WO2018042448A1 - Purification de gaz hybride - Google Patents

Purification de gaz hybride Download PDF

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Publication number
WO2018042448A1
WO2018042448A1 PCT/IN2016/050386 IN2016050386W WO2018042448A1 WO 2018042448 A1 WO2018042448 A1 WO 2018042448A1 IN 2016050386 W IN2016050386 W IN 2016050386W WO 2018042448 A1 WO2018042448 A1 WO 2018042448A1
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WO
WIPO (PCT)
Prior art keywords
gas
impurities
unit
adsorption
enriched
Prior art date
Application number
PCT/IN2016/050386
Other languages
English (en)
Inventor
Sriganesh Gandham
Venkateswarlu Choudary Nettem
Sheshachala S N
Annaji Rajiv Kumar TOMPALA
Arun KUNIYIL
Original Assignee
Hindustan Petroleum Corporation Limited
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 Hindustan Petroleum Corporation Limited filed Critical Hindustan Petroleum Corporation Limited
Publication of WO2018042448A1 publication Critical patent/WO2018042448A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/0042—Degasification of liquids modifying the liquid flow
    • B01D19/0052—Degasification of liquids modifying the liquid flow in rotating vessels, vessels containing movable parts or in which centrifugal movement is caused
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • 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
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/16—Hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/404—Further details for adsorption processes and devices using four beds

Definitions

  • the present subject matter relates, in general, to gas purification and, in particular, to purification of a mixed gas feed to produce a product gas.
  • Gases such as hydrogen, oxygen and nitrogen are widely used in fertilizer industries, chemical processing plants, refineries, and steel industries.
  • pure hydrogen is used for desulfurization of petroleum products in refineries, in fertilizer industries, and for fats and oil hydrogenation.
  • the gases are generally produced at industrial scale by utilizing gas purification techniques.
  • One such gas purification technique is Pressure Swing Adsorption (PSA).
  • PSA Pressure Swing Adsorption
  • the PSA technique is used for separation and purification of hydrogen from a mixed gas feed containing one or more undesirable gases as impurities.
  • the PSA technique generally includes subjecting the mixed gas feed to a cyclic process of adsorption, desorption, and regeneration through sequential valve operations.
  • the mixed gas feed is introduced at high pressure to adsorption beds within a PSA unit.
  • the high pressure of the mixed gas feed facilitates loading of gas molecules of the impurities on adsorbent surface to separate the impurities from the mixed gas feed and provide hydrogen gas.
  • Desorption is performed by decreasing pressure of the adsorption beds and separating the impurities from the adsorption materials to obtain regenerated adsorption beds.
  • FIG. 1 illustrates a gas purification system, in accordance with an implementation of the present subject matter
  • FIG. 2 illustrates a flowchart of a method of purifying a mixed gas feed to produce hydrogen, in accordance with an implementation of the present subject matter.
  • product gases are obtained at industrial scale by utilizing gas purification units installed in industries and chemical processing plants to purify large volume of gases.
  • the gas purification units may have multiple vessels or adsorption beds having adsorption materials through which a mixed gas feed having other gases and particles as impurities is passed.
  • the adsorption materials adsorb the impurities from the mixed gas feed and provide a pure form of a product gas.
  • the multiple adsorption beds are used for purifying large volumes of mixed gas feed and therefore, with time, may become saturated and show reduced adsorption efficiency.
  • the adsorption materials are generally regenerated at a positive pressure.
  • the regeneration of the multiple adsorption beds may separate the impurities from the adsorption material such that the adsorption beds may regain adsorption efficiency and can be used for subsequent cycles of purification.
  • regenerating the adsorbent materials at the positive pressure may have lower efficiency of regeneration and reduced desorption efficiency of the regenerated adsorption materials. Therefore, such regenerated adsorption materials may have decreased efficiency of separating the impurities from the mixed gas feed and may have to be regenerated in short intervals, thereby reducing overall efficiency of the process.
  • the product gas supplied by such gas purification units is generally impure and includes traces of impurities in form of other gases and particles.
  • impurities in the product gas may alter properties of the product gas and may affect usage and application of the product gas. For instance, the impurities may reduce calorific value of the product gas, thereby reducing burning efficiency of the product gas in furnaces.
  • the gas purification units utilize large adsorption beds having bulk amount of adsorption materials to treat the mixed gas feed and supply the product gas. Such large adsorption beds and bulk amount of adsorption materials occupy large space and incur high capital and running expenses for the industries.
  • the present subject matter describes a gas purification system to purify a mixed gas feed and provide a product gas.
  • the gas purification system may include a Rotating Packed Bed (RPB) unit and a Pressure Swing Adsorption (PSA) unit coupled to the RPB unit.
  • the RPB unit may include a gas inlet, a solvent inlet, a solvent outlet, and a gas outlet.
  • the PSA unit may include an inlet, multiple adsorption beds, a product gas outlet and an impure gas outlet.
  • the inlet of the PSA unit may be coupled to the gas outlet of the RPB unit to receive a gas treated by the RPB unit.
  • the gas inlet of the RPB unit may receive a mixed gas feed.
  • the mixed gas feed may include multiple impurities, such as bulk impurities and finer impurities.
  • the bulk impurity may include heavy hydrocarbons
  • carbon dioxide gas Finer impurities may include light hydrocarbon impurities, inert gases like Nitrogen, Argon, , and carbon monoxide.
  • the solvent may be utilized to eliminate a first set of impurities from the mixed gas feed in the RPB unit to obtain an enriched gas.
  • the enriched gas may then be supplied through the gas outlet to the PSA unit.
  • the first set of impurities may include one or more impurities present in the mixed gas feed, such as heavy hydrocarbons, light hydrocarbons, and carbon dioxide gas.
  • the inlet of the PSA unit may receive the enriched gas through the gas outlet of the RPB unit.
  • the enriched gas may then be passed through multiple adsorption beds in the PSA unit.
  • the multiple adsorption beds may adsorb a second set of impurities from the enriched gas to obtain a product gas.
  • the product gas may then be supplied through the product gas outlet of the PSA unit.
  • the second set of impurities may include one or more impurities present in the enriched gas, such as one or more finer impurities and may be removed from the PSA unit through the impure gas outlet.
  • the gas purification system purifies a mixed gas feed to produce a product gas efficiently by removing bulk impurities in the RPB unit and the finer impurities in the PSA unit.
  • the gas purification system facilitates a compact PSA unit having reduced quantities of adsorbent materials for purification of the gas.
  • the gas purification system facilitates purification of the mixed gas feed and regeneration of the adsorption beds at lower or negative pressures. Therefore, the gas purification system is space and process efficient and saves capital and running expenses. Further, the gas purification system reduces amount of hydrocarbon gas processed in a given time in a given space thereby enhancing safety of a user operating the gas purification system.
  • FIG. 1 illustrates a gas purification system 100, in accordance with an implementation of the present subject matter.
  • the gas purification system 100 may include a Rotating Packed Bed (RPB) unit 102 and a Pressure Swing Adsorption (PSA) unit 104 coupled to the RPB unit 102.
  • RPB Rotating Packed Bed
  • PSA Pressure Swing Adsorption
  • multiple RPB units may be used instead of single RPB unit 102.
  • the multiple RPB units may be connected in either series or in parallel to each other.
  • the RPB unit 102 may include a gas inlet 106, a gas outlet 108, a rotor 110 housed in a rotor vessel (not shown in the figure) and a shaft 112.
  • the gas inlet 106 may be coupled to the rotor vessel to receive a mixed gas feed.
  • the gas inlet 106 may either be an inlet nozzle or a central hollow pipe to receive the mixed gas feed and the gas outlet 108 may be a central hollow pipe to supply an enriched gas.
  • the rotor 110 may be a movable part of the RPB unit and may include one or more sets of concentric rings of packing elements 114, stacked together in a manner as shown in the figure.
  • the rotor 110 may also include one or more sets of metallic rings (not shown in the figure).
  • the sets of metallic rings may be placed in between the sets 114 of the concentric rings at regular or variable intervals. Placement of the metallic rings in between the sets of the concentric rings 114 helps in achieving a desired stiffness or mechanical strength of the rotor 110 thereby reducing fatigue in the rotor 110.
  • the rotor 110 may be housed inside a rotor vessel
  • the rotor 110 may further include one or more metallic plates 116-1 and 116-2, individually referred to as the metallic plate 116 and collectively referred to as the metallic plates 116, hereinafter.
  • the metallic plates 116 may be circular in shape.
  • the metallic plates 116, the sets of the concentric rings 114 and the metallic rings may be stacked together using a plurality of fasteners, such as a tie -rod.
  • the metallic plate 116 may have a gap 118 for facilitating inflow of a solvent and outflow of a product gas.
  • the shaft 112 may be a low weight metallic shaft with one end of the shaft 112 connected to a motor (not shown in the figure) through a removable coupling.
  • the motor may facilitate rotation of the shaft 112 and thereby rotation of the rotor 110.
  • the shaft 112 may be connected to the metallic plate 116-1 through a flange (not shown in the figure).
  • mechanical seals may be connected to the shaft 112 and the rotor vessel for averting any leakage of the solvent and the mixed gas feed from inside the rotor vessel to outside environment.
  • a solvent inlet pipe 120 may be close to the gas outlet 108 for facilitating inflow of a solvent.
  • the solvent may outflow from the RPB unit 102 through a liquid outlet 122.
  • the solvent may include bulk impurities.
  • the RPB unit 102 may include a solvent distribution system to uniformly distribute and contact of gas and liquid inside the RPB unit (102).
  • the PSA unit 104 may include an inlet 124, and multiple adsorption beds 126-1, 126-2,
  • adsorption beds 126-1, 126-2, 126-3, and 126-4 have been described in the figure. However, it would be noted that there may be more than four adsorption beds in the PSA unit 104 based on amount of gas to purify.
  • the multiple adsorption beds 126-1,...., 126-n have been collectively referred to as adsorption beds 126 and individually as adsorption bed 126.
  • the PSA unit 104 may include a product gas outlet 128, and an impure gas outlet 130.
  • the inlet 124 may be a feed inlet line coupled to the gas outlet 108 of the RPB unit 102 to receive the enriched gas from the gas outlet 108 and supply the enriched gas to the adsorption beds 126.
  • the adsorption beds 126 may include adsorption materials having porous solids with high surface area to adsorb finer impurities remaining in the enriched gas.
  • one of the adsorption beds 126-1 may include different layers of adsorbent materials.
  • the adsorption bed 126-1 may include a mixture of aluminum and silicon based adsorbent material as first layer 132-1 placed at the bottom of the adsorption bed 126-1, followed by a second layer 134-1 of carbon based adsorbent material above the first layer 132-1, followed by a third layer 136-1 of zeolite based adsorption material above the second layer 134-1 and followed by a fourth layer 138-1 of cation exchanged zeolite based adsorbent material above the third layer 136-1.
  • the adsorbent bed 126-2 may include four layers 132-2, 134-2, 136-2, and 138-2
  • adsorbent bed 126-3 may include 132-3, 134-3, 136-3, and 138-3
  • adsorbent bed 126-4 may include the four layers of adsorbent materials 132-4, 134-4, 136-4, and 138-4.
  • the multiple layers of adsorption material may be selected based on type of impurities which are to be eliminated by adsorption beds 126 within each zone.
  • the different adsorbent materials may adsorb different types of impurities from the enriched gas.
  • the aluminum silicon mixture may adsorb moisture and heavy hydrocarbon impurities
  • the carbon based adsorbent material may adsorb light hydrocarbon impurities and carbon dioxide.
  • the zeolite based adsorbent material may adsorb dilute impurities as light hydrocarbons and carbon monoxide and the cation exchanged zeolite based adsorbent material may adsorb inorganic impurities such as carbon monoxide, Oxygen, Nitrogen, and Argon.
  • the adsorption beds 126 may be arranged within the PSA unit 104 such that one or more adsorption beds 126 may be removed from the PSA unit 104 and one or more adsorption beds may be added to the PSA unit 104, while the unit is operating, with a smooth switching over algorithm intended for ease of operation and enhanced intrinsic safety of the plant. Further, the dimensions, such as length, capacity and diameter may be determined based on amount of enriched gas feed to be purified by the adsorption beds 126.
  • a pure product gas may outflow through the product gas outlet 128, and impurities may be removed in form of an impure gas through the impure gas outlet 130.
  • a vacuum regeneration unit (not shown in the figure) may be coupled to the PSA unit 104.
  • the vacuum regeneration unit may be a vacuum pump to apply a negative pressure on the multiple adsorption beds 126 for regenerating the adsorption beds 126 at considerably lower pressures for enhancing the extent of regeneration.
  • the gas inlet 106 may receive a mixed gas feed.
  • the mixed gas feed may include the product gas, for instance hydrogen, along with other gases as impurities.
  • the hydrogen may be present in about 10 to 95 mole percentage (%) within the mixed gas feed.
  • composition of the mixed gas feed may be as given in table 1.
  • Table 1 illustrates the composition of the mixed gas feed provided to the RPB unit 102.
  • the left most column describes the product gas and the other gases present as impurities within the mixed gas feed.
  • the remaining columns describe proportion of the gases in weight within the mixed gas feed,
  • the right most column describes the weight in mole % of the gases.
  • hydrogen gas may be present in 68 mole %
  • Carbon monoxide (CO) may be present in 2 mole %
  • methane (CH 4 ) in 3 mole %.
  • the mixed gas feed may be supplied radially inward to the rotor -110 with a pressure.
  • the mixed gas feed may be supplied at a pressure of about 20 kg/cm .
  • the pressure of the mixed gas feed may be a value within the range 5 kg/cm 2 to 120 kg/cm 2.
  • the mixed gas feed may flow through the set of packed elements 114 and the solvent such that the first set of impurities, referred to as bulk amount of impurities, such as carbon dioxide may be eliminated from the mixed gas feed.
  • up to 90 % of weight of the impurities are eliminated from the mixed gas feed after flowing through the packed elements 114 and the solvent.
  • the gas so obtained after removal of the bulk impurities may have second set of impurities or remaining impurities, and may be referred to as the enriched gas. Thereafter, the enriched gas may be supplied through the gas outlet 108.
  • the solvent with the bulk impurities may be supplied out into the outside environment through the liquid outlet 122 in the RPB unit 102.
  • the enriched gas may have a higher proportion of the product gas, for instance hydrogen in the enriched gas.
  • the composition of the enriched gas may be as shown in table 2.
  • the enriched gas may include hydrogen in 93 mole %, CO in 2 mole %, C0 2 in 1 mole %, H 2 0 in 1 mole %, and CH 4 in 3 mole %. Therefore, in the enriched gas the proportion of hydrogen increases.
  • the enriched gas may be received by the inletl24 of the PSA unit 104.
  • the enriched gas may then be introduced to the multiple adsorption beds 126 one after another.
  • the adsorption beds 126 may include adsorbent materials to adsorb the remaining impurities from the enriched gas.
  • the impurities may be eliminated when molecules of the adsorbent material form bonds with molecules of the impurities. The bonding of the molecules on the adsorbent materials may trap the impurities on the surface of adsorbent materials thereby separating the impurities from the enriched gas.
  • the feeding of the enriched gas to the multiple adsorption beds 126 may eliminate the remaining impurities from the enriched gas to provide a product gas.
  • the product gas may be hydrogen gas.
  • the product gas is obtained at the product gas outlet 128 of the PSA unit 104 and the remaining impurities may be removed from the PSA unit 104 in form of impure gas through the impure gas outlet 130.
  • the hydrogen so purified as a product gas may be 99.999 pure.
  • the bulk impurities may be removed by the RPB unit 102, and the multiple adsorption beds 126 may have to eliminate the remaining impurities which may be very less in amount compared to original mixed gas feed.
  • the adsorption beds used for eliminating the remaining impurities may have reduced dimensions.
  • applying a vacuum regeneration unit may enhance the performance of the PSA unit by higher level of desorbing of the impurities from the multiple adsorption beds 126.
  • the adsorbent materials may be desorbed by releasing bonds of the molecules of the remaining impurities and the surface molecules of the adsorbent materials.
  • desorption may be performed at a negative pressure having any value in between the range of -0.1 kg/cm 2 g to -0.9 kg/cm 2 g. After desorption of the adsorbent materials the adsorbent materials are regenerated with enhanced capacity to adsorb the impurities in subsequent cycles of operation.
  • FIG. 2 illustrates method 200 in accordance with implementations of the present subject matter.
  • the order in which the method 200 is described is not intended to be construed as a limitation, and any number of the described method blocks may be combined in any order to implement the method 200 or an alternative method.
  • FIG. 2 illustrates a method for purifying a mixed gas feed to produce a product gas, according to an implementation of the present subject matter.
  • a mixed gas feed is received by a RPB unit.
  • the mixed gas feed is received by the gas inlet 106 of the RPB unit 102.
  • the first set of impurities is adsorbed to obtain an enriched gas.
  • a solvent within the RPB unit 102 adsorbs the first set of impurities from the mixed gas feed.
  • the enriched gas is supplied to a pressure swing adsorption unit through a gas outlet.
  • the PSA unit includes multiple adsorption beds to purify the enriched gas.
  • the enriched gas is fed to the multiple adsorption beds to eliminate the second set of impurities from the enriched gas to obtain a product gas.
  • the enriched gas is passed through multiple adsorption beds 126 of the PSA unit 104.
  • the product gas may be provided through the outlet of the PSA unit.
  • the gas purification system 100 is space and cost efficient.
  • the gas purification system 100 may have increased purification efficiency in producing the product gas thereby enhancing overall processing capacity. Further, the product gas so obtained through the gas purification system 100 may have high purity which can be used for any applications irrespective of the sensitiveness of consumer plant unit towards low levels of impurities in the product gas stream. [0041] Although implementations for the rotating packed bed assembly as per the present subject matter have been described in a language specific to structural features and/or applications, it is to be understood that the present subject matter is not necessarily limited to the specific features or applications described. Rather, the specific features and applications are disclosed as exemplary implementations.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Separation Of Gases By Adsorption (AREA)

Abstract

L'invention concerne un système de purification de gaz (100). Le système de purification de gaz (100) comprend une unité de lit fixe rotatif (RPB) et une unité d'adsorption modulée en pression (PSA). L'unité RPB (102) comprend une entrée de gaz (106) pour recevoir la charge de gaz mixte comprenant de multiples impuretés, un solvant pour éliminer un premier ensemble d'impuretés afin d'obtenir un gaz enrichi, et une sortie de gaz (108) pour fournir le gaz enrichi. L'unité PSA (104) comprend une entrée (124) couplée à la sortie de gaz (108) de l'unité RPB pour recevoir le gaz enrichi, de multiples lits d'adsorption (126) pour éliminer un second ensemble d'impuretés du gaz enrichi, et une sortie de gaz de produit (128), pour fournir un gaz de produit.
PCT/IN2016/050386 2016-08-31 2016-11-04 Purification de gaz hybride WO2018042448A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IN201621029821 2016-08-31
IN201621029821 2016-08-31

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2020012493A1 (fr) * 2018-07-09 2020-01-16 Hindustan Petroleum Corporation Limited Appareil d'élimination d'oxydes de soufre à partir de gaz d'échappement marins

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0307843A1 (fr) * 1987-09-16 1989-03-22 Air Products And Chemicals, Inc. Production d'hydrogène et d'oxyde de carbone
EP2335803A1 (fr) * 2009-12-08 2011-06-22 Yang, Hsien Ming Dispositif absorbant du dioxyde de carbone dans l'air
EP2486966A1 (fr) * 2011-02-09 2012-08-15 Alstom Technology Ltd Lit fixe rotatif
US20130004383A1 (en) * 2011-06-30 2013-01-03 Fluor Technologies Corporation Stand-alone flue gas recirculation fan

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0307843A1 (fr) * 1987-09-16 1989-03-22 Air Products And Chemicals, Inc. Production d'hydrogène et d'oxyde de carbone
EP2335803A1 (fr) * 2009-12-08 2011-06-22 Yang, Hsien Ming Dispositif absorbant du dioxyde de carbone dans l'air
EP2486966A1 (fr) * 2011-02-09 2012-08-15 Alstom Technology Ltd Lit fixe rotatif
US20130004383A1 (en) * 2011-06-30 2013-01-03 Fluor Technologies Corporation Stand-alone flue gas recirculation fan

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2020012493A1 (fr) * 2018-07-09 2020-01-16 Hindustan Petroleum Corporation Limited Appareil d'élimination d'oxydes de soufre à partir de gaz d'échappement marins

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