EP0634618B1 - Procédé autoréfrigéré de fractionnement cryogénique et de purification de gaz et échangeur de chaleur pour la mise en oeuvre de ce procédé - Google Patents

Procédé autoréfrigéré de fractionnement cryogénique et de purification de gaz et échangeur de chaleur pour la mise en oeuvre de ce procédé Download PDF

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Publication number
EP0634618B1
EP0634618B1 EP94401517A EP94401517A EP0634618B1 EP 0634618 B1 EP0634618 B1 EP 0634618B1 EP 94401517 A EP94401517 A EP 94401517A EP 94401517 A EP94401517 A EP 94401517A EP 0634618 B1 EP0634618 B1 EP 0634618B1
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Prior art keywords
circuit
gas
condensate
circuits
purified
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EP94401517A
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German (de)
English (en)
French (fr)
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EP0634618A1 (fr
Inventor
Henri Paradowski
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Francaise dEtudes et de Construction Technip SA
Technip Energies France SAS
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Francaise dEtudes et de Construction Technip SA
Technip SA
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B1/00—Compression machines, plants or systems with non-reversible cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J3/0252—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 hydrogen
    • 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
    • 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
    • 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
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
    • F25J5/007—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger combined with mass exchange, i.e. in a so-called dephlegmator
    • 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
    • F25J2200/80—Processes or apparatus using separation by rectification using integrated mass and heat exchange, i.e. non-adiabatic rectification in a reflux exchanger or dephlegmator
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/902—Apparatus
    • Y10S62/903—Heat exchange structure

Definitions

  • the subject of the present invention is a method of cryogenic fractionation and of gas purification, as defined in the preamble of claim 1.
  • Certain gases include both constituents which are fairly easily liquefiable at low temperature and constituents which are more difficult to liquefy or non-liquefiable. It is therefore common to try to separate them by cooling in order to condense the elements which are more easily liquefiable and thus separate them from the constituents which are more difficult to liquefy or non-liquefiable.
  • mixtures of different hydrocarbons or non-hydrocarbon components such as nitrogen, hydrogen, argon and / or carbon monoxide and, for example , catalytic cracking or steam cracking gases.
  • reflux exchangers also known as “dephlegmators”
  • external refrigeration being usually supplied countercurrently through a refrigeration cycle or by dynamic gas expansion. This limits the use of these techniques to the temperatures at which the refrigeration cycles are available and to cases where the expansion of the effluents, for example hydrogen or methane, is possible.
  • the technique consists in cooling the gas to be purified in a first exchanger, in separating the non-gas condensed from the first condensate formed, for example in a fractionation column, to further cool the uncondensed gas in a second exchanger to form a second condensate, to separate this second condensate from the uncondensed gas in a separator and to return the second condensate to the column as reflux.
  • the uncondensed gas separated from the second condensate constitutes the purified gas.
  • the cooling agent for the two exchangers consists of the first condensate which is subjected to vaporization by expansion and passes successively through the second then the first exchanger.
  • the purified gas can itself pass through the second and then the first exchanger.
  • the method and the device of the invention have the advantage of not generally requiring refrigeration using refrigerants foreign to the installation and of not requiring expansion of the constituent (s) ) the most difficult to liquefy (s) of the treated gas mixture.
  • This last point is important because, on the one hand, liquefaction techniques most often require the application of high pressure and, on the other hand, certain separate gases obtained such as, for example, hydrogen and / or carbon monoxide are often reactants for chemical reactions which must themselves be carried out under high pressure. It would therefore be uneconomic to expand these gases during cryogenic separation and then have to recompress them.
  • the method and the device of the invention are more economical than the known method of self-refrigeration because they require only a unitary exchanger which is less expensive than the multiple devices (at least two exchangers, a fractionation column , a separator and many circuits) of the known method. They also reduce heat losses and avoid high expenses for insulating circuits and devices.
  • the gases to which the invention applies are mixtures of at least two, and preferably at least three, different chemical components and of different boiling (or condensation) temperatures under the conditions of the process, and, for example, a mixture of hydrogen, methane and at least one C2 hydrocarbon such as ethane or ethylene, with or without higher hydrocarbons (C3 or more).
  • Other mixtures also contain carbon monoxide and / or nitrogen.
  • the invention uses a unitary heat exchanger (a unitary heat exchange zone) as defined in claim 8.
  • One of the circuits called the reflux circuit or first circuit, is arranged essentially in an upper portion. of the exchanger (the exchange zone), that is to say in a relatively cooler portion of the exchanger. It is preferably a "non-tortuous" circuit, that is to say in which the condensed liquid can flow in a generally descending direction.
  • Another circuit (fifth circuit), preferably of the tortuous type, not suitable for reflux of liquid, is essentially arranged in a lower portion of the exchanger (the exchange zone), that is to say in a portion relatively cooler of the exchanger.
  • circuit of the tortuous type directed generally vertically, is meant a circuit such that the fluid which is introduced therein at the base can progress generally from the bottom upwards without significant reflux of the liquid portions of this fluid, which supposes, by example, an average slope less steep than in the above-mentioned reflux circuit; in other words, all or almost all of the fluid (liquid and gaseous) will follow a generally ascending path in this circuit of tortuous type and will be collected at the top of said circuit, the point (or zone) of discharge being located in a portion intermediate of the heat exchanger, for example in the vicinity of the first third or half the height of the exchanger.
  • the aforementioned tortuous circuit is in whole, or almost in whole, at a level lower than the reflux circuit, and, even better, than the two circuits are arranged substantially one above the other in the exchanger.
  • the second, third and fourth circuits can be tortuous or not, preferably non-tortuous.
  • the five aforementioned circuits are in heat exchange relationship with each other at each level of the exchanger where they are present, which supposes that the exchanger is preferably made of a good heat conductive material, with walls as thin as possible compatible with the resistance of the materials and having a high exchange surface. Specialists can easily make such exchangers from the previous indications.
  • the aforementioned multi-component gaseous fluid (at least two and preferably at least three condensable components) is circulated from bottom to top in the fifth circuit, located in a lower portion of the exchanger, in conditions of temperature and pressure such that it can partially condense without backflow into said circuit.
  • the mixture of gas and liquid (first condensate) withdrawn from the top of the fifth circuit is separated into a gas phase and a liquid phase, in a separation zone.
  • the resulting gas phase is circulated from bottom to top in the first circuit (reflux circuit) preferably located above the fifth circuit, as indicated above.
  • the second condensate thus formed can be mixed with the first condensate already present in the separation zone or be collected separately.
  • the uncondensed gas collected at the top of the first circuit is returned to the exchanger by the aforementioned second circuit to circulate there from top to bottom against the current of the fluids circulating in the first circuit and in the fifth circuit. It comes out heated by constituting the purified gas, formed of the most volatile elements of the gaseous supply fluid.
  • the liquid phase of the separation zone consisting of the first condensate alone or of the mixture of the first and second condensates, is circulated from the bottom to the top in the aforementioned third circuit where it undergoes sub-cooling. It is then relaxed, statically or dynamically, and circulated from top to bottom in the aforementioned fourth circuit of the exchanger where it vaporizes thanks to the heat removed from the fluids of the tortuous circuit, the first circuit and the third circuit.
  • the gas stream discharged at the bottom of the fourth circuit contains the least volatile constituents of the gaseous supply fluid. It can, if desired, be partially recycled or otherwise treated.
  • only part of the gaseous phase collected at the head of the first circuit is sent to the second circuit; the other part is expanded and used in the heat exchanger in the downward direction, either by passing through a sixth exchange circuit or, preferably, by passing through the fourth circuit, in admixture with the expanded liquid phase of the (or ) condensate (s) introduced therein, to allow vaporization at higher pressure.
  • the production of purified gas under high pressure is less important, but this does not present any drawback when the gas stream from the fourth circuit is recycled or the gas stream from the sixth circuit is recompressed.
  • Preferably 90 to 98% by mole of the gaseous phase collected at the head of the first circuit is sent to the second circuit and the other part (2 to 10 mol%) is expanded and joined to said liquid phase of the fourth circuit.
  • part of the gas to be purified does not pass through the fifth circuit and is sent directly to the gas-liquid separation zone or to the first circuit.
  • a fraction of 80 to 95 mol% of the gas passes through the fifth circuit, and a fraction of 5 to 20 mol% is sent to the separation zone. It is thus possible to maximize the quantity of purified gas obtained by the second circuit.
  • Yet another variant consists in supplying a liquid phase of external origin to the exchanger, under conditions where this liquid phase can relax and evaporate after expansion during its passage from top to bottom in the exchanger.
  • This liquid phase of external origin can first pass through the exchanger from bottom to top by an auxiliary circuit to undergo sub-cooling there before descending by an auxiliary circuit. This is advantageous when starting the installation to facilitate and accelerate its cooling. More simply, if its composition is compatible with that of the liquid of the third circuit, it can be mixed with the latter before the entry thereof into the third circuit or only before the entry of said liquid into the fourth circuit.
  • the condensation rate of the gaseous supply fluid in the fifth circuit is also advantageous to adjust the condensation rate of the gaseous supply fluid in the fifth circuit to a value of 2 to 20% by mole.
  • the temperature and pressure conditions in the unitary heat exchange zone of the invention depend, obviously, the composition of the feedstock, and the technician will be able to choose these conditions in each particular case using his knowledge, the main thing being to operate under conditions allowing partial condensation of the fluid. food. Due to the fact that it is a cryogenic process, the operation is carried out below ambient temperature, for example between 0 ° C. and -150 ° C. depending on the gas treated and the pressure chosen. As, moreover, an expansion of the condensates is provided, one advantageously operates at a super-atmospheric pressure, for example between 5 and 100 bars. Below are values given as examples.
  • the invention also relates to a heat exchanger making it possible to implement the method described above.
  • This exchanger is characterized in that it comprises at least five distinct circuits, generally vertical, designated respectively first, second, third, fourth and fifth circuits, in indirect heat exchange relationship with each other at each level of said exchanger, said circuits forming a unitary assembly, the first circuit being of the non-tortuous type and the fifth circuit of the tortuous type, the first circuit being disposed at a level higher than that of the fifth circuit, at least one direct junction between the top of the first circuit and the top of the second circuit, at least one junction through an expansion means between the top of the third circuit and the top of the fourth circuit, at least one zone of separation of phases connected by its upper part to the base of the first circuit, by its lower part to the base of the third circuit and laterally at the top of the fifth circuit.
  • the first circuit is superimposed on the fifth circuit.
  • FIGS 1 and 2 attached illustrate the invention without limitation.
  • the heat exchanger E1 has five main circuits C1 to C5 corresponding respectively to the first, second, third, fourth and fifth circuits of the process.
  • the gas to be purified is sent by lines 1 and 3 to the circuit C5 and leaves it by line 2 in the mixed gas / first condensate phase.
  • the two phases separate in the flask B1: the gas phase is sent by line 16 to the circuit C1; it undergoes cooling there and a second condensate forms and flows back through line 17.
  • the uncondensed gas leaves at the head and is sent by lines 5 and 7 to circuit C2. It comes out warmed at the bottom of this circuit by line 14. This gives the purified gas or the lightest fraction of the charge.
  • the condensates coming from circuits C5 and C1 respectively by lines 2 and 17 are mixed and sent by line 4 to circuit C3 where they undergo sub-cooling. They come out at the head by line 8, pass through the expansion valve V1 and are sent to circuit C4 by line 9. They can pass through a balloon B2, in which case the gas phase and the liquid phase are sent to C4 respectively by the lines 18 and 19 to point 10.
  • the condensates vaporized leaves the circuit C4 via line 11. These are the least volatile fractions of the charge.
  • part of the gas from the circuit C1 is taken from line 5 and sent through the expansion valve V2 and line 6 to the cylinder B2.
  • part of the starting gas is sent to the balloon B1 through the line 15 and the valve V4.
  • a liquid phase compatible with the condensate of line 4 is sent by line 12 to an auxiliary circuit C6 to undergo sub-cooling there before passing through line 13 and the expansion valve V3 and sent to the balloon. B2, preferably by line 9.
  • each circuit is separated from the neighboring circuit by a vertical sheet like the sheets 20, 21, 22, etc.
  • each circuit is of the multi-channel type, circuits C1 and C3 being examples of this, in fact we see vertical sheets such as 23 (corrugated sheet) or 24 (flat partition). ) dividing the circuits into a plurality of elementary channels such as 25 and 26.
  • channels 2, 16 and 17 relating to the fifth (2) and first (16 and 17) circuits of Figure 1, with their equivalents 2 ', 16', 17 ', 2'',16'' and 17 ".
  • the lateral conduits 2, 16, 17 (and their prime and second equivalents) are connected to separate balloons B1 or to a common elongated balloon B1.
  • Valves V2, V3 and V4 are closed.
  • Line 6,111,703 kmol / h of hydrogen-enriched gas containing less than 1 mol% of ethylene is collected under a pressure of 34.7 bar abs and 10.086 kmol / h of gas highly enriched in ethylene in line 12 under a pressure of 1.8 bar abs.
  • the latter gas can be sent to a distillation column to obtain an even richer stream of ethylene.
  • Table 1 The current compositions of the installation are shown in Table 1.
  • Example 2 The procedure is as in Example 1, however, partially opening the valve V2 to allow the vaporization of the fluid circulating in the circuit 4 at higher pressure.
  • Tables 2 and 6 give respectively the compositions of the fluids, at the inlet and at the outlet, and the operating conditions.
  • Example 3 The procedure is as in Example 3 with, in addition, partial opening of the valve V3 allowing the introduction of a distillate consisting of a 50/50 mixture by volume of methane and ethylene, obtained by rectification of the purified gas from a previous operation.
  • Such an operating mode is used when starting the installation to facilitate its cooling.
  • Tables 4 and 8 give the compositions of the fluids and the operating conditions.
  • TABLE 1 Gas to be purified (line 1) Purified gas (line 14) Separate gas (line 11) Molar composition Hydrogen % mol 62.3100 67.7567 1.9871 Carbon monoxide % mol 0.3814 0.4073 0.0941 Methane % mol 31.3551 31.0198 35.0688 Acetylene % mol 0.0369 0.0013 0.4312 Ethylene % mol 5.4370 0.8057 56.7295 Ethane % mol 0.4784 0.0092 5.6743 Propylene % mol 0.0012 0.0000 0.0149 Temperature ° C -93.00 -95.00 -100.00 Pressure abs bar 35.00 34.70 1.80 Molar flow Kmol / h 121,788 111.703 10,086 Gas to be purified (line 1) Purified gas (line 14) Separate gas (line 11) Molar composition Hydrogen % mol 62.3100 67.7566 12.87

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
EP94401517A 1993-07-15 1994-07-01 Procédé autoréfrigéré de fractionnement cryogénique et de purification de gaz et échangeur de chaleur pour la mise en oeuvre de ce procédé Expired - Lifetime EP0634618B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9308695A FR2707745B1 (fr) 1993-07-15 1993-07-15 Procédé autoréfrigéré de fractionnement cryogénique et de purification de gaz et échangeur de chaleur pour la mise en Óoeuvre de ce procédé.
FR9308695 1993-07-15

Publications (2)

Publication Number Publication Date
EP0634618A1 EP0634618A1 (fr) 1995-01-18
EP0634618B1 true EP0634618B1 (fr) 1997-09-03

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US (1) US5461870A (zh)
EP (1) EP0634618B1 (zh)
JP (1) JPH07167556A (zh)
KR (1) KR950003753A (zh)
CN (1) CN1102879A (zh)
BR (1) BR9402812A (zh)
CO (1) CO4410270A1 (zh)
DE (1) DE69405330T2 (zh)
ES (1) ES2109631T3 (zh)
FR (1) FR2707745B1 (zh)
MY (1) MY111414A (zh)
RU (1) RU2126519C1 (zh)

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US5596883A (en) * 1995-10-03 1997-01-28 Air Products And Chemicals, Inc. Light component stripping in plate-fin heat exchangers
DE19645077C1 (de) * 1996-10-31 1997-10-16 Paul Haslauer Behandlungsanlage zur Durchführung eines Wannen- und/oder Dampfbades
US5937656A (en) * 1997-05-07 1999-08-17 Praxair Technology, Inc. Nonfreezing heat exchanger
US5802871A (en) * 1997-10-16 1998-09-08 Air Products And Chemicals, Inc. Dephlegmator process for nitrogen removal from natural gas
CN1186942A (zh) * 1997-10-27 1998-07-08 易元明 工业废气深冷净化与发电的工艺方法及其装置
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US6295836B1 (en) * 2000-04-14 2001-10-02 Praxair Technology, Inc. Cryogenic air separation system with integrated mass and heat transfer
US6237366B1 (en) * 2000-04-14 2001-05-29 Praxair Technology, Inc. Cryogenic air separation system using an integrated core
US6266977B1 (en) 2000-04-19 2001-07-31 Air Products And Chemicals, Inc. Nitrogen refrigerated process for the recovery of C2+ Hydrocarbons
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MY111414A (en) 2000-04-29
CO4410270A1 (es) 1997-01-09
BR9402812A (pt) 1995-04-04
ES2109631T3 (es) 1998-01-16
US5461870A (en) 1995-10-31
RU94026286A (ru) 1996-08-10
RU2126519C1 (ru) 1999-02-20
DE69405330D1 (de) 1997-10-09
CN1102879A (zh) 1995-05-24
DE69405330T2 (de) 1998-04-02
FR2707745B1 (fr) 1995-10-06
EP0634618A1 (fr) 1995-01-18
KR950003753A (ko) 1995-02-17
JPH07167556A (ja) 1995-07-04
FR2707745A1 (fr) 1995-01-20

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