash steaming in the expansion stage-5- This paper size is applicable to the Chinese National Standard (CNS) M specification (2f〇X297mm) (Please read the precautions on the back before filling this page). Installation. Nail line 426665, 4 A7 __.______ B7_ V. Description of the invention (3) The gas is generally collected by the JL cycle for liquefaction, or used as fuel gas for power generation. As mentioned before, the main operation problem of natural gas liquefaction is to remove the residual amount of benzene and other aromatic compounds from the natural gas stream immediately before the main part of the gas stream is liquefied, and this component precipitates and solidifies, resulting in pipelines and main processes. Equipment and congestion. As an example, such a blockage can significantly reduce the heat transfer efficiency and output of the heat exchanger ' especially the plate-fin heat exchanger β for technical and economic reasons ' does not require complete removal of impurities such as benzene. However, its viscosity needs to be reduced. Removal of pollution from nature * can be achieved by the same type of cooling used in the liquefaction process, where the pollution is condensed according to its individual condensation temperature. Except for the fact that the gas needs to be cooled to a lower temperature for liquefaction, the basic cooling technology is the same as for liquefaction and separation, except for the separation of benzene pollution. According to this, for the residual benzene, it is only necessary to cool the natural gas to the temperature of the condensed part-gas. This can be formed in a freeze separation tower contained at an appropriate point in the LNG recovery process to separate the condensed benzene from the main gas stream. Printed by the Shellfish Consumer Cooperative of the Central Standards Bureau of the Ministry of Economic Affairs. In the effective operation of the attention of the frozen separation tower, it is necessary to use the condensed liquid at the freezing temperature to be drawn from the tower for the warm and dry gas flow entering the cold elephant separation tower Heat exchange. However, the problem with this heat exchange process is caused by the excessive temperature difference between the two flows supplied to the heat exchanger. Because the actual temperature difference may exceed 100 times, the thermal shock of the heat exchanger may be damaged or the service life of the heat exchanger device composed of general materials will be shortened. The heat exchanger control. Another problem in dealing with the methane-rich air flow is the lack of the main part of the paper. -6-This paper χ 赖 " Lai Zhongguan Household Materials (CNS) (210x297 male thin) ~~ 426665 A7 -------------- __—__ B7 V. Description of the Invention (4)-Cost effective equipment for recovering higher molecular weight hydrocarbons from gaseous gas stream before liquefied gas stream, or residual gas stream is returned to pipeline or other processing steps. Recovered higher molecular weight hydrocarbons typically have a higher valence of the components remaining in this gas stream on a per unit mass basis. Summary of the month-the purpose of the present invention is to remove residual benzene and aromatics from a gas stream that is mainly liquefied by methane. Another object of the present invention is to remove higher molecular weight hydrocarbons from a methane-based gas stream. "Yet another object of the present invention is to remove most of the liquefied methane-based South molecular weight hydrocarbons. Yet another object of the present invention is to remove benzene, other aromatic and / or higher molecular weight hydrocarbons from a gas stream using methane as the king I in a manner of effective energy. Yet another object of the present invention is a method for removing benzene, other aromatic and / or higher molecular weight hydrocarbons that is compatible or integrated with technologies that are consistently used in gas plants. Printed by a cooperative and yet another object of the present invention is a relatively simple, small, and cost effective method and apparatus for removing benzene, other aromatics, and 7 or higher molecular weight hydrocarbons from a methane-based gas stream. ; Another object of the present invention is to remove benzene from methane-dominated oxygen streams compatible with or compatible with the use of t technology in a plant producing liquefied natural gas, other aromatic and / or Method for high molecular weight hydrocarbons. Yet another object of the present invention is to provide a heat exchanger control that overcomes the above and other problems associated with handling cryogenic fluids. This paper was transferred from Shicaiguanjia (CNS) A4 · (2 [Qx297 male thin) Printed by the Central Consumers' Bureau of the Ministry of Economic Affairs and Consumer Cooperatives 426665 4 A7 B7 5. Invention Description (5) Another object of the present invention is Provide improved control methods to reduce the initial equipment temperature requirements of heat exchange devices, and cost. A more specific purpose is to control the temperature of the heat exchanger so that the cooling of the multi-temperature hot fluid flow to the low-temperature fluid flow will not cause thermal shock to the heat exchanger device. Yet another object of the present invention is to control a heat exchanger to assist the start-up of a refrigeration separation tower. In a specific example of the present invention, benzene and / or other aromatics are removed from a methane-based gas stream by a process including the following :-( 1) Before the main part of the gas stream is liquefied, a minor Part of the gas stream mainly dominated by oxane condenses immediately, so a two-phase flow is generated. (2) The two-phase flow is fed into the upper section of the stripping column, and (3) less removal from the upper section of the stripping column. Aromatic gas stream, (4) remove the aromatic-rich liquid stream from the lower section of the stripper, (5) through indirect heat exchange, strip the aromatic-rich liquid stream and the pinane-rich stripper The gas stream is in contact, thus producing a warm aromatic-containing stream and a cooled stream of enriched gaseous stripping gas, and (6) feeding this cooled stream of methane-rich stripped gas to a stripping tower In the lower paragraph. And optionally (7) the less aromatic gas stream is fed into a liquefaction step, in which a major part of the gas stream is liquefied, thereby producing liquefied natural gas. In another specific example of the present invention, the higher molecular weight hydrocarbons in the methane-based gas stream are removed and concentrated by the following methods: (1) the methane-based gas stream is a minor part Condensing to produce a two-phase flow, (2) feeding the two-phase flow into the upper section of the stripper, (Γ) removing a gas stream of less carbon from the upper section of the stripper, and (4) from the Polycarbonate-rich liquid stream is removed in the lower part of the stripper. (5) Polycarbonate-rich liquid is made through indirect heat exchange. -8- This paper size applies to China National Standard (CNS) A4 (210X297). (Mm) (Please read the notes on the reverse side before filling out this page). Order 'Printed by the Consumers' Cooperative of the Central Standards Bureau of the Ministry of Economic Affairs 4 2 6 6 6 5 ^ A7 B7 V. Description of Invention (6) " The stream is in contact with the methane-rich stripping gas stream, thereby producing a warm polycarbon-rich stream, and a cooled methane-rich stripping gas stream, and (6) the methane-rich stripping gas The stream is fed into the lower section of the stripper. In yet another object of the present invention, the present invention is a device including the following: (1) a condensate in which a gaseous stream consisting mainly of oxane in a minor portion is condensed, thereby generating a two-phase flow condenser, (2) a Feeding the two-phase flow, and the steam and liquid stream produced by the tower, the stripping tower (3) contains the indirect heat exchange between the gas stream and the liquid stream, thus generating the heat exchange between the cooling gas stream and the warm liquid stream A prepared heat exchanger, (4) a duct for the two-phase gas flow between the condenser and the upper section of the stripper, and (5) a duct connected to the upper section of the stripper to remove the vapor stream. (6) a duct for the liquid flow between the stripper and the heat exchanger, (7) a duct for the cooled gas flow between the heat exchanger and the stripper (8) a pipe connected to the heat exchanger for the warm liquid flow of the heat exchanger, and (9) a pipe connected to the heat exchanger for the gas flow to the heat exchanger catheter. In still another specific example of the present invention, the foregoing and other objects and advantages are achieved by installing a bypass pipe of warm fluid in a controlled heat exchanger for processing low-temperature fluid and warm fluid, wherein the bypass pipe The control valve in the middle is operated in response to the temperature ratio of the heat exchange fluid. According to another specific example of the present invention, the automatic start-up control includes a high selector for temporarily selecting the temperature to operate the flow of the warm fluid assisting the start-up of the tower, and the operation of switching to the flow of warm gas to the temperature required for the reaction. {Please read the precautions on the back before filling this page). -9- This paper size is applicable to Chinese National Standard (CNS) A4 specification (2iOX297 mm) Chinese Patent Specification for Revised Patent Application No. 106889 (12,87) Month) Λ: B 'correction belongs to ^ Supplementary Fans] 2. f ί Printing by the Central Bureau of Standards of the Ministry of Economic Affairs f Printed by a person V. Brief description of the invention-Figure 1 illustrates the gas flow mainly based on pinane Simplified flow chart of the method for producing frozen LNG in the method and apparatus of the present invention for removing benzene, other aromatic and / or higher molecular weight hydrocarbons. FIG. 2 is a simplified flowchart illustrating the method and apparatus illustrated in FIG. 1 in detail. Figure 3 is a diagrammatic illustration of the cold-kill separation tower of the present invention and an integrated control system for maintaining a heat exchange fluid. Figure 4 is a schematic illustration of the temporary temperature used to automatically start the freezing separation tower as shown in Figure 3. 0 The main symbols of the drawing are significant. 2 High-stage propane cooler 10 Separation tank 22 Cooler 24, 26 Indirect heat exchange equipment 28 Low-order propane cooler / concentrator 42 High-grade ethylene cooler 54 Low-grade ethylene cooler 60 String 62 62 Heat exchanger 66 Indirect heat exchange equipment 74 Main pinane economizer 78 Expansion valve 87 Second methane economizer -10 -This paper size applies Chinese National Standard (CNS) ΛΊ size {210X 297 Gongcheng) (Please read the precautions on the back before filling this page)

4 26665, Patent Order No. 86106889, Request for Amendment to the Chinese Manual (December 87) Λ 7 Amendment 87 is called "Fifth, the description of the invention (7a Printed by the Central Standards Bureau of the Ministry of Economic Affairs, Shellfish Consumer Cooperatives, 91 expansion valve 93 expansion Valve 100 Natural gas feed 102 Cooled natural gas feed 103 Remove C3-rich liquid phase conduit 104 Vapor phase conduit 108 Become the gas stream of feed (methane-rich stripping gas) in heat exchanger 62 109 Cooled rich Duct with methane stripping gas 110 Cooled chimney-rich tube-112 Methane-rich stripping gas 114, 117 Duct-rich liquid stream 116 Duct-rich gas stream 118 Conduit connected to column 60 two-phase flow 120 Conduit of methane-rich vapor flow 122 Liquefied flow 124 Liquefied flow conduit 130 Liquid phase conduit 132 Cooling liquid conduit 134 Cooling liquid phase conduit 142 at about atmospheric pressure The LNG product tube 543 Control valve 700 Proportion calculator-702 Temperature transducer 704 Temperature transducer 10a (Please read the precautions on the back before filling this page)

This paper size is applicable to China National Standards (CNS) A4 (210X 297) and printed by the Consumer Cooperatives of the Central Standards Bureau of the Ministry of Economic Affairs 4 266 6 5 Zhengbei No. 86ΐ〇6889 箄 Application for Profit ΛΊ This year aa : Correction page of the Chinese manual (December 87) ^ Supplement i 5. Description of the invention (7b) 706 Temperature signal indication of the liquid inflow conduit 109 · 708 The actual temperature output signal of the liquid inflow conduit 117 indicates 710 signals 706 and 708 The output signal represents the set point of the desired temperature ratio of the 712 proportional controller 714 liquid inflow conduits 109 and 114. The output signal represents the difference between the 716 signals 710 and 714. The output signal represents the 718 branch conduit. The present invention is applied to (1) the removal of benzene and / or its aromatics from a methane-based gas stream requiring most condensation, and (2) a methane-based gas requiring most condensation Streams remove more expensive, higher molecular weight hydrocarbons. This technique is also used for such general recovery from pristane-based flows (eg, natural gas liquid removal from natural gas). Benzene and other aromatics have the only problem due to their relatively high melting temperatures. TC。 As an example, the melting point of benzene containing 6 carbon atoms is 5.5 ° C, and the boiling point is 80. TC. Hexane (also containing 6 carbon atoms) has a melting point of -95 ° C and a boiling point of 68.95 ° C. Therefore, when compared with other hydrocarbons of similar molecular weight, the blocking and / or blocking of process equipment and conduits by benzene and other aromatic compounds is more problematic. The aromatic compound used here is a compound characterized by the presence of at least one benzene ring. As for the users here, high-molecular-weight hydrocarbons are hydrocarbons with a molecular weight greater than that of ethane, and the term can be used interchangeably with multi-carbon hydrocarbons. -10b- This paper size applies to Chinese National Standard (CNS) Λ4 specification (210X 297 mm) (Please read the precautions on the back before filling this page)

426665 Printed by the Consumer Cooperatives of the Central Bureau of Standards of the Ministry of Economic Affairs A7 B7 V. Description of the Invention (8) _ For simplicity and clarity, the following restrictions will be limited to the cooling and cooling of natural gas streams, the process of the present invention for manufacturing liquefied natural gas, Device. More specifically, 'the following description will be directed to the removal of benzene and / or other aromatics and / or high molecular weight hydrocarbons (polycarbons) in a liquefaction process using a cascade refrigeration cycle. However, the applicability of the invention and its apparatus described herein is not limited to the use of a cascade refrigeration cycle or a liquefaction system that does not process natural gas streams. This process and its equipment are used in any circulation system, including methane-based gas streams that can block or close process equipment, especially benzene and / or polycarbons used to condense the flow of heat exchangers Aromatic, or (b) for some reason, higher molecular weight hydrocarbons need to be removed and recovered from a methane-based gas stream. Liquefaction of natural gas streams Leng Kang Gongwei has various forms; the most effective and useful is step operation, and this type is combined with expansion cooling. Moreover, because the liquefied natural gas (LNG) manufacturing method includes the separation of hydrocarbons whose fraction is greater than pinane as its first part, the convergence of LNG refrigeration manufacturing workers can effectively describe similar removal of C2 + hydrocarbons from natural gas streams. Factory. In a preferred embodiment using a cascade refrigerant system, the present invention relates to the use of a multi-stage propane cycle, a multi-stage ethane or acetam cycle, and & a closed oxane cycle, followed by a single or multi-stage expansion account Circulation 'to further cool and reduce the pressure to near atmospheric pressure, or (b) use a portion of the feed gas as a source of methane, which contains multiple cycles of 3 多, to further cool down and reduce the pressure to near atmospheric opening Continuous cooling of the gas stream at one of the end-methane cycles' continuously cools the natural gas stream at, for example, a high pressure of about 650 psia. Cold-11 _ This paper size applies to Chinese National Standards (CNS) (210X297 ^ centi) · f 阅读 Please read the notes on the back before filling out this page} 装-线 4? Β6 6 5 Staff Consumption of Central Bureau of Standards, Ministry of Economic Affairs Printed by the cooperative A7 B7 V. Description of the invention (9) However, in the sequence of the cycle, 'the refrigerant with a higher boiling point is used first, then the refrigerant with a medium boiling point is used', and finally the refrigerant with the lowest boiling point is used. A pretreatment device is a device that removes unwanted components such as acid gas, mercaptan, mercury, and moisture from a natural gas feed stream that is delivered to the device. The composition of this gas stream can vary significantly. As used herein, a natural gas stream is any stream that primarily includes methane produced from a major portion of a natural feed stream that includes, for example, at least 85 vol% methane, with the remainder being ethane, higher hydrocarbons, nitrogen , Carbon dioxide and minor amounts of _, such as mercury, hydrogen sulfide, mercaptans. The pre-treatment step may be a separation step flowing above the Rochor cycle or below one of the early stages of cooling in the initial cycle. The following is an unlisted part of the equipment available for those skilled in the art to use immediately. Acid gas and less mercaptans are removed together by using an aqueous amine-containing solution. This processing step is generally carried out above the cooling stage used in the initial cycle. The main part of the water system is cooled after the liquid flows under the gas compression and the initial cooling cycle and under the first cooling stage of the initial cooling cycle, and the β-mercury system is removed by two-phase gas-liquid separation. The absorbent bed removes β residual water and acid gas at one time through the use of an appropriately selected absorbent bed, such as a renewable molecular sieve. The process of using an absorbent bed is generally located in the first cooling stage of the initial cooling cycle. Downstream flow_ The natural gas stream obtained is usually transported to the liquefaction process under high pressure, or compressed to high pressure. The history of this high pressure: the force is greater than 500 psia, preferably about 500 to about 900 psia, more preferably about 550 to about 675 psial Even more preferably about 575 to about 650 psia, and most preferably about 600 psia. The flow pressure is generally close to or slightly higher than normal temperature. Typical temperature ranges are from 60 ° F to 120T. -12- The size of this paper is applicable to China National Standard (CNS) A4 (210 × 297 mm) (Please read the precautions on the back before filling out this page)-Pack. Order 4126665 Printed by A7, Consumers Cooperative of Central Standard Bureau, Ministry of Economic Affairs B7 V. Description of the invention (10) As mentioned earlier, the natural gas flow at this point is still in many multi-stages (such as three stages), or with many refrigerants, preferably three are connected by heat exchange cooling. For a given cycle The overall cooling efficiency can be improved when the number of stages is increased, but this increase in efficiency is achieved by a relative increase in net capital cost and process complexity. The feed gas is preferably first sealed by using a relatively high boiling point refrigerant The effective number of freezing stages in the freezing cycle is usually two stages, preferably two to four stages, and most preferably three stages. The main part of this refrigerant preferably includes Cd'propylene or its mixture, and more It is preferably propane, and it is preferable that the refrigerant basically contains propane. Subsequently, the feed gas of the process flows through the effective number of stages in the second closed refrigeration ring, generally two stages, preferably two to four stages, and more it is good The second or third stage is heat exchanged with a refrigerant having a lower boiling point. The refrigerant preferably comprises a major portion of ethane, ethylene or a mixture thereof, more preferably ethylene, and most preferably the refrigerant contains substantially ethylene. Each of the cooling stages listed above for each refrigerant includes a separate cooling zone. Throughout the natural milk feed stream will contain (: 2+ component amounts in one or more of the cooling stages that result in the formation of a liquid rich in C2 +. This liquid system is removed by gas-liquid separation equipment, preferably one or more gas-liquid separators. Generally, the continuous cooling of natural gas in each section is controlled, so as much as possible to remove C2 and higher from the gas Molecular weight hydrocarbons to produce a first gas stream mainly methane 'and a second liquid stream containing significant amounts of ethane and multi-carbon components. An effective amount of gas / liquid separation equipment is located at the planned location for flow under the cooling zone In order to remove the liquid stream rich in C2 + components, the correct position of the gas / separator will depend on the number of operating parameters considered by those skilled in the operation of LNG plants and gas plant operators, such as the C2 + composition of the natural milk feed stream. End product Required 13- Sheets U Applicable to China National Standards (CNS) A "(2 Euros 297 Gongchu (Please read the precautions on the back before filling this page)

Printed by the Shellfish Consumer Cooperative of the Central Bureau of Standards, the Ministry of Economic Affairs 2 6 6 6 5 A7 ___________ B7 V. Description of the Invention (11) ‘: ~~: BTU content in other applications, C2 + component 値 for other applications, and other factors. Hydrocarbons or streams can be demethanated via a single stage flash or fractionation column. In the former case, the gas stream containing methane can be returned directly to the liquefaction process under pressure. C 2 + hydrocarbon streams or streams or deoxane-derived c 2 + hydrocarbon streams can be used as fuel or can be further processed, such as fractionation in one or more fractionation zones, to make specific chemical rich ( For example, C2, C3, q and c5 +) flow separately. In the final stage of the second cooling cycle, the main part of the gas stream, which is mainly methane, is condensed (i.e. liquefied), preferably all. In one of the preferred specific examples to be discussed in detail in the following paragraphs, the method and apparatus of the present invention for removing benzene, other aromatic and / or polycarbons can be used at this position in the process. The process pressure at this position is only slightly lower than the pressure of the feed gas in the first stage of the first cycle. The liquefied natural milk flow is further cooled in the third step or cycle through one of two specific examples. In a specific example, the liquefied natural gas stream is indirectly heat-exchanged with a second closed and closed refrigeration cycle, where the condensed gas stream is passed through the number of effective stages, generally 2; preferably 2 to 4; and It is preferably 3 low-temperature cooling, and the cooling is cooled by a third refrigerant having a lower boiling point than the refrigerant used in the second cycle. This refrigerant preferably comprises a major portion of the torrefaction 'and most preferably is mainly methane. In a second and preferred embodiment using an open methane refrigeration cycle, the liquefied natural gas stream is cooled in a main methane economizer 'in a manner described below by contact with flash gas at low temperature. In the fourth cycle or step, the liquefied gas is cooled by the expansion and separation of the flash gas of the self-cooling liquid. In the method to be described, the nitrogen and condensed products removed from the system are part of this step or separated. -14- This paper applies the Ningguo National Standard (〇 阳) 6 4 specifications (210 parent 297 mm) {Please read the precautions on the back before filling out this page}. Dare to order. -IJ. · Printed by Zhengong Consumer Cooperative, Central Procurement Bureau, Ministry of Economic Affairs 4266 6 5 A7 ____ __B7____ 5. Description of the invention (12 ) " The main factors that distinguish between a closed cycle and an open cycle are the initial temperature at which the liquefied stream flashes to near atmospheric pressure, the relative amount of flash steam generated during the flash, and the nature of the flash steam. Therefore, the main part of the flash steam is recycled to the methane compressor in the open cycle system, and the flash steam in the closed cycle system is generally used as fuel. In the fourth cycle or step of the open or closed cycle pinane system, the liquefied product is expanded at least once, preferably two to four times, and more preferably three times (where Joule-Thomson is used for each expansion) (Hydraulic expander) cooling 'followed by separation of gas and liquid products with a separator. When using a hydraulic separator and proper operation, the greater the efficiency of power recovery, the greater the temperature at which the flow is reduced 'and the less steam generated in the flashing step is often more cost effective, even with the capital generated by the expander And operating costs. In a specific example of use in an open circuit system, the additional cooling of the high-pressure liquefied product prior to flashing may be through one or more hydraulic expanders. A part of this flow is flashed first, and then it is carried out by using a heat exchange device between the flash flow, and the high pressure liquefied stream is cooled before flashing. The flashed product is recycled back to the appropriate location for the open methane cycle (based on temperature and pressure considerations). The liquid products prepared to enter the fourth cycle are at about 600 pSia. The preferred flash pressures for the three-stage flash process are about 19061 and 14.7 psia. In the open loop and loop system, the steam to be flashed or surplus in the nitrogen separation step and the flash to be expanded in the expansion flash step are used as the coolant in the third step or the ring. Closed cycle · In the system, the steam in the flash stage can also be used as a coolant or fuel in the cycle. In an open or closed circulation system f, flashing of the liquefied stream to near atmospheric pressure will produce a temperature of _24 ° C. _ -15. This paper will be applicable to CNS Standard (4) (21 ()) < 297: --- (please «read the precautions on the reverse side before filling out this page)-Binding and ordering ___---- 426665 Printed by the Consumers' Cooperative of the Central Standards Bureau of the Ministry of Economic Affairs A7 B7 V. Invention Description (13) to -260 ° F LNG product. When a small amount of nitrogen is present in the feed stream, in order to maintain the BTU content of the liquefied product within acceptable limits, the nitrogen must be concentrated and removed at certain locations in the process. Various techniques for this purpose are known to those skilled in the art. The following are examples. When using an open pinane cycle and the nitrogen concentration in the feed is low (generally less than about 1.0 vol%) 'Removal of nitrogen is generally by removing the small side stream at the high pressure input or output cylinder of the methane compressor Reached. For a closed cycle with a nitrogen concentration of 1 to 5 vol% in the feed gas, the liquefied stream is usually flashed to near atmospheric pressure in a single stage in a single stage, and is generally passed through a flash drum i with nitrogen. Engine gas turbine fuel gas. LNG products are now sent to the wrong store at near atmospheric pressure. When the nitrogen concentration in the incoming feed gas is about ^ to about 15 vol%, and an open cycle is used, the flashing step may be performed before the fourth cooling step by making the liquefied gas flow of the third cooling cycle. The flash vapor will contain a small concentration of nitrogen and can then be used as a fuel gas. A typical flash pressure for removing nitrogen at these concentrations is about 400 psia. When the nitrogen concentration in the feed stream is greater than about 1.5 vol% and an open or closed cycle is used, the 'flash evaporation step' cannot provide sufficient nitrogen removal. In this case, a nitrogen rejection column will be used, which produces a nitrogen-rich vapor stream and a liquid-to-body stream. In a preferred embodiment using a nitrogen removal column, the high pressure liquefied methane flowing to a methane economizer is divided into first and second parts. The first part is flashed to about 400 psia and the two-phase mixture is fed as a feed stream to a nitrogen removal column. The second part of the high-pressure liquefied methane stream is further cooled by passing through a methane economizer to be described later, and then flash-evaporated to 400 psia, and the obtained two-phase mixture or its liquid portion is fed into work -16- ----- ^ _ | P ---- Undress! (Please read the precautions on the back before filling out this page}-, 1T. I ~ '' Printed by the Central Bureau of Standards, Ministry of Economic Affairs and Consumer Cooperation Du printed 426665

A A7 _______B7_ V. Description of the invention (14) The upper section of the tower can be flowed back like a reflux flow. The nitrogen-rich vapor stream generated at the top of the nitrogen rejection column is generally used as fuel. The liquid stream generated at the bottom of the tower is fed into the first stage of methane expansion. The natural gas liquefaction standard in the preliminary process of the Zoran gas liquefaction system uses one or more kinds of cold; the east agent 'f the heat energy transmission of the natural gas stream. Into the refrigerant and finally transfer this thermal energy to the environment. Basically, a refrigeration system that functions as a heat pump by removing heat from the natural gas flow as a flow is planned to cool to a lower temperature. The liquefaction process uses many types of cooling, including (but not limited to) (a) indirect heat exchange, (b) evaporation, and (c) expansion or decompression. As used herein, indirect heat exchange refers to a process in which the refrigerant or coolant cools the substrate to be cooled, and there is no actual physical contact between the refrigerant and the substrate to be cooled. Specific examples include heat exchange in tube and shell heat exchangers, shabu-type heat exchangers and brass aluminum plate fin heat exchangers. The physical state of the refrigerant and the substance to be cooled can be changed according to the system and the type of heat exchanger selected. Therefore, in the process of the present invention, generally, a shell and tube heat exchanger is used. When the refrigerant is liquid and the substance to be cooled is liquid or gaseous, but when the refrigerant is gas and the substance to be cooled is liquid In general, plate-fin heat exchangers are generally used. Finally, when the substance to be cooled is liquid or gas, and is cold; when the agent is exchanged from the liquid phase to the gaseous state in heat exchange, a drum heat exchanger is generally used. -Evaporative cooling means that the system is maintained at a constant pressure by evaporating or-part of the substance <evaporative cooling substance. Therefore, during the evaporation process, the part of the evaporation substance is _ -17- The paper size is suitable for household materials (cns ----------- installation ------ order ------ line 丨* '(Please read the precautions on the back before writing this page) 426665 A7 B7 V. Description of the invention (15) Self-maintaining liquid part absorbs heat, and therefore cools the liquid part β Finally swelling or decompressing Cooling refers to the cooling that occurs when the overall force of a gas-'liquid- or two-phase system is reduced by a pressure reducing device. In one specific example, the expansion device is a Joule-Thomson expansion valve. In another specific example, the expansion The equipment is a hydraulic or gas expander. Due to the expansion of the expander's self-expanding process, the process temperature may be lower when it is expanded. In the following discussion and appendix, the discussion or drawings can be passed through the refrigerant flow section The flow valve 'then sequentially separates the gas-liquid portion in the refrigerant cooler or condenser (' where indirect thermal breakdown also occurs_ ') describing its expansion. Although this simplified system is operational' and sometimes due to its Cost and simplicity are better, it may be more efficient to expand and separate, and then partially expanded like the separation step For example, 'combining the throttling chamber and flash drum before heat exchange between the cooler or condenser. In another practical example, the throttle or expansion valve may not be a separate item, but it may be a refrigerant cooler Or an integral part of the condenser (ie, flash evaporation occurs when the liquefied refrigerant enters the cooler). In a similar manner, multiple flow cooling of the chilled freezing section can be in a single tank (ie, cooler) or in multiple tanks Occurred. The former is generally better from the perspective of capital equipment costs. In the first cooling cycle printed by the Central Standards Bureau of the Ministry of Economic Affairs, the Consumer Cooperative, the cooling is provided by a higher boiling point gaseous refrigerant (preferably propane). The pressure of liquefaction by heat transfer between the heat exchange medium is ultimately used as the environment of the heat sink, the heat sink is usually atmospheric 'fresh water' salt water, earth or two or more of the foregoing. Cold condensate S is subjected to one or more expansions via a suitable expansion device: 'This results in a two-phase mixture with a distinctly low temperature. Among them, the main flow is divided into at least two separated flows, preferably two to four flows -18 97mm) Wood and paper scale—Chinese national standard 426665 A7 B7 Printed by the Consumers' Cooperative Office of the Central Standards Bureau of the Ministry of Economic Affairs of the People's Republic of China. 5. Description of the invention (16 and the best two flows, where each flow expands to the design pressure. Each flow is combined with .- or more selected flows to provide evaporative cooling through indirect heat transfer. One ratio is the natural gas flow to be liquefied. The number of separated refrigerant flows will be equivalent to the number of cold; Individually flowing evaporated refrigerants are returned to the appropriate section of the refrigerant compressor (for example, the two separated streams are equivalent to a section of a shrinking machine). More specifically, in the specific example, all liquefied refrigerants are expanded to a predetermined pressure, And this flow is then used to indirect heat exchange with one or more selected flows to provide evaporative cooling. The second flow is the natural gas stream to be liquefied. A part of the liquefied cold bath agent is removed from the indirect heat transfer equipment to expand to a lower pressure and a relatively low temperature expansion cooling, wherein it provides evaporative cooling through indirect heat transfer and one or more specified flows, and other flows For natural gas a to be liquefied, usually, this specific example will use two such expansion cooling / evaporative cooling steps, preferably two to four times, and most preferably three times. As in the first specific example, the refrigerant vapor in each step is returned to the appropriate input &amp;: of the stage compressor. In the preferred example of the step, the liquefied cooling body of the preferred boiling point cold bead agent (that is, the refrigerant used in the second and third cycles) may be indirectly passed by its selected higher Buddha point refrigerant flow, indirectly. Heat exchange allows these flows to cool. This cooling method is called &quot; step cooling V. In fact, "higher boiling point refrigerants function as heat sinks for low boiling point refrigerants. The thermal energy flows from the natural gas that is to be liquefied to the lower stagnation point of the cooling agent. Water, brine, atmosphere) are pumped (ie, delivered) to one or more higher-boiling refrigerants before being sent to the atmosphere. For example, in the first cycle, the refrigerant used in the second and third cycles is compressed by a multi-stage compressor to a predetermined 19- each paper Λ degree applies Chinese National Standard (CNS) A4 (2 丨 0χ297 mm) (please first Read the notes on the back and fill out this page) Install '4266 6 5 ^ A7 f —---------: ___ B7 V. Description of the invention (17) &lt; Pressure. When economically possible, compressed refrigerant vapor is first indirectly heat-exchanged and cooled with one or more coolants (such as air, water, and fresh water) that are directly coupled to the environmental radiator. This cooling may be interstage cooling between the shrinking sections and / or cooling of the compression products. The compressed stream is further cooled by indirect heat exchange with the aforementioned cooling section of one or more higher boiling point refrigerants. The second cycle refrigerant (preferably ethylene) is preferably subjected to indirect heat transfer, and it is first cooled (that is, cooled between stages and / or after compression) with one or more coolants directly coupled to the environmental receiver. Then, further cooling, And finally contacted the cooling section of the highest boiling point refrigerant used in the first and second, or the first, second, and third first cycles in sequence in order to liquefy α. The second and first circulating refrigerants are preferably ethylene, respectively. And propane. When using three refrigerant stepped closed-cycle systems, the refrigerant in the third cycle is compressed in a staged manner, preferably through indirect heat transfer to the ambient heat to be selectively cooled (ie, cooled between stages and / or after compression). , And then indirect heat exchange cooling with all or selected cooling sections in the first and second cooling cycles which preferably use Cp * and ethylene respectively. Preferably, this flow is in continuous contact with each of the colder stages of the cooling agent in the first and second cooling cycles in a continuous manner. _ Printed by the Consumer Cooperatives of the Central Bureau of Standards of the Ministry of Economic Affairs "installation-(please read the note on the back ^ § # before filling out this page) η As shown in Figure 1 of the open-cycle cascade refrigeration system, the first The first and second cycles are operated in a similar manner to the aforementioned closed cycle &lt;?. However, the open loop circulation system can easily be compared with the general closed loop; the eastern loop distinguishes β as previously discussed in the fourth loop or step pattern As mentioned, a significant part of the LNG stream that existed under high pressure was gradually cooled to the atmosphere in an expansive manner -20- This paper size applies to China National Standard (CNS) Α4 (210X297 mm) Λ 266 6 5 λ Printed by the Consumer Cooperatives of the Central Commission of the Ministry of Economic Affairs A7 B7 V. Description of the invention (18) Press' Cool to about -260T. In each step, a significant portion of the methane-rich vapor at a given pressure is produced. Each vapor stream preferably undergoes the apparent heat transfer 'in a methane economizer and is preferably returned to the input stage of the compressor stage at near normal temperature. During the flow through the methane economizer, the flash steam and the warm stream are designed to contact each other in a countercurrent manner and in order to maximize the cooling of the warm stream. The pressure selected for expansion cooling is such that the volume of gas produced in each stage plus the compressed volume of vapor in the adjacent lower stage results in effective overall operation of the multi-stage compressor. The cooling between the stages and the final compressed gas is better, and it is better to heat directly with the environment through and! § Combining one or more coolants is achieved by heat exchange. The compressed methane-rich flow is further cooled in the first and second cycles by indirect heat exchange with a refrigerant, preferably all phases of the refrigerant used in the first cycle, and more preferably the first two phases , And preferably only the first stage. The cooled methane-rich stream is then flash-vaporized in a methane economizer, cooled by indirect heat, and combined with the natural gas feed stream at the location in the liquefaction process, where the natural gas feed stream and the cooled s containing The methane wave is under similar temperature and pressure conditions, preferably before entering one of the cooling stages of acetam, and more preferably before the ethylene cooling stage. The main part of the gauge A has been liquefied (ie, the ethylene condenser). . In the most specific example of the transmission between the star and the obstacle and the circulation, the steps are to return the refrigerant gas flow to the input cylinder of its individual compressor at normal temperature or near normal temperature; Good process efficiency. This step not only improves the trimming efficiency, but also exposes the compressor components and greatly reduces the difficulty in freezing conditions. This is achieved by using the thermal state of printing, where the main part of the flow includes liquid, and before flashing, _______ -21-this paper ^^ i ^ gT ^ T7 ^ 72! _QX297 public funding) (Please read the precautions on the back first) (Fill in this page again)-Install. Printed by the Central Laboratories of the Ministry of Economic Affairs, Shellfish Consumer Cooperative, 4 266 6 5 λ Α7 ____; _; ____B7 V. Description of Invention (19) 'to flow in the same or lower flow cycle The expansion step (i.e. stage) or one or more vapor streams generated in the steps is cooled by indirect heat exchange. In closed systems, economizers are preferably used to obtain additional cooling from the flash steam in the second and third cycles. When using an open methane cycle system, the flash vapor in the fourth stage is preferably returned to one or more economizers, where (the work) is cooled by the indirect heat exchange liquefied product stream before each decompression stage. 'And (2) before these flows, or flows are combined with the main natural gas feed stream', these vapors are cooled by compressed vapor from the open methane cycle via indirect heat exchange_ β These cooling steps include the three-stage cooling previously discussed, It will be discussed in more detail in the discussion of FIG. In a specific example of using ethylene and methane in the second and third cycles, the contacting may be performed through a series of ethylene and methane economizers. In the preferred embodiment illustrated in FIG. 1 and discussed in more detail later, the process uses a economizer that is primarily ethylene, a economizer that is primarily oxane, and one or more additional methane economizers. These additional economizers refer here to a second methane economizer, a third methane economizer, etc., and each of these additional methane economizers corresponds to a flow-through flash evaporation step under separation. Removal of benzene, other aromatic and / or multi-carbon fumes. Benzene is removed from a gas stream dominated by methane. The process of the present invention for other aromatic and / or higher molecular weight hydrocarbons is extremely energy efficient and simplified. The process. 1 至 20 mol% '好 Because of the way of operation, the tower referred to here performs a steam distillation fractionation function (stripping tower. This process includes cooling the gas stream mainly methane, so that the total gas stream is 0.1 to 20 mol% 1) .5 to about 10 mol%, and more preferably about 1.75 to about 6.0 mol% condensate, thus forming a two-phase flow. The most appropriate mole percentage is based on the composition of the gas that has undergone liquefaction, and-familiar with this technique (please read the precautions on the back before filling this page) • Packing. Order-, less thread --- -22- this The paper size is applicable to the Chinese Standard (CNS) A4 specification (210X2971%) i426665 The consumer cooperation of the Central Standards Bureau of the Ministry of Economic Affairs, Du printed A7 ________B7 V. Description of the invention (20) The parameters related to other processes determined by the person. In the system, the desired two-phase flow is made by cooling the entire feed stream to the required liquid percentage. In a preferred embodiment, the gas stream is first cooled to near the liquefaction temperature, and then divided into a first flow and The second flow. The first flow is additionally cooled and partially condensed, and then combined with the second flow, thereby generating a two-phase flow containing the required percentage of liquid. This latter method is better because it is easy to combine operation and process control One-phase flow is re-fed into the upper section of the tower 'where this flow is in contact with the scrubbing vapor stream in the lower part of the tower, thus generating a liquid stream rich in broken materials that functions as a return flow' and produced by the tower Vapor stream with few carbons. As used herein, "multi-cracks" refers to any major organic compound with a molecular weight greater than that of Ethyl shuttle. This tower is unique in that, as mentioned above, in which it does not need to produce reflux. It is not necessary to re-boil the boiler. As described above, the "methane-rich stripping gas is fed into the tower. D. This flow is preferably generated from the upper flow position, where the cooled methane-based gas flows through Some degree of cooling and liquid removal. Prior to introduction to the bottom of the tower, this gas stream is cooled by indirect contact (preferably counter-current) with the liquid product produced by the bottom of the tower, thereby producing a warm, polycarbon-rich flow And cooled methane-rich stripping gas stream. When cooling, the methane-containing stripping gas reservoir can be partially condensed, and the resulting two-phase cooled methane-rich stripping gas can be fed directly into the tower. Cooling the steam containing solid C3 + ingredients with a small amount of C3 + ingredients instead of the regenerating ~ 3% vapour containing C3 + ingredients can significantly reduce the problem of fluids in towers approaching critical conditions. Composition of ingredients-23- —. ^ ^ Μ binding ------ line I q (Γ (Please read the precautions on the back before filling out this page) This paper size applies Chinese National Standard (CNS) A4 specification (21 〇 × 297mm) 426665 A7 B7 Printed by the Consumer Cooperatives of the Central Standards Bureau of the Ministry of Economic Affairs 5. Description of the invention (21) Lia This factor becomes particularly apparent when operating in a better pressure range of about 550 to about 675 psia The critical temperature and pressure of methane are 64T and 673.3, pisa. The critical temperature and pressure of propane are 206 2 ^ and 617 4 psia, and the critical temperature and pressure of n-butane are 305 and 551 25 psia. The presence of an acceptable amount of the C3 + component will (1) lower the critical pressure, and therefore a better operating pressure for the process, and (2) increase the critical temperature. The resulting effect makes it more difficult to separate the components via vapor / liquid contact. Differentiate the application of methane-rich stripping gas cooled on steam and the second of the reboiler due to the temperature difference between the individual stream &amp; and the liquid effluent in the final stage. Because a cooled methane-rich stripping gas is better than a similar steam warmer in a reboiler ', this better flow has a greater ability to strip the lighter liquid phase. The temperature difference between the liquid flowing from the tower and the stripping gas from the effluent reaching the tower is preferably 20 to 110 ° C, more preferably 40 to 90 ° C, and most preferably about 60 to 80T. The number of theoretical plates in the tower will depend on the composition of the vapor stream flowing into the tower, the temperature and flow rate, and the composition of the two-phase stream fed into the upper stage of the tower, the temperature, the flow rate and the liquid to vapor ratio. This decision is the theoretical number of beta holders that are familiar to those skilled in the art. It can be filled by various towers (such as collars, saddles, etc.) or in different contact sections of the tower (such as the holder) or The combination is determined. Usually 'two (2) to fifteen (15) theoretical segments are required, more preferably three (3) to ten (10) segments, still more preferably four to eight (8) segments, and preferably about five Theoretical section β When the tower straight is greater than six (6) feet, the support system is generally better. Search. The liquefaction system for open circulation is a courtesy example. The flowcharts and devices listed in Figures 1 and 2 are open cycles. Step liquefaction process 24- Private paper size applies Chinese National Standard (CNS) Α4 specifications (21〇297mm I:; ^-1 pack — (Please read the precautions on the back before filling this page)

, 1T -1 — n J — · Printed by the Consumer Cooperatives of the Central Standards Bureau of the Ministry of Economic Affairs 4266 6 5 A7, — _ _____B7_ V. A better specific example of the invention description (22), with a description of it. The shortcoming of the preferred embodiment is the nitrogen removal system, as this system is based on the nitrogen content of the feed gas. However, as described in the nitrogen removal techniques discussed previously, the preferred etiquette method is known to those skilled in the art. Figures 3 and 4 detailed for illustrative purposes are the freezing towers of the present invention, and in particular the method of cooling and controlling the temperature of the stripping gas to be fed into the freezing tower. Those skilled in the art should understand that Figures 1-4 are only diagrams, and therefore many of the equipment items required for operation in a commercial plant are cleared for clarity. This item may include, for example, compressor control, flow, and level measurement. And its controllers, additional temperature and pressure controls, pumps, motors, filters, additional heat exchangers, valves and more. These projects will operate the plant in accordance with standard engineering. To help understand Figures 1, 2, 3, and 4, item numbers 1 to 99 are equivalent to the process tanks and equipment of the liquefaction process. Item numbers 100 to 199 correspond to a major portion of a flow line or conduit containing methane, and item numbers 200 to 299 correspond to a flow line or conduit containing ethyl cryogen or ethylene as the case may be. Item numbers 300 to 399 correspond to flow lines or pipes containing refrigerant propane. Where possible, the numbering system used in Figure 1 can be used in Figures 2, 3, and 4. In addition, the following numbering system is added to the additional components, but it is not shown in FIG. Item numbers 400 to 499 are equivalent to additional moving lines or conduits. Item numbers 500 to 599 correspond to additional process equipment such as tanks, towers, heat exchange equipment and valves, including process control valves. Item numbers 600 to 7 9 9 are usually related to process control systems (except r control valves), and in particular include sensors, transducers, controllers and setpoint inputs. In most control systems, electrical, pneumatic or hydraulic signals are used. -25- This paper size applies to China National Standard (CNS) A4ii grid (210x ^ 97 mm 1 '' ''

---- Μ ----- ~ Pulling clothes! (谙 Please read the notes on the back before filling out this page J -5 426665 Printed by A7 B7, Shellfish Consumer Cooperative, Central Standards Bureau, Ministry of Economic Affairs V. Certain combinations of invention description (23). However, any other category is used in use Signal transmissions that are compatible with the process and equipment are within the scope of the present invention. Β The invention described in the figure, as the straight line of the signal line is the dotted line in the figure. These lines are preferably electrical or pneumatic signal lines. The signals provided by transducers are usually electrical. However, the signals provided by flow sensors are usually pneumatic. For simplicity, the conversion of these signals is usually not described because it is known in the art. Or, if the flow is measured in a pneumatic form, it must be converted into an electric form, if it is to be transmitted in an electric form by a mobile transducer. 'Refer to Figure 1, a gas propane system; ^ It is driven by an unillustrated gas turbine drive Compression in multi-stage compressor 18. Three-stage compression is better to exist in a single unit, although each stage of compression can be a separate unit, and the unit is mechanically combined with a single-drive appliance to drive. Compression The compressed propane is liquefied through a duct 300 to a cooler 200 ′. Before flash evaporation, the pressure and temperature of a representative liquefied propane refrigerant is about 100 times and about 19 psia. Although not illustrated in FIG. 1 Medium's better separation tank is located at the flow below the cooler 20 and above the decompression equipment (as described in the expansion valve i 2) to remove the remaining light components from the liquefied propane. This tank can include a single stage The gas-liquid separator may be more complicated 'and includes an accumulator section, a condenser section and an absorber section, the latter two of which can be continuously operated or periodically connected to remove residual light components from propane. The flow or cooler in this tank The flow of 20 passes through the conduit 302 to the decompression equipment, as described in the expansion valve 12, where the pressure of the liquefied propane is reduced, so part of it is evaporated or flashed. The resulting two-phase product flows through the conduit 3 〇 4 into the high-end propane sintering cooler 2 'wherein the gas propane refrigerant is introduced through conduit 152, the natural gas feed is introduced through conduit 100, and the gas is introduced through conduit 202 -26-t Guan Jiapi ((Please read the back first (Please fill in this page again) ii. 426 665 A7 B7 V. Description of the invention (24) Ethylene refrigerant is cooled by indirect heat exchanger equipment 4, 6 and 8 respectively, so it is made into cooling gas flow generated by ducts 154 '102 and 204, respectively. In duct 154 The gas is fed into the main methane economizer 74, which will be described in detail in the following paragraphs, and the flow is cooled by the indirect heat exchange equipment 98. The resulting cooled compressed methane circulation stream generated through the duct 158 is then mixed with polycarbons. Remove the vapor stream of the small carbon in the duct 60 of the tower 60 and combine it and feed it into the methane condenser 68. Printed by the consumer cooperation of the Central Bureau of Standards of the Ministry of Economic Affairs (please read the precautions on the back first) Fill in this page again)-The propane gas coming from the cooler 2 is returned to the compressor 18 through the duct 3 06. This gas is fed into the upper part of the compressor 18 into the tank. The pressure of the remaining liquid propane is reduced through the pressure reducing device through the conduit 308 ', as described by the expansion valve 14. At this time, the other part of the liquefied propane is flashed, and the resulting two-phase flow is fed into the cooler through the conduit 310. In 22, the coolant of the cooler 22 is thus provided. The cooling feed gas from the cooler flows through the conduit 102 to the separation tank 10, where the separated gas and liquid phase rich in C3 + component liquid phase is removed through the conduit 103. The gas phase is removed via conduit 104 and subdivided into two separate streams delivered via conduits 106 and 108. The flow in the conduit 106 is fed into a propane cooler 22. The flow in the duct 108 becomes the feed to the heat exchanger 62, and finally the ethylene refrigerant that has reached the multicarbon removal tower 60o cooler 2 is introduced into the cooler 22 through the duct 204 to be electrically charged. In the cooler 22, the feed gas stream (also referred to herein as a methane-rich stream) and the ethylene refrigerant stream are cooled by indirect heat exchange equipment 24 and 26, respectively. As a result, a cooled stream of methane and ethylene-rich cryogens is generated via the conduits 110 and 206. Therefore, the evaporation part of the propane refrigerant is separated, and it is input to the middle section of the compressor 18 through the conduit 3 1 1 and the liquid propane refrigerant from the cooler 22 is moved through the conduit 314-27. This paper standard applies to the Chinese national standard隼 （CNS &gt; Α4 Specification {210X297 公 嫠） 426665. Printed by the Consumer Cooperatives of the Central Standards Bureau of the Ministry of Economic Affairs, printed A7 B7 V. Description of the invention (25) Except for flash evaporation through pressure reducing equipment, such as the description of the expansion valve 14, and then It is fed via a catheter 3 1 6 into a third stage cooler 28. As illustrated in FIG. 1, the methane-rich flow flows through the conduit 110 and flows from the middle propane cooler 22 to the low propane cooler / condenser 28. In this cooler, the flow is cooled by the indirect heat transfer device 30. In the same way, the ethylene cooler flows from the middle propane cooler 22 to the lower propane cooler / condenser 28 through the duct 206. In the latter, the ethylene refrigerant is condensed or almost condensed by the indirect heat transfer device 32 '. All condensing. \ Evaporated propane is removed from the low stage propane cooler / condenser 28 'and returned to the low stage inlet at compressor 18 via conduit 320. Although FIG. 1 illustrates that the flow cooling provided by the conduits 11 and 206 occurs in the same tank, the cooling of flow 1 10 and the cooling or condensation of flow 2 can occur separately in the separation tank (for example, separation The cooling occurs in the cooler and the separation. In a similar manner, the multi-flows are cooled in a general tank (such as a cooler) before the surface cooling step can be performed in the separation tank. The previous combination is a better specific example because many The cost of the tank and the need for less factory space. As shown in Figure 1, 'methane-rich leaving the low-stage propane cooler flows through the pipe 112 and is introduced into the high-stage acetone cooler 42. The ethylene refrigerant leaves the low-stage propylene gauge cooling through the pipe 208 The device 28, and preferably through the conduit 209, is fed into a separation tank 37 for removing light components, and the condensed ethylene is removed through the conduit 21. The separation tank is similar to the previously described for removing liquefied propane refrigerant. Lighter components have similar tanks and may be single-stage gas-liquid separators or multi-stage operations that may provide greater selectivity to remove lighter components from the system. Ethylene refrigerants used here are typically at about Under the temperature of -24T and the pressure of about 285 psia. Through the catheter-28- This paper size is applicable to China National Standard (CNS) A4 size (2 [0 × 297 mm) (Please read the precautions on the back before filling this page) -Load-

, 1T The Central Bureau of Standards, Ministry of Economic Affairs, Shellfish Consumer Cooperation, Du printed 426665 A7 -----. B7 V. Description of the invention (26): ~: '--210 of the ethylene cooling agent to flow to the heat In the device 34, it is cooled by the indirect thermal father replacement device 38, and is removed through the duct 211, and is passed to a pressure reducing device such as a bulbous room 40 (at this time, the refrigerant is flashed to a predetermined temperature and pressure, And the tube 214 is fed to the high-level cooler 42 through the tube 212, and then the tube 214 is cooled down and removed, and the five-way indirect heat exchange equipment is moved to the second-party thermostat "(wherein the reed gas functions as a coolant and the second vapor passes through The ducts 2 and 6 were removed from the ethylene economizer and fed to the high inlet of the ethylene economizer 48. The ethylene refrigerant that had not evaporated in the high ethylene economizer 42 was removed through the duct 218 and sealed. The ethylene economizer 34 is further cooled by the indirect heat exchange equipment 50, and the I & 220 is removed from the ethylene economizer and flashed in a decompression device such as the expansion valve 52. At this time, The obtained two-phase product is introduced into the low-stage ethylene cooler 54 through the pipe 2 2 2. The I-pipe 116 is removed from the ethylene cooler 42 of the hafnium section and is a flowing stream rich in oxane. The flow is then condensed by the cooling part provided by the heat exchange device 56 in the low-stage ethylene cooler 54, so a two-phase flow flowing through the pipe ii 8 to the benzene / aromatic / polycarbonate removal tower 60 is generated. As mentioned earlier, the flow of pits containing pits in the duct is separated 'so it flows through ducts 106 and 108 a duct 108 &lt; contents (herein referred to as methane-rich stripping gas) first It is fed into the heat exchanger 62 'this flow is cooled by the indirect heat exchange device 66' and thus becomes a cooled methane-rich stripping gas stream, and then flows through the conduit 109 to the benzene / polycarbonate removal tower 6. .Liquid containing significant concentration of benzene, other aromatic and / or multi-carbon hydrocarbon components is removed from the benzene / polycarbonate removal tower 60 through the conduit 114, and preferably functions as a pressure reducing device 9 7 The flow control equipment (preferably the control valve) is flashed and conveyed to the heat exchange through a pipe i 1 7-This paper size applies to the Chinese National Standard (CNS) A4 specification (210X297 cm) * # n 「装 II Order 11 I line __ y .-- 1 ff '(Please read the precautions on the back before filling this page) Ministry of Economy Central Standard Bureau Consumer Consumption Cooperative Seal 426665 'A7 ____- B7 V. Description of the Invention (27)… Device 6 2. Better, flow flashing through the flow control device 9 7 flash to a pressure of about or greater than that of the methane compressor The pressure at the upper stage of the input cylinder. Flashing also provides a large cooling capacity for this flow. In the heat exchanger 62, the flow carried by the conduit 1 1 7 provides cooling capacity through the indirect heat exchange device 6 4 and jl through the conduit The flow of 1 1 7 provides cooling capacity via indirect heat exchange equipment 64, and JL leaves the heat exchanger via conduit 119. In the benzene / aromatic / polycarbonate removal tower 60, the two-phase flow introduced through the conduit i 18 comes into contact with the cooled methane-rich stripping gas flow introduced through the conduit 109 in a countercurrent manner, thus generating a through conduit 1 2 0 benzene / polycarbonate-rich vapor stream, rich in oxane, and 1-17 benzene / polycarbonate-rich liquid stream flowing through the duct. The flow in the conduit 119 is rich in benzene, other aromatics and / or other polycarbons. This flow is sequentially divided into liquid and vapor portions, or is preferably flashed or saturated in tank 67. In each case, the liquid stream is rich in benzene, other aromatic and / or multi-carbon soot components, and is made through the conduit 123, and the second forma-rich vapor stream is made through the conduit 1 2 1. In the preferred embodiment shown in FIG. 1, the flow in the conduit 1 2 1 is then combined with the second flow conveyed through the conduit 1 2 8 and the combined flow is fed to the methane compressor 8 3 through the conduit 1 4 0 High pressure input cylinder. As described above, the gas in the duct 154 is fed into the main methane economizer 74 and flows therein to be cooled by the indirect heat exchange device 98. The resulting cooled compressed methane cycle or refrigerant flow in the resulting duct 158 is combined with the non-polycarbonate-free vapor stream from the multicarbon removal tower 60 conveyed through the duct 120 in a preferred embodiment and fed into the lower section Condenser 68. In the low-end ethylene condenser, this flow is the liquid effluent from the low-end ethylene cooler 54, which is indirectly -30- (please read the precautions on the back before filling in this X) — installed. This paper size applies to China National Standard (CNS) A4 specification (210 X 297 mm) ^ 66 6 5 Printed by the Consumer Cooperatives of the Central Standards Bureau of the Ministry of Economic Affairs A7 B7 V. Description of the invention (28) _ The heat exchange equipment 70 is cooled and condensed and arrives via the duct 226 Low section ethylene condenser 68. The condensed pinane-rich product from the low-stage condenser is produced and produced through the conduit 122. Combining the steam from the low-stage ethylene cooler 54 extracted through the duct 224 and the steam from the low-stage ethylene condenser 68 extracted through the duct 228, and passing through the duct 230 to the ethylene economizer 34, the vapor functions in the same way Coolant via indirect heat exchange equipment 58. The flow then passes through the duct 2 3 2, from the ethylene thermostat 34 to the low section of the ethylene compression 4 8. As shown in FIG. 1, the compressor effluent from the steam introduced from the lower side is removed through the duct 2 3 4, cooled by the inter-stage cooler 71, and returned to the compressor 48 via the duct 236 for It is better to inject β in a high section flow existing in the duct 216. These two sections are single components, although they can be separate components, and these components can be mechanically coupled into a common drive β compressor. The compressed ethylene product passes through the duct. 200 travels to the down-flow cooler 72. As before, the product from the cooler flowing through the conduit 202 is introduced into the high-stage propane cooler 2. The liquefied stream in conduit 1 2 2 typically has a temperature of about -125T and a pressure of about 600 psi. This flow passes through the main methane economizer 74 through the conduit 1 2 2, where the flow is further cooled by the indirect heat exchange device 76 as described later. From the main pinane economizer 74, the liquefied gas passes through the conduit 124, and its pressure is reduced by a pressure reducing device, as shown by the expansion valve 78, which of course evaporates or flashes a part of the gas flow. The flow of flash evaporation is then passed to the methane high-stage flash drum 80, which is separated into a gas phase discharged through a conduit 126 and a liquid phase discharged through a conduit 130. The gas phase is then transmitted to the main methane economizer via conduit 126, where the vapor functions as a coolant through indirect heat exchange equipment 82. Vapor Pass -31-This paper size applies to China's National Standard (CNS) A4 specification (210X297 mm)! .---; -------- "Installation 丨-(Jing first read the precautions on the back before filling in this page ] Order printed by the Central Consumers ’Bureau of the Ministry of Economic Affairs and the Consumers’ Cooperative Cooperative 4266 6 5 β Α7 __— — · ___ Β7 V. Description of the invention (29) — The duct 128 leaves the main methane economizer, and the gas flow conveyed by the duct 121 Combined with these flows, it is fed into the high-pressure input cylinder of the shrinking machine 83. The liquid phase in the pipe '130 passes through the second methane economizer 87, and the liquid is vaporized by the flowing vapor and passed through the indirect heat exchange equipment. 8 8 Further cooling. The cooled liquid leaves the second methane economizer 87 through the conduit 132 and is expanded or flashed through a pressure reducing device such as the expansion valve? 1 to further reduce the pressure and cause the second part to evaporate. The flash stream is then passed to the middle section of the burner flash trap 92 ', where it is divided into a gas phase passing through the tube 136 · and a liquid phase passing through the tube 1 &lt; 3 4. The gas phase flows through each tube 1 3 6 , Reached the second Jialuo economizer 87, the vapor of which passes the indirect heat exchange equipment 89 cooling liquid The body passes through the duct 130 to 87. The duct U8 is used as a flow duct between the heat exchange equipment 89 in the second methane economizer 87 and the heat exchange equipment 95 in the main nail burner 74. The vapor passes through the duct 140 leaves the main formazan economizer 74, and the pipe 140 is connected to the middle stage input of the methane compressor 83. The liquid phase leaving the middle stage flash drum 9 2 via the pipe 1 3 4 is passed through as shown in the expansion valve 9 3 The decompression device decompresses. Then, the third part of the liquefied gas is evaporated or flashed. The fluid from the expansion valve 93 is passed to the last or lower stage flash drum 94 »In the flash drum 94, the vapor phase separates and passes through The duct 144 reaches the second methane economizer 8 7 (the function of the vapor therein is the same as that of a 90 ° coolant for heat exchange through Fujian). The duct leaves the second methane economizer via the duct 146. The duct 164 and the first methane economizer 7 4 is connected (the function of the steam in it is like the coolant through the indirect heat exchange device 96), and finally, the duct Η8 which is in communication with the low-pressure cylinder of the compressor 83 leaves the first methane economizer. Liquefied natural gas product from flash drum 9 4 through conduit 1 4 2 -32- 本Zhang scale applicable Chinese National Standard (CNS) Α4 specification (2! 0Χ297 mm) (Please read the back of the precautions to fill out this page) installed.

1 1-I--! * I--I

A 66 6 5 Printed by the Consumers ’Cooperative of the Central Bureau of Standards, Ministry of Economic Affairs A7 B7 V. Description of invention (30) to the storage unit. The low-pressure, low-temperature LNG evaporates the vapor stream from the storage unit, and, depending on the situation, the vapor cooled back from the operating pipeline of the combined LNG load system, preferably by making this flow or flows and the conduit 144, 146 or 1 4 8 One of the existing low-pressure flash vapors is combined with recovery; the selected conduit is mainly to meet the steam flow temperature as much as possible. As shown in _1, the high, middle and low sections of compressor 83 are better combined into a single unit. However, sections can exist as separate units, where the units are mechanically coupled together and driven by a single drive. The compressed gas from the low-stage section passes through the interstage cooler 85 and is combined with the medium-pressure gas in the duct 140 before compression in the second section. The compressed gas from the middle section of the compressor 83 passes through the interstage cooler 84 and is combined with the high-pressure gas in the duct M0 before the third section is compressed. The compressed gas is discharged from the high-stage methyl alcohol compressor through the conduit 15, cooled in the cooler 86, and reaches the high-pressure propane cooler through the conduit 1 52 as described above. Figure 1 shows the expansion of the liquefied phase using an expansion valve that can subsequently separate the gas and liquid parts in a cooler or condenser. Although this simplified diagram is operational and used in some cases', it is often more efficient and effective to perform partial evaporation and separation steps in individual equipment, such as using expansion before separating vapor or liquid into a propane freezer Valve and separation flash _ steaming bucket. In a similar method, it is ideal to use a hydraulic expander as part of the means to reduce the pressure of some process fluids that have undergone expansion, so that work can be extracted and the two-phase temperature can be reduced. — Regarding the compressor / drive unit used in this process, Figure 1 shows the individual compressors / drives used in the compressor, ethylene and open cycle methane compression stages. -33- Binding ------ ¾1 «--- 1 (Please read the precautions on the back before filling this page) (This paper size applies to Chinese National Standards (CNS) (2 [0; &gt; &lt; 297 race) Printed by the Central Bureau of Standards, Ministry of Economic Affairs, Consumer Cooperatives 426665

A A7 ____B7 V. Description of the Invention (31) '~~:-Unit. However, in any preferred specific example of the disclosed process, the process can be significantly improved by replacing the single compressor / drive unit shown with a multiple compression series including a parallel combination &lt; two or more compressors / drivers As a result, it becomes impossible to provide a voice reduction machine / drive unit, and the process can still be operated with reduced capacity. The process and equipment of this hair-suction and hair-bearing seat are the best specific examples of benzene, other aromatic and / or multi-carbon hydrocarbon component removal processes and related devices. As shown previously, the two-phase liquid stream fed into the benzene plant aromatics / polycarbonate removal tower 60 via the conduit 1 1 8 comes from the cooling provided by the heat exchanger 56 in the ethylene cooler 54 and is supplied to the conduit 116 Cooling of liquid stream and partial condensation. In a specific example, the entire fluid flow in the 'cathode 1 16 is cooled. In the preferred embodiment shown in FIG. 2, the two-phase liquid flow is obtained by cooling and partial condensation of the liquid flow in the conduit 116, and this portion is then combined with the remaining liquid flow through the conduit 1 16 . Referring to Fig. 2, the liquid flow delivered through the conduit 1 16 is split into a first liquid flow into the conduit 450 and a second liquid flow into the conduit 452. The liquid flow in the conduit 45 flows through the optional valve 5 3 2 (preferably a hand control valve) and flows into the conduit 454, which can transfer the first liquid flow to the ethylene cooler 54, wherein the liquid flow passes through the indirect The heat exchange device 56 is partially condensed at least once and flows out of the device through a conduit 458. The second fluid in conduit 452 flows through valve 530 (preferably a control valve) into conduit 456, which is then combined with the first fluid flow delivered through conduit 458. The combined liquid stream (now a two-phase liquid stream) is delivered to the tower 60 via a conduit 1 1 8. From an operational perspective, the length of the conduit 118 should be sufficient to ensure proper mixing of the two flows to bring them close to equilibrium conditions. Two-phase flow in the conduit 1 1 8 -34- ί; --Γ— "Packing II (I read the precautions on the back first and then fill out this page) The paper size of the book is applicable to the Chinese National Standard (CNS) Α4 Specifications (210X297mm) ~ ii Printed by the Consumers 'Cooperative of the Central Standards Bureau of the Ministry of Economic Affairs 426665 A7 | ____ B7 V. Description of the Invention (32)' The amount of liquid in '32 is better controlled by maintaining the flow at the required temperature. This system Complete the 'temperature conversion equipment 688 and induction equipment, such as a thermometer located in the conduit 118 to provide an input signal 686 to the temperature controller 682. It is also provided to the controller by the operator or the computer carry method for the set point temperature signal 684 ^ The controller 682 senses the difference between the 2 inputs and sends a signal 6 8 0 to the flow control valve 5 3 0 located in the duct. The flow of the flowing part is transmitted through the duct 116 without heat exchange in the cooler 54. The reactor device 56 is cooled. The transmission signal 68 is amplified to represent the control required to maintain the desired flow rate in the duct ΐ8 to control the% 530 position. The feed stream to the process step (with benzene removed, Other aromatic and / or poly The hydrocarbon component) is a two-phase process stream from the ethylene cooler 54 that is transmitted to the upper section of the column 60 through the conduit 118 and a methane-rich A it oxygen gas that is transmitted through the conduit 108. Although shown in FIG. Produced by the feed gas from the first 1¾ stage of the sintering process, the flow of Zhao Zhao 'This flow can be generated from any location in the process, or it can be an externally enriched smelting flow. As shown in Figure 2, At least a portion of the methane-rich stripper gas is passed through an indirect heat exchange device 62 and cooled in a heat exchanger 62 before entering the bottom of the column 60. The effluent stream from the process step of the present invention is generated through a duct 12 The multi-carbon-free gas flow from the column 60 and the temperature-heated multi-carbon-rich flow generated through the duct 1; 9. As described in FIG. 2, the multi-carbon-rich flow is from the column It is produced by 60%, and is heated in the heat exchanger 62 through the indirect heat exchange device 66. The tower effluent produced through the conduit 1 1 4 is in this way>, but is fed into the tower through the conduit 丨 09. Stripping gas. The number of theoretical stages in column 60 depends on the composition of the feed stream to the column and -35-

-I J- s V / JP- 426685. Printed by the Consumer Cooperatives of the Central Standards Bureau of the Ministry of Economic Affairs Α7 Β7 V. Description of Invention (33) 疋. Passing 4, requires two (2) to fifteen (15) theoretical paragraphs. The preferred number of stages is three (3) to ten (10), more preferably four (4) to eight (8), and from the viewpoint of operation and cost, the preferred number is about five (5). The theoretical section can be made by filling, plates / pans or combinations thereof. Generally, filling is preferably a tower with a diameter of less than about six (6) feet, and the plates / trays on the tower are greater than about six (6) feet in diameter. As illustrated in Figure 2, the upper section of the two-phase flow feed tube 118 is designed to assist gas / liquid separation. The tower section preferably contains equipment for removing or misting the liquid from the vapour stream. This equipment is located between the entry point of the duct η 8 and the exit point of the duct 12. As shown in FIG. 2, the polycarbon-rich liquid flow generated through the conduit 1] 4 flows through the control valve 9 7 and the conduit 1 1 7 and is sent to the heat exchanger 6 2, where the liquid passes through an indirect heat exchange device 64 provides cooling, and the heat is generated from the heat exchanger 62 via conduit 119 as a warm, multi-carbon rich stream. Depending on the operating waste of the lower flow process, the cooling capacity of this liquid stream can be increased by flashing to a lower pressure through the control valve 9 7. The process stream generated via the catheter 1 19 can be used directly or subsequently processed to remove lighter components. In the preferred embodiment illustrated in Fig. 2, the demethanizer 67 is fed in a flowing manner. The flow rate of the polycarbonate-rich liquid from the column 60 can be controlled by various methods immediately available to those skilled in the art. The eyebrow control device described in Brow 2 is a better device, and includes a level controller device 600, an induction device, and a signal transmitter connected to the level control device. The operability is configured in the lower section of the tower 60. . The controller 60CT generates an output signal 602, which displays the flow rate in the conduit 114 required to maintain the desired liquid level of the tower 60, or displays that the actual liquid level has exceeded a predetermined liquid level. Flow Measurement Equipment and Transmitter-36- This paper size is in accordance with China National Standards (CNS) A4 (210X297 mm) (Please read the precautions on the back before filling this page) * 1Τ line 426665 A7 B7 V. Description of the invention (34) Du Yinzhuang, a male laborer's consumer cooperation contract with the Central Bureau of Standards and Quarantine of the Ministry of Economic Affairs, is operatively arranged in the conduit 114 to generate an output signal indicating the solid flow velocity of the fluid in the conduit 114. The flow control device is preferably located above the control valve to prevent induced two-phase flow. The signal 602 is provided as a setpoint signal for the convection controller 608. The signals 602 and 608 are compared in the flow controller 608 respectively to the output signals 614 of the health controller 608 which respond to the difference between the signals 602 and 606. A signal 614 is provided to the control valve 97, and the valve 97 is actuated by the sensing signal 614. The setting signal (not described) of the required liquid level in the tower 60 represents that the liquid can be manually input by the operator into the controller 60 (), or on the contrary, controlled by a controlling digital computer. Depending on the operating conditions, the operator or computer logic is used to determine whether the control depends on the level or flow rate. Relative to the variable flow rate input of signal 606 and the selected setting signal, controller 608 provides an output signal 614 that reflects the differences between the respective input and setting signals. The signal is amplified to represent the position of the control valve 97 required to maintain the flow rate of the fluid substantially equal to the required flow rate, or the fluid level substantially equal to the required level. In heat exchanger 62, a multi-carbon-rich stream that cools the methane-rich stripping gas stream is passed through conduit H7 to the heat exchanger. The multi-carbon-rich liquid stream flows through the heat exchange device 6 6 ′ and is generated by the heat exchanger through the duct 9. -Into the tower, the extent to which the methane-rich gas stream is cooled by a flow with polycarbons can be controlled by various methods known to those skilled in the art. In a specific example, 'all the stripping gas rich in torrefaction is fed into the heat exchanger, and the liquid flow rate of the multi-carbon-rich liquid used for heat exchange, the heat transfer surface area used for the heat transfer, and / or the fluid flow The residence time of heating or cooling is used as a parameter to control the degree of cooling. In a preferred specific example, please note the item of pristane-rich transported through the catheter 108, and then 'order' the line -37- This paper size applies to China National Standard (CNS) A4; Grid II (210 × 297) 〉 Printed by the Consumers Cooperative of the Central Standards Bureau of the Ministry of Economic Affairs 4 ^ 6665 &quot; A7 _____ --_ B7 V. Description of the Invention (35) The stripping gas flows through the control valve 500 and enters the duct 400, and flows It is separated and transmitted through the ducts 402 and 403. The flow flowing through the duct 403 and finally flows through the heat exchange device 64 in the heat exchanger 62. The equipment for operating the relative flow velocity of the fluid in the ducts 402 and 403 is installed In the duct 402 or 403. The device illustrated in Figure 2 is a simple manual control valve, 502 and 504, which are attached to the ducts 404 and 407. However, the position is controlled by the controller Operation, and the input of the controller includes the set point and the signal flow in the conduit (as discussed above with the multi-break logistics) control valve can replace one or both of the manual control. In any case, operate this The valve makes the temperature difference between the pipes n 7 and 404 reach the heat exchanger 62. Over 50 times, otherwise it will cause damage to the heat exchanger. The cooled fluid hides the indirect heat exchange device 64 through the duct 405, and passes through the duct 407 at the junction with the uncooled rich entertainment system> The stripping gas is combined to form a cooled methane-rich stripping gas stream that is sent to the tower via a conduit. The operational configuration in conduit 1 0 9 is a flow transfer device 6 1 6 which is connected to a flow sensing device [if generating output Signal 618 (which indicates the actual flow rate of the fluid in the catheter) orifice plate (not shown)]. Signal 6 1 8 is provided by the process variable input to the flow controller 620. It is also provided manually or via computer output It is the set point of the flow rate represented by the signal 6 2 2. _The buckle controller also provides an output signal 624, which indicates the difference between the individual input and the set point signal, and it is enlarged to indicate that the catheter is maintained in 10 9 The position of the control valve required for the desired flow rate. — In another specific example, the relative flow rate of the fluid flowing through the ducts 402 and 403 can be provided by a temperature sensing device and a transducer connected to the device (if Requires -38- (Please read first Note to fill out the back of this page). · Loaded

* tT J1. This paper size is applicable to China National Sample (CNS) A4 specification (210X297 mm) 4266 65 A7 B7 V. Description of the invention (36) '~:' Required 'in the catheter 1009, and use the obtained The output and set-point temperature are used as input control of the flow controller, which will produce a difference in the sensing two signals and an output signal indicating the scale of the control valve position required to maintain the desired flow rate in the conduit 109. This control valve can replace the manual valve 502 and / or 504. Printed by Shellfish Consumer Cooperative, Central Bureau of Standards, Ministry of Economic Affairs In another specific example described in Figure 3, the temperature of the stripping gas sent to tower 60 is controlled in the following manner. The temperature transducer 700 is operatively configured in the catheter 1 17 (measuring equipment, such as a thermometer, provides an output signal 7 08 that represents the exact temperature of the fluid flowing through the catheter 1 17. The signal 7 08 is based on The first type of proportional computer 700 is provided. The proportional computer 700 also provides a second temperature signal 706 representing the temperature of the fluid flowing into the conduit 109. The signal 706 is generated in the temperature transducer 702, which The output signal 7 〇 6 is a reaction sensing element, such as a thermometer that is operatively configured in the catheter 1 009. Relative to the signal 7 〇 and 7 0 'proportional computer 7 〇〇 provides representative signals 7 0 6 and 7 0 8 ratio The output signal. Signal 7 i 〇 is used as the input of the proportional controller 712. The proportional controller 712 also provides a setpoint signal 714, which indicates the temperature ratio required for the flow of gifts in the conduits 109 and 114. Inductive signal 710 And 714, the proportional controller 712 provides an output signal that senses the difference between the signals 710 and 714. The signal 716 is scaled to indicate that the desired ratio represented by the setpoint signal 7 1 4 is maintained. The required control-the position of 阙 5 3 4 ( Operationally It is arranged in the conduit 7 1 8. The control valve 5 3 4 is actuated by the sensing signal 7 1 6. According to the best control method described in FIG. 4 (which uses the same reference numerals for the components shown in the previous figure) ), The automatic start of the tower 60 is assisted by the high selector 728. It should be noted that the set point 724 of the temperature controller 722 is the same as the tower -39- This paper size applies the Chinese National Standard (CNS) A4 grid (210X297 mm) '4 Printed by the Central Laboratories of the Ministry of Economic Affairs, Machining and Consumer Cooperatives 266 65 Λ Α7 ________ Ξ__ V. Description of the invention (37) The setting required at a liquid compatible temperature in 60. However, at startup, the catheter 10 &gt; Medium The temperature will be normal temperature or near normal temperature β. According to this, the connection signal 726 directly sent to the operation valve 536 will cause the valve 536 to close, and the warm dry gas will not flow to the refrigeration separation tower 60 during startup. This problem can be as follows The description above is overcome by a temporarily selected signal 742 sent to the operation valve 536. The sensor is dedicated to the signals 706 and 724, and the temperature controller 722 provides an output signal 726 that senses the difference between the signals 706 and 724. The signal 726 indicates that the fluid in the conduit 109 is maintained True temperature The required operability at the desired temperature represented by signal 724 is the position of the control valve 5 3 6 in the conduit 1 08. However, as mentioned above, the expectation of the setpoint signal 724 does not enable the tower to start. Accordingly, signal 726 It is supplied to the signal selector 728. The signal selector 728 also provides a control signal 742 that senses the difference between the signals 736 and 740, and is scaled to maintain the temperature of the fluid in the conduit 119 which is substantially equal to the desired temperature represented by the signal 740. 5 3 6 The indication of the position. When the tower starts, the exact temperature of the fluid in the conduit 119 will be lower than the desired temperature indicated by signal 740. Accordingly, the connection of signal 742 to valve 536 will cause valve 536 to open, thereby reducing the temperature represented by signal 706. The high selector 7 2 8 determines which control signals 726 and 742 enable the 阙 536 to operate. The startup proceeds like this. The feed gas is introduced into the top of the freezing separation column 60 in the upper stage. When the temperature of the feed gas is cooled to the condensation temperature at which impurities are to be removed, the liquid begins to form a level in the column 60. The liquid level controller 6 0 0 senses the liquid level and its output opens the response signal 114 and the valve 97 »The low-temperature liquid is passed to the heat exchanger 62 and exchanges heat with the warm and dry gas flow through the duct 108 and the valve 536. Valve 5 3 6 starts to open with signal 74 2 at the set point temperature. Qian-40- This paper is suitable for China National Standards (CNS) lying secret (210X297mm) '' (Please read the precautions on the back before filling this page). Packing _ Printed by the Central Standards Bureau of the Ministry of Economic Affairs System 426665 A7 -__ _________B7 V. Description of the invention (38) ~~ '--- After the gas mud is started, the temperature transducer 702 senses the rapid cooler temperature of the signal 72 6 selected by the high selector 728. The start-up controller assists the operator in providing smooth and safe start-up and reduces the need for attention. The warm, multi-carbon-rich stream from the heat exchanger 62 is fed through a conduit 119 to a demethanizer column 67, which contains a rectification and stripping section. The rectification and stripping sections may contain different stages (such as trays, plates), or provide continuous mass transfer via tower packing (such as saddles, grid rings, woven wiring) or a combination of the foregoing. Generally, for towers with a diameter of less than about six (6) feet, filling is better, but for towers with a diameter of more than about six (6) feet, it is better to use different stages. The number of theoretical stages for both the rectification and stripping stages depends on the desired composition of the final product and the composition of the feed stream. Preferably, the stripping or lower section contains 4 to 20 theoretical sections', more preferably 8 to 12 theoretical sections, and most preferably about 10 theoretical sections. In a similar manner, the above or tower section preferably contains 4 to 20 theoretical sections, more preferably 8 to 13 theoretical sections, and most preferably contains about theoretical sections. A general reboiler 5 2 4 is provided at the bottom to obtain stripped steam. In the preferred embodiment shown in FIG. 2, the liquid from the lowest section of the demethanizer reaches the reboiler through the conduit 428, where the fluid is a heating medium conveyed through the conduit 44 and passed through the indirect heat exchange device 5 2 5 is heated, and is connected to the flow control valve connected to the pipeline 4 4 4 in sequence. The pipeline 4 of ZZ6 returns to the same as 2 ". The steam from the reboiler returns to the demethanizer tower through the pipeline 430, and the liquid passes Remove the pot. This flow in the conduit 432 may be combined in the conduit 436 with a second liquid flow formed by the visual duct-shaped conduit 434 at the bottom of the demethanizer as appropriate. In this case, the total liquid flow that may be generated by the demethanizer through the conduit 436 and / or 4 32 may flow through the cooler 5 2 0 and be guided by the conduit -41-This paper size applies to China National Standard (CNS) A4ii (210 X 297 mm) J ~ 丨 T ---- jT Pack I- (Please read the precautions on the back before filling in this page}

'1T 4 266 6 5 Λ Α7 ___________ Β7__ V. Description of the Invention (39)' 438 The device for generating β control fluid is inserted into one or both of the above-mentioned catheters. In a specific example shown in FIG. 2, the flow control device includes a control valve 5 2 2 inserted between the conduits 4 3 8 and 1 2 3. The position of the control valve 5 2 2 is operated by the flow controller 632, which senses the difference between the solid flow velocity of the fluid in the conduit 438 indicated by the set point signal 628 and signal 631 of the level control device 626. The setpoint flow rate of the liquid level controller 6 2 6 6 3 0 can be provided by the operator or computer digital input. The output of the controller 632 is a signal 634, which represents the position of the control valve 5 2 2 required to maintain the desired flow rate in the conduit 438 to maintain the desired liquid level in 67. _ Although various control techniques can be used to adjust the flow rate of the stripping vapor sent to the tower 67 via the conduit 430, the preferred technique is based on the temperature of the return vapor. The temperature transducing device 636 in combination with a sensing device (such as a thermometer located in the conduit 430) can provide an input signal 638 to the temperature controller 6 4 2. It is also provided by the operator or computer to the controller to set the temperature signal 0040. The difference between the two inputs of the controller 642 is to send a signal 644 to a conduit containing a heating medium (preferably a conduit 440 or 444, preferably a conduit 444) in the flow control valve 5 2 6. The transmission signal 644 represents a way to maintain the position of the control valve 526 required to obtain the desired temperature in the conduit 440. The novel goal of the S. beta f armor stripper tower is to generate a returning liquid. As shown in FIG. 2, the product from the top of the column leaves the demethanizer column 67 via the duct 41. At this time, at least a part of the flow is partially condensed when passing through the heat exchange device 510 in the fast heat exchanger 62. It is cooled by a polycarbonate-rich liquid product from a polycarbonate removal tower 60. In the preferred specific example, -42- which is rich in polycarbons is applicable to the national standard of China (CNS> A4 size (210X297))-(Please read the precautions on the back before filling this page) -Load-

Printed on line 1T, printed by the Consumer Cooperatives of the Central Standards Bureau of the Ministry of Economic Affairs 426665, A7 B7 V. Description of the invention (milk) The printed products of the Central Standards Bureau of the Ministry of Economic Affairs, Shellfish Consumer Cooperatives, printed products of Zhao are first used to cool at least part of the overhead The effluent vapor stream is then used to cool the methane-rich stripping gas stream. The condensed liquid formed by cooling the polycarbon-rich liquid stream becomes the reflux source of the demethanizer tower 67. Preferably, the heat exchange between the two indication streams occurs in a countercurrent manner. In the specific example, 'the entire flow can be flowed to the heat exchanger 62 as described above to cool all + methane stripping gas "In the preferred specific example shown in FIG. 2, the vapor product of the overhead distillate is divided into The airflow flowing in the ducts 412 and 414. The flow in the duct 4 1 4 is cooled in the heat exchanger 62 by passing the flow through the heat exchange device 5 1 0 in the exchanger 62, and the resulting cooling flow is generated through the duct 4 18. The relative velocity of the steam flow in the ducts 4 1 2 and 4 1 4 or 4 1 8 is controlled by a flow control device, preferably a flow control valve. The overhead vapor can pass through it without flowing through the heat exchanger. So avoid the two-phase flow Zhao Zhi's control. The vapor flowing in the duct 4 1 2 flows through the flow control device 5 1 2 and is generated therefrom via the duct 416. Combining the conduits 416 and 418 thus results in a combined cooled two-phase flow through the conduit 4 2 0. Disposed in the duct 4 2 0 is a temperature transducing device 646 ′ combined with a temperature sensing device (preferably a thermometer), and provides the temperature controller 6 5 2 with a signal 648 representing the exact temperature of the fluid flowing in the duct 420. The required temperature 650 is also entered into the controller 652 manually or via a computer. Based on the comparison between the winter input and the setting 650 via the transducing device 646, the controller 652 then provides an output signal 654 to the valve 512, which scales to operate the valve 512 in an appropriate manner, so Zhao Jin or maintains the set point. The two fluids in the obtained conduit 420 are fed into the separator 514 ', and a methane-rich vapor stream is generated from the separator 514 through the conduit 422, and a reflux liquid flow is passed through the conduit 4 2 4. In another preferred specific example, the aforementioned method is used, but 43- this paper size applies the Chinese National Standard (CNS) Cong Mi (2) 〇) & 297 public love (Please read the precautions on the back before filling this page ).

Line -1T V m · 4 4 Printed by the Shellfish Consumer Cooperative of the Central Bureau of Standards of the Ministry of Economic Affairs 4 2 6 6 6 5 A7 ______B7 V. Description of the Invention (41) &quot; The carbon-rich stream in the duct 117 is cooled through the duct Before the flow conveyed by 414 'is first used to cool the flow conveyed through the duct 4 1 4. As shown in Figure 1, the methane-rich vapor stream in conduit 1 21 is returned to the open pinane cycle to be subsequently liquefied. The pressure of the demethanizer and its equipment is controlled by the automatic operation of a pressure-transducing device 656 which is operable to be disposed in the conduit 422. The control side of the 518 control β control valve is connected to the conduit 4 2 2 and the wheel exit side. The upper connecting pipe 121 is preferably directly or indirectly connected to the low-pressure input cylinder of the methane compressor. The pressure transducing device 656 combined with the induction device provides a signal 6 5 8 to the pressure controller 6 60, which represents the pipe 422. The actual pressure. The set pressure signal 662 is also used as an input to the pressure controller 660. The controller then generates a sensor signal 664 which represents the difference between the pressure sensor signal 658 and the setting signal 662. Signal 664 is then scaled in a manner that makes valve 518 act to approach or set pressure. In a specific example, the controller, the control valve, and the pressure-sensing transducing device 656, as the case may be, are included in a single device known as a back pressure regulator. The reflux of the separator finally flows into the demethanizer. In the preferred embodiment illustrated in FIG. 2, the return flow leaves the separator 5 1 4 through the conduit 4 2 4, flows through the pump 516, and then flows through the conduit 425, the control valve 519, and the conduit 426. Device tower in the upper section. In this specific example, the flow velocity of the return flow is controlled by the input of the liquid level control device 666 of the induction device which is located in the lower section of the separator 5 1 4. The controller 666 generates the number '668 of the flow velocity in the duct 426 required to maintain the liquid level in the separator 514, and the signal 668 is used as the setting input of the flow controller 670, and the signal 671 which also presents the actual flow rate in the duct 425 is also fed. . The controller 670 generates a signal 674 again to control -44 * This paper ^^ is applicable to Zhongguanjiapi (€ Gang 44 specification (2 丨 (^ 297mm) '— J--Ί ----- "installation- -(Please read the precautions on the back before filling out this page) -11 426665 Α7 Β7 Printed by Zhengong Consumer Cooperative, Central Standards Bureau, Ministry of Economic Affairs V. Invention Description (42) Between 5 and 19, which represents the difference between the signals, and Used to provide the appropriate liquid flowing through the flow control valve 51 minutes, and thus control the level in the separator 514. The controllers previously discussed can use various conventional control modes, such as proportional, proportional integral, proportional integral-derivative (PID) In the preferred specific example described in Figure 4, 'for the calculation of the control signal required for the measurement process variables and the $ point supplied to the computer', the better is a digital computer with support for adjustment. Digital computers that allow actual environment operation and software to read external variables and transmission signals to external devices are applicable. The PID controllers shown in Figures 2, 3, and 4 can use various control modes, such as proportional , Proportional integral or proportional integral_derivative. Better In the specific example, a proportional-integral mode is used. However, any controller that has two or more input signals and generates a representative. Comparing the amplified output signals of the two input signals is within the scope of the present invention. The controller marks the output signal For those skilled in control system technology. Basically, the output of the controller can be marked to represent any required factor or variable. An example is the comparison of the expected temperature and the actual temperature by the controller. The output may be required to equalize the desired and actual temperature. The signal of the control &quot; gas flow rate indicates β. In other words, the same output signal can be marked with 'to represent the pressure required to equalize the expected and actual temperature. If the controller The output can be between 0 and 10 units, then the controller signal can be marked, so the output has a level equivalent to 5 units of 50% or a specific flow rate or a specific temperature. The transduction device is used to measure the characteristics according to various i numbers The parameters of the process, so it can produce various forms or layouts. For example, the control elements of this system can use electrical analog, digital electronics, pneumatic, hydraulic, mechanical Or other similar type -45- (Please read the notes on the back of this page and then fill in) loaded _ set k

r * /) ί _ 1 I A7 4266 6 5 ^ __ B7 V. Description of the invention (43) ~ type equipment or a combination of such equipment. I;; "install-(Please read the precautions on the back before filling out this page) Selecting the control loop is used in various process conditions to select the appropriate control action. Generally, the general control signal is The second control signal with a higher priority in the process conditions is suppressed. For example, harmful conditions can be avoided or desired features (such as automatic start-up) can be implemented with a temporarily selected second control signal. Used in feedback control systems Hardware and / or software are known in the field of process plant control. For example, see Chemicals Handbook. Fifth Edition, McGraw.

Hill ', pp. 22-1 to 22-147 "Specific freezing methods, substances, equipment and control equipment items are indicated here. It is important to understand that this specific description is not intended to be limiting, but only for illustration and listing. The best mode according to the present invention is shown.

Example I Printed by Shellfish Consumer Cooperative, Central Standard Bureau of the Ministry of Economic Affairs This example shows that through computer simulation, benzene and polycarbons are removed from a methane-based flow before the main part of the methane-based flow is liquefied The efficiency of the process described in the previous description. The flow rates shown here are present in a 2.5 million metric tons / year LNG plant using the liquefaction technology listed in Figures 1 and 2. α The benzene concentration in the methane-based gas stream used in this example is the natural gas stream in many processes Representative. However, gas streams dominated by pinane are considered to be relatively deficient in polycarbons (ie, C3 +). Similar results were obtained using Hyprotech's Process Simulation HYSIM »386 / C2.10» Prop. PkgPR / LK "— the ones listed in Table 1 are the inflow and effluent stream compositions sent to the multi-carbon removal tower, temperature, Force and phase conditions. This simulation is based on 5 theoretical sections -46- This paper size is applicable to Chinese National Standard (CNS) A4 (210 X 47 mm) 4 266 6 5, A7 B7 v Central Standards Bureau of the Ministry of Economic Affairs *: Industrial Consumption The cooperative prints the tower of the invention description (44). Partially condensed flow (also known as two-phase flow) (the main part of which is then liquefied) is first fed into the uppermost stage of the tower (phase 1). The temperature of this flow was 112 &gt; 5 ° F and the pressure was 587.0 psia. As mentioned earlier, this flow is partially condensed, so the flow is 98.24 mole% vapor. The cooled pristane-rich stream stripping system fed in the lowest stage (stage 5) comes from the upper flow position as described in FIG. This flow is cooled from about 63 ° F to -10 ° C through countercurrent heat exchange with the polycarbonate-rich liquid flow made in stage 5. During this heat exchange process as described in FIG. 2, this flow is heated from about −78 T to about 62 ° C. This flow can also be used to cool the overhead vapors from the demethanizer column. Table 2 lists the simulated temperature, pressure and relative flow rate of each phase based on the middle stage of the tower. The individual liquid and vapor equilibrium compositions are listed in Table 3 for each segment. The warmed multi-carbon-rich stream is then fed into a decanter pit containing the rectification and stripping section to produce a stream rich in oxane / ethane, which is preferably recirculated in the reverse direction and fed into methylbenzene The high section of the shrinking machine is input into the cylinder and the natural gas-rich liquid flow. The efficiency of the aromatic / polycarbonate removal process is illustrated by comparing the combined nitrogen, formazan, and benzyl alcohol mole ratios in the feed streams sent to stages i and 5 and the products in stage 1. The contention of each flow is 100%; the ratios are pan, 99.89 and 99.94 mole percentages respectively. This process therefore produces more product streams of these light components than the two gas feed streams. The efficiency of the process used to remove the aromatics of benzene and polycarbons is a concentration defined by comparing the mole percentage of the component in the liquid product of stage 5 divided by the mole percentage of the component in the vapor product of stage 5 Than description. Use Benzene-47- Turning Towels (CNS) on this paper scale Α4 · _ (2) (3χ297 公 董) --- (Please read the precautions on the back before filling this page)-Binding · Thread 66 Ό A7 B7 Printed by the Consumer Cooperatives of the Central Bureau of Standards of the Ministry of Economic Affairs 5. Description of the invention (45) 'As an example' The individual mole fractions are 0.1616E-O4 and 0,00352. This results in a concentration ratio of approximately 2 2 0. Explanation ' An additional basis for the efficiency of this process is the liquid product stream made from the concentration ratio of the C3 + component in the feed streams sent to stages 1 and 5. This ratio ranges from about 45 for propylene to about 200 for n-octane The individual ratios between the product streams changed from about 50 to about 50 to about 20,000 for normal-sinusoids. Example II This example shows the computer simulation of the main flow of methane, as shown above. The efficiency of the process described in the description of the removal of benzene and multi-carbon components from the flow of toluene burning before partial liquefaction is required. The indicated flow rate exists at 2.5 times using the liquefaction technology listed in Figures 1 and 2 10,000 metric tons / year of lng workers. The concentration of benzene in the methane-based gas stream used in this example is many in the process. However, the concentration of ethane and polycarbons in the gas stream has increased significantly, which means that there are more gas streams and more loads in the process of removing these components and benzene. This example is detailed The ability of the Ming process to remove benzene and multi-carbon hydrocarbons at the same time β In addition, this example shows that the benzene removal process can tolerate the obvious process damage that significantly increases the concentration of ethane and multi-carbon hydrocarbons without significantly affecting the benzene removal process. Efficiency and operability. Moreover, this example illustrates the ability of the process to recover multi-carbon hydrocarbons as a difficult to liquefy stream. Similar results were obtained using Hyprotech, Process Simulation HYSIM '386 / C2.10 Prop. Pkg PR / LK The ones listed in Table 4 are the temperature, pressure and phase conditions of the influent and effluent stream composition sent to the multi-carbon transfer tower. This simulation is based on a tower with 5 theoretical sections. Part of the condensation Flow (also known as two-phase flow) (the main part of it _ -48-) This paper size applies the standard of middle-paid family (c called eight 4 threats (2 [QX297 公 楚) &quot; ---- ~~ ί Please first Read the notes on the back and fill out this page} • Equipment. --6. Printed by the Consumer Cooperative of the Central Bureau of Standards of the Ministry of Economic Affairs 4266 6 5 λ Α7 Β7 '' &quot; 1 —. —. I V. Description of the invention (46) and then liquefaction) First feed into the upper stage of the tower (stage 丨). The temperature of this flow is -91'2 ° F, and the pressure is 596.0 psia. »As mentioned before, this flow is partially condensed ', so the flow is 94,04 mol% of steam. Feed into the lowest stage (stage 5) The methane-rich stream stripping system is from the upper flow location described in Figure 1. This flow is cooled to about -10 ° C with the liquid product stream produced in stage 5, countercurrent heat exchange. As can be seen from the table, this flow is partially concentrated during the cooling process. The ones listed in Table 5 are the simulated temperature, pressure and platform-to-velocity of each phase based on the middle section of the tower. Each of the paragraphs listed in Table 6 is the equilibrium composition of each liquid and steam. The efficiency of the multi-carbon removal process is combined by comparing the feed streams sent to stages i and 5 and the products of stage 1. Description of nitrogen, methane and ethane mole percentages. These percentages are 97.85, 97.30 and 99.37 mole percentages, respectively. This process therefore produces a product stream of significantly more of these light components than the two gas feed stream. The efficiency of the process for removing benzene and polycarbon aromatics is illustrated by comparing the concentration ratio for benzene as defined in Example 1. Individual mole fractions are 0.003E-04 and 0.00923. This results in a concentration ratio of about 30. An additional basis for explaining the efficiency of this process is that the concentration ratio of the C3 + component in the feed streams sent to stages 1 and 5 'is a liquid product stream made from stage i. This ratio ranges from about 19 in propylene to about 30 in n-octane. The individual ratios between the product streams changed from about 67 for propane to 19,000 for n-octane. -49- I paper size is applicable to China National Cricket (CMS) A4 size (210x297 male shame) ----- (Please read the precautions on the back before filling this page) Binding '4266 6 5, A7 B7 V. Description of the invention (47) Printed by the Consumer Cooperatives of the Central Standards Bureau of the Ministry of Economic Affairs I \ Composition and properties of the feed stream and similar product streams Feed stream 1-Product stream 1 Accompanying section 1 Accompanying section 5 Phase 1 Accompanying section nitrogen 5 0.0022 0.0007 0.002169 0.000107 co:. 0.75S7H-04 0.8806E-04 0.000075 0.000279 methane 0.9726 0.9686 '' 0.974167 0.55917S 1 ethylene oxide 0.0242 0.0296 0.0000 0.0000 0.023043 0357346 〇.〇〇〇〇〇〇〇.〇〇〇 〇〇〇 Propane 0.0005 0.0006 0.000404 0.026993 iso-butane 0.8998E-04 0.0001 0.000055 0.009050 n-butane 0.0001 0.000 i 0.000059 0.013291 iso-pentane OJ442E-04 0.403IE-04 0,000011 0.006026 n-pentane OJ340E ^ O4 0.403 IE-04 0.88ΪE, 05 0.006391 n-hexan 02424E-04 OJ023E-O4 '0.257E-05 0.005627 n-heptane 0.3230E-04 0.403 IE-04 0.125E-05 0.008054 n-octane OJ615E-04 OJ015E -04 0.221E-06 0.004132 benzene 0.1616E-04 0.20I5E-04 0.25SH-05 0.003526 n-nonane 0.0000 0.0000 0,000,000 〇〇〇〇〇〇〇〇Temperature-112.45eF -10.00eF -1I2J2 ° F -7S.09 * F pressure 587.01 psia 601.00 psia 587.00 psia 589.00 psia vapour% 98,24% 100% 100% 0.00% method to break Moore / hour) _ 60347.00 1203 ^ 0 61311.53 238.40 1 composition is Mo'er part base -50------ --- 7 &quot; Installation ------ Order ------ line --1--1.- ff (Please read the precautions on the back before filling this page) This paper is also applicable to Chinese national standards ( CNS) A4 specification (2 丨 OX297 mm) 4 2 6 6 6 5 ”a? B7 V. Description of the invention (48) \ Table 2 Simulation results of flow characteristics and fluid properties in the tower. 1. Section number temperature ° F Flow rate (lb mol / hr) Pressure, body vapor feed product stream I 5S7.0 -112.3 10603-'60347.01 61311.53 2 -587.5 -10S_2 917.8. 2024.9 5E8.0 • 101.1 761.5 1S82.4 4 SS8.5- 90.S 619.0 1726.1 5 589.0 -78.1 1583.5 '1203; »3 238.5 * The feed from i to 喑 1 is 98.24 mole% steam. 3 Product removed from stage 1, 100 mole% vapor. Feed from 4 to 陏 5, 100 mole% steam. Product removed from hydrazone section 5, 5.0 mole% vapor. -— &Lt; &quot; 丨 一 ----- (— fitting—— &lt; read the precautions on the back of the stain before filling in this page) Order printed by the Staff Consumer Cooperative of the Central Standard Bureau of the Ministry of Economy Applicable to China National Standard (CMS) A4 specification (2 丨 〇 X 297 mm) Λ2666 5 A7 B7 V. Description of the invention (49) Printed by the Shellfish Consumer Cooperative of the Central Standards Bureau of the Ministry of Economic Affairs \ Table 3 Simulated liquids leaving the theoretical sections / Vapor stream composition (mole parts) | Nitrogen CO: τ ethane ethane propane iso-butane n-butane phase I vapor 0.002169 0.00075 0.974167 0.023043 '0.000404 0.000055 0.000055 • liquid radon 0.000772 0.000173 0.874962 0.105444 0.006229 0.002030 0.002965 phase 2 Vapor 0.000811 0.000110 0.967766 0.030734 0.000436 0.000057 0.000059 Liquid 0,000263 0.000252 0.832784 0.145068 0.007288 0.002348 0.003425 &quot; Phase 3 vapor 0.000565 0.000144 0.954226 0.04439S 0.000514 0.000063 0.000064 Liquid 0.000159 0.000317 0.761049 0111924 0.00202 0.00286 0.00 0.004 0.004152 0.004152 0.000082 0. 000080 Liquid 0.000131 0.000329 0.669188 0J95174 0.013204 0.003786 0.005372 Phase 5 Vapor 0.000571 0.000154 0.913194 0.084077 0.00154S 0.000194 0.000191 Liquid 0.000107 0,000279 0.559178 0J57346 0.026933 0.009050 0.013291 -52- This paper is in accordance with the Chinese national standard (CNS &gt; A4% (210X) ) (Please read the notes on the back before filling out this page)-装., -Ιτ

4 266 6 5 ^ AV B7 V. Description of the invention (50) Printed by the Consumers' Cooperatives of the Central Bureau of Standards of the Ministry of Economic Affairs. Table 3 Simulated liquid / vapor composition (morning) leaving each theoretical section (Performance) Iso- 戍N-N-pentane n-hexane n-Heptane-n-Xinxuan * Benzene segment 1. Vapor 0.0000 Π S.81E-06. 2.S7E-06 125E-06 Z21E-07 2.58E-06 'Liquid Zhao 0.001331 0.001408 0.001236 0.001768 0.000907 0.000775 Dark segment 2 Vapor 0.00011 8.54E-06 239Έ ^) 6 1.Ι2E-06 I.90E-07 2.35E-06 Liquid 0.001536 0.001625 0.001427 0.002042 0.001047 0.000894 Stage 3 Vapor 0.00011 S.64E-06 2JOH -06 1.03EΌ6 L68E-07 2.17E-06 Liquid 0.001854 0.001961 0.001720 0.00246] 0.01262 0.001078 Paragraph 4 Vapor 0.000014 0.000010 2.60E-06 '1.Ι4Ε-06 1.80E-〇7 23 IE-06 Liquid 0.002328 0.002446 0.002125 0.00303] 0.001554 0.001332 Dark segment 5 Vapor 0.000033 0.000024 6.08EΌ6, 2.57E-06 3.93 £ -07 4.83E-06 liquid 0.006026 0.006391 0.005627 0.008054 0.004132 0.003526 -53- (Please read the precautions on the back before filling this page). This paper line scale applicable Chinese National Standard (CNS) A4 size (210 X 297 mm ί 426665. A7

7 B V. Description of the invention (51) Printed by the Consumer Cooperatives of the Central Bureau of Standards of the Ministry of Economic Affairs 4 \ Composition and properties of feed stream and analog product stream (Mole parts) Jinke stream 1 Product stream 1 Section 1 Stage 5 accompany section] nitrogen dark section 5 0.0024 0.0006 0.002301 0.000060 C02 0.7074E-04 0.SS51E-04 0.000072 0.000106 methane 0.9478. 0.9361 0.966005 0.3468S9 oxide 0.0283 0.0363 0.025421 0J45714 b 0.0000 0.0000 〇.〇〇〇〇〇〇〇 association. 〇〇〇〇〇〇 Propion antibody 0.0120 0,0145 0.005277 0 ^ 27598 iso-butane 0.0024 0.0030 0.000467 0.062744 n-butane 0.0028 0.0036 0.000367 0.07S635 iso-penta 0.0010 0.0013 0.000049 0.030295 n-pentane 0.0008 0.0011 0.000026 0.024383 n- Hexane 0,0013 0.0018 0.000012 0.043792 n-heptane 0.0007 0,0010 0.I70E-05 0.024376 n-octane 0.0002 0.0003 0.111E-06 0.006019 benzene 0.0003 0.0004 0JZS3E-05 0.009229 n-nonane 0.4853E-05 0.6724E -, 05 0.851E-09 0.000160 temperature -91.20 ° F -10.00eF -88.19 ° F -3L98eF pressure 596.01 psia 610 psia 596.00 psia 59S.00 psia vapor% 94.04¾ 98.94 % 100% 0.00% Flow rate mol / h 57109.78 766S.00 62724.19 2053,60 1 The composition is based on mol content -54- This paper size applies Chinese National Standard (CNS) A4 specification UlOX297 mm) 1 · --7 ----- 「Installation ------ Order ------ (. Line I *-f (please read the precautions on the back before filling this page)) Printed by the Industrial and Commercial Cooperatives 4266 6 5, A7 B7 V. Description of the invention (52) Table 5 Simulation results of the flow characteristics and flow characteristics in the tower Dark section number Pressure temperature eF — Flow rate (pound mol / hour) Liquid. _-Steam-feed product stream i 1 596.0 -88.2 3345.9 57109.8 '62724 ^ 1 2 -596.5 -67.6 2905.8 8960J 3 597.0 -52.5 2680.0 8520J2 4 597 * 5 -423 2439 * 5 8294,4 5 598.0 • 32.0 8053.9 7668.0 ^ 2053.6 '^ The feed to the accompanying section 1 was 94.04 mole% steam. 3 Product removed from stage I, 100 mole% vapour. ^ Feed to stage 5, 98.94 mole% vapour. Product removed from stage 5, 5.0 mole% vapor. — ·-； ----- 「I—— (Please read the precautions on the back before filling this page) -55- This paper size applies to China National Standard (CNS) A4 (210 X 297 mm) 426665

7 7 AB V. Description of the invention (53), Table 6 Simulated liquid / vapor composition (mole fraction) leaving each theoretical section | nn cos pinane ethyl iso-butane-n-butane: stage 1 vapor: 0.00231 0.000072 0.966005 0.025421 0.005277 0.000467 0.000367 Liquid Miscellaneous 0.000359 0.000153 0.589261 0.132705 0.130329 0.033700 0.041711 _ ... .... Paragraph 2 Vapor 0.000640 0.000108 0.941610 QM7V92 0.00XS98 0.000776 0.000615 Liquid 0.000085 0.000178 0.476845 0.190340 0.161161 0.039734 0.048783 480 Vapor 陏 Segment 0.013142 0.001134 0.000905 Liquid 0.000069 0.000 J 57 0.415375 0.208673 0.187549 0.044244 0.053S20 Dark segment 4 Vapor 0.000569 0.000106 0.913713 0.064872 0.017638 0.001540 0.001229 Liquid 0.000065 0.000130 0J80377 0.191896 0.216335 0.050645 0.061013 Sui204 5 Vapor 0.000582 0.000497 0.001 0.02 0.099 0.0993 0.9993 0J22759S 0.062744 0.078635 (Please read the precautions on the back before filling this page) -In the gutter economy department Printed by the Central Bureau of Standards Consumer Cooperatives-56- This paper size is applicable to China National Standard (CNS) A4 (210 X MM mm) 426665. A? B7 V. Description of the invention (54) Table 6 Simulation without theories Liquid / Vapor Composition (Mole Parts) (碛) Iso-pentane n-pyridine n-hexane n-heptane n-octylbenzene E-nonane hydrazone 1 Vapor 0.000049 0.0C0026 0.000012 1.70E-06 -L1IE-07 2.S3H-06 8.51E-10, Yea 0.015796 0.012679 0.022699 0.012625 0.003116 0.0047S4 0.0000S3 Phase 2 — Vapor 0.000084 0.000046 0.000021 326E ^ 6 223E-07 4.90E * O6 1.78E-09 liquid 0.018298 0, 014662 0.026170 0,014543 0.0035SS 0.005516 0.000095 Phase 3 Vapor 0.000126 0.000069 0.000034 S.40E-06 3.S7E-07 ΊΜΈτ06 321Ε-09 Liquid 0.01W70 0.015971 0.02S4I4 0.015775 0.003S9] '0.00598 $ 0,000103 Steam segment 0 , 000171 0.000095 0.000047 7.71Ή-06 5.67E4Π 0.000010 4.S2E-09 liquid 0.022257 0.017730 0.03J3IA 0.017348 0.004276 0,006598 0.000114 dark segment 5 vapor 0.000273 0.000154 0.000079 0.000013 9.77E-07 0.000017 8.41E -09 Liquid 0.030295 0.0243S3 0.043792 0.024376 0.006019 -0.009229 0.000160 C Please read the notes on the back before filling out this page) Packing--¾ Printed by the Employees' Cooperatives of the Central Standards Bureau of the Ministry of Economic Affairs Home Sample Standard (CNS) A4 Regulation Road (210X 2 ~ 7mm)

Claims (1)

Printed by the Central Government Bureau of the Ministry of Economic Affairs and Consumer Cooperatives ft 4 2 66 6 5 λ Patent Application No. 86106889 Patent Amendment of Chinese Patent Application Range (November 89) Α8 Β8 C8 D8 Revised Benefit range tonic * 1. A method for removing and concentrating higher molecular weight hydrocarbons from a gas stream mainly based on formazan, including the following steps: (a) Make the secondary part of the gas stream mainly methane Condensation, thus producing a one-phase flow, (b) feeding the two-phase flow into the upper section of the tower, (c) removing a less carbon-rich gas stream from the upper section of the stripper, (d) from the steam The lower part of the lifting tower removes the polycarbon-rich liquid stream. (E) Through indirect heat exchange, the polycarbon-rich liquid stream is brought into contact with the methane-rich stripping gas stream, thus generating a warm rich The flow of polycarbons and the cooled methane-rich stripping gas stream; (f) feeding the cooled methane-rich stripping gas stream into the lower section of the tower; and (g) the two-phase stream and the cooled The methane-rich stripping gas stream is contacted in the column, thereby producing a polycarbon-free gas stream and a polycarbon-rich liquid stream. 2. The method according to item 1 of the scope of patent application, wherein step (a) includes dividing a gas stream mainly composed of methane into a first flow and a second flow, and cooling the first flow, thereby generating a partially condensed first Flow, and a first flow and a second flow combining the part of the condensation, thus producing the two-phase flow. 3. The method according to item 2 of the scope of patent application, wherein the amount of liquid in the two-phase flow is determined by measuring the temperature of the two-phase flow equivalent to the liquid content required under equilibrium conditions for the methane-based gas flow, and maintaining the first flow. Fixed / second speed, and cooling the temperature of the two-phase flow in the flow, and adjust the reaction ________ (install ______ order --- t please read the precautions on the back and fill in this f) this paper For the standard, China National Sample Standard (CNS) A4 (210X297 mm) 8 8 8 8 ABCD 426665 a Patent Application Scope—The second flow velocity of the phase flow temperature, so that the two-phase flow temperature is the calculated two-phase flow temperature control. 4. The method according to item 1 of the scope of patent application, further comprising the following steps: (h) before step (a), contact the first refrigerant flow by passing the flow through at least one indirect heat exchange device, so Generate a cooled methane-based airflow, and pass the cooled methane-based airflow through at least one indirect heat exchange device, contact the second refrigerant stream to continuously cool the methane-based airflow, of which the second cold The boiling point of the agent stream is lower than the boiling point of the first refrigerant stream, so that a feed stream is sent to step (a). 5. The method according to item 4 of the scope of patent application, wherein the main part of the first refrigerant stream includes propane, and the main part of the second refrigerant stream includes ethane, ethylene or mixtures thereof 6. According to the scope of patent application The method of item * further includes: (0 extract the side flow from the air stream mainly dominated by burning at the flow under one of the indirect heat exchange equipment, and use the side flow as the rich in step (e) Methane-containing stripping gas β 7. The method according to item 4 of the scope of the patent application, wherein the first cold is contacted by at least-an indirect heat exchange device; the cooling of the east stream includes the milk stream to be cooled according to Continuously flowing through two or more interfacing heat exchange equipment 'and the first refrigerant sent to each indirect heat exchange equipment is flashed to a lower temperature and pressure in a sequential manner, and where at least one indirect Heat exchange equipment, the cooling system in contact with the second refrigerant stream includes the air stream to be cooled to flow through two or more indirect heats in order.-This paper is especially used in China National Standard Half (CNS) Α4ί) (洛 （2 [〇x297 ^ 瘦 y * (please first Please read the notes on the back of the product, and then fill out this page.) Install, tr Printed by the Ministry of Economic Affairs and the Central Bureau of Work and Consumer Cooperatives Printed by the Ministry of Economic Affairs and the Central Government of the Bureau of Work and Consumer Cooperatives 4 266 6 5 ^ as C8 _____ D8 Sixth, the scope of patent application ~~~ ^ --- exchange equipment, and the second refrigerant sent to each heat exchange equipment are flashed to a lower temperature and pressure in a consistent and sequential manner. 8 'According to the scope of patent application The method of item 7, wherein three indirect heat exchange devices are used for the cooling of the first refrigerant, and two or three indirect heat exchange devices are used for the cooling of the second refrigerant stream. 9. According to the scope of patent application The method of item 7, wherein the pressure of the feed gas mainly based on formazan is 500 to 900 psia 〇10. The method of item 7 of the scope of the patent application, wherein the pressure of the feed gas based on formazan is 575 Up to 650 psia. 11. The method according to item 10 of the patent application park, further comprising: (i) inserting a side flow from a gas stream mainly dominated by torrefaction at the flow under one of the indirect heat exchange equipment, and Use this side flow as the rich in step (e) Stripping gas from methane 12. The method according to item 1 of the scope of patent application, further comprising: (h) feeding the warm polycarbonate-rich flow of step (e) into a waste separator, reboiler and In the demethanizer of the condenser, a multi-carbon-rich liquid stream and a methane-rich vapor stream are thus made. 13. According to the method of claim 12 in the scope of the patent application, the cooling function of the main part of the condenser is provided by The multi-carbon-rich liquid stream generated in step (d) or step (e) is provided. 14. The method according to item 12 of the scope of patent application 'wherein the cooling function of the main part of the condenser is provided by indirect heat The exchange device 'is provided in contact with the carbonaceous-rich liquid stream of step (d), and the resulting treated carbonaceous-rich liquid stream becomes a polycarbonate-containing feed stream to step (e) . -3- The paper size is applicable «« Furniture Standard (CNS &gt; A4 Washing (210x297mm) (Jingxian W read the precautions on the back before filling out this page), Ding-St 42666B A8 B8 C8 D8 Ministry of Economic Affairs Printed by the Central Bureau of Shellfish Consumer Cooperatives *. Application for patent scope 15, according to the method of item i 3 of the patent scope, where the cooling function is divided into the first steam stream and the first steam stream The two vapors and streams' are cooled or partially condensed by indirect heat exchange with the multi-carbon-rich liquid stream in step (d), thereby generating a cooled, partially condensed first flow, combined with the first The flow and the second flow, the combined flow is fed into a gas-liquid separator, which is provided by the reflux flow and methane-rich vapor flow that are sent to the fractionation column. 16. According to item 15 of the scope of the patent application Method, in which the flow rate of the reflux flow is calculated by calculating the temperature of the two-phase flow corresponding to the required liquid content under equilibrium conditions for the overhead distillate vapor flow, measuring the first flow maintaining a constant flow rate, and cooling the flow Two phase flow temperature 'and adjust The flow rate of the second flow that reflects the temperature of the two-phase flow is controlled so that the temperature of the two-phase flow is the calculated temperature of the two-phase flow. According to the method of the scope of application for item 13, another step is included between steps (d) and (e) The additional steps are: (i) Flashing the polycarbonate-rich liquid stream to a low pressure, thereby further reducing the temperature of the flow. 18. According to the method of item 7 of the patent application scope, the additional step is (j ) Condensing a non-carbonaceous gas stream, thus producing a liquefied natural gas stream. 19. The method according to item 18 of the scope of the patent application, wherein the condensation includes passing the non-carbonaceous gas stream through cooling with the second refrigerant stream. Indirect heat exchange equipment. 20 · Method according to item 19 of the scope of the patent application 'wherein the pressure of the methane-based gas stream is 500 to 900 psia. 4 The paper is selected to make the national standard (CNS) M wash building (2IOX297 mm) (Please read the notes on the back before filling out this page) Binding Application Patent Fangu A8 B8 C8 D8 Printed by the Consumers' Cooperatives of the Central Automobile Bureau of the Ministry of Economic Affairs 2 square In addition, the steps include (k) flashing the liquefied product of step (j) to atmospheric pressure in one or more steps so as to produce an LNG product stream and one or more methane vaporized oxygen I streams; (0 will step 骡(K) the main vapor stream is compressed to a pressure of 500 to 900 psia; (m) the compressed vapor stream of the cooling step (1); and (η) the obtained cooling liquid stream and the feeding step (a) are fed with methane The main gas stream or the product combination of one of the heat exchange devices connected between step (h). 22. The method according to item 21 of the patent application scope, wherein the step (h) -rich vapor stream is in step (I) is combined with one of the vapor streams of step (k). 23- The method according to item 2i of the scope of patent application, wherein the pressure of the methane-based gas stream and the gas stream from step (1) is 575 to 650 psia. 24. The method according to item 1 of the scope of patent application, where the tower provides two to fifteen theoretical sections of gas-liquid contact. 25. The method according to item i of the scope of patent application, 'where the tower provides three to ten gases. -The theoretical section of liquid contact. 26. According to the method of item 23 of the scope of patent application, the order of the tower provides two to fifteen theoretical sections of gas-liquid contact. 27. According to the method of item 23 of the scope of the patent application, the tower is provided with three to ten theoretical segments of gas-liquid contact = 28. — a kind of f-removing gas and other aromatics The size of the square wood paper is in Chinese National Standard (CNS) A4 (210X297 mm) (Please read the precautions on the back before filling this page) Binding. Order 3 ». Α8 A Β8 C8; ---- ~ --- 7 λ Patent application scope D8 Printing method of the Central Government Bureau of the Ministry of Economic Affairs, Consumer Cooperatives, including the following steps: (a) Condensing the secondary part of the aunt; the main gas stream is condensed, so Two-phase flow, (b) feeding the two-phase flow into the upper section of the tower, (c) removing less benzene / aromatic gas stream from the upper section of the stripper, (d) from the stripper The lower stage removes the benzene / aromatic-rich liquid stream, (e) contacts the stony / aromatic-rich liquid stream with the methane-rich stripping gas stream through indirect heat exchange, thereby generating a warm rich Benzene / aromatic flow and cooled methane-rich stripping gas stream; (0 feed this cooled methane-rich stripping gas stream into In the lower section; and (g) contacting the two-phase stream and the cooled methane-rich stripping gas stream in the column, thereby producing a benzene / aromatic-free gas stream and a benzene / aromatic-rich liquid stream. 29. The method according to item 28 of the scope of the patent application, wherein step (a) includes dividing the methane-based gas flow into a first flow and a second flow to cool the first flow, thereby generating a partially condensed first flow. A flow, and a first flow and a second flow that combine the partial condensation, thus producing the two-phase flow "30. According to the method of item 29 in the scope of the patent application, wherein the amount of liquid in the two-phase flow is determined by The temperature of the two-phase flow equivalent to the liquid content required under equilibrium conditions for the methane-based air flow, the measurement of a certain flow rate to maintain the first flow, and the temperature of the two-phase flow that cools the flow, and adjust the anti-6-this paper For the scale, use the two naked rates of Shen Guo (〇 ^> 8 4 specifications (210 father 297 mm) (please read the note on the back before filling this page) binding 4266 65, A8 B8 C8 D8 Bureau of Industry and Consumer Cooperatives, India The beneficial range should be the second-phase flow temperature of the second flow velocity 'making the two-phase flow temperature to be the calculated two-phase flow temperature control. 31. The method according to item 28 of the scope of patent application' also includes the following step screw: (h ) Prior to step (a), the flow is brought into contact with the first refrigerant stream by passing the flow through at least one indirect heat exchange device, thereby generating a chillane-based gas stream, and cooling the methane-based gas stream Flowed through at least one indirect heat exchange device 'in contact with the second cold; east agent stream to continuously cool the main methane gas stream', where the boiling point of the second refrigerant stream is lower than the boiling point of the first refrigerant stream, thus generating a sending step (A) The feed stream. 32. The method according to item 31 of the scope of the patent application, wherein the main portion of the first refrigerant stream includes propylene and the main portion of the second refrigerant stream includes ethane, ethylene, or a mixture thereof. 33. The method according to item 31 of the scope of the patent application 'still includes: (i) extracting the side flow from the gas stream mainly dominated by torrefaction at the flow under one of the indirect heat exchange equipment, and using that side flow as The stripping gas rich in Jiapo in step (e). 34. The method according to item 31 of the scope of patent application, wherein the cooling system in contact with the first refrigerant stream by at least one indirect heat exchange device comprises passing the gas stream to be cooled through two or more indirect streams in a continuous manner. Heat exchange equipment, and the first refrigerant sent to each indirect heat exchange equipment is flashed to a lower temperature and pressure in a consistent manner, and at least one indirect heat exchange equipment is used to cool the second refrigerant; The cooling contacted by the agent flow includes causing the air flow to be cooled to sequentially flow through two or more indirect dimensions of the paper. National Standards (CNS) 6-4 gauge pan (2! 0 × 297 mm) --- ----- ΐ 装 — (Please read the note on the back ^ before filling out this page) Order the paper size printed by the Central Standards Bureau of the Ministry of Economic Affairs, Shellfish Consumer Co., Ltd. and use the Chinese National Standard (CNS) A4 (210X297 male dust) 4 2 6 6 6 5 A8 B8 C8 ____— D8 6. Apply for patent Fangu heat exchange equipment, and the second refrigerant sent to each indirect heat exchange equipment is flashed to the Low temperature and pressure. 35. The method according to item 34 of the scope of patent application, wherein the cooling system for the first refrigerant uses three indirect heat exchange devices, and the cooling system for the second refrigerant stream uses two or three indirect heat exchange devices. According to the method in the scope of application for the patent No. 34, the pressure of the feed gas mainly based on Jiejie is from 500 to 900 psia. 37. The method according to item 34 of the scope of patent application, wherein the pressure of the feed gas mainly composed of methane is 575 to 650 psia. 38. The method according to item 37 of the scope of application for patents, further comprising: (i) taking the side flow of the main air stream mainly from tofu and using the side flow as the flow under one of the indirect heat exchange equipment; The methane-rich stripping gas in step (e) is used. 39. The method according to item 28 of the scope of patent application, further including: (h) adding the warm 冨 / benzene-containing flow word of step (e) into the fractionation including fractionator, reboiler and condenser In the reactor tower, a benzene / aromatic-rich liquid stream and a methane-rich vapor stream are thus made Φ 40. According to the method in the scope of patent application No. 39, the cooling function of the main part of the condenser is performed by step (d ) Or step (e) provides a benzene / aromatic rich stream. 41. The method according to item 39 of the scope of patent application, wherein the cooling function of the main part of the condenser is provided by flowing through the indirect heat exchange equipment and in contact with the benzene / aromatic rich liquid stream of step (d), And the resulting stupid / aromatic-rich liquid stream is sent to step (e) with benzene / aromatic -8- — 1 (please read the note on the back ^ before filling this page) binding Ordered by the Ministry of Economic Affairs of the Central Bureau of quasi-government shellfish consumer cooperation Du printed 426665 β Α8 Β8 C8 ___ D8 6. The patent application scope feed flow. 42. The method according to item 40 of the scope of patent application, wherein the cooling function is divided into a first vapor stream and a second vapor stream by separating the vapor stream distilled from the top of the column, and the benzene-rich / Aromatic liquid flow indirect heat exchange 'cools or partially condenses the first flow, thereby generating cooling, partially condensed first flow, combining the first flow and the second flow' feeds the combined flow into the gas -In the liquid separator, it is provided by the reflux flow and methane-rich vapor flow that are sent to the branch tower. 43. The method according to item 42 of the scope of the patent application, wherein the flow rate of the reflux flow is calculated by maintaining the first-phase temperature of the two-phase flow equivalent to the required liquid radon content under equilibrium conditions for the vapor flow of the overhead distillate, and measuring the first A certain flow rate of the flow, and a temperature of the two-phase flow that cools the amount of the flow, and the flow rate of the second flow that adjusts the temperature of the one-phase flow is adjusted so that the temperature of the two-phase flow is the calculated temperature of the two-phase flow. 44. According to the method of the scope of patent application No. 40, the additional steps included between step snails (d) and (e) are: (i) the benzene / aromatic rich liquid stream is flashed to a low pressure, so The temperature of the flow is further reduced. 45. The method according to item 44 of the scope of the patent application, further comprising the step of (j) condensing a benzene-free / aromatic gas stream, thereby producing a liquefied natural gas stream. 46. The method according to item 45 of the patent application park, wherein the condensing comprises passing a benzene-free / aromatic gas stream through an indirect heat exchange device cooled by the second refrigerant stream. The size of this paper adopts the Chinese National Standards (CNS) M specifications (210X297 mm) -------- f Loading ------ ΐτ ------ ^ 』(Please read« Note on the back page, please fill out this page again} 888ύο ABCD 266 6 5 VI. Patent Application Range 47: According to the method of Patent Application Range Item 46, the pressure of the methane-based gas flow is 500 to 900 psia. 48 · According to The method claimed in item 47 of the patent application scope further comprises the step of (k) flashing the liquefied product of step (j) to atmospheric pressure in one or more steps, thereby producing an LNG product stream 'and one or more methane distillations (1) compressing the main vapor stream of step (k) to a pressure of 550 to 900 psia; (m) cooling the compressed vapor stream of step (1); and (η) combining the resulting cooling liquid stream with Combining the products obtained by feeding the gas stream dominated by methane in step (a) or one of the heat exchange equipment connected between step (h). 49. The method according to item 48 of the scope of patent application, wherein step (h) is rich in The vapor stream of methane is combined with one of the vapor streams of step (k) before step (0). The method of item 8 'wherein the pressure of the methane-based gas stream and the pressure of the gas stream from step (1) is 575 to 65 psia. 51. According to the method of patent application No. 28, wherein the tower provides two to fifteen A theoretical section for gas-liquid contact. 52. The method according to item 28 of the patent application scope, in which the tower provides three to ten theoretical sections for gas-liquid contact. 33. A method according to item 50 scope of the patent application. Among them, the tower provides two to fifteen theoretical segments of gas-liquid contact. 54. According to the method of applying for patent No. 50 in the patent park, the tower provides three to -10- of this paper. (CNS) M-shaped (21 () &gt; &lt; 297 male 0 —- (Please read the note on the back before filling out this page) Bookbinding Ministry of Economic Affairs, Ministry of Economic Affairs, Bureau of Economic Affairs, Printing, Ministry of Economic Affairs Central government bureau shellfish consumer cooperation. Printed by the agency 4266 6 5 &gt; A8 B8 C8 D8 --------------. ——— #, Ten patent applications for gas-liquid contact Theoretical paragraph 55. A device for removing and concentrating higher molecular weight hydrocarbons from a methane-based gas stream, including: U) a condenser (b) A tower for extracting lighter components from a liquid phase of a two-phase liquid-gas methanol stream using a cooled formic acid-rich stripping gas: (c) Heat exchange providing indirect heat exchange between two fluids (D) a conduit for passing a two-phase flow to the tower between the condenser and the upper section of the tower; (e) a second conduit for connecting the upper section of the tower for removing the vapor stream from the tower; (f) the The tower and the heat exchanger are used as conduits for cooling airflow of the heat exchanger; (g) The tower and the heat exchanger are used as conduits for liquid flow from the tower; (h) Ducts for the warm liquid flow of the heat exchanger; and (i) ducts connected to the heat exchanger for the flow of air to the heat exchanger. 56. The device according to item 55 of the scope of patent application, further comprising: (j) a first conduit: (k) a separation device connected to the first conduit; (l) a second and third conduit connected to the separation device, wherein The second pipe is connected to the condenser; (m) the control valve connected to the third guide and pipe on the input side: -11-This paper size applies the Chinese National Standard (CNS) S1 wash grid (2 〖0x297 mm) (Please read the precautions and fill in this page first) Order 426665 A8 B8 C3 D8 Printed by the Central Ministry of Economic Affairs and the Li Bureau of Beigong Consumer Cooperative «. 'Scope of patent application (n) connected to the output side of the control valve; (〇) the joining or joining equipment of the conduit of the component (£ 1) and the conduit of the component (d) before being connected to the tower; (p) in the conduit of the component (d) between the joining equipment, and Temperature sensing equipment with sensing element connected to the tower; and (q) control valve operatively attached to element (m) and control equipment operatively responding to input and temperature setting of temperature sensing equipment received from element (P) 》 57. The device according to item 55 of the scope of patent application, Comprising (i) of the catheter (g) under reduced pressure in the apparatus. 58_Apparatus according to item 55 of the scope of patent application, wherein the tower contains 2 to 12 theoretical sections. 59. Apparatus according to item 55 of the scope of patent application, further including one or more heat exchanges arranged in a continuous manner. Equipment, used to make the general fluid flowing through the heat exchanger continuously flowing between the heat exchange equipment, and the last pipe is connected to the condenser of element (a), sent to and from each heat exchanger, The refrigerant is used to flow the refrigerant to each heat exchanger, and the conduit of element (i) is in fluid communication with one of the above-mentioned conduits for general fluid flow between the heat exchangers. 60. Apparatus according to item 59 of the scope of patent application, wherein propane is used as a refrigerant in at least two heat exchange equipment; and acetylene, ethyl ether or a mixture thereof is used as refrigerant in at least two heat exchanger equipment . 61. The device according to item 55 of the scope of patent application, including: (j) fractionation tower; -12- This paper scale is free to use China «Furniture Ratio (CNS) A Gu I grid (2 丨 0X297 mm) ( (Please read the precautions on the back before filling this page) Binding H: In the Ministry of Economic Affairs * 橾 Associate Bureau Bei Gong Xiao F cooperative print 4 2 6 6 6 5 A8 J B8 C8 __ D8 6. Scope of patent application (k) Re-boiler; (l) condenser; (m) an overhead distillate duct that connects the upper section of the tower and the condenser to remove the overhead distillate vapor, connects the condenser to the tower, and makes the reflux liquid cross The return duct is connected to the condenser to remove the vapor product duct of uncondensed vapor; (η) Connect the lower section of the tower to the bottom duct of the reboiler to return the stripped steam to the vapor duct in the tower, and connect To the reboiler, remove the bottom product line of the non-evaporated product from the reboiler; and the conduit of element (h) is connected to the fractionation column at a point between the top and bottom theoretical section. 62. The device according to item 61 of the scope of the patent application, in which the condenser of element (1) includes indirect heat exchange equipment and coolant, and this equipment is a conduit connected to the cooling side of the refrigeration equipment and the component (g) The joint is provided. 63. The device according to item 61 of the scope of patent application, further includes (0) a pressure reducing device located in a duct (g), wherein the condenser of the component (1) includes an indirect heat exchange device and a coolant sent to the device It is provided by the pipe joint connecting the cooling surface of the indirect heat exchange equipment and the downstream component (g) of the decompression equipment (0). 64. The device according to item 61 of the scope of the patent application, further comprising: (〇) the conduit of the condenser connected to the component (a), (P) the compression of the vapor conduit line connected to the input (red) to the component (m) And (q) at the output cylinder of the compressor element (p), connected to the element (〇) -13- This paper size uses two Chinese standards (CMS) 8 4 size (210X297 male dust)- ------- f Pack 丨 .----- Order ------ ί '(Please note the items on the back of wtl before filling in the page) 4 2 66 6 5 Aa * Ao B8 C8- -~ ----____ 6. The conduit of the patent-applied duct β 65. The device according to item 5 of the scope of the patent application, including: (j) Fractionation tower: (k) Re-boiler; U) Condenser (M) Connect the upper section of the tower to the condenser to remove the overhead vapor pipe from the overhead vapor, connect the condenser and the tower, and the return pipe to return the reflux fluid to the condenser to remove Vapor product duct for uncondensed vapor; (η) Connect the lower section of the tower to the bottom duct of the reboiler, return the stripped steam to the vapor duct of the tower, and connect to the reboiler; self-recook Removal of unvaporized product of the bottom product in line, and wherein the midpoint position of the catheter-based device (h) of the. 66. The device according to item 65 of the scope of patent application, further comprising: (〇) a compressor connected to the vapor conduit line of the component (m) at the input cylinder, and (P) an output cylinder connected to the compressor to the application It is one of the general flow ducts of Patent Fanyuan No. 59. Printed by the Ministry of Economic Affairs and the Central Government Bureau of the Ministry of Economic Affairs and Cooperatives (please read and read the notes on the back and fill in this page) 67. — A device for providing a heat exchanger to control the separation tower, including: (a) using A refrigeration separation tower that partially condenses the feed gas stream in the LNG recovery process; (b) equipment that produces a liquid condensate stream from the refrigeration separation tower; (c) a heat exchanger combined with the refrigeration separation tower; (d) Equipment for passing the liquid condensate stream through the heat exchanger; and • 14-This paper size applies to the country's national rate (CNS) A4 specification (2 丨 0 &gt; &lt; 297 mm) 426665 Λ Α8 Β8 C8- --- --- D8 _ VI. Patent application scope (e) The warm dry air stream is passed through the heat exchanger and then sent to the equipment of the refrigeration separation tower, where the warm dry air stream is indirect heat Exchange, cooling with the liquid condensate stream of the heat exchanger; (f) which has a first control valve configured for operation to allow the warm, dry air stream to bypass the heat exchanger bypass duct; (g) The actual temperature of the warm and dry air stream representing the exit of the heat exchanger Equipment for the first signal; (h) equipment for generating a second signal representing the actual temperature of the liquid condensate stream entering the heat exchanger; (0 for dividing the first signal by the second signal to A device generating a third signal representing the ratio of the first signal to the second signal; (j) a fourth signal for establishing the expected value of the ratio represented by the third signal; (k) comparing the third signal with the The fourth signal equipment to establish a fifth signal that reflects the difference between the three signals and the four signals, where the fifth signal is marked to represent the actual ratio represented by the third signal is substantially equal to the fourth signal The expected ratio indicated is the position of the first control valve required; and the employee ’s cooperative of the Cooperative Bureau of the Ministry of Economic Affairs is printed (please read the precautions on the back before filling this page) (m) reflect the fifth signal Equipment for operating the first control valve in the bypass duct. 68. The device according to item 67 of the scope of patent application, further comprising: establishing markings required to maintain the desired liquid level in the refrigeration separation tower The liquid The sixth signal of the condensate flow stream equipment: -15- and this paper ": _ scale Bu neutralized with abusers out of home (Fang milk) eight Regulation ^ 4 cells (210 &gt; &lt; 297 mm) - 426 665 ** Equipment for controlling the flow rate of the liquid condensate stream in response to the sixth signal. (Please read the precautions on the reverse side before filling out this page) 69. The device according to _Please Patent No. 6 8 also includes: a second control valve operatively configured to control the flow of the warm and dry air flow; and the reaction A device selected from the group consisting of the following temperature versus temperature to operate the second control valve: l The actual temperature at which the warm dry air stream leaves the heat exchanger; and 11 The actual temperature at which the liquid condensate stream leaves the heat exchanger. 70. The device according to item 69 of the scope of patent application, wherein the device for operating the second control device comprises: establishing a device representing a seventh signal of the actual temperature of the liquid condensate stream leaving the heat exchanger; establishing a representative Equipment for the eighth signal of the desired temperature of the liquid condensate stream leaving the heat exchanger; comparison of the seventh signal and the eighth signal equipment by the Central Labor Bureau of the Ministry of Economic Affairs, Zhengong Consumer Cooperative, to establish a response to the seven signal The ninth signal that is different from the eight signal, wherein the ninth signal is marked to represent the actual temperature of the liquid condensate stream leaving the heat exchanger indicated by the seventh signal is substantially equal to the eighth signal The position of the second control valve required for the desired temperature; a device for establishing a tenth signal representing the actual temperature of the warm and dry airflow leaving the heat exchanger indicated by the second signal; comparing the second signal And the equipment of the tenth signal 'to establish a response -16 * This paper size is in accordance with the Chinese standard i CNS) A4 this grid (210X297 mm) ^ 26665 The patent claims the eleventh signal between the second signal and the tenth signal difference, where the eleventh signal is marked to represent the actual temperature of the warm and dry airflow leaving the heat exchanger is substantially The position of the second control valve equal to the desired temperature represented by the tenth signal; a device for establishing the twelfth signal selected as one of the ninth signal and the eleventh signal having a higher value ; And an apparatus for activating the second control valve that responds to the twelfth signal. 71. A control device having a method in which the temperature in a heat exchanger operatively connected to a bypass duct of a first control valve is connected to a refrigeration separation tower that removes benzene contamination from the feed stream and the LNG recovery process. In combination, the method includes: extracting a liquid condensate stream at a freezing temperature from the refrigeration separation tower: passing the liquid condensate stream through the heat exchanger; passing a warm dry air stream through the heat exchanger, and then introducing the warm dry air stream In the refrigerated separation tower, the warm and dry airflow is indirectly heat exchanged, and the liquid condensate in the heat exchanger is used to warm; a signal representing the actual temperature of the warm and dry airflow leaving the heat exchanger is established; a representative is established A second signal leaving the heat exchanger of the temperature of the liquid condensate stream; dividing the first signal by the second signal to establish a third signal representing a ratio of the first signal to the second signal; establishing a representative signal representing the The fourth signal that the third signal wants; -17- This paper size is in use «« Home Standard (CNS) A4 Washing Pile (210XW7 mm). {装 ir- (Please read the note on the back first (Please fill in this page for the matters needing attention)) Printed bags for shellfish consumer cooperatives of the Central Procurement Bureau of the Ministry of Economic Affairs 426665 Printed by the Shellfish Consumer Cooperative of the Central Bureau of Economic Affairs of the Ministry of Economic Affairs11. Applying for a special application ® ^ Compare the third signal and the fourth signal and establish a fifth signal that reflects the difference between the three signals and the tetrasine, of which the fifth The signal is marked to represent the position of the first control valve required to maintain the actual ratio indicated by the third signal substantially equal to the desired ratio indicated by the fourth signal; and the fifth signal is reflected to operate the The first control valve in the bypass conduit. 72. The method according to item 7 of the scope of patent application, further comprising the following steps: establishing a sixth signal marked to represent the flow rate of the liquid condensate stream required to maintain the desired liquid level in the refrigeration separation tower; and controlling the reaction The flow rate of the liquid condensate stream should be the sixth signal. 73. According to the method of claim 7, wherein the second control valve is operatively configured to control the flow rate of the warm drying air stream, the method further includes the following steps: the reaction is selected from the group consisting of the following temperature versus temperature, Make the second control room operate: 1 'the actual temperature at which the warm and dry air stream leaves the heat exchanger; and ii. The actual temperature at which the liquid condensate stream is difficult to open the heat exchanger a 74-according to item 73 of the scope of the patent application A method, wherein the step of operating the second control valve includes: a seventh signal from a construction representative representing the actual temperature of the liquid condensate stream leaving the heat exchanger; establishing a desired temperature representing the liquid condensate stream leaving the heat exchanger -1β-This paper is difficult for those who are in trouble 丨 0X297 mm) (Please read the precautions on the back before filling this page) 袈 4 2 666 5 A8 BS C8 D8 6. The eighth signal of the scope of patent application; Compare the seventh signal and the eighth signal to establish a ninth signal that reflects the difference between the seven signal and the eight signal, where the ninth signal is marked to represent the seventh signal table The actual temperature of the liquid condensate stream leaving the heat exchanger is substantially equal to the position of the second control valve required by the desired temperature represented by the eighth signal. Tenth signal of the actual temperature of the warm and dry air stream of the device: comparing the second signal and the tenth signal to establish an eleventh signal that reflects the difference between the second signal and the tenth signal, of which the eleventh signal The position of the second control valve marked to represent that the actual temperature of the warm and dry airflow leaving the heat exchanger is substantially equal to the desired temperature represented by the tenth signal; the selection is established as having a higher value The ninth signal and the twelfth signal of one of the eleventh signals; and actuating the second control valve that reflects the twelfth signal β 75. The method according to item 71 of the scope of patent application, wherein the The LNG recovery process is a cascade refrigeration process using three different types of freezing aa (please read the precautions on the back before filling this page). The paper size is free to use China * furniture standard (CNS) A4 ^ (210X297 mm)