CN1509262A - Method for ethane recorery, using refrigeration cycle with a mixture of at least two coolants, gases obtained by said method and instalation thereof - Google Patents

Method for ethane recorery, using refrigeration cycle with a mixture of at least two coolants, gases obtained by said method and instalation thereof Download PDF

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Publication number
CN1509262A
CN1509262A CNA028055640A CN02805564A CN1509262A CN 1509262 A CN1509262 A CN 1509262A CN A028055640 A CNA028055640 A CN A028055640A CN 02805564 A CN02805564 A CN 02805564A CN 1509262 A CN1509262 A CN 1509262A
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CN
China
Prior art keywords
refrigeration agent
interchanger
refrigeration
cooled
stream
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CNA028055640A
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Chinese (zh)
Inventor
翰瑞·帕拉多武斯基
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Technip Energies France SAS
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Technip France SAS
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Publication of CN1509262A publication Critical patent/CN1509262A/en
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/09—Purification; Separation; Use of additives by fractional condensation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/82—Processes or apparatus using other separation and/or other processing means using a reactor with combustion or catalytic reaction
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/12—Refinery or petrochemical off-gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/62—Ethane or ethylene
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/18—External refrigeration with incorporated cascade loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/902—Details about the refrigeration cycle used, e.g. composition of refrigerant, arrangement of compressors or cascade, make up sources, use of reflux exchangers etc.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • General Chemical & Material Sciences (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention concerns a method and an installation for refrigerating gas mixtures, for cryogenic separation of a pressurised gas (1) constituents. The method comprises a refrigerating cycle wherein a fluid (13) is separated in a separator tank (B2) into a less volatile fraction (4), for producing refrigeration at a relatively high first temperature in an exchanger (E1), and into a more volatile second fraction (5) for producing refrigeration at a relatively low temperature in an exchanger (E2). The heated and expanded fractions (4, 5) are brought together then compressed in a compressor (K1). A fraction (26) derived from said compressor (K1) is cooled to supply the fraction (13).

Description

The refrigeration cycle that utilization has a mixture of at least two kinds of refrigeration agents reclaims the method for ethane, the gas that utilizes this method to obtain, and operating equipment
Technical field
According to a first aspect of the present invention, the present invention relates generally to gas industry, relate in particular to reclaim to be included in and comprise methane and C 2With the ethane in the gas under pressure of higher hydrocarbon, operate the method for multicomponent refrigeration cycle.
Background technology
Term " multicomponent refrigeration cycle " should be understood to the refrigeration cycle of the refrigerant mixture that a kind of utilization is made up of at least two kinds of refrigeration agents.
More particularly, according to a first aspect of the present invention, the present invention relates to reclaim to be included in comprise methane and C 2With the ethane in the gas under pressure of higher hydrocarbon, operate a kind of method of refrigeration cycle, wherein less relatively volatile first refrigeration agent is compressed, cools off and expands, so that be used to cool off a described separated gas under pressure or first product separation to, the first high relatively temperature of wanting later on, and wherein more relatively volatile second refrigeration agent is compressed, cools off and expands, so that be used to cool off at least the second product separation that obtains from described gas under pressure later on to the second low relatively temperature.
Such refrigerating method is well known to those skilled in the art, and uses many years.
These refrigerating methods have the shortcoming about running cost, and this is because due to the energy expenditure relevant with the low thermodynamic(al) efficiency of these refrigeration cycle.
This known method also has the shortcoming about running cost, and these shortcomings are because difficult in maintenance, and frequent intervention work, and for example the intervention work that gas booster compressor, pump or other measurement and operating device are carried out produces.
Itself just needs too much cost these shortcomings, makes that prolongation is to the serial time of the capital investment of this equipment because producing interruption.
Summary of the invention
In view of this, first purpose of the present invention is to provide a kind of method, and, according to the general definition that provides in the superincumbent preface, the principal character of described method is, described first and second refrigeration agents are used as a kind of mixture when they are compressed and cool off, then, this mixture is separated into the first part that mainly comprises less relatively volatile first refrigeration agent and the second section that comprises relative more volatile second refrigeration agent, first refrigeration agent uses with the form of described first part, be used to be cooled to the first high relatively temperature, described second refrigeration agent uses with the form of described second section, is used to be cooled to the second low relatively temperature.
This method makes it possible to the running cost of limiting device, particularly energy expenditure owing to have higher thermodynamic(al) efficiency, in addition, about safeguarding, by two refrigeration pipes are merged into one, has reduced the quantity of the device in the equipment.Thereby, simplified attended operation, shortened the required time of reason of definite equipment failure, compare with the equipment that uses the method for utilizing prior art, shortened any production break period.
According to the first aspect of method of the present invention, first part can be cooled, be inflated in first interchanger, thereby produces the first expansible part, then, before being introduced into the lower pressure stage of compressor, is heated in first interchanger.
According to the first aspect of method of the present invention, second section can be cooled in first interchanger, expands in second interchanger then, in second interchanger, be heated then, and and expansible first part mixing.
First aspect according to method of the present invention, third part can be extracted out from first part after first part cools off in first heat exchanger, and third part can expand in first interchanger and heat, so that the 4th part of an expansible and heating is provided, it can be introduced into the medium pressure grade of compressor.
First aspect according to method of the present invention, gasiform the 5th part can from compressor (K1) to extract out in the compressed refrigeration agent of middle pressure, the 4th part a little more than expansible and heating, be cooled then and expand into and the identical pressure of described the 4th part, partially mixed with the described the 4th then.
According to the second aspect of method of the present invention, the mixture that first and second refrigeration agents can be used as with the 3rd refrigeration agent is used.
According to the second aspect of method of the present invention, described refrigeration agent can be methane, ethene and propane.
According to the third aspect of method of the present invention, the present invention relates to a kind of gas of the enrich methane that obtains by method of the present invention and a kind of product of enrichment ethane, and the enrichment C by method acquisition of the present invention 2Product with higher hydrocarbon.
According to the fourth aspect of method of the present invention, the present invention relates to a kind of equipment, be used for reclaiming to be included in comprising methane and C 2And the ethane in the gas under pressure of higher hydrocarbon, particularly operate with the multicomponent refrigeration cycle, described equipment uses refrigeration cycle, and comprise and be used for compression, cooling and expansion phase are to the device of few volatile first refrigeration agent, be used for by means of the described separated gas under pressure or the device of first product separation to, first a high relatively temperature wanted of described first refrigerant cools, and be used for compressing, cooling and expansion phase are to the device of many volatile second refrigeration agents, be used for by means of the device of described second refrigerant cools from least the second isolating product to one second a low relatively temperature of described gas under pressure acquisition, it is characterized in that, first and second refrigeration agents are used as a kind of mixture and use when they are compressed and cool off, and described equipment comprises and is used for described mixture separation is become mainly to contain the first part of few relatively volatile first refrigeration agent and the device of the second section that mainly contains relative volatile second refrigeration agent how, described first refrigeration agent is used with the form of described first part, be used to be cooled to the first high relatively temperature, described second refrigeration agent is used with the form of second section, is used to be cooled to the second low relatively temperature.
Description of drawings
Explanation below reading by the reference accompanying drawing will be expressly understood the present invention and other purpose, feature, details and advantage of the present invention more, and described accompanying drawing only provides with way of example, and is not used in restriction the present invention, wherein:
Fig. 1 is the functional block diagram according to the equipment of an embodiment of prior art; And
Fig. 2 is the functional block diagram according to the equipment of the preferred embodiments of the present invention.
Embodiment
Following symbol can be read from these two figure: FC represents flow director, and GT represents gas turbine, and LC represents fluid level controller, PC representative pressure controller, SC representation speed controller, TC representation temperature controller.
For clarity and conciseness, the pipeline that uses in the equipment illustrated in figures 1 and 2 will be with representing with the label that wherein mobile gas part is identical.
Referring to Fig. 1, shown equipment is intended to be used to handle the exsiccant cracked gas, especially, on the one hand, is used for separating mainly by there not being C basically 2Methane and the part formed of higher hydrocarbon, on the other hand, be used to separate mainly by ethane and other C 2Basically the part that does not have the higher hydrocarbon composition of methane.
This equipment has 3 independently pipelines.First pipeline is corresponding to the path by the gas stream warp that will be purified, and second pipeline is corresponding to the refrigeration cycle of refrigeration unit, and the refrigeration agent of described refrigeration unit is an ethene, and the 3rd pipeline is the refrigeration cycle of the refrigeration unit of propane corresponding to its refrigeration agent.
Or rather, in first pipeline, cracked gas 1, it obtains under 15 ℃ and 18 crust, and flow is 3903kmol/h, by being cooled off in interchanger E1, so that obtain-17.52 ℃ and the 17.8 refrigerative gases 302 that cling to.The latter is further cooled in the second interchanger E2, so that obtain 303 ,-30.00 ℃ of part agglomerative refrigerative fluids, and 17.6 crust.Stream 1 is by 0.1% carbonic acid gas, 24.3% methane, and 74.4% ethane and 1.2% propane are formed.
Fluid 303 is introduced into container V1 then, and it is carried out separating of its liquid composition and gaseous component there:
The stream 304 of-gas phase, it is to obtain under the flow of 2219kmol/h, in interchanger E3, be cooled to-60 ℃, and partly condensed, so as to obtain 17.4 the crust under fluid 305.Described fluid 305 is by the top of feed-in distillation column T1;
-liquid phase stream 306, it is to obtain under the flow of 1684kmol/h, is driven by pump P1 and flows into the pipeline that comprises controlled valve 321, the aperture of described controlled valve depends on the fluid level controller among the container V1, so that export one-29.8 ℃ and 19.6 streams 307 that cling to.Then described stream is introduced the middle part of distillation column T1.
Top at distillation tower T1 produces 308 ,-65.79 ℃ of steam, 17.2 crust, and flow is 1358kmol/h, it is cooled in interchanger E4, so that obtain 309 ,-90 ℃ of part agglomerative fluids, 17.0 crust.Described fluid is divided into gas part 310 and liquid portion 311 then in container V2, wherein gas part 310 quantity are 971kmol/h, carbonic acid gas by 0.1%, 94.9% methane and 5.0% ethane are formed, liquid portion 311 quantity are 387kmol/h, carbonic acid gas by 0.4%, 47.6% methane and 52.0% ethane are formed, and it is driven along pipeline 312 by pump V2.Described pipeline 312 comprises controlled open valve 322, and the aperture of described valve depends on the flow in the described pipeline.
Then the liquid portion of carrying is incorporated into the last step of distillation tower T1 in pipeline 312.
Gas part 310 from container V2, its temperature is-90.0 ℃, flow through interchanger E6 so that one-35.0 ℃ heated part 313 is provided, the described then part 313 heat exchanger E7 that flows through, so that provided a heated part 326 before by controlled open valve 317, the aperture of open valve 317 depends on the pressure in the pipeline 326.After product left valve 317, it is collected under 20 ℃ paid pipeline 320, and leaves equipment.
Have several pallets in the bottom of distillation column T1, they connect in pairs by heating pipe line, there is shown wherein two.They are pipeline 315,316 and 318,319.Each of these heating pipe lines constitutes a horizontal reboiler under the situation of pipeline 315,316, constitute a distillation tower bottom reboiler under the situation of pipeline 318,319.
Mobile fluid in pipeline 315, its flow is 3000kmol/h, temperature is-20.6 ℃, in heat exchanger E1, be heated by carrying out heat exchange with cracked gas 1, so that the fluid 316 of-16.61 ℃ heating is provided, be introduced into the pallet of the pallet below that is used to reclaim fluid 315 then.Mobile fluidic temperature is regulated by means of the controlled open valve in the branch road that places pipeline 315,316 323 in described pipeline 315,316, and it is not by interchanger E1.The aperture of described valve 323 is by the temperature regulator control that links to each other with pipeline 302.
Similarly, mobile fluid in pipeline 318, its flow is 3341kmol/h, temperature is-16.15 ℃, be positioned at the following one-level of the one-level that the fluid 316 of heating is introduced into, being heated by carrying out heat exchange with the refrigeration agent that is made of propane in heat exchanger E5, is the fluid 319 of-14.87 ℃ heating thereby temperature is provided.This fluid is introduced in the pallet of the pallet below that is used to reclaim fluid 318.The fluidic temperature of described pipeline 318,319 of flowing through is conditioned by means of controlled open valve 324, and described valve is set at and is used in the branch line of the refrigeration agent of carrying in the pipeline 220,221, and described branch line is by interchanger E5.The aperture of described valve 324 is by the temperature regulator control that links to each other with pipeline 319.
At last, at the residual liquid that the bottom of distillation tower T1 obtains, it contains abundant C 2And higher hydrocarbon, at-14.87 ℃, 17.4 crust, flow is to be recovered by pipeline 314 under the 2932kmol/h.Described pipeline 314 has valve 325, and its aperture is by the fluid level controller control that is used at the liquid of the bottom of distillation tower T1.
In second pipeline, it is the refrigeration cycle of the refrigeration unit of ethene corresponding to its refrigeration agent, liquid ethylene stream 100, and flow is 2570kmol/h, and temperature is-30 ℃, and pressure is 19.58 crust, is reclaimed from storage vessel V5.Described stream 100 is divided into:
(a) first-class 117, its flow is 1993kmol/h, and its expansion becomes 6.79 crust, is cooled to-63 ℃ by making it through valve 120, so that stream 101 is provided, itself and stream 104 mix, so that produce stream 102, its feed-in has the interchanger E3 of refrigerating ethene.The aperture of valve 120 is controlled by the fluid level controller among the interchanger E3.
(b) second stream 114, its flow is 577kmol/h, expanding becomes 18.58 crust, and is cooled to-80 ℃ in interchanger E6, adds hot-fluid 115 so that produce one.
Flow is that the stream 115 of 577kmol/h is divided into:
(a) first-class 116, its flow is 417kmol/h, expand into 1.83 crust, is cooled to-93 ℃ by making it through valve 121, so that stream 106 is provided, its feed-in has the interchanger E4 of refrigerating ethene.The aperture of valve 121 is controlled by the fluid level controller in the interchanger E4.In addition, described fluid level controller carries out servocontrol by another fluid level controller that is included among the independent container V2;
(b) flow is second stream of 160kmol/h, and it flows in the pipeline with valve 122, and the aperture of described valve depends on the flow in the pipeline 105, so that produce one-79 ℃, and the stream 104 of 6.79 crust.Described stream 104 and stream 101 mix, so that produced a stream 102 before it is introduced into interchanger E3.
The ethene that evaporation is included among the interchanger E4 makes that stream 8 can be from the top output of distillation tower T1, so that cool off.Obtain-93 ℃ like this, the ethene vapour stream 107 of 1.83 crust, it is sent to the lower pressure stage of compressor K1 by suction container V3.
The feasible stream 4 from container V1 of ethene that evaporation is included among the interchanger E3 is cooled.Thereby obtain one-62.83 ℃, and the ethene vapour stream 103 of 6.79 crust, it is sent to the medium pressure grade of compressor K1 by suction container V4.
The ethene of the compression that obtains in the outlet of K1 provides one 17.75 ℃, 20.6 crust, the fluid 112 of 2570kmol/h, by means of making it then by interchanger E8, be cooled and condense, produce one-7 ℃, 20.1 the part 118 of crust, then by interchanger E9, thereby produced one-30 ℃, the parts 119 of 19.6 crust have the container V5 of liquid ethylene in feed-in before.
In the 3rd pipeline, it is the refrigeration cycle of the refrigeration unit of propane corresponding to refrigeration agent, and from 42 ℃, the storage receptacle V6 of 18 crust takes out the petrogas stream 220 that flow is the pressurization of 4340kmol/h.Described stream 220 carries out heat exchange and is cooled by flowing fluid in interchanger E5 and in pipeline 18,19, thereby provides one 33.64 ℃, the refrigerative fluid 221 of 17.5 crust.In by cooling line, make it pass through interchanger E5, the pipeline with valve 24 makes the energy exchange in E5 to be conditioned.
Then the cold fluid 221 of 4340kmol/h is divided into two streams:
4030kmol/h's is first-class 200, makes it pass through valve 226 and expands, so that 3.46 crust ,-10 ℃ stream 201 are provided.The aperture of valve 226 is controlled by the fluid level controller among the interchanger E8.Stream 201 is fed into the interchanger E8 with refrigerating propane;
Second stream 222 of 310kmol/h, it is cooled in interchanger E7, so that produce-25 ℃ stream 223.
Stream 223 is expanded by valve 229, and the aperture of described valve is by the flow control in the pipeline, thereby produces the expansion flows 224 of 1.48 crust.
The propane stream 201 that is introduced into interchanger E8 is partly evaporated, so that produce the gas phase 203 of 1387kmol/h and the liquid phase 204 of 2643kmol/h.Described stream 204 is divided into two streams:
The stream 205 of 1700kmol/h makes it pass through valve 227 and expands, and its aperture depends on the liquid level that keeps in interchanger E9, so that 1.48 crust that are fed to the interchanger E9 with refrigerating propane ,-33 ℃ stream 206 are provided;
The stream 208 of 943kmol/h makes it pass through valve 228 and expands, and its aperture depends on the liquid level that keeps in interchanger E2, so that 1.48 crust that are fed to the interchanger E2 with refrigerating propane ,-33 ℃ stream 225 are provided.
Stream 225 and 224 was merged before being introduced into interchanger E2, thereby formed stream 209.
The propane of evaporation in interchanger E2 makes stream 2 be cooled and is condensed partly.Obtain like this-33 ℃, the propane vapor stream 210 of 1.48 crust and mix from the gas stream 207 of interchanger E9, thus forming stream 211, it at first is admitted to and sucks container V7, is admitted to the lower pressure stage of compressor K2 then.
The propane of evaporation in interchanger E9 makes stream 118 be cooled, and by local coagulation.Obtain like this-33 ℃, the propane vapor stream 207 of 1.48 crust and mix from the gas stream 210 of interchanger E9, thus forming stream 211, it at first is admitted to and sucks container V7, is admitted to the lower pressure stage of compressor K2 then.
The propane of evaporation in interchanger E8 makes stream 112 be cooled, and by local coagulation.-10 ℃ of acquisition like this, the propane vapor stream 203 of 3.46 crust at first is admitted to and sucks container V8, is admitted to the medium pressure grade of compressor K2 then.
Compressor K2 provides 78.02 ℃, the propane gas of the thermo compression of 18.6 crust, and its flow is 4340kmol/h.This stream 217 is cooled in the first interchanger E10, thereby provides one 52.36 ℃, and the cooling flow 218 of 18.3 crust is cooled in the second interchanger E11 then, so that provide 42 ℃, and the liquid flow 219 of 18.0 crust.Then the latter is stored among the container V6.
Referring now to Fig. 2,, shown equipment is intended to be used to handle the exsiccant cracked gas, especially, on the one hand, is used for separating mainly by there not being C basically 2Methane and the part formed of higher hydrocarbon, on the other hand, be used to separate mainly by ethane and other C 2Basically the part that does not have the higher hydrocarbon composition of methane.
This equipment has 2 independently pipelines.First pipeline is corresponding to the path by the gas stream warp that will be purified, and second pipeline is corresponding to the refrigeration cycle of refrigeration unit, and the refrigeration agent of described refrigeration unit is the mixture of at least 3 kinds of different products, and specifically, they are propane, ethene and methane.
Or rather, in first pipeline, cracked gas 1, it obtains under 15 ℃ and 18 crust, and flow is 3903kmol/h, by in interchanger E1, being cooled to-60 ℃, 17.7 crust, described interchanger is a kind of plated exchangers, so that obtain refrigerative gas 303.The latter is sent to the top of distillation column T1.Stream 1 is by 0.1% carbonic acid gas, 24.3% methane, and 74.4% ethane and 1.2% propane are formed.
With with the identical mode of the described processing of Fig. 1, produce steam 308 at the top of distillation tower T1, its temperature be-66.21 ℃, pressure is 17.0 to cling to, flow is 1342kmol/h, it is cooled in interchanger E2, so that the fluid 309 of local coagulation is provided.Stream 308 and 309 is by 0.16% carbonic acid gas, and 81.8% methane and 18.0% ethane are formed.Flow 309 then and in container V2, be separated into gas part 310 and liquid portion 311.Described liquid portion 311 is comprising under action of gravity in the pipeline of controlled open valve 322 to be carried, and the aperture of described valve depends on the liquid level of container V1.
Then, liquid portion 311 is introduced the last level of distillation tower T1.
By 0.1% carbonic acid gas, 94.9% methane and 5.0% ethane are formed from the gas part 310 of container V2.This part enters-90 ℃ heat exchanger E2, so that obtain-70 ℃ part 326 of a heating, then then by interchanger E1, and by controlled valve 317, the aperture of described valve depends on the pressure in the pipeline 326.After leaving valve 317, product is being collected in payment pipeline 320 under 39 ℃, and leaves equipment.
In the bottom of distillation column T1, have several pallets, they connect in pairs by heating pipe line, there is shown wherein two.They are pipeline 315,316 and 318,319.Each of these heating pipe lines constitutes a horizontal reboiler under the situation of pipeline 315,316, constitute the bottom reboiler of a distillation tower under the situation of pipeline 318,319.
Mobile fluid in pipeline 315, its flow are 1000kmol/h, and temperature is-40.7 ℃, are heated in heat exchanger E1, so that the fluid 316 of-19.4 ℃ heating is provided, are introduced into the pallet of the pallet below that is used to reclaim fluid 315 then.Mobile fluidic temperature is regulated by means of the controlled open valve in the branch road that places pipeline 15,16 323 in described pipeline 315,316, and described branch line is not by interchanger E1.The aperture of described valve 323 is located at mobile fluid in the pipeline 316 and the temperature regulator control in the downstream of mobile fluid blended position in the branch line with valve 323 by what link to each other with pipeline 316.
Similarly, mobile fluid in pipeline 318, its flow are 3790kmol/h, and temperature is-17.36 ℃, are heated in heat exchanger E1, so that the fluid 319 of one-14.94 ℃ heating is provided.This fluid is introduced in the pallet of the pallet below that is used to reclaim fluid 318.The fluidic temperature of described pipeline 318,319 of flowing through is conditioned by means of controlled open valve 324, and described valve is set in the branch line of pipeline 315,316, and described branch line is by interchanger E1.The aperture of described valve 324 is located at mobile fluid in the pipeline 319 and the temperature regulator control in the downstream of mobile fluid blended position in the branch line with valve 324 by what link to each other with pipeline 316.
At last, at the residual liquid that the bottom of distillation tower T1 obtains, it contains abundant C 2And higher hydrocarbon, being recovered by pipeline 314, described pipeline 314 has valve 325, and its aperture is by the fluid level controller control that is used at the liquid of the bottom of distillation tower T1.The temperature of described liquid is-14.94 ℃, and pressure is 17.4 crust, the carbonic acid gas by 0.1%, and the propane of 1% methane and 97.4% ethane and 1.5% is formed.
In second pipeline, it is the refrigeration cycle of refrigeration unit of the mixture of at least 3 kinds of products corresponding to its refrigeration agent, frigorific mixture 13 is by 5% methane 12,25% ethene 3 and 70% propane 2 constitute, its temperature is 42 ℃, pressure is 27.79 crust, flow is 3970kmol/h, described frigorific mixture is divided into first part 4 in container V2, the second section 5 that it mainly contains the first part 4 of less volatile first refrigeration agent 2 and mainly contains more volatile second refrigeration agent 3 and more volatile the 3rd refrigeration agent 12.
Constitute the stream 5 of the gas phase of separation vessel V2, it is by 9.8% methane, and 36.3% ethene and 53.9% propane constitute, and flow is 1469kmol/h, by cooling in heat exchanger E1 with condense, so that be provided at the stream 14 that obtains under-60 ℃.
Stream 14 is cooled off in interchanger E2, so that be provided at-90 ℃, the stream 15 that 27.1 crust obtain down.Stream 15 expands by valve 16, is 2.3 crust thereby pressure is provided, and temperature is-96 ℃ a stream 17.The aperture of valve 16 is regulated by the temperature regulator in pipeline 310.
Stream 17 is heated in interchanger E2, and is partly evaporated, and makes the refrigeration requirement of satisfying interchanger E2, is-67.9 ℃ so that provide temperature in the outlet of interchanger, and pressure is the streams 18 of 2.2 crust.
Constitute the stream 4 of the liquid phase of separation vessel V2, it is by 2.2% methane, and 18.3% ethene and 79.5% propane constitute, and flow is 2501kmol/h, is cooled off in heat exchanger E1, so that be provided at the stream 19 that obtains under-60 ℃.Then stream 19 is separated into two streams:
Stream 8, its flow is 1000kmol/h, it is expanded by valve 20 becomes 8.1 crust, thereby produces stream 21.The latter is evaporated in interchanger E1 and heats, thereby produces 38.5 ℃, the stream 9 of 7.8 crust;
Stream 22, its flow is 1501kmol/h, it is expanded by valve 23 becomes 2.2 crust, mixes with stream 18 then, thereby produces stream 6.The latter's temperature is-64.93 ℃, and pressure is 2.2 crust, the methane by 6.0%, and 27.2% ethene and 66.8% propane constitute, and are evaporated in interchanger E1 and heat, thereby be provided at 38.5 ℃, the stream 7 under 1.9 crust.
Stream 7 is sent to the lower pressure stage of compressor K1 by suction container V3.Stream 11, it is from compressor K1, is 2970 kmol/h corresponding to the flow of all stream 7 of the lower pressure stage that enters compressor, at 8.0 crust, is introduced into water interchanger E11 under 113.75 ℃, so that produce 42.0 ℃, the cold flows 25 of 7.7 crust.
Stream 9 flows by sucking container V4, mixes with stream 25 then, thereby stream 10 is provided, and flow is 3970kmol/h, and 41.01 ℃, 7.7 crust.Then flow 10 medium pressure grades that are introduced into compressor K1.
From the stream 26 of the high pressure stage of compressor K1, flow is 111.66 ℃ for the 3970kmol/h temperature, and pressure is 28.39 crust, is cooled in water interchanger E10, so that 54.36 ℃ stream 27 is provided.At last, stream 27 is cooled to 42.0 ℃ in water interchanger E12, thereby produces stream 13.
Provide the performance characteristic of two kinds of processing below by means of synopsis.
The comparison of compressor power (kilowatt)
(power according to 82% polytropic efficiency)
Ordinary method (Fig. 1) According to method of the present invention (Fig. 2)
Ethylene compressor ????2124
Propane compressor ????7406
The refrigerant mixed compressor ????8708
Amount to ????9530 ????8708
Can save 9.4% power according to method of the present invention.
The comparison of chilled water interchanger
Ordinary method Method of the present invention
The water interchanger The heat (kW) of exchange ??MTD ??(℃) Exchange area (m 2) The heat (kW) of exchange ??MTD ??(℃) Exchange area (m 2)
??E10 ??3239 ????22.1 ????293 ????5989 ????35.2 ????341
??E11 ??16426 ????8.88 ????3700 ????4451 ????24.4 ????365
??E12 ????8211 ????6.88 ????2388
Amount to ??19665 ????3993 ????18651 ????3094
Compare with ordinary method, little by 29% according to the area of the chilled water interchanger of method of the present invention, the consumption of water few 5.4%.
The comparison of low-temperature switch
Ordinary method Method of the present invention
Interchanger The heat (kW) of exchange ??MTD ??(℃) Exchange area (m 2) The heat (kW) of exchange ??MTD ??(℃) Exchange area (m 2)
????E1 ????2000 ????11.2 ????357 ????30100 ????7.27 ????8286
????E2 ????5658 ????6.74 ????1679 ????2367 ????3.49 ????1356
????E3 ????5514 ????15.7 ????702
????E4 ????1397 ????11.4 ????245
????E5 ????1258 ????53.2 ????47
????E6 ????606 ????8.59 ????141
????E7 ????570 ????12.4 ????595
????E8 ????929 ????11.0 ????169
????E9 ????7500 ????3.75 ????4000
Amount to ????25432 ????7935 ??32467 ??9642
Compare with known method, the total exchange area that uses according to method of the present invention is big by 21%, yet the cost of interchanger of the present invention is lower.
The quantity of equipment item relatively
Ordinary method Method of the present invention
Low-temperature switch ????9 ????2
The water interchanger ????2 ????3
Container ????8 ????4
Distillation tower ????1 ????1
Compressor ????2 ????1
Pump ????2 ????0
Amount to ????24 ????11
Method of the present invention has only 11 equipment item, and known method has 24 equipment item.
The comparison of Controlling System quantity:
Ordinary method The inventive method
Flow control ????3 ????1
Liquid level control ????7 ????2
Temperature control ????2 ????4
Pressure-controlling ????1 ????1
Amount to ????13 ????8
Method of the present invention has 8 Controlling System, and ordinary method has 13 Controlling System.
Therefore, method of the present invention is favourable when producing the gas of purifying.When implementing method of the present invention, just realized purpose of the present invention, can make methane and other component separating simultaneously with high sensitivity.
Thereby the result who is obtained by the present invention provides major advantage, simplifies and save greatly the structure and the technology of equipment greatly, and makes the method for these equipment of operation simplify, and has improved the quality of the product that is obtained by these methods.

Claims (11)

1. one kind is used for reclaiming to be included in comprising methane and C 2With the ethane in the gas under pressure (1) of higher hydrocarbon, operate a kind of method of refrigeration cycle, wherein less relatively volatile first refrigeration agent (2) is compressed, cooling and expansion, so that be used to cool off a described separated gas under pressure (1) or first product separation to, the first high relatively temperature of wanting later on, and wherein more relatively volatile second refrigeration agent (3) is compressed, cooling and expansion, so that be used at least the second product separation that cooling obtains from described gas under pressure (1) later on to the second low relatively temperature *1, *2 is characterized in that, described first and second refrigeration agents (2,3) when being compressed and cooling off, they are used as a kind of mixture, then, this mixture is separated into the first part (4) that mainly comprises less relatively volatile first refrigeration agent (2) and the second section (5) that comprises relative more volatile second refrigeration agent (3), first refrigeration agent is used with the form of described first part, be used to be cooled to the first high relatively temperature, described second refrigeration agent uses with the form of described second section, is used to be cooled to the second low relatively temperature.
2. in accordance with the method for claim 1, it is characterized in that first part (4) is cooled, expands in first interchanger (E1), thereby produce first expansible part (6), then, in the lower pressure stage that is introduced into compressor (K1) (7) before, in described first interchanger, be heated.
3. in accordance with the method for claim 2, it is characterized in that second section (5) is cooled in first interchanger (E1), in second interchanger (E2), expand then, in described second interchanger, be heated then, and and expansible first part (6) mixing.
4. according to claim 2 or 3 described methods, it is characterized in that, third part (8) is drawn out of from described first part (4) after first part (4) cools off in first heat exchanger (E1), and described third part (8) expands in described first interchanger (E1) and heats, so that the 4th part (9) of an expansible and heating is provided, it is introduced into the medium pressure grade (10) of compressor (K1).
5. in accordance with the method for claim 4, it is characterized in that, gasiform the 5th part (11) from compressor (K1) to be drawn out of in the compressed refrigeration agent of middle pressure, the 4th part (9) a little more than expansible and heating, be cooled then and expand into and the identical pressure of described the 4th part, partially mixed with the described the 4th then.
6. according to the described method of any one claim of front, it is characterized in that the mixture of described first and second refrigeration agents (2,3) conduct and the 3rd refrigeration agent (12) is used.
7. in accordance with the method for claim 6, it is characterized in that described refrigeration agent can be methane, ethene and propane.
8. the gas of an enrich methane that obtains by the described method of top any one claim.
9. the product of a kind of enrichment ethane that obtains by any one described method of claim 1-7.
10. one kind is passed through the enrichment C that any one described method of claim 1-7 obtains 2Product with higher hydrocarbon.
11. an equipment is used for reclaiming to be included in comprising methane and C 2And the ethane in the gas under pressure of higher hydrocarbon (1), described equipment comprises and is used for compressing, cooling and expansion phase are to the device of few volatile first refrigeration agent (2), be used for by means of the described separated gas under pressure (1) or the device of first product separation to, first a high relatively temperature wanted of described first refrigerant cools, and be used for compressing, cooling and expansion phase are to the device of many volatile second refrigeration agents (3), be used for by means of the device of described second refrigeration agent (3) cooling from least the second isolating product to one second a low relatively temperature of described gas under pressure (1) acquisition, it is characterized in that, first and second refrigeration agents (2,3) being used as a kind of mixture when they are compressed and cool off uses, and described equipment comprises the first part (4) and the device that mainly contains relative volatile second refrigeration agent (3) second section (5) how that is used for described mixture separation is become mainly to contain few relatively volatile first refrigeration agent (2), described first refrigeration agent is used with the form of described first part, be used to be cooled to the first high relatively temperature, described second refrigeration agent is used with the form of second section, is used to be cooled to the second low relatively temperature.
CNA028055640A 2001-02-26 2002-02-04 Method for ethane recorery, using refrigeration cycle with a mixture of at least two coolants, gases obtained by said method and instalation thereof Pending CN1509262A (en)

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FR0102582A FR2821351B1 (en) 2001-02-26 2001-02-26 METHOD FOR RECOVERING ETHANE, IMPLEMENTING A REFRIGERATION CYCLE USING A MIXTURE OF AT LEAST TWO REFRIGERANT FLUIDS, GASES OBTAINED BY THIS PROCESS, AND IMPLEMENTATION INSTALLATION
FR01/02582 2001-02-26

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102893108A (en) * 2009-09-30 2013-01-23 国际壳牌研究有限公司 Method of fractionating a hydrocarbon stream and an apparatus therefor
CN103827614A (en) * 2011-03-30 2014-05-28 阿尔斯通技术有限公司 Cryogenic CO2 separation using a refrigeration system
CN113454411A (en) * 2018-10-09 2021-09-28 查特能源化工股份有限公司 Dehydrogenation separation device with mixed refrigerant cooling function
US11629912B2 (en) 2018-10-09 2023-04-18 Chart Energy & Chemicals, Inc. Dehydrogenation separation unit with mixed refrigerant cooling

Families Citing this family (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002289444A (en) * 2001-03-23 2002-10-04 Fdk Corp High frequency power inductance element
US7264654B2 (en) * 2003-09-23 2007-09-04 Kalex, Llc Process and system for the condensation of multi-component working fluids
US7082787B2 (en) * 2004-03-09 2006-08-01 Bp Corporation North America Inc. Refrigeration system
US8087248B2 (en) 2008-10-06 2012-01-03 Kalex, Llc Method and apparatus for the utilization of waste heat from gaseous heat sources carrying substantial quantities of dust
US8695344B2 (en) * 2008-10-27 2014-04-15 Kalex, Llc Systems, methods and apparatuses for converting thermal energy into mechanical and electrical power
US8176738B2 (en) 2008-11-20 2012-05-15 Kalex Llc Method and system for converting waste heat from cement plant into a usable form of energy
US8474263B2 (en) 2010-04-21 2013-07-02 Kalex, Llc Heat conversion system simultaneously utilizing two separate heat source stream and method for making and using same
US9045697B2 (en) * 2012-03-05 2015-06-02 Uop Llc Distillation column heat pump with compressor inlet superheater
US9040765B2 (en) * 2012-03-29 2015-05-26 Uop Llc Methods and apparatuses for isomerization of paraffins
US8833077B2 (en) 2012-05-18 2014-09-16 Kalex, Llc Systems and methods for low temperature heat sources with relatively high temperature cooling media
US11236941B2 (en) * 2017-12-15 2022-02-01 Saudi Arabian Oil Company Process integration for natural gas liquid recovery
CN109028758A (en) * 2018-08-07 2018-12-18 中国石油工程建设有限公司 A kind of natural gas ethane recovery device and method to be freezed using azeotrope
US20230076753A1 (en) * 2021-09-02 2023-03-09 Brian Frankie Liquified natural gas processing cold box with internal refrigerant storage

Family Cites Families (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1135871A (en) * 1965-06-29 1968-12-04 Air Prod & Chem Liquefaction of natural gas
US3970441A (en) * 1973-07-17 1976-07-20 Linde Aktiengesellschaft Cascaded refrigeration cycles for liquefying low-boiling gaseous mixtures
US4203742A (en) * 1978-10-31 1980-05-20 Stone & Webster Engineering Corporation Process for the recovery of ethane and heavier hydrocarbon components from methane-rich gases
FR2545589B1 (en) * 1983-05-06 1985-08-30 Technip Cie METHOD AND APPARATUS FOR COOLING AND LIQUEFACTING AT LEAST ONE GAS WITH LOW BOILING POINT, SUCH AS NATURAL GAS
US4504296A (en) * 1983-07-18 1985-03-12 Air Products And Chemicals, Inc. Double mixed refrigerant liquefaction process for natural gas
US4507133A (en) * 1983-09-29 1985-03-26 Exxon Production Research Co. Process for LPG recovery
US4617039A (en) * 1984-11-19 1986-10-14 Pro-Quip Corporation Separating hydrocarbon gases
US4851020A (en) * 1988-11-21 1989-07-25 Mcdermott International, Inc. Ethane recovery system
FR2681859B1 (en) * 1991-09-30 1994-02-11 Technip Cie Fse Etudes Const NATURAL GAS LIQUEFACTION PROCESS.
US5390499A (en) * 1993-10-27 1995-02-21 Liquid Carbonic Corporation Process to increase natural gas methane content
TW366410B (en) * 1997-06-20 1999-08-11 Exxon Production Research Co Improved cascade refrigeration process for liquefaction of natural gas
US5953935A (en) * 1997-11-04 1999-09-21 Mcdermott Engineers & Constructors (Canada) Ltd. Ethane recovery process
US6244070B1 (en) * 1999-12-03 2001-06-12 Ipsi, L.L.C. Lean reflux process for high recovery of ethane and heavier components
US6311516B1 (en) * 2000-01-27 2001-11-06 Ronald D. Key Process and apparatus for C3 recovery

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102893108A (en) * 2009-09-30 2013-01-23 国际壳牌研究有限公司 Method of fractionating a hydrocarbon stream and an apparatus therefor
CN102893108B (en) * 2009-09-30 2014-12-24 国际壳牌研究有限公司 Method of fractionating a hydrocarbon stream and an apparatus therefor
CN103827614A (en) * 2011-03-30 2014-05-28 阿尔斯通技术有限公司 Cryogenic CO2 separation using a refrigeration system
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US11629912B2 (en) 2018-10-09 2023-04-18 Chart Energy & Chemicals, Inc. Dehydrogenation separation unit with mixed refrigerant cooling

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WO2002068366A1 (en) 2002-09-06
AR032835A1 (en) 2003-11-26
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US20040069015A1 (en) 2004-04-15
FR2821351A1 (en) 2002-08-30
BR0207301A (en) 2004-02-10

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