EP2665678A1 - Process and apparatus for production of ammonia synthesis gas and pure methane by cryogenic separation - Google Patents

Process and apparatus for production of ammonia synthesis gas and pure methane by cryogenic separation

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Publication number
EP2665678A1
EP2665678A1 EP11856493.9A EP11856493A EP2665678A1 EP 2665678 A1 EP2665678 A1 EP 2665678A1 EP 11856493 A EP11856493 A EP 11856493A EP 2665678 A1 EP2665678 A1 EP 2665678A1
Authority
EP
European Patent Office
Prior art keywords
nitrogen
gas
liquid
column
phase separator
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP11856493.9A
Other languages
German (de)
French (fr)
Other versions
EP2665678A4 (en
Inventor
Jean-Marc Tsevery
Antoine Hernandez
Yuan-jun HU
Yanfang Liu
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP2665678A1 publication Critical patent/EP2665678A1/en
Publication of EP2665678A4 publication Critical patent/EP2665678A4/en
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/506—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification at low temperatures
    • 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
    • F25J3/0223—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis 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
    • F25J3/0228—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
    • F25J3/0276—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 H2/N2 mixtures, i.e. of ammonia synthesis 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • 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
    • F25J2200/72—Refluxing the column with at least a part of the totally 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
    • 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
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • 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
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • 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
    • F25J2210/42—Nitrogen
    • 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
    • F25J2215/02—Mixing or blending of fluids to yield a certain product
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/02—Separating impurities in general from the feed stream
    • 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/02—Integration in an installation for exchanging heat, e.g. for waste heat recovery
    • 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
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop

Definitions

  • the present invention relates to a process and apparatus for the production of ammonia synthesis gas and pure methane by cryogenic separation of a feed gas.
  • the feed gas preferably contains at least 75%. hydrogen and at least 5%. methane.
  • the term "pure methane” means that the methane produced contains at least 80% methane, preferably at least 85% methane and preferably less than 2% nitrogen, or even less than 1.5% nitrogen.
  • Ammonia synthesis plants are fed by a mixture of hydrogen and nitrogen in stoichiometric proportions. Certain components, such as argon, methane, oxygen, carbon monoxide or carbon dioxide are considered as inert or catalyst poisons for the synthesis process.
  • This hydrogen which is to be mixed with the nitrogen needs to be purified.
  • This hydrogen may be produced by a steam reformer or a coal gasification process for example.
  • an off gas from an acetylene plant is treated by partial condensation to produce a hydrogen stream and the hydrogen stream is sent to a nitrogen wash column.
  • the liquid from the partial condensation is further treated in a column.
  • One object of the present invention is to treat the liquid from the partial condensation to produce a methane rich stream.
  • it is desired to produce a methane riche stream containing very little nitrogen. If the methane is subsequently used to generate synthesis gas, the presence of nitrogen in the methane increases the size of the heaters and the unit used to form the gas.
  • a process for the production of ammonia synthesis gas and pure methane by cryogenic separation of a feed gas containing at least 75% hydrogen as well as methane and nitrogen, preferably at least 5% nitrogen wherein the feed gas is cooled in a heat exchanger and partially condensed, the partially condensed feed is sent to a phase separator, the gas from the phase separator is sent to a nitrogen wash column, liquid nitrogen is sent to the top of the nitrogen wash column and ammonia synthesis gas is removed from the top of the nitrogen wash column, the liquid from the phase separator is expanded and sent to a separation column, a nitrogen enriched gas stream is removed from the top of the column and a nitrogen depleted liquid stream rich in methane is removed from the bottom of the column and the nitrogen depleted liquid stream rich in methane is vaporised to form a pure methane product.
  • the nitrogen enriched gas stream contains at least 50% nitrogen and/or at least 20% carbon monoxide.
  • the nitrogen depleted stream contains at least 80% methane, preferably at least
  • the gas from the phase separator contains at least 90% hydrogen.
  • the nitrogen wash column operates at between 25 and 35 bars.
  • the separation column operates at between 1.5 and 8 bars.
  • the separation column has a bottom reboiler and at least a part of the feed gas and/or a gas derived from the feed gas is used to heat the bottom reboiler.
  • the separation column has a top condenser and wherein liquid nitrogen is vaporised in the top condenser, the nitrogen enriched gas stream is partially condensed in the top condenser and the liquid from the phase separator is sent to an intermediate region of the separation column.
  • the separation column has no top condenser and wherein liquid from the phase separator is sent to the top of the separation column.
  • liquid from the bottom of the nitrogen wash column is vaporised in the heat exchanger.
  • the liquid sent to the separation column from the phase separator contains at least 65% methane, preferably at least 70% methane and at least 5% nitrogen, preferably at least 10% nitrogen.
  • an apparatus for the production of ammonia synthesis gas and pure methane by cryogenic separation of a feed gas containing at least 75% hydrogen as well as methane and nitrogen, preferably at least 5% nitrogen comprising a heat exchanger wherein the feed gas is cooled and partially condensed, a phase separator, a conduit for sending the partially condensed feed to the phase separator, a nitrogen wash column, a separation column, a conduit for sending gas from the phase separator to the nitrogen wash column, a conduit for sending liquid nitrogen to the top of the nitrogen wash column, a conduit fro removing ammonia synthesis gas from the top of the nitrogen wash column, a valve for expanding liquid from the phase separator connected to the separation column via a conduit, a conduit for removing a nitrogen enriched gas stream from the top of the column and a conduit for removing nitrogen depleted liquid stream rich in methane from the bottom of the column and means for vaporising the nitrogen depleted liquid stream rich in methane to
  • the separation column has a bottom reboiler and comprising a conduit for sending at least a part of the feed gas and/or a gas derived from the feed gas to heat the bottom reboiler.
  • the apparatus comprises means for cooling and partially condensing the feed gas to form a gas and a liquid and means for sending at least a part of the gas resulting from the partial condensation to the reboiler.
  • the apparatus comprises a conduit for sending liquid from the bottom of the nitrogen wash column to the top of the separation column.
  • the separation column has a top condenser and the apparatus comprises a conduit for sending liquid nitrogen to the top condenser, a conduit for sending the nitrogen enriched gas stream to the top condenser and a conduit for sending the liquid from the phase separator to an intermediate region of the separation column.
  • the separation column has no top condenser and the apparatus comprises a conduit for sending liquid from the phase separator to the top of the separation column.
  • a hydrogen rich gas derived from a Rectisol unit ® has previously been purified in a molecular sieve purification unit to remove carbon dioxide and methanol.
  • This feed gas 1 at between 30 and 40 bars and at -53°C contains at least 75% hydrogen, at least 2% nitrogen and at least 6% methane and may also contain carbon monoxide, argon or hydrocarbon impurities, such as ethane.
  • the feed gas 1 is divided in two parts 5, 3.
  • One part 5 is cooled in the main exchanger line 7 and partially condensed before being sent to first phase separator 9.
  • the main heat exchanger line is in two sections 7, 85, section 7 being the colder of the two.
  • the vapour phase 6 from the phase separator 9 is mixed with the other part 3 of the feed gas to form gas stream 11
  • the gas stream 11 is sent to bottom reboiler 21 of the separation column 19 and then to a second phase separator 23.
  • the gas 25 from the second phase separator 23 is sent to the main heat exchanger line 7 to be cooled and then to the third phase separator 31.
  • the gas 25 may be mixed with part 81 of feed gas 11 after expansion in valve 81.
  • the top gas from the third separator 31 is sent to the bottom of nitrogen washing column 45 as feed.
  • the top gas 33 contains 93% H 2 ; 4% N 2 ; 2% CO and 1% CH 4 .
  • the liquid 35 from the third phase separator 31 is sent to separation column 19 after expansion in valve 37.
  • the liquid 35 contains at least 65% methane or even at least 70% methane with at least 5% nitrogen or even at least 10% nitrogen, the balance being made up of hydrogen, carbon monoxide and other impurities.
  • the bottom liquid 39 of the column contains at least 80 % methane, preferably at least 85% methane with less than 2 % of N 2 , still more preferably with less than 1.5% nitrogen.
  • the CH 4 rich liquid is expanded in valve 41 and sent to fourth phase separator 17.
  • the liquid 73 from the fourth phase separator 17 after vaporization and warming up in the main heat exchanger line 7 is sent to battery limit to be used for example as feed to steam reformer after compression.
  • the gas 71 from the fourth phase separator 17 is also sent to the battery limit after warming in the main heat exchange line 7.
  • Top gas 43 from the separation column 19 contains at least 50% nitrogen, at least
  • the separation column 19 has no top condenser.
  • Reboiling duty of separation column 19 is provided by cooling down of the feed gas 1 and/or a gas derived from the feed gas 1 by cooling and phase separation. Liquid 13 from the first phase separator 9 is expanded in valve 15 and sent to the fourth phase separator 17.
  • Liquid 27 from the second phase separator 23 is expanded in valve 29 and sent to the fourth phase separator 17.
  • the high pressure nitrogen gas HPN 2 65 at around 40 bars is cooled down and liquefied in the main exchanger line 7. Part of the high pressure nitrogen HPN 2 is sent to the top of the column 45 and the rest of the HPN 2 part 59 is mixed with H 2 rich gas 57 coming from nitrogen wash column 45 according to the requirements of the ammonia synthesis.
  • One part 69 of the product forming ammonia synthesis gas from the top of the nitrogen washing column 45 is warmed up to ambient temperature through the main exchanger line 85.
  • Another part 67 of the ammonia synthesis gas product will be warmed up in the Rectisol ® exchanger for cold recovery.
  • the ammonia synthesis gas 67, 69 contains 75% hydrogen and 25% nitrogen.
  • the nitrogen wash column bottom liquid 47 is expanded in valve 49 to low pressure (for example 3-5 bar) and sent to a fifth phase separator 51.
  • the gas 53 and the liquid 55 are sent to the main exchanger line 7 separately for cold recovery. These two fluids 53, 55 are mixed after vaporization of the liquid and sent to the battery limits as the fuel gas.
  • the cold balance is achieved by injection of liquid nitrogen supplied at battery limit from an air separation unit.
  • the nitrogen wash column 45 operates at between 25 and 35 bars and the separation column 19 at between 1, 5 and 7 bars.
  • the hydrogen rich gas derived from a Rectisol unit ® has previously been purified in a molecular sieve purification unit to remove carbon dioxide and methanol.
  • This feed gas 1 at between 30 and 40 bars and at -53°C contains at least 75 % hydrogen, at least 2% nitrogen and at least 6% methane and may also contain carbon monoxide, argon or hydrocarbon impurities, such as ethane.
  • the feed gas 1 is divided in two parts 5, 3. One part 5 is cooled in the main exchanger line 7 and partially condensed before being sent to first phase separator 9. .
  • the vapour phase 6 from the phase separator 9 is mixed with the other part 3 of the feed gas to form gas stream 11
  • the gas stream 11 is sent to bottom reboiler 21 of the separation column 19 and then to a second phase separator 23.
  • the gas 25 from the second phase separator 23 is sent to the main heat exchanger line 7 to be cooled and then to the third phase separator 31.
  • the gas 25 may be mixed with part 81 of feed gas 11 after expansion in valve 81.
  • the top gas from the third separator 31 is sent to the bottom of nitrogen washing column 45 as feed.
  • the top gas 33 contains 93% H 2 ; 4% N 2 ; 2% CO and 1% CH 4 .
  • the liquid 35 from the third phase separator 31 is sent to the middle of the separation column 19 after expansion in valve 37.
  • the liquid 35 contains at least 65% methane or even at least 70% methane with at least 5% nitrogen or even at least 10% nitrogen, the balance being made up of hydrogen, carbon monoxide and other impurities.
  • the bottom liquid 39 of the column contains at least 80% methane, preferably at least 85% methane with less than 2 % of N 2 , still more preferably with less than 1.5% nitrogen.
  • the CH 4 rich liquid is expanded in valve 41 and sent to fourth phase separator 17.
  • the liquid 73 from the fourth phase separator 17 after vaporization and warming up in the main heat exchanger line 7 is sent to battery limit to be used for example as feed to steam reformer after compression.
  • the gas 71 from the fourth phase separator 17 is also sent to the battery limit after warming in the main heat exchange line 7.
  • Top gas 43 from the separation column 19 contains at least 50% nitrogen, at least 20% carbon monoxide and a little hydrogen and methane and is sent to top condenser 75 to be condensed by heat exchange with liquid nitrogen LIN. Part 43 of the top gas is used as fuel after being warmed up in the main exchanger line 7.
  • Reboiling duty of separation column 19 is provided by cooling down of the feed gas 1 and/or a gas derived from the feed gas 1 by cooling and phase separation.
  • Liquid 13 from the first phase separator 9 is expanded in valve 15 and sent to the fourth phase separator 17.
  • Liquid 27 from the second phase separator 23 is expanded in valve 29 and sent to the fourth phase separator 17.
  • the high pressure nitrogen gas HPN 2 65 at around 40 bars is cooled down and liquefied in the main exchanger line 7. Part of the high pressure nitrogen HPN 2 is sent to the top of the column 45 and the rest of the HPN 2 part 59 is mixed with H 2 rich gas 57 coming from nitrogen wash column 45 according to the requirements of the ammonia synthesis.
  • One part 69 of the product forming ammonia synthesis gas from the top of the nitrogen washing column 45 is warmed up to ambient temperature through the main exchanger line 7.
  • Another part 67 of the ammonia synthesis gas product will be warmed up in the Rectisol ® exchanger for cold recovery.
  • the ammonia synthesis gas 67, 69 contains 75% hydrogen and 25% nitrogen.
  • the nitrogen wash column bottom liquid is expanded in valve 49 to low pressure (for example 1.5 - 7 bar) and sent to the top of the separation column 19 in liquid form.
  • Vaporised nitrogen 77 from the condenser 75 is warmed in the main heat exchanger 7.
  • the cold balance is achieved by injection of liquid nitrogen supplied at battery limit from an air separation unit.
  • FIG 3 a variant of Figure 1 is shown with a sixth phase separator in series with the fifth phase separator.
  • a hydrogen rich gas derived from a Rectisol unit ® has previously been purified in a molecular sieve purification unit to remove carbon dioxide and methanol.
  • This feed gas 1 at between 30 and 40 bars and at -53°C contains at least 75% hydrogen, at least 2% nitrogen and at least 6% methane and may also contain carbon monoxide, argon or hydrocarbon impurities, such as ethane.
  • the feed gas 1 is divided in two parts 5, 3. One part 5 is cooled in the main exchanger line 7 and partially condensed before being sent to first phase separator 9. .
  • the vapour phase 6 from the phase separator 9 is mixed with the other part 3 of the feed gas to form gas stream 11
  • the gas stream 11 is sent to bottom reboiler 21 of the separation column 19 and then to a second phase separator 23.
  • the gas 25 from the second phase separator 23 is sent to the main heat exchanger line 7 to be cooled and then to the third phase separator 31.
  • the gas 25 may be mixed with part 81 of feed gas 11 after expansion in valve 81.
  • the top gas from the third separator 31 is sent to the bottom of nitrogen washing column 45 as feed.
  • the top gas 33 contains93% H 2 ; 4% N 2 ; 2% CO and 1% CH 4 .
  • the liquid 35 from the third phase separator 31 is sent to separation column 19 after expansion in valve 37.
  • the liquid 35 contains at least 65% methane or at least 70% methane with at least 5% nitrogen or even at least 10% nitrogen, the balance being made up of hydrogen, carbon monoxide and other impurities.
  • the bottom liquid 39 of the column contains at least 80 % methane, preferably at least 85% methane with less than 2 % of N2, still more preferably with less than 1.5% nitrogen.
  • the CH 4 rich liquid is expanded in valve 41 and sent to fourth phase separator 17.
  • the liquid 73 from the fourth phase separator 17 after vaporization and warming up in the main heat exchanger line 7 is sent to battery limit to be used for example as feed to steam reformer after compression.
  • the gas 71 from the fourth phase separator 17 is also sent to the battery limit after warming in the main heat exchange line 7.
  • Top gas 43 from the separation column 19 contains at least 50% nitrogen, at least 20% carbon monoxide and a little hydrogen and methane and is used as fuel after being warmed up in the main exchanger line 7.
  • the separation column 19 has no top condenser.
  • Reboiling duty of separation column 19 is provided by cooling down of the feed gas 1 and/or a gas derived from the feed gas 1 by cooling and phase separation.
  • Liquid 13 from the first phase separator 9 is expanded in valve 15 and sent to the fourth phase separator 17.
  • Liquid 27 from the second phase separator 23 is expanded in valve 29 and sent to the fourth phase separator 17.
  • the high pressure nitrogen gas HPN 2 65 at around 40 bars is cooled down and liquefied in the main exchanger line 7. Part of High pressure nitrogen HPN 2 is sent to the top of the column 45 and the rest of the HPN 2 part 59 is mixed with H 2 rich gas 57 coming from nitrogen wash column 45 according to the requirements of the ammonia synthesis.
  • One part 69 of the product forming ammonia synthesis gas from the top of the nitrogen washing column 45 is warmed up to ambient temperature through the main exchanger line 7.
  • Another part 67 of the ammonia synthesis gas product will be warmed up in the Rectisol ® exchanger for cold recovery.
  • the ammonia synthesis gas 67, 69 contains 75% hydrogen and 25% nitrogen.
  • the nitrogen wash column bottom liquid 47 is expanded in valve 49 to medium pressure (for example 7-14 bar) and sent to a fifth phase separator 51.
  • the gas 53, rich in hydrogen, is sent to the main exchanger line 7 for cold recovery.
  • Gas 53 can be sent to the inlet of the Rectisol ® recycle compressor to increase the hydrogen yield.
  • the liquid from the fifth phase separator 51 is expanded in valve 89 and then sent to sixth phase separator 91.
  • the gas 93 from the sixth phase separator 91 is warmed in heat exchangers 7, 85 and the liquid 95 is vaporized in heat exchange line 7 and warmed in heat exchanger 85.
  • the cold balance is achieved by injection of liquid nitrogen supplied at battery limit from an air separation unit.
  • the nitrogen wash column 45 operates at between 25 and 35 bars and the separation column 19 at between 1, 5 and 7 bars.

Abstract

A process for the production of ammonia synthesis gas and pure methane by cryogenic separation of a feed gas containing at least 75% hydrogen as well as methane and nitrogen, the feed gas is cooled in a heat exchanger and partially condensed, the partially condensed feed is sent to a phase separator, the gas from the phase separator is sent to a nitrogen wash column, liquid nitrogen is sent to the top of the nitrogen wash column and ammonia synthesis gas is removed from the top of the nitrogen wash column, the liquid from the phase separator is expanded and sent to a separation column, a nitrogen enriched gas stream is removed from the top of the column and a nitrogen depleted liquid stream rich in methane is removed from the bottom of the column and the nitrogen depleted liquid stream rich in methane is vaporized to form a pure methane product.

Description

PROCESS AND APPARATUS FOR PRODUCTION OF AMMONIA SYNTHESIS GAS AND PURE METHANE BY CRYOGENIC SEPARATION The present invention relates to a process and apparatus for the production of ammonia synthesis gas and pure methane by cryogenic separation of a feed gas.
The feed gas preferably contains at least 75%. hydrogen and at least 5%. methane. The term "pure methane" means that the methane produced contains at least 80% methane, preferably at least 85% methane and preferably less than 2% nitrogen, or even less than 1.5% nitrogen.
All the purities in this document are expressed in molar percentages. All pressures are absolute pressures.
Ammonia synthesis plants are fed by a mixture of hydrogen and nitrogen in stoichiometric proportions. Certain components, such as argon, methane, oxygen, carbon monoxide or carbon dioxide are considered as inert or catalyst poisons for the synthesis process.
Thus the hydrogen which is to be mixed with the nitrogen needs to be purified. This hydrogen may be produced by a steam reformer or a coal gasification process for example.
It is known from DE-A-2814660 to produce the ammonia synthesis gas by washing the hydrogen in a nitrogen wash process in which liquid nitrogen is sent to the top of the wash column.
In this case, an off gas from an acetylene plant is treated by partial condensation to produce a hydrogen stream and the hydrogen stream is sent to a nitrogen wash column. The liquid from the partial condensation is further treated in a column.
One object of the present invention is to treat the liquid from the partial condensation to produce a methane rich stream. In particular, it is desired to produce a methane riche stream containing very little nitrogen. If the methane is subsequently used to generate synthesis gas, the presence of nitrogen in the methane increases the size of the heaters and the unit used to form the gas.
In addition, if the synthesis gas formed using the nitrogen containing methane is in its turn used to feed a methanol synthesis unit, the presence of nitrogen reduces the product because it increases the size of the purge stream
It is consequently desirable to reduce the nitrogen content of the stream. According to an object of the invention, there is provided a process for the production of ammonia synthesis gas and pure methane by cryogenic separation of a feed gas containing at least 75% hydrogen as well as methane and nitrogen, preferably at least 5% nitrogen wherein the feed gas is cooled in a heat exchanger and partially condensed, the partially condensed feed is sent to a phase separator, the gas from the phase separator is sent to a nitrogen wash column, liquid nitrogen is sent to the top of the nitrogen wash column and ammonia synthesis gas is removed from the top of the nitrogen wash column, the liquid from the phase separator is expanded and sent to a separation column, a nitrogen enriched gas stream is removed from the top of the column and a nitrogen depleted liquid stream rich in methane is removed from the bottom of the column and the nitrogen depleted liquid stream rich in methane is vaporised to form a pure methane product.
According to further optional embodiments:
- the nitrogen enriched gas stream contains at least 50% nitrogen and/or at least 20% carbon monoxide.
- the nitrogen depleted stream contains at least 80% methane, preferably at least
85% methane , and at most 2% nitrogen , preferably at most 1.5% nitrogen.
- the gas from the phase separator contains at least 90% hydrogen.
- the nitrogen wash column operates at between 25 and 35 bars.
- the separation column operates at between 1.5 and 8 bars.
- the separation column has a bottom reboiler and at least a part of the feed gas and/or a gas derived from the feed gas is used to heat the bottom reboiler.
- feed gas is cooled and partially condensed to form a gas and a liquid and at least a part of the gas resulting from the partial condensation is used to reboil the separation column.
- liquid from the bottom of the nitrogen wash column is sent to the top of the separation column.
- the separation column has a top condenser and wherein liquid nitrogen is vaporised in the top condenser, the nitrogen enriched gas stream is partially condensed in the top condenser and the liquid from the phase separator is sent to an intermediate region of the separation column.
-the separation column has no top condenser and wherein liquid from the phase separator is sent to the top of the separation column.
- liquid from the bottom of the nitrogen wash column is vaporised in the heat exchanger. - the liquid sent to the separation column from the phase separator contains at least 65% methane, preferably at least 70% methane and at least 5% nitrogen, preferably at least 10% nitrogen.
According to a further object of the invention, there is provided an apparatus for the production of ammonia synthesis gas and pure methane by cryogenic separation of a feed gas containing at least 75% hydrogen as well as methane and nitrogen, preferably at least 5% nitrogen comprising a heat exchanger wherein the feed gas is cooled and partially condensed, a phase separator, a conduit for sending the partially condensed feed to the phase separator, a nitrogen wash column, a separation column, a conduit for sending gas from the phase separator to the nitrogen wash column, a conduit for sending liquid nitrogen to the top of the nitrogen wash column, a conduit fro removing ammonia synthesis gas from the top of the nitrogen wash column, a valve for expanding liquid from the phase separator connected to the separation column via a conduit, a conduit for removing a nitrogen enriched gas stream from the top of the column and a conduit for removing nitrogen depleted liquid stream rich in methane from the bottom of the column and means for vaporising the nitrogen depleted liquid stream rich in methane to form a pure methane product.
According to further optional features:
- the separation column has a bottom reboiler and comprising a conduit for sending at least a part of the feed gas and/or a gas derived from the feed gas to heat the bottom reboiler.
- the apparatus comprises means for cooling and partially condensing the feed gas to form a gas and a liquid and means for sending at least a part of the gas resulting from the partial condensation to the reboiler.
- the apparatus comprises a conduit for sending liquid from the bottom of the nitrogen wash column to the top of the separation column.
- the separation column has a top condenser and the apparatus comprises a conduit for sending liquid nitrogen to the top condenser, a conduit for sending the nitrogen enriched gas stream to the top condenser and a conduit for sending the liquid from the phase separator to an intermediate region of the separation column.
- the separation column has no top condenser and the apparatus comprises a conduit for sending liquid from the phase separator to the top of the separation column.
- a conduit for sending liquid from the bottom of the nitrogen wash column to be vaporised in the heat exchanger. The invention will be described in more detail, referring to Figures 1 to 3 which represent processes according to the invention.
In Figure 1, a hydrogen rich gas derived from a Rectisol unit ® has previously been purified in a molecular sieve purification unit to remove carbon dioxide and methanol.
This feed gas 1 at between 30 and 40 bars and at -53°C contains at least 75% hydrogen, at least 2% nitrogen and at least 6% methane and may also contain carbon monoxide, argon or hydrocarbon impurities, such as ethane. The feed gas 1 is divided in two parts 5, 3. One part 5 is cooled in the main exchanger line 7 and partially condensed before being sent to first phase separator 9. The main heat exchanger line is in two sections 7, 85, section 7 being the colder of the two.
The vapour phase 6 from the phase separator 9 is mixed with the other part 3 of the feed gas to form gas stream 11 The gas stream 11 is sent to bottom reboiler 21 of the separation column 19 and then to a second phase separator 23. The gas 25 from the second phase separator 23 is sent to the main heat exchanger line 7 to be cooled and then to the third phase separator 31. The gas 25 may be mixed with part 81 of feed gas 11 after expansion in valve 81. The top gas from the third separator 31 is sent to the bottom of nitrogen washing column 45 as feed. The top gas 33 contains 93% H2; 4% N2; 2% CO and 1% CH4.
The liquid 35 from the third phase separator 31 is sent to separation column 19 after expansion in valve 37. The liquid 35 contains at least 65% methane or even at least 70% methane with at least 5% nitrogen or even at least 10% nitrogen, the balance being made up of hydrogen, carbon monoxide and other impurities. The bottom liquid 39 of the column contains at least 80 % methane, preferably at least 85% methane with less than 2 % of N2, still more preferably with less than 1.5% nitrogen. The CH4 rich liquid is expanded in valve 41 and sent to fourth phase separator 17. The liquid 73 from the fourth phase separator 17 after vaporization and warming up in the main heat exchanger line 7 is sent to battery limit to be used for example as feed to steam reformer after compression. The gas 71 from the fourth phase separator 17 is also sent to the battery limit after warming in the main heat exchange line 7.
Top gas 43 from the separation column 19 contains at least 50% nitrogen, at least
20% carbon monoxide and a little hydrogen and methane and is used as fuel after being warmed up in the main exchanger line 7. The separation column 19 has no top condenser.
Reboiling duty of separation column 19 is provided by cooling down of the feed gas 1 and/or a gas derived from the feed gas 1 by cooling and phase separation. Liquid 13 from the first phase separator 9 is expanded in valve 15 and sent to the fourth phase separator 17.
Liquid 27 from the second phase separator 23 is expanded in valve 29 and sent to the fourth phase separator 17.
The high pressure nitrogen gas HPN2 65 at around 40 bars is cooled down and liquefied in the main exchanger line 7. Part of the high pressure nitrogen HPN2 is sent to the top of the column 45 and the rest of the HPN2 part 59 is mixed with H2 rich gas 57 coming from nitrogen wash column 45 according to the requirements of the ammonia synthesis.
One part 69 of the product forming ammonia synthesis gas from the top of the nitrogen washing column 45 is warmed up to ambient temperature through the main exchanger line 85. Another part 67 of the ammonia synthesis gas product will be warmed up in the Rectisol ® exchanger for cold recovery.
The ammonia synthesis gas 67, 69 contains 75% hydrogen and 25% nitrogen.
The nitrogen wash column bottom liquid 47 is expanded in valve 49 to low pressure (for example 3-5 bar) and sent to a fifth phase separator 51. The gas 53 and the liquid 55 are sent to the main exchanger line 7 separately for cold recovery. These two fluids 53, 55 are mixed after vaporization of the liquid and sent to the battery limits as the fuel gas.
The cold balance is achieved by injection of liquid nitrogen supplied at battery limit from an air separation unit.
The nitrogen wash column 45 operates at between 25 and 35 bars and the separation column 19 at between 1, 5 and 7 bars.
In Figure 2, a different separation column is used, having a top condenser 75 in addition to bottom reboiler 21. The fifth phase separator 51 is eliminated.
The hydrogen rich gas derived from a Rectisol unit ® has previously been purified in a molecular sieve purification unit to remove carbon dioxide and methanol.
This feed gas 1 at between 30 and 40 bars and at -53°C contains at least 75 % hydrogen, at least 2% nitrogen and at least 6% methane and may also contain carbon monoxide, argon or hydrocarbon impurities, such as ethane. The feed gas 1 is divided in two parts 5, 3. One part 5 is cooled in the main exchanger line 7 and partially condensed before being sent to first phase separator 9. .
The vapour phase 6 from the phase separator 9 is mixed with the other part 3 of the feed gas to form gas stream 11 The gas stream 11 is sent to bottom reboiler 21 of the separation column 19 and then to a second phase separator 23. The gas 25 from the second phase separator 23 is sent to the main heat exchanger line 7 to be cooled and then to the third phase separator 31. The gas 25 may be mixed with part 81 of feed gas 11 after expansion in valve 81. The top gas from the third separator 31 is sent to the bottom of nitrogen washing column 45 as feed. The top gas 33 contains 93% H2; 4% N2; 2% CO and 1% CH4.
The liquid 35 from the third phase separator 31 is sent to the middle of the separation column 19 after expansion in valve 37. The liquid 35 contains at least 65% methane or even at least 70% methane with at least 5% nitrogen or even at least 10% nitrogen, the balance being made up of hydrogen, carbon monoxide and other impurities. The bottom liquid 39 of the column contains at least 80% methane, preferably at least 85% methane with less than 2 % of N2, still more preferably with less than 1.5% nitrogen. The CH4 rich liquid is expanded in valve 41 and sent to fourth phase separator 17. The liquid 73 from the fourth phase separator 17 after vaporization and warming up in the main heat exchanger line 7 is sent to battery limit to be used for example as feed to steam reformer after compression. The gas 71 from the fourth phase separator 17 is also sent to the battery limit after warming in the main heat exchange line 7.
Top gas 43 from the separation column 19 contains at least 50% nitrogen, at least 20% carbon monoxide and a little hydrogen and methane and is sent to top condenser 75 to be condensed by heat exchange with liquid nitrogen LIN. Part 43 of the top gas is used as fuel after being warmed up in the main exchanger line 7.
Reboiling duty of separation column 19 is provided by cooling down of the feed gas 1 and/or a gas derived from the feed gas 1 by cooling and phase separation.
Liquid 13 from the first phase separator 9 is expanded in valve 15 and sent to the fourth phase separator 17.
Liquid 27 from the second phase separator 23 is expanded in valve 29 and sent to the fourth phase separator 17.
The high pressure nitrogen gas HPN2 65 at around 40 bars is cooled down and liquefied in the main exchanger line 7. Part of the high pressure nitrogen HPN2 is sent to the top of the column 45 and the rest of the HPN2 part 59 is mixed with H2 rich gas 57 coming from nitrogen wash column 45 according to the requirements of the ammonia synthesis.
One part 69 of the product forming ammonia synthesis gas from the top of the nitrogen washing column 45 is warmed up to ambient temperature through the main exchanger line 7. Another part 67 of the ammonia synthesis gas product will be warmed up in the Rectisol ® exchanger for cold recovery.
The ammonia synthesis gas 67, 69 contains 75% hydrogen and 25% nitrogen.
The nitrogen wash column bottom liquid is expanded in valve 49 to low pressure (for example 1.5 - 7 bar) and sent to the top of the separation column 19 in liquid form. Vaporised nitrogen 77 from the condenser 75 is warmed in the main heat exchanger 7.
The cold balance is achieved by injection of liquid nitrogen supplied at battery limit from an air separation unit.
In Figure 3 a variant of Figure 1 is shown with a sixth phase separator in series with the fifth phase separator. As before a hydrogen rich gas derived from a Rectisol unit ® has previously been purified in a molecular sieve purification unit to remove carbon dioxide and methanol.
This feed gas 1 at between 30 and 40 bars and at -53°C contains at least 75% hydrogen, at least 2% nitrogen and at least 6% methane and may also contain carbon monoxide, argon or hydrocarbon impurities, such as ethane. The feed gas 1 is divided in two parts 5, 3. One part 5 is cooled in the main exchanger line 7 and partially condensed before being sent to first phase separator 9. .
The vapour phase 6 from the phase separator 9 is mixed with the other part 3 of the feed gas to form gas stream 11 The gas stream 11 is sent to bottom reboiler 21 of the separation column 19 and then to a second phase separator 23. The gas 25 from the second phase separator 23 is sent to the main heat exchanger line 7 to be cooled and then to the third phase separator 31. The gas 25 may be mixed with part 81 of feed gas 11 after expansion in valve 81. The top gas from the third separator 31 is sent to the bottom of nitrogen washing column 45 as feed. The top gas 33 contains93% H2; 4% N2; 2% CO and 1% CH4.
The liquid 35 from the third phase separator 31 is sent to separation column 19 after expansion in valve 37. The liquid 35 contains at least 65% methane or at least 70% methane with at least 5% nitrogen or even at least 10% nitrogen, the balance being made up of hydrogen, carbon monoxide and other impurities. The bottom liquid 39 of the column contains at least 80 % methane, preferably at least 85% methane with less than 2 % of N2, still more preferably with less than 1.5% nitrogen. The CH4 rich liquid is expanded in valve 41 and sent to fourth phase separator 17. The liquid 73 from the fourth phase separator 17 after vaporization and warming up in the main heat exchanger line 7 is sent to battery limit to be used for example as feed to steam reformer after compression. The gas 71 from the fourth phase separator 17 is also sent to the battery limit after warming in the main heat exchange line 7.
Top gas 43 from the separation column 19 contains at least 50% nitrogen, at least 20% carbon monoxide and a little hydrogen and methane and is used as fuel after being warmed up in the main exchanger line 7. The separation column 19 has no top condenser.
Reboiling duty of separation column 19 is provided by cooling down of the feed gas 1 and/or a gas derived from the feed gas 1 by cooling and phase separation.
Liquid 13 from the first phase separator 9 is expanded in valve 15 and sent to the fourth phase separator 17.
Liquid 27 from the second phase separator 23 is expanded in valve 29 and sent to the fourth phase separator 17.
The high pressure nitrogen gas HPN2 65 at around 40 bars is cooled down and liquefied in the main exchanger line 7. Part of High pressure nitrogen HPN2 is sent to the top of the column 45 and the rest of the HPN2 part 59 is mixed with H2 rich gas 57 coming from nitrogen wash column 45 according to the requirements of the ammonia synthesis.
One part 69 of the product forming ammonia synthesis gas from the top of the nitrogen washing column 45 is warmed up to ambient temperature through the main exchanger line 7. Another part 67 of the ammonia synthesis gas product will be warmed up in the Rectisol ® exchanger for cold recovery.
The ammonia synthesis gas 67, 69 contains 75% hydrogen and 25% nitrogen.
The nitrogen wash column bottom liquid 47 is expanded in valve 49 to medium pressure (for example 7-14 bar) and sent to a fifth phase separator 51. The gas 53, rich in hydrogen, is sent to the main exchanger line 7 for cold recovery. Gas 53 can be sent to the inlet of the Rectisol ® recycle compressor to increase the hydrogen yield.
The liquid from the fifth phase separator 51 is expanded in valve 89 and then sent to sixth phase separator 91. The gas 93 from the sixth phase separator 91 is warmed in heat exchangers 7, 85 and the liquid 95 is vaporized in heat exchange line 7 and warmed in heat exchanger 85.
The cold balance is achieved by injection of liquid nitrogen supplied at battery limit from an air separation unit.
For all the figures, the nitrogen wash column 45 operates at between 25 and 35 bars and the separation column 19 at between 1, 5 and 7 bars.

Claims

Claims
1. Process for the production of ammonia synthesis gas and pure methane by cryogenic separation of a feed gas containing at least 75% hydrogen as well as methane and nitrogen, preferably at least 5% nitrogen wherein the feed gas is cooled in a heat exchanger (7) and partially condensed, the partially condensed feed is sent to a phase separator (31), the gas from the phase separator is sent to a nitrogen wash column (45), liquid nitrogen is sent to the top of the nitrogen wash column and ammonia synthesis gas (57,67,69) is removed from the top of the nitrogen wash column, the liquid from the phase separator is expanded and sent to a separation column (19), a nitrogen enriched gas stream (43) is removed from the top of the column and a nitrogen depleted liquid stream (39) rich in methane is removed from the bottom of the column and the nitrogen depleted liquid stream rich in methane is vaporised to form a pure methane product (71, 73). 2. Process according to Claim 1 wherein the separation column (19) has a bottom reboiler (21) and at least a part (3) of the feed gas and/or a gas (6) derived from the feed gas is used to heat the bottom reboiler.
3. Process according to Claim 2 wherein feed gas is cooled and partially condensed to form a gas (6) and a liquid (13) and at least a part of the gas resulting from the partial condensation is used to reboil the separation column (19).
4. Process according to any preceding claim wherein liquid (47) from the bottom of the nitrogen wash column (45) is sent to the top of the separation column (19).
5. Process according to any preceding claim wherein the separation column (19) has a top condenser (75) and wherein liquid nitrogen is vaporised in the top condenser, the nitrogen enriched gas stream is partially condensed in the top condenser and the liquid from the phase separator (31) is sent to an intermediate region of the separation column
6. Process according to any of Claims 1 to 4 wherein the separation column (19) has no top condenser and wherein liquid from the phase separator (31) is sent to the top of the separation column.
7. Process according to Claim 6 wherein liquid from the bottom of the nitrogen wash column (47, 55, 95) is vaporised in the heat exchanger.
8. Process according to any preceding claim wherein the liquid sent to the separation column from the phase separator contains at least 65% methane, preferably at least 70% methane and at least 5% nitrogen, preferably at least 10% nitrogen.
9. Apparatus for the production of ammonia synthesis gas and pure methane by cryogenic separation of a feed gas containing at least 75% hydrogen as well as methane and nitrogen, preferably at least 5% nitrogen comprising a heat exchanger (7) wherein the feed gas is cooled and partially condensed, a phase separator (31), a conduit for sending the partially condensed feed to the phase separator, a nitrogen wash column (45), a separation column (19), a conduit for sending gas from the phase separator to the nitrogen wash column, a conduit for sending liquid nitrogen to the top of the nitrogen wash column, a conduit fro removing ammonia synthesis gas from the top of the nitrogen wash column, a valve (37) for expanding liquid from the phase separator connected to the separation column via a conduit, a conduit for removing a nitrogen enriched gas stream from the top of the column and a conduit for removing nitrogen depleted liquid stream rich in methane from the bottom of the column and means (7) for vaporising the nitrogen depleted liquid stream rich in methane to form a pure methane product.
10. Apparatus according to Claim 9 wherein the separation column (19) has a bottom reboiler (21) and comprising a conduit for sending at least a part of the feed gas and/or a gas derived from the feed gas to heat the bottom reboiler.
11. Apparatus according to Claim 10 comprising means for cooling and partially condensing the feed gas to form a gas and a liquid and means for sending at least a part of the gas resulting from the partial condensation to the reboiler (21). 12. Apparatus according to any of Claims 9 to 11 comprising a conduit for sending liquid from the bottom of the nitrogen wash column (45) to the top of the separation column (19).
13. Apparatus according to any of claims 9 to 12 wherein the separation column(19) has a top condenser (75) and comprising a conduit for sending liquid nitrogen to the top condenser, a conduit for sending the nitrogen enriched gas stream to the top condenser and a conduit for sending the liquid from the phase separator (31) to an intermediate region of the separation column
14. Apparatus according to any of Claims 9 to 12 wherein the separation column (19) has no top condenser and comprising a conduit for sending liquid from the phase separator (31) to the top of the separation column.
15. Process according to Claim 14 comprising a conduit for sending liquid from the bottom of the nitrogen wash column (45) to be vaporised in the heat exchanger (7).
EP11856493.9A 2011-01-17 2011-01-17 Process and apparatus for production of ammonia synthesis gas and pure methane by cryogenic separation Withdrawn EP2665678A4 (en)

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