US3401111A - Hydrogen compression by centrifugal compressors - Google Patents

Hydrogen compression by centrifugal compressors Download PDF

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Publication number
US3401111A
US3401111A US562619A US56261966A US3401111A US 3401111 A US3401111 A US 3401111A US 562619 A US562619 A US 562619A US 56261966 A US56261966 A US 56261966A US 3401111 A US3401111 A US 3401111A
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United States
Prior art keywords
hydrogen
compressor
compression
butane
hydrocarbon
Prior art date
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Expired - Lifetime
Application number
US562619A
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English (en)
Inventor
Steven B Jackson
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.)
Fluor Corp
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Fluor Corp
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 Fluor Corp filed Critical Fluor Corp
Priority to US562619A priority Critical patent/US3401111A/en
Priority to GB58966/67A priority patent/GB1190450A/en
Priority to FR136013A priority patent/FR1565433A/fr
Priority to NL6800849A priority patent/NL6800849A/xx
Priority claimed from DE19681645748 external-priority patent/DE1645748A1/de
Application granted granted Critical
Publication of US3401111A publication Critical patent/US3401111A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/22—Separation of effluents
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D25/00—Pumping installations or systems

Definitions

  • ABSTRACT OF THE DISCLOSURE The invention is predicated upon utilization of multistage centrifugal compressors for elevating an essentially hydrogen stream to high pressures required for such known oil rening or conversion processes as hydrocracking or hydrotreating, and the employment of a method for reducing the number of required compressor stages by introduction to the hydrogen stream in advance of compression, butane or its molecular equivalent in the 30 to 80 molecular weight range, so that the hydrocarbon content of the stream will be in the 1% to 12% range and suiciently high to materially increase the effective pressure to which the hydrogen is elevated by the compression, the added hydrocarbon being derivable from an essentially C., fraction of the hydrogen-hydrocarbon reactor output.
  • This invention relates generally to the compression of gaseous hydrogen or predominately hydrogen streams by multi-stage centrifugal compressors of the (eg. Clark, Elliot or Ingersoll Rand) types commonly used for field, renery, or chemical plant gas compression.
  • multi-stage centrifugal compressors of the (eg. Clark, Elliot or Ingersoll Rand) types commonly used for field, renery, or chemical plant gas compression.
  • These are multi-stage in employing a succession of pressure increasing impellers, 'as Well as in accommodating impeller series in each of successive case sections of the compressors.
  • the successive case stages are customarily connected in tandem to a common drive shaft which is connected to a common driver and gear speed changer if required.
  • 1t is the operation of multiple case stage centrifugal compressors with which the invention is primarily concerned.
  • centrifugal compressors of the types named instead of reciprocating or piston type compressors.
  • centrifugal compressors capable of raising the hydrogen pressures to the high levels indicated.
  • the major conside-rations are the greater number of compressor stages required and corresponding high initial compressor costs, as well ⁇ as the expense of mechanical maintenances that may result from a greater number of stages, rand the loss of reliability in dependence on increased complexity of the rotating equipment.
  • One of my major objectives is to achieve hydrogen compression employing a lesser number of compressor stages, to a high level beyond the normal capability of such stages and thus to eliminate the necessity for costly extra stages.
  • 'Ihis objective is achieved by providing for the presence in the hydrogen undergoing compression of a relatively small mole or volume percentage, about 1% to 12% of hydrocarbon in the 30 to 80 molecular weight range, preferably butane or mixed hydrocarbons of about the molecular weight equivalent of butane.
  • the hydrogen Will undergo compression to consequentially higher pressure by a given compressor, and therefore it becomes possible to employ a reduced number of compressor stages and correspondice ingly reduced compressor cost, to achieve high level hydrogen compression.
  • high compression of substantially pure hydrogen might require tive or six case compressor stages
  • butane or equivalent addition to the hydrogen may permit its corresponding compression using only three compressor stages. It is considered that the equipment economics justify the butane occasioned increase in the volume of 'gas to be compressed.
  • the invention has further objects in reference to its particular applicability to hydrocarbon-hydrogen reaction or hydrogen treating processes, well known as hydrocracking or hydrotreating, wherein hydrogen is contacted at high pressures for reactive conversion of selected oil stocks or fractions.
  • hydrocracking or hydrotreating wherein hydrogen is contacted at high pressures for reactive conversion of selected oil stocks or fractions.
  • Such processes adapt to the purposes of the present invention in requiring recovery and recirculation of hydrogen which normally is required to be present in the reactor in excess of actual reaction requirements, as Iwell as being productive of low boiling hydrocarbons useable as supplement for the hydrogen compression.
  • an oil feed appropriate Afor hydrocracking such a's virgin or catalytically cracked gas oil, or for hydrotreating, e.g. gas oil in the boiling range of diesel oil needing reduction in sulfur content or increase in cetane number to meet product specifications, is introduced to the system through line 10 and pumped through heating facility 11 and thence by way of line 12 to a hydrocracking or hydrotreating unit which may include one or more reactors 13 wherein the oil feed undergoes conversion at high pressure that may range between about 500 and 4,000 pounds per square inch, and at temperatures in the order of about 500 F.
  • the unit 13 may serve to contact the heated oil feed with catalyst appropriate to the type of conversion, as is generally known in the art of hydrogen conversion processes.
  • a predominately hydrogen gas stream e.g. about hydrogen
  • a centrifugal compressor generally indicated at 15, which as previously indicated, comprises a series of case stages 16 individually containing their respective impeller series.
  • the hydrogen feed is progressively increased in pressure to the level required for the oil feed conversion in unit 13, the compressor discharge being taken through line 17 to lbe combined with the line 10 oil feed going to heater 11.
  • the normally liquid and gaseous, or entirely gaseous mixture resulting from the conversion in unit 13 is discharged therefrom through line 18 and subjected to cooling as by passage through exchanger 19 and air cooler 20 beyond which the cooled and partially condensed mixture enters separator 21.
  • the discharge from compressor 15, may enter the system at any suitable location retentive of the recycle.
  • the discharge from compressor 15 may be routed instead through line 25 and introduced elsewhere into the system loop, as to the suction ⁇ side of compressor 23.
  • the most advantageous point for introduction of hydrogen makeup from compressor into the system loop is subject to calculation for a given case in hand.
  • the effluent from separator 21 containing the liquefied butane equivalent compression supplement as well as reaction products is shown to be taken through line 26 for fractionation by suitable or conventional equipment diagrammatically indicated at 27 and which is productive of a fraction having average molecular weight in the to 80 range, or desirably a fraction which is largely butane.
  • Residual or product hydrocarbon leaves the fractionation stage through line 28.
  • Separated butane or equivalent is taken through line 29 as supplement to manufactured or by-product hydrogen being -fed to the system through line 30.
  • the streams may be introduced to a contactor 31 from which a gaseous butane and hydrogen mixture is taken as the line 14 feed to the compressor 15.
  • Unvaporized material from separator 31 may be returned to the fractionation section through line 32.
  • the proportion of butane or equivalent thus added to the hydrogen feed is so controlled as not to consequentially exceed the quantity of hydrocarbon required for the desired elevation of the hydrogen compression by compressor 15.
  • the butane supplement will be so controlled as to constitute -between about 1 and 12%, and most often in the range of about 5 to 10% by volume of the feed to the compressor, the quantity added being dependent primarily on the purity and average molecular weight of the manufactured and/or -byproduct hydrogen feed introduced in line 30.
  • the byproduct hydrogen feed may be most commonly a byproduct of catalytic reforming operations. This byproduct hydrogen normally contains hydrocarbon impurities (methane through butane). These impurities are variable depending on operations and catalyst condition in the reformer. Another objective of the invention thus becomes apparent, i.e. to control the quantity of butane supplement so that the desired elevation of hydrogen compression is constant regardless of variation in hydrogen feed purity.
  • butane equivalent supplement hydrocarbon One of the major criteria for selecting the butane equivalent supplement hydrocarbon is that it should condense essentially into the liquid phase in separator 21.
  • the quality of recycle passing through line 24 and 24, thence back to unit 13 is judged primarily by its hydrogen content. If the supplemental material can be essentially liquefied in separator 21, this material will not build up in concentration in the vapor phase and therefore will influence the hydrogen content of the recycle only to a very limited extent.
  • the number of compressor stages 16 required may be such as to involve excessively high compressor cost in proportion to the number of required stages. For example, for hydrogen compression to around 1,600 pounds per square inch, six case stages normally could be required. By reason of butane or equivalent addition to the line 14 feed, the resulting increased density given the gaseous mixture permits corresponding or equivalent hydrogen compression, eg. to 1,60() pounds, by a lesser number of compressor stages, which in the example given may reduce to three and with corresponding reduction in the cost of the compressor installation.
  • the method of claim 1 including also the steps of contacting the compressed gas with relatively high boiling hydrocarbons for conversion by hydrogen reaction therewith to produce a mixture of lighter hydrocarbons, higher boiling liquid hydrocarbons and residual unreacted hydrogen, separating the unreacted hydrogen from said mixture by partial condensation and fractionating the resultant predominately hydrocarbon mixture to separate said lighter hydrocarbons, and returning the separated lighter hydrocarbons to said feed stream as said hydrocarbon added thereto.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US562619A 1966-07-05 1966-07-05 Hydrogen compression by centrifugal compressors Expired - Lifetime US3401111A (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
US562619A US3401111A (en) 1966-07-05 1966-07-05 Hydrogen compression by centrifugal compressors
GB58966/67A GB1190450A (en) 1966-07-05 1967-12-28 Hydrogen Compression by Centrifugal Compressors
FR136013A FR1565433A (enrdf_load_stackoverflow) 1966-07-05 1968-01-15
NL6800849A NL6800849A (enrdf_load_stackoverflow) 1966-07-05 1968-01-19

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
US562619A US3401111A (en) 1966-07-05 1966-07-05 Hydrogen compression by centrifugal compressors
GB58966/67A GB1190450A (en) 1966-07-05 1967-12-28 Hydrogen Compression by Centrifugal Compressors
FR136013 1968-01-15
DE19681645748 DE1645748A1 (de) 1968-01-19 1968-01-19 Wasserstoffverdichtung durch Kreiselkompressoren
NL6800849A NL6800849A (enrdf_load_stackoverflow) 1966-07-05 1968-01-19

Publications (1)

Publication Number Publication Date
US3401111A true US3401111A (en) 1968-09-10

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US562619A Expired - Lifetime US3401111A (en) 1966-07-05 1966-07-05 Hydrogen compression by centrifugal compressors

Country Status (4)

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US (1) US3401111A (enrdf_load_stackoverflow)
FR (1) FR1565433A (enrdf_load_stackoverflow)
GB (1) GB1190450A (enrdf_load_stackoverflow)
NL (1) NL6800849A (enrdf_load_stackoverflow)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3532467A (en) * 1967-09-01 1970-10-06 Chevron Res Hydrogen manufacture with integrated steam usage
US3656905A (en) * 1970-11-02 1972-04-18 Chevron Res Hydrogen manufacture
US3699218A (en) * 1970-06-12 1972-10-17 Chevron Res Hydrogen manufacture
US3870435A (en) * 1969-07-09 1975-03-11 Pilot Pen Co Ltd Visual recording method and means
US3965253A (en) * 1972-05-01 1976-06-22 Shell Oil Company Process for producing hydrogen
US4229602A (en) * 1978-12-04 1980-10-21 Phillips Petroleum Company Dehydrocyclization process
EP3789616A1 (de) * 2019-09-09 2021-03-10 Siemens Aktiengesellschaft Verfahren zur verdichtung von wasserstoff, anordnung
FR3108390A1 (fr) * 2020-03-23 2021-09-24 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Installation et procédé de réfrigération d’hydrogène
US11453950B1 (en) 2021-03-15 2022-09-27 Air Products And Chemicals, Inc. Method and apparatus for dosing hydrogen in a centrifugal compression system
CN115142081A (zh) * 2021-03-15 2022-10-04 气体产品与化学公司 一种用于在离心式压缩机中压缩氢气的工艺和装置
CN115142080A (zh) * 2021-03-15 2022-10-04 气体产品与化学公司 一种用于在离心式压缩机中压缩氢气的工艺和装置
IT202200015174A1 (it) * 2022-07-20 2024-01-20 Nuovo Pignone Tecnologie Srl Metodo e sistema per un'efficiente compressione di idrogeno

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3992167A (en) * 1975-04-02 1976-11-16 Union Carbide Corporation Low temperature refrigeration process for helium or hydrogen mixtures using mixed refrigerant

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3008895A (en) * 1959-08-25 1961-11-14 Union Oil Co Production of high-octane gasolines
US3141748A (en) * 1961-11-20 1964-07-21 Exxon Research Engineering Co Hydrogen purification process

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3008895A (en) * 1959-08-25 1961-11-14 Union Oil Co Production of high-octane gasolines
US3141748A (en) * 1961-11-20 1964-07-21 Exxon Research Engineering Co Hydrogen purification process

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3532467A (en) * 1967-09-01 1970-10-06 Chevron Res Hydrogen manufacture with integrated steam usage
US3870435A (en) * 1969-07-09 1975-03-11 Pilot Pen Co Ltd Visual recording method and means
US3699218A (en) * 1970-06-12 1972-10-17 Chevron Res Hydrogen manufacture
US3656905A (en) * 1970-11-02 1972-04-18 Chevron Res Hydrogen manufacture
US3965253A (en) * 1972-05-01 1976-06-22 Shell Oil Company Process for producing hydrogen
US4229602A (en) * 1978-12-04 1980-10-21 Phillips Petroleum Company Dehydrocyclization process
EP3789616A1 (de) * 2019-09-09 2021-03-10 Siemens Aktiengesellschaft Verfahren zur verdichtung von wasserstoff, anordnung
WO2021190892A1 (fr) * 2020-03-23 2021-09-30 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Installation et procédé de réfrigération d'hydrogène
FR3108390A1 (fr) * 2020-03-23 2021-09-24 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Installation et procédé de réfrigération d’hydrogène
US12320586B2 (en) 2020-03-23 2025-06-03 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Facility and method for hydrogen refrigeration
US11453950B1 (en) 2021-03-15 2022-09-27 Air Products And Chemicals, Inc. Method and apparatus for dosing hydrogen in a centrifugal compression system
CN115142081A (zh) * 2021-03-15 2022-10-04 气体产品与化学公司 一种用于在离心式压缩机中压缩氢气的工艺和装置
CN115142080A (zh) * 2021-03-15 2022-10-04 气体产品与化学公司 一种用于在离心式压缩机中压缩氢气的工艺和装置
EP4060089A3 (en) * 2021-03-15 2022-10-12 Air Products and Chemicals, Inc. Process and apparatus for compressing hydrogen gas in a centrifugal compressor
EP4060089B1 (en) 2021-03-15 2023-09-13 Air Products and Chemicals, Inc. Process and apparatus for compressing hydrogen gas in a centrifugal compressor
US11773873B2 (en) 2021-03-15 2023-10-03 Air Products And Chemicals, Inc. Process and apparatus for compressing hydrogen gas in a centrifugal compressor
US11926906B2 (en) 2021-03-15 2024-03-12 Air Products And Chemicals, Inc. Process and apparatus for compressing hydrogen gas in a centrifugal compressor
IT202200015174A1 (it) * 2022-07-20 2024-01-20 Nuovo Pignone Tecnologie Srl Metodo e sistema per un'efficiente compressione di idrogeno

Also Published As

Publication number Publication date
NL6800849A (enrdf_load_stackoverflow) 1969-07-22
FR1565433A (enrdf_load_stackoverflow) 1969-05-02
GB1190450A (en) 1970-05-06

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