US3467842A - Open magnetohydrodynamic cycle and method of operation of magnetohydrodynamic cycle - Google Patents

Open magnetohydrodynamic cycle and method of operation of magnetohydrodynamic cycle Download PDF

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Publication number
US3467842A
US3467842A US650019A US3467842DA US3467842A US 3467842 A US3467842 A US 3467842A US 650019 A US650019 A US 650019A US 3467842D A US3467842D A US 3467842DA US 3467842 A US3467842 A US 3467842A
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gases
cycle
magnetohydrodynamic
mhd
gas
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US650019A
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English (en)
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Jean Marie Pierre Carrasse
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Societe Generale de Constructions Electriques et Mecaniques
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Societe Generale de Constructions Electriques et Mecaniques
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    • H—ELECTRICITY
    • H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
    • H02K—DYNAMO-ELECTRIC MACHINES
    • H02K44/00—Machines in which the dynamo-electric interaction between a plasma or flow of conductive liquid or of fluid-borne conductive or magnetic particles and a coil system or magnetic field converts energy of mass flow into electrical energy or vice versa
    • H02K44/08—Magnetohydrodynamic [MHD] generators
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01J—ELECTRIC DISCHARGE TUBES OR DISCHARGE LAMPS
    • H01J45/00—Discharge tubes functioning as thermionic generators
    • H—ELECTRICITY
    • H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
    • H02N—ELECTRIC MACHINES NOT OTHERWISE PROVIDED FOR
    • H02N3/00—Generators in which thermal or kinetic energy is converted into electrical energy by ionisation of a fluid and removal of the charge therefrom

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  • the present invention relates to open magnetohydrodynamic cycles, and more particularly to a method of operating such an open magnetohydrodynamic cycle in ⁇ VhlCh a fraction, preferably a major fraction, of the gases from the magnetohydrodynamic nozzle are recovered.
  • the hyperoxygenation is supplied not to increase the temperature level but rather to increase the energy which can be obtained from the MHD nozzle; further, it reduces or even entirely avoids dilution of gases from the nozzle by nitrogen from the air, and permits ready recovery of the thermo energy of the recycled gas without decrease of energy yield.
  • the hyperoxygenation if sufiicient, further permits the introduction into the chemical converter (in which the fuel and the gas obtained from the MHD nozzle are mixed) of a quantity of gases including oxidizing elements (CO H O) which are necessary to obtain on the one hand complete conversion of the combustible substance and of the other desirable operating temperatures, that is, temperatures in the neighborhood of 1,350 'K., or less.
  • the presence of nitrogen would otherwise result in an increase in temperature due to an excess of heat content if the necessary oxidizing gases were introduced into the chemical converter; or, an insufficient amount of oxidizing gases if desired temperatures only are to be obtained.
  • the mass of the recycled gas is decreased by the amount of energy contained therein, which energy is converted into chemical form.
  • the temperature levels of the recycled gases, after mixture with a combustible substance, enable the elimination of a substantial portion of the original gases from' the MHD tube, in accordance with known methods.
  • the treatment of the combustible substance in gaseous phase can readily be done for example by washing and furthermore permits the eventual elimination from the plasma of deleterious substances, such as sulphur compounds, so that the gases emitted from the MHD generator subsequently are devoid of such substances; the technical problems of the construction of combustion chambers and the MHD nozzles and the electrodes is thus simplified.
  • That portion of the gas which comes from the MHD nozzle which is not eventually recycled can be utilized as a heat source to generate steam, or it may be substantially cooled otherwise. It does not pose a problem of high temperatures and the consequent difficulties with construction materials.
  • FIGURE 1 illustrates, in schematic form, an MHD cycle in accordance with the invention
  • FIGURES 2 and 3 represent dilferent embodiments of cycles in accordance with the invention
  • FIGURE 4 in partly perspective, partly sectional view, illustrates a chemical converter useful in the cycle in accordance with the present invention.
  • FIGURE 1 Referring now to the drawings and more particularly to FIGURE 1:
  • An MHD nozzle 1 is supplied from a combustion chamber 2.
  • the gases coming from the MHD chamber 1, at a temperature of about 2,400 K. are divided into two paths, 3 and 4.
  • the gases along path 3 are led to a chemical converter 5, to be described in detail below, where they are mixed with a combustible substance supplied at 6.
  • the heat energy of the gas from the MHD nozzle 2, in the guide tube 3, is utilized to obtain endothermic reactions between the combustible substance admitted at 6 and the gases themselves, serving as oxidizing agents.
  • the caloric energy of the gas from tube 3, obtained from the MHD nozzle 1, at a temperature of about 2,400 K. is converted partly into chemical form, partly into heat energy and partly into losses to the walls.
  • the endothermic reaction of conversion causes absorption of energy of approximately 35 percent of the total energy content of the combustible substance introduced into the chemical converter. This energy may thus be recycled without necessity of heat exchanges, because it is obtained directly by mixing in the converter.
  • the speed of the gas from the MHD nozzle can be utilized to improve and speed up the mixture of oxidizing gases and combustible substance, particularly by obtaining a rapid rotation of the gaseous masses.
  • the temperature Within the chemical converter 5 is approximately between 1,200 K. to 1,350 K. Seed, primarily in the form of carbonates, or potassium sulfate, respectively, is thus in liquid form and may be recovered to a great part from the bottom of the chemical converter, as seen at 7, in accordance with processes Well known and utilized, for example, in the cellulose industry. Separation of the gaseous current into its liquid components is further improved by the rotation to which the gaseous masses in the apparatus 5 are subjected.
  • the gas leaving the converter 5 at 8, which is principally composed of carbon monoxide and hydrogen, with an excess of carbon dioxide and water vapor, are led to a heat recovery and heat exchanger apparatus 9.
  • the temperature is decreased to the region of about 500 K.
  • the gases are led to a scrubber or washing tower 11.
  • External regeneration of the cleaning substance permits extraction of the remainder of the seed at 12, in solution; and at 13 carbon dioxide and water vapor absorbed during the washing step.
  • the mixture of carbon monoxide, and hydrogen is taken out of the washing tower 11 at 14, at a temperature of about 300 K., for further utilization as combustible substance in the combustion chamber 2.
  • the portion of the gas following the path 4 is led through a heat recovery and heat exchanger apparatus 15, through a passage 16, and exhausted at 17 in a smokestack.
  • the temperature to which the substance admitted at 19 is raised can be about 900 K.
  • Recuperators 15 and/or 9 are utilized to preheat the substances from the washing tower 11 at its exit 14 to a temperature of from 1,200 K. to about 1,300 K., in a heat exchanger tube 21.
  • the gases are further, preferably, compressed in a single or multi-stage compressor 22.
  • the main drive of the compressor is not shown, and may be obtained directly from gas turbines or from other prime mover.
  • the combustible substance is introduced into the combustion chamber 2 to 23.
  • Heat exchanger tubes 24, 25 further utilized in heat exchangers 15 and 9 respectively, are elements of a water boiler to supply a conventional turbine 26, driving a con ventional alternator 27.
  • the conventional steam-turbinegenerator arrangement is not shown in detail since it is well known, and the steam for the drive of the turbine is a by-product when practicing the present invention.
  • FIGURE 2 shows a modification of the cycle in accordance with FIGURE 1, in which all of the gas coming from the MHD nozzle 1 is taken to the chemical converter 5.
  • the temperature is preferably preliminarily decreased to a range of about 2,000 K. in the heat exchanger 28, which further includes boiler tubes 29 for a conventional .4 turbine 26 with a generator 27. A portion of the gas may be taken off by a chimney 30, after supplementary cooling.
  • Heat exchangers 9 and 15 of FIGURE 1 can then be replaced by a single heat exchanger 31, utilized to preheat at the same time oxygen admitted at 19 as well as combustion substance obtained from the chemical converter 5.
  • FIGURE 3 illustrates a further embodiment of the invention, in which cooling of the gas obtained from the MHD nozzle 1 is done in several stages.
  • the gas following path 4 is led, in succession, to a boiler 32, through a passage 33, through a heat exchanger 34 having a passage 35 and a further boiler 36 having a passage 37 before being exhausted through a chimney or Smokestack at 17.
  • the gas following path 3, which would be approximately percent of the total amount of gases obtained from the MHD nozzle 1 is mixed in chemical converter 5 with combustible substance at 6, leaving at a temperature of about 1,3S0 K. to be led in succession to a boiler 38, through a passage 39, and to heat exchangers 40, 41.
  • Heat exchanger 40 is utilized to preheat slightly hyperoxygenated air applied at 19.
  • the combustion gas obtained from the washing tower 11 at outlet 14, after being compressed, is slowly reheated to about 900 K. in passage 43 of heat exchanger 41; and then led through tube 44 of heat exchanger 34 for a rapid increase to a temperature of about 1,373 K.
  • the conventional turbine-generator set 26, 27 is supplied with steam from lines 45, 46 and 47 obtained from boiler tubes in boilers 38, 36 and 32, respectively.
  • FIGURE 4 is an example of a chemical converter havinga vertical axis.
  • the oxidizing gases from the MHD nozzle 1 are applied by a channel 48. They enter at a high speed, for example, in the order of about 50 meters per second.
  • the direction of tube 48 is not radial, but rather tangential, so that the gases within the converter 5 will have a rapid rotational movement.
  • Combustible supporting substance for example, as a liquid
  • a liquid is applied through tube 49 and distributed by injection nozzles 50, located around the circumference of the converter, so as to be atomized or pulverized in recirculating zone, for example, the vortex such that droplets of liquid of combustible substance are rapidly heated, evaporated, and at least partially decomposed by contact with the gas at a somewhat moderate temperature, and in a zone of the converter where the conversion reactions are not too rapid. Only towards the end of that recirculating zone will be combustible substance subjected to attack by oxidizing gases.
  • the amount of gas entering at tube 48 and the amount of substance supplied through inlet 49 readily permits determination of the reaction temperatures, for example, to set it between 1,000 and l,100 C., of the reactions within reaction chamber 51.
  • the reaction of oxidation of carbon, and decomposition of molecules of the combustible substance are endothermic.
  • the temperature of the oxidizing gases decreases rapidly and the converter, over practically its entire volume, will be at a temperature similar to the exit temperature of the converted gases.
  • the converted gases leave by a central orifice 52 at the lower end of the converter.
  • the rapid rotational movement of the gas in the converter improves the separation of the compositions which constitute the input gases applied through tube 48, which may be liquid. Melting temperatures of potassium carbonate and potassium sulfate are actually below the temperatures of the gases in the converter. Original material introduced through tube 48 and not converted can also be removed through the base of the converter.
  • the upper region of the converter is preferably cooled by a water jacket 53, having an outer metallic cover 54;
  • the interior can be lined by a refractory layer 55, for example, alumina, having a thickness of about 50 mm., for example.
  • a refractory layer 55 for example, alumina, having a thickness of about 50 mm., for example.
  • the lower part of the converter need not be specially cooled.
  • the envelope may simply be insulated .by an internal refractory layer 56 of alumina, and insulated with brick work 57; an external metallic cover 58 is provided.
  • the upper and lower portions are connectcd by mean-s of flanges 59.
  • Cycle 1 Direct cycle, utilizing as combustible substance slightly hyperoxygenated air (O +3N reheated to 2,000 K. with heat obtained from the gases from the MHD nozzle;
  • Cycle 2 Chemical conversion cycle in accordance with the present invention, utilizing slightly hyperoxygenated gas (O +3N and reheat of the conversion gas and the combustion substance to about 1,370 K.;
  • Cycle 3 -Chemical conversion cycle in accordance with the invention, utilizing 95 percent pure oxygen, reheated to 900 K., and further reheat of the conversion gas to about l,373 K.
  • the temperature of the gases from the MHD nozzle are substantially constant at about 2,400 K.
  • the recoverable energy from the MHD nozzle is the portion directly transformed into electricity and the energy which is lost to wall losses. This last energy is usually utilized to heat water for a conventional steam turbine-generator assembly. It is not separately considered herein because, as a first approximation, it may be considered to be the same for all three cases.
  • Method as claimed in claim 1 including the step of mixing said mixture of a combustible substance and said major fraction of gas recovered from said magnetohydrodynamic nozzle in a chemical converter.
  • Method as claimed in claim 2 including the step of preheating said hyperoxygenated combustion supporting substance by gases obtained from said chemical converter.
  • Method as claimed in claim 2 including the step of supplying a steam boiler with gases obtained from said chemical converter to supply heat thereto.
  • Method as claimed in claim 2 including the step of water cleaning the mixture of a combustible substance and said major fraction of gas recovered from said magnetohydrodynamic nozzle; and the further step of further preheating said cleaned mixture.
  • Method as claimed in claim 2 including the step of passing said major fraction of gas recovered from the magnetohydrodynamic nozzle to a heat exchanger; and then passing said gas into said chemical converter.
  • Method as claimed in claim 6 including the step of passing water through said heat exchanger to generate steam.
  • Method as claimed in claim 1 including the step of subjecting said mixture of a combustible substance and said major fraction of gas recovered from said MHD nozzle to an endothermic reaction to convert heat energy into chemical energy whereby the temperature of said mixture and gases will decrease.
  • Method as claimed in claim 2 including the step of introducing said major fraction of gases recovered from said MHD nozzle into a cylindrical reaction chamber in a tangential direction to obtain rapid circular movement of said gases, having a vortex.
  • Method as claimed in claim 2 including the step of preheating said hyperoxygenated combustion substance by gases obtained from said magnetohydrodynamic nozzle.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Engineering & Computer Science (AREA)
  • Power Engineering (AREA)
  • Treating Waste Gases (AREA)
US650019A 1966-06-30 1967-06-29 Open magnetohydrodynamic cycle and method of operation of magnetohydrodynamic cycle Expired - Lifetime US3467842A (en)

Applications Claiming Priority (1)

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FR2693A FR1492980A (fr) 1966-06-30 1966-06-30 Perfectionnement aux cycles magnétohydrodynamiques ouverts

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BE (1) BE700335A (fr)
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NL (1) NL6709145A (fr)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3720850A (en) * 1970-04-30 1973-03-13 Westinghouse Electric Corp Magnetohydrodynamic power system with semi-closed cycle
US4163910A (en) * 1977-01-31 1979-08-07 Combustion Engineering, Inc. Vapor generator and MHD power plant
US4200815A (en) * 1978-09-19 1980-04-29 The United States Of America As Represented By The United States Department Of Energy MHD Generating system
US4287443A (en) * 1979-09-20 1981-09-01 Aladiev Ivan T Liquid-metal magnetohydrodynamic converter
US4336469A (en) * 1980-11-13 1982-06-22 Combustion Engineering, Inc. Method of operating a MHD power plant
US4346316A (en) * 1980-05-19 1982-08-24 Combustion Engineering, Inc. Apparatus for retrofitting an existing steam generator with an MHD topping unit
US4516043A (en) * 1980-10-16 1985-05-07 The Regents Of The University Of California Method and apparatus for generating electrical energy from a heated gas containing carbon particles
USH410H (en) 1981-11-02 1988-01-05 The United States Of America As Represented By The United States Department Of Energy Open-cycle magnetohydrodynamic power plant based upon direct-contact closed-loop high-temperature heat exchanger
AT521022B1 (de) * 2018-06-13 2019-10-15 Gs Gruber Schmidt Gmbh Erzeugung von Dimethylether aus Kohlendioxid und Wasserstoff mit Hilfe eines thermoionischen und magnetohydrodynamischen Generators
AT521191A1 (de) * 2018-04-25 2019-11-15 Gs Gruber Schmidt Dimethylether und Dibuthylether als Brennstoff für die Erzeugung von elektrischer und thermischer Energie mit Hillfe eines Plasmagenerators

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4345173A (en) * 1980-08-12 1982-08-17 The United States Of America As Represented By The United States Department Of Energy Method of generating electricity using an endothermic coal gasifier and MHD generator

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3214615A (en) * 1962-06-15 1965-10-26 Westinghouse Electric Corp Magnetohydrodynamic generator apparatus

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3214615A (en) * 1962-06-15 1965-10-26 Westinghouse Electric Corp Magnetohydrodynamic generator apparatus

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3720850A (en) * 1970-04-30 1973-03-13 Westinghouse Electric Corp Magnetohydrodynamic power system with semi-closed cycle
US4163910A (en) * 1977-01-31 1979-08-07 Combustion Engineering, Inc. Vapor generator and MHD power plant
US4200815A (en) * 1978-09-19 1980-04-29 The United States Of America As Represented By The United States Department Of Energy MHD Generating system
US4287443A (en) * 1979-09-20 1981-09-01 Aladiev Ivan T Liquid-metal magnetohydrodynamic converter
US4346316A (en) * 1980-05-19 1982-08-24 Combustion Engineering, Inc. Apparatus for retrofitting an existing steam generator with an MHD topping unit
US4516043A (en) * 1980-10-16 1985-05-07 The Regents Of The University Of California Method and apparatus for generating electrical energy from a heated gas containing carbon particles
US4336469A (en) * 1980-11-13 1982-06-22 Combustion Engineering, Inc. Method of operating a MHD power plant
USH410H (en) 1981-11-02 1988-01-05 The United States Of America As Represented By The United States Department Of Energy Open-cycle magnetohydrodynamic power plant based upon direct-contact closed-loop high-temperature heat exchanger
AT521191A1 (de) * 2018-04-25 2019-11-15 Gs Gruber Schmidt Dimethylether und Dibuthylether als Brennstoff für die Erzeugung von elektrischer und thermischer Energie mit Hillfe eines Plasmagenerators
AT521191B1 (de) * 2018-04-25 2020-02-15 Gs Gruber Schmidt Dimethylether und Dibuthylether als Brennstoff für die Erzeugung von elektrischer und thermischer Energie mit Hillfe eines Plasmagenerators
AT521022B1 (de) * 2018-06-13 2019-10-15 Gs Gruber Schmidt Gmbh Erzeugung von Dimethylether aus Kohlendioxid und Wasserstoff mit Hilfe eines thermoionischen und magnetohydrodynamischen Generators
AT521022A4 (de) * 2018-06-13 2019-10-15 Gs Gruber Schmidt Gmbh Erzeugung von Dimethylether aus Kohlendioxid und Wasserstoff mit Hilfe eines thermoionischen und magnetohydrodynamischen Generators

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FR1492980A (fr) 1967-08-25
BE700335A (fr) 1967-12-01
NL6709145A (fr) 1968-01-02

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