Classifications

• • 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
  • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
  • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
  • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
  • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
  • C01B3/382—Multi-step processes
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
  • C01B2203/14—Details of the flowsheet
  • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
  • C01B2203/143—Three or more reforming, decomposition or partial oxidation steps in series
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
  • C01B2203/14—Details of the flowsheet
  • C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
  • C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
  • C01B2203/82—Several process steps of C01B2203/02 - C01B2203/08 integrated into a single apparatus

Definitions

• the method of producing synthesis gas for ammonia from hydrocarbons ( ⁇ , ⁇ , 4376758) is known, including: heating of raw hydrocarbons; Separation of the original steam and carbon mixture into two feeds, one of the feeds
• the present invention compares with that of ⁇ , ⁇ , 3441393 is a saving of 30% of the cost of carbohydrate consumption.
• 35 ⁇ dna ⁇ for u ⁇ azann ⁇ g ⁇ s ⁇ s ⁇ ba ⁇ a ⁇ a ⁇ e ⁇ n ⁇ nee ⁇ e ⁇ - ⁇ ivn ⁇ e is ⁇ lz ⁇ vanie ⁇ a ⁇ aliza ⁇ a in ⁇ tsesse ⁇ a ⁇ v ⁇ y ⁇ n- ve ⁇ sii ⁇ b ⁇ i ⁇ ⁇ v ⁇ a ⁇ uglev ⁇ d ⁇ dn ⁇ y mixture znachi ⁇ el- - 3-rd consumption of carbohydrate for consumption, a large content of in- tegrated metal in the industrial mixture due to the consumption of waste water.
• ba is an increase in the efficiency of the use of the catalytic converter, which reduces the volume of the system (reduction of the volume). This, however, is only available at the stage of the initial adiabatic coupled with an inoperative temperature.
• the indicated method is used to describe - - the second one is the conversion of hydrocarbon raw materials in the range of pressures from 25 to 50 bar and the temperature at the beginning of the process at 450 ° to 700 ° C when the pressure is turned on:
• the 5th part of the Republican Conversion is from 680 ° C to 790 ° C). There is a commercially available supply of 700 ° C to 900 ° C;
• the main object of the present invention has been set to by changing the conditions of the sale of an open communication service.
• the 35th gas supplied to the primary part is mixed before heating with the heater in the volumetric part of the medium: acid, equal to 0.5: 30.0.
• - 5 - ⁇ lag ⁇ da ⁇ ya zayavlyaem ⁇ mu iz ⁇ b ⁇ e ⁇ eniyu s ⁇ al ⁇ v ⁇ zm ⁇ zhn ⁇ decrease zi ⁇ ⁇ as ⁇ d ⁇ isl ⁇ ds ⁇ de ⁇ zhascheg ⁇ gas and, sled ⁇ va ⁇ eln ⁇ and ⁇ as ⁇ d ele ⁇ ene ⁇ gii on eg ⁇ ⁇ yuluchenie and ⁇ a ⁇ zhe umenshi ⁇ ⁇ as ⁇ d uglev ⁇ d ⁇ d ⁇ v, ⁇ eagi ⁇ uyuschi ⁇ ⁇ isl ⁇ ds ⁇ de ⁇ zhaschim with gas-5 z ⁇ m on s ⁇ adii v ⁇ ichn ⁇ y ⁇ a ⁇ - ⁇ isl ⁇ dn ⁇ y ⁇ nve ⁇ sii.
• the total reduction in energy consumption in comparison with the obsolete method is 0.6 ⁇ _ ⁇ _ ⁇ .
• ⁇ s ⁇ ve ⁇ s ⁇ vii the claimed iz ⁇ b ⁇ e ⁇ eniem
• tseles ⁇ b ⁇ azn ⁇ is ⁇ lz ⁇ va ⁇ in ⁇ aches ⁇ ve ⁇ e ⁇ l ⁇ n ⁇ si ⁇ elya v ⁇ dyan ⁇ y ⁇ a ⁇ and / or U di ⁇ sid ugle ⁇ da
• the inventive ⁇ is intended for use in both commercial and commercial carcasses, such as - 6 - for example, methane, ethane, ⁇ an and ⁇ ⁇ me ⁇ i; vy ⁇ shie uglev ⁇ d ⁇ - ⁇ dy on ⁇ ⁇ dyaschie ⁇ ya ⁇ i n ⁇ malny ⁇ u ⁇ l ⁇ viya ⁇ in gaz ⁇ b ⁇ azn ⁇ m or zhid ⁇ m ⁇ yanii.
• the 10th paired gas mixture has a temperature of -39 ° C.
• ⁇ ⁇ ve ⁇ e ⁇ vii ⁇ claimed iz ⁇ b ⁇ e ⁇ eniem, ⁇ luchen- hydrochloric ⁇ a ⁇ -gaz ⁇ vuyu ⁇ me ⁇ nag ⁇ evayu ⁇ d ⁇ ⁇ em ⁇ e ⁇ a ⁇ u ⁇ y 480-570 ° C and ⁇ ed ⁇ ch ⁇ i ⁇ eln ⁇ d ⁇ ⁇ em ⁇ e ⁇ a ⁇ u ⁇ y 540-570 ° C and ⁇ dve ⁇ gayu ⁇ ⁇ edva ⁇ i ⁇ eln ⁇ y ⁇ a ⁇ v ⁇ y ⁇ a ⁇ ali ⁇ iche ⁇ y ⁇ nve ⁇ ii ⁇ i i ⁇ -
• a partial gas with a temperature of 440-5 ⁇ 0 ° C is used to increase the pressure of the gas inlet
• the paired investment in this case is carried out in accordance with the endothermic reaction of the Republic of Korea and the use of the traditional, for example, is not nickel.
• the process gas has a temperature of 650-850 ° C, which is a direct coupled to a catalytic converter, which is mainly driven by gas emissions.
• the indirect gas supplied to the secondary circuit has a temperature not exceeding 900 ° C.
• the acid-supporting gas is heated by mixing the heater with a voltage of 0.5 mm before the specified temperature is mixed.
• the lower part (0.5) of the indicated volumetric load is determined by the condition of safe operation of the process, if it is inadvertent
• an oxygen-containing gas is inadequate and consumes gas, for example, water vapor, carbon dioxide, nitrogen, and argon. According to the claimed invention, it is preferable in terms of the quality of the boiler and the use of water vapor and / or carbon dioxide.
• the ZS is 20 ° 30 ° C longer than LYSY than after the last conversion.
• the pressure is relieved on the burner, and the temperature is better than ⁇ - ⁇ ⁇ ⁇ C, more than 500 ° C.
• the target process is under pressure on the stage of the furnace: the conversions, it is cooled down, the temperature is 620 ° C, which eliminates the need for energy - 0 -
• a special solution of the target preparation by introducing ⁇ at least a fraction of the acid-containing gas is 960 ° ⁇ , and after the introduction of 970 ° ⁇ .
• the collection of the residual methane in the target production makes up 0.5% of the volume.
• a heated mixture of 500 ° C is also sold here with a steam mixture with a ratio of 2 _ _ 0 5
• the original carbon mixture is at a temperature of 4 ° C and is heated at 540 ° 0 and is priced at a state of aciabatic
• the target product is directly affected by the condition of the original convention, Hz and cooler
• the intentional use of the invention does not include the use of ammonia, methane, EXTREME, and also the invention.

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• Chemical & Material Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Organic Chemistry (AREA)
• Inorganic Chemistry (AREA)
• Engineering & Computer Science (AREA)
• Combustion & Propulsion (AREA)
• General Health & Medical Sciences (AREA)
• Health & Medical Sciences (AREA)
• Hydrogen, Water And Hydrids (AREA)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Catalysts (AREA)
• Physical Or Chemical Processes And Apparatus (AREA)
• Cosmetics (AREA)

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Publications (1)

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Citations (5)

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• 1989
  • 1989-12-08 DE DE19893991744 patent/DE3991744T/de not_active Withdrawn
  • 1989-12-08 WO PCT/SU1989/000305 patent/WO1991004222A1/ru active Application Filing
• 1990
  • 1990-09-06 PT PT95234A patent/PT95234A/pt not_active Application Discontinuation
  • 1990-09-11 FR FR9011222A patent/FR2652073A1/fr active Pending
  • 1990-09-13 ES ES9002370A patent/ES2022042A6/es not_active Expired - Fee Related
  • 1990-09-13 IT IT04827190A patent/IT1242707B/it active IP Right Grant
  • 1990-09-19 CA CA002025740A patent/CA2025740A1/en not_active Abandoned
  • 1990-09-20 CN CN90107959.6A patent/CN1050363A/zh active Pending
• 1991
  • 1991-05-20 GB GB9110895A patent/GB2244494A/en not_active Withdrawn
  • 1991-05-21 DK DK095391A patent/DK95391A/da unknown

Patent Citations (5)

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