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WO2019056119A1 - Reformeur rotatif - Google Patents

Reformeur rotatif Download PDF

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Publication number
WO2019056119A1
WO2019056119A1 PCT/CA2018/051190 CA2018051190W WO2019056119A1 WO 2019056119 A1 WO2019056119 A1 WO 2019056119A1 CA 2018051190 W CA2018051190 W CA 2018051190W WO 2019056119 A1 WO2019056119 A1 WO 2019056119A1
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WO
WIPO (PCT)
Prior art keywords
reformer
combustion
gas
stream
engine
Prior art date
Application number
PCT/CA2018/051190
Other languages
English (en)
Inventor
Behzad BAHTOOI
Debanjan CHAKRABARTI
Christopher Lundy
Bryan IMBER
Original Assignee
International Composting Corporation
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 International Composting Corporation filed Critical International Composting Corporation
Publication of WO2019056119A1 publication Critical patent/WO2019056119A1/fr

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02B—INTERNAL-COMBUSTION PISTON ENGINES; COMBUSTION ENGINES IN GENERAL
    • F02B53/00—Internal-combustion aspects of rotary-piston or oscillating-piston engines
    • F02B53/02—Methods of operating
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01C—ROTARY-PISTON OR OSCILLATING-PISTON MACHINES OR ENGINES
    • F01C1/00—Rotary-piston machines or engines
    • F01C1/22—Rotary-piston machines or engines of internal-axis type with equidirectional movement of co-operating members at the points of engagement, or with one of the co-operating members being stationary, the inner member having more teeth or tooth- equivalents than the outer member
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02B—INTERNAL-COMBUSTION PISTON ENGINES; COMBUSTION ENGINES IN GENERAL
    • F02B53/00—Internal-combustion aspects of rotary-piston or oscillating-piston engines
    • F02B53/04—Charge admission or combustion-gas discharge
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02B—INTERNAL-COMBUSTION PISTON ENGINES; COMBUSTION ENGINES IN GENERAL
    • F02B55/00—Internal-combustion aspects of rotary pistons; Outer members for co-operation with rotary pistons
    • F02B55/08—Outer members for co-operation with rotary pistons; Casings
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2201/00—Preparation of ozone by electrical discharge
    • C01B2201/10—Dischargers used for production of ozone
    • C01B2201/14—Concentric/tubular dischargers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04C—ROTARY-PISTON, OR OSCILLATING-PISTON, POSITIVE-DISPLACEMENT MACHINES FOR LIQUIDS; ROTARY-PISTON, OR OSCILLATING-PISTON, POSITIVE-DISPLACEMENT PUMPS
    • F04C2210/00—Fluid
    • F04C2210/10—Fluid working
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
    • Y02T10/00—Road transport of goods or passengers
    • Y02T10/10—Internal combustion engine [ICE] based vehicles
    • Y02T10/12—Improving ICE efficiencies

Definitions

  • the invention is in the field of chemical and mechanical engineering, particularly the use of an internal combustion engine to produce gases containing carbon monoxide and hydrogen from partial oxidation of hydrocarbon fuels.
  • Stranded gas has been used to refer to hydrocarbon gases that are wasted or unused.
  • Stranded gas in the form of landfill gas or flare gas offers a rich, albeit typically contaminated, pool of methane.
  • landfill gases and other biogases produced in anaerobic digestion generally contain methane along with significant quantities of C0 2 , N 2 and at least some impurities such as H 2 S and mercaptans.
  • these potential resources often do not warrant development of the infrastructure necessary to extract value. As a result, they are mostly combusted and vented to the atmosphere or left untapped - stranded.
  • Stranded gas can for example be converted to synthesis gas (CO + H 2 ) via a variety of processes such as steam methane reforming, dry methane reforming, partial oxidation, or autothermal (adiabatic oxidative) reforming.
  • synthesis gas CO + H 2
  • Conventional reactors typically utilize nickel based catalysts for the reforming or partial oxidation process, while some plasma reformers utilize a plasma arc instead of a catalyst bed.
  • N is the number of moles and M is the molar mass.
  • the molar mass of air is approximately 28.97 g/mol.
  • the molar mass of methane is 16.04 g/mol.
  • dry air can be approximated as consisting of 21 % oxygen and 79% nitrogen, or in molar terms 3.76 moles of nitrogen per mole of oxygen.
  • the balanced chemical reaction for stoichiometric combustion of methane in dry air is accordingly:
  • the stoichiometric amount of combustion air is accordingly 2 moles of oxygen plus 2 x 3.76 moles of nitrogen, for a total of 9.52 moles of air per mole of methane, which is an air fuel ratio of 17.19:
  • the actual amount of air used in a combustion processes may be expressed in terms of the air-fuel equivalence ratio (lambda): AF actual / AF stoichiometric .
  • the air-fuel equivalence ratio for an excess of air (a lean mixture), will be greater than 1 .
  • the air-fuel equivalence ratio for a lack of adequate air (a rich mixture), will be less than 1 .
  • the fuel-air equivalence ratio (phi) is the reciprocal of the air-fuel equivalence ratio: [0008]
  • Rxn 2 complete combustion
  • Rxn 3 partial oxidation of methane to produce carbon monoxide and hydrogen
  • Rxn 2 CH 4 + O.50 2 ⁇ CO + 2H 2 ... (Rxn 3)
  • Rxn 2 rapid exothermic complete combustion reactions
  • Rxn 4 steam methane reforming
  • Rxn 5 dry methane reforming
  • Synthesis gas can for example be used for the synthesis of oxygenated compounds such methanol, ethanol, formaldehyde, acetic acid or methyl acetate. Synthesis gas can also be utilized to produce liquid fuels and petrochemicals via the Fischer - Tropsch synthesis process. Synthesis gas can also be used as a precursor for processes that generate a relatively pure hydrogen gas stream using a water gas shift reactor and a membrane based separation system.
  • a rotary internal combustion methane reformer comprising a housing having an intake port and an exhaust port.
  • the housing defines a confined two-lobed epitrochoid space accessed by the ports, within which a three-sided rotor rotates eccentrically on a stationary gear so as to turn an output shaft through approximately 1080 degrees of rotation for every 360 degree rotation of the rotor.
  • the rotation of the rotor within the housing is driven by a four step Otto cycle methane oxidation process carried out in working chambers defined by the rotor and the housing, so that the working chambers successively expand and contract to effect intake, compression, combustion and exhaust phases of the cycle.
  • the combustion phase of the cycle typically involves spark initiated auto-thermal reformation of methane introduced through the intake port. This combustion may for example take place during an extended period of rotor motion, for example over approximately at least 100, 105, 1 10, 1 15 or 120 degrees of rotor rotation.
  • Combustion thereby produces a synthesis gas comprising carbon monoxide and hydrogen that is exhausted through the exhaust port.
  • the reformer may be adapted so that at least some minimum threshold value of methane entering the reformer at the intake port is converted to oxidation products in the synthesis gas that is exhausted through the exhaust port, such as 50, 55, 60, 65, 70, 75, 80, 85, 90 or 95%.
  • the reformer may be adapted so that the combustion phase of each cycle takes place during a defined, relatively prolonged, combustion time period, for example being at least 5, 6, 7, 8, 9 or 10 milliseconds.
  • the reformer may be adapted so that the combustion phase of each cycle takes place at a selected combustion temperature, for example of 850 to 1400°C. Similarly, the reformer may be adapted so that the combustion phase takes place at a selected combustion pressure, for example of from 20 to 40 bars.
  • the reformer may be adapted so that the back pressure at the exhaust port is above a threshold value, for example being at least 0.1 , 0.5, 1 , 5, 10, 20 or 30 barg.
  • the reformer may be adapted so that the fuel entering the intake port comprises air and methane.
  • the air- fuel ratio may for example be variable between selected values, for example of from 4.29 to 17.19.
  • the spark initiated auto-thermal reformation may for example be initiated by at least 2 spaced apart spark sources, and the multiple spark sources may provide sparks at different times.
  • Figure 1 schematically depicts the operation of the Wankel Rotary Engine.
  • Figure 2 is a schematic illustration of a process for producing liquid fuels as well as petrochemicals via Fischer - Tropsch synthesis using a rotary engine reformer.
  • Figure 3 is a schematic illustration of a process a for producing methanol using a rotary engine reformer.
  • Figure 4 is a schematic illustration of a process for producing hydrogen gas using a rotary engine reformer.
  • the rotary engine nominally has 1 .5 times more time to accomplish each stroke (the output shaft spins three times as fast as the rotor).
  • the Wankel compression and combustion strokes may be prolonged, by virtue of inlet and exhaust port geometry, and may for example occupy up to approximately 120 degrees of rotor (not shaft) rotation.
  • Rxn 4 steam methane reforming reactions
  • Rxn 5 dry methane reforming reactions
  • the rotor speed will be approximately 1 ,666 rpm, or 27 rotations/second, taking 36 milliseconds/revolution, and affording 12 milliseconds for the combustion phase of each cycle including a relatively isochoric period of 3 milliseconds.
  • the pistons move up and down once for every shaft rotation, and the duration of the combustion downstroke is accordingly only 6 milliseconds, with no significant isochoric period.
  • a Wankel engine still affords 7.5 milliseconds for each combustion phase, which is 25% longer than in the piston engine operating at 5000 rpm.
  • Each face of the rotor is provided with a "rotor depression" which provides a path for the partially burned air-fuel mixture to navigate the otherwise narrow clearance between the rotor housing and rotor. Adjusting the shape of the rotor depression accordingly provides a means for confining the partial
  • the shape of this chamber can accordingly be tuned to optimize partial oxidation.
  • the rotor depression also provides for a combustion chamber with a relatively high surface to volume ratio, increasing the effectiveness of any autothermal reforming catalyst deposited on the rotor depression.
  • rotary reformers make use of the typical double consecutive spark ignition system of the Wankel, providing tow (or more) sparks in each combustion cycle.
  • the timing and position of these sparks may accordingly be adapted to increases the methane conversion rate - for example compared to a typical piston engine.
  • a rotary reformer may be operated with a relatively higher back pressure on the exhaust.
  • Wankel engines are relatively insensitive to exhaust back pressure, a feature that is related to minimization of dead space and the relatively complete exhaust cycle of the Wankel.
  • the relatively high pressure of the exhausted reformed gas may for example be used in downstream processes, in some cases obviating the need for a compressor.
  • the ability to apply backpressure in a piston engine is limited, in part because of problems that arise because of the sealing mechanism around valve seats.
  • the combustion chamber of a rotary engine has a higher surface area to chamber volume ratio than a reciprocating engine, and its shape results in a longer flame travel distance.
  • the trailing section of the combustion chamber where final or secondary combustion occurs is a narrow, wedge-shaped section which has the capacity to quench combustion.
  • the higher combustion chamber surface to volume ratio means that there is a greater, relatively cool, wall area which also has the capacity to quench combustion (reducing peak temperatures and pressures in the combustion chamber). This typically results in a high quenching effect at the trailing portion of the charge.
  • the charge is swept forward by the moving chamber at relatively high velocity, facilitating turbulent mixing of gases. In effect, This reduces the octane requirement of the engine.
  • a rotary engine will generally accommodate fuels having a modest octane number requirement, in comparison to the compression ratio, and a corresponding ability to burn a variety of fuel mixtures, such as fuels with lower calorific value, for example landfill gases.
  • a Wankel Rotary engine ( Figure 1 ) can consist of two or more separate housings, each containing a symmetric three faced rotor. The rotary motion of multiple rotors in the engine is offset and coupled through the eccentric shaft. An oxidant-fuel mixture is passed into the combustion chamber through a fuel mixer and trapped between one face of the rotor and the walls of the combustion chamber. The motion of the rotor in the combustion chamber compresses the gas mixture between the wall and the rotor face.
  • One or, more typically two, spark plugs are located at the point of highest compression of the fuel air mixture, operating to ignite the mixture.
  • the ignition of the oxidant-fuel mixture initiates the combustion or partial combustion reactions (Rxn 2 and 3 respectively) which being exothermic release large amounts of heat.
  • the equilibrium of the reforming reactions influences the final distribution of the synthesis gas products. Driven by these reactions, the rotor moves forward generating mechanical power through the connected eccentric shaft arrangement, while simultaneously allowing the product gas mixture to expand and cool.
  • FIG. 1 the phases of an Otto cycle in a rotary engine are illustrated.
  • face C of the rotor is about to initiate the intake phase
  • face A of the rotor has completed the intake phase and is about to initiate the compression phase
  • Face B of the rotor in Part 1 of Figure 1 has completed the post combustion expansion phase and is about to initiate the exhaust phase.
  • face C is in the middle of the intake phase
  • face A is in the middle of the compression phase
  • face B has initiated the exhaust phase with the combusted gas exiting through the exhaust port.
  • face A has completed the compression phase and the spark has ignited the fuel-oxidant mixture.
  • Face C and B are in the middle of the intake and exhaust phases respectively.
  • face A has completed the combustion phase and the expansion phase has been initiated.
  • one spark plug ignites the oxidant - fuel mixture in the combustion chamber prior to the gas mixture attaining maximum
  • the partial oxidation or combustion reactions are active while compression is occurring.
  • the second spark plug is activated, so as to facilitate completion of the combustion or partial oxidation reactions.
  • the flame from the combustion provides a medium for the progression of secondary reactions in the system such as the steam methane reforming or dry methane reforming (Rxn 4 and 5 respectively).
  • the oxidant-fuel mixture is compressed to the maximum value, at which point both the spark plugs are activated simultaneously to ignite the air-fuel mixture.
  • both the spark plugs may be activated before or after this point simultaneously, to ignite the air-fuel mixture.
  • the fuel - oxidant mixture is fed to the
  • combustion chamber at ambient conditions, for example at approximately 25 °C. Following the combustion or partial combustion reactions, the exhaust gas is decompressed and exits the combustion chamber at or above ambient pressure.
  • the fuel-oxidant mixture is fed to the combustion chamber at pressures above ambient, for example at 0-3 barg and temperatures ranging from 0 °C to over 100°C.
  • the exhaust gas is decompressed and exits the combustion chamber at or above ambient pressure.
  • the exhaust gas may be utilized to operate a turbocharger.
  • the exhaust gas is decompressed to a pressure higher than inlet pressure.
  • the products of the combustion exit the engine at elevated pressures, for example up to 30 barg. Expanding the products of combustion to pressures higher than the inlet pressure decreases the power produced by the engine and increases the temperature of the syngas.
  • one combustion chamber may operate under complete combustion conditions, for example using a variety of fuels, such as methane or gasoline, while the other combustion chamber operates in a partial oxidation mode.
  • the exhaust from the chamber operating under partial oxidation conditions can be regulated to provide an exhaust flow at relatively high outlet pressures.
  • the thermal energy available in the exhausted syngas may be recovered, for example using Stirling engine or Organic Rankine Cycle and generate mechanical or electrical energy.
  • the heat recovered from the syngas can be utilized for making steam or generating cooling load using absorption chillers.
  • the fuel for the process can generally be any gas containing CH4 as a major constituent, for example natural gas, flare gas and biogas.
  • the oxidant for the process can for example be air, or oxygen enriched air, or pure oxygen.
  • Oxygen enriched air can for example contain a nitrogen to oxygen ratio ranging between 3.76 and 0.
  • Mixtures of fuel to oxidant having CH :0 2 ratios ranging from 0.5 to 2 can for example be fed to the combustion chamber through the intake manifold of the engine.
  • a diluent in the form of water, tail gas, nitrogen, argon, C02 or a combination of these gases can for example be added to the air- fuel mixture for the purpose of temperature control, and/or as well as reaction control.
  • tail gas may include the un- condensable component of the product mixture obtained from the Fischer-Tropsch synthesis reactor system downstream of the engine reformer.
  • the oxidant-fuel mixture is premixed and sent into the combustion chamber through the intake manifold/port of the engine.
  • the oxidant-fuel mixture may be optimized such that the system has sufficient oxygen to sustain the combustion flame for the entire mixture to undergo reaction, but at the same time, not enough to allow complete combustion of CH to form C0 2 and H 2 0.
  • the exhaust gas will in general contain a mixture of CO, C0 2 , H 2 and H 2 0, with small amounts of CH and other gaseous hydrocarbons.
  • Some embodiments may have a water gas shift reactor downstream of the exhaust gas stream to adjust the H 2 :CO ratio in the exhaust gas from the system.
  • additional steam or water may for example be injected into the water gas shift reactor along with the exhaust gas from the reformer to obtain a synthesis gas product with H 2 :CO ratio value between 2 and 2.1 in accordance with requirements of certain downstream processes, such as the Fischer-Tropsch synthesis process or a methanol synthesis process.
  • the fuel gas may for example be cleaned of H 2 S and excess C0 2 using pressure swing adsorption, Selexol® or Rectisol® solvent base absorption or other technologies for acid gas removal.
  • no gas cleanup system will be utilized either upstream or downstream of the engine reformer.
  • the fuel gas may for example be mixed with an oxidant and fed to the engine reformer directly.
  • the exhaust gas containing CO, C0 2 , N 2 , H 2 and H 2 0, with small amounts of CH and other gaseous hydrocarbons may be cooled to remove the H 2 0.
  • the tail gas of the downstream process may be mixed with the original feed fuel gas and recycled to the engine reformer.
  • multiple engine reformers can be made to operate in parallel to process a larger quantity of fuel.
  • the model described as follows has been used to exemplify the operation of the rotary reformer.
  • the notations for the model are as follows: engine volume capacity (Capacity engine ); the engine speed in revolutions per minute (Speed rpm ) and revolutions per second (Speed rps ); the volumetric turnover (V engine ); torque of engine ( ⁇ ); power of engine (P engine )] compression ratio of turbo (CR Turb0 ); compression ratio of engine(CR engine ); enthalpy of component i at temperature T and pressure P (Hi (T, P)); entropy of component i at temperature T and pressure P (S ( (r, P)); specific heat of component i at temperature T for constant pressure (C P .
  • Stage 2 - Compression stage of rotary engine Gas mixture entering the rotary engine at temperature and pressure respectively and undergoing adiabatic
  • Stage 3 - Combustion stage of rotary engine The gas mixture entering at temperature and pressure respectively, is ignited by means of a spark
  • the temperature is determined by considering an energy loss factor
  • Stage 4 - Decompression Stage The combustion gas mixture beginning this stage at temperature and pressure respectively, is decompressed and
  • the efficiency of decompression or mechanical efficiency can be represented as
  • This example illustrates a modeled process, implemented as set out above, that involves integrating a 1 .3 L Wankel rotary engine reformer with a Fischer - Tropsch synthesis reactor, using 100 % CH as reforming feed at atmospheric pressure and 25°C as the inlet conditions to the reformer. Air is used as the oxidant. Both combustion chambers of the rotary engine reformer are operating under partial oxidation condition. No gas cleanup system is applied. The mechanical efficiency of the engine is modeled to be 85%. The engine is modeled operating at 5000 rpm with a compression ratio of 7.65: 1 .
  • FIG. 1 A schematic diagram for such a process is presented in Figure 2.
  • a mixture of 1 .07 mol/s of CH and 3.3 mol/s of air (Stream 101 ) is fed to the rotary engine reformer to generate a synthesis gas mixture (Stream 102) containing CH , C0 2 , CO, H 2 , H 2 0 and N 2 flowing at 4.37 mol/s at a temperature 836 °C and a pressure of 4.7 barg.
  • This represents an air fuel ratio of 5.57, approaching the idealized AF 4.29 for partial oxidation:
  • the AF can for example be varied between 4.29 to 17.19.
  • the mechanical motion of the rotor is coupled with a power generator to offset the energy requirement in the overall process loop.
  • the mechanical power generated by the engine is 15.22 kW.
  • the synthesis gas mixture is allowed to cool to 350 °C in a heat exchanger and the cooled synthesis gas (Stream 103) passes through a water gas shift reactor.
  • the water gas shift reactor increases the H 2 :CO ratio of the synthesis gas to 2.1 and the gas (Stream 104) is then sent to a chiller to cool to 25°C.
  • the compositions of the gas streams 101 , 102 and 104 are presented in Table 1 . Table 1 . Composition of fluid streams in process illustrated in Figure 2.
  • the cooled synthesis gas (Stream 105) is pressurized to 30 bars in a compressor. A compressor operating at 100 % efficiency would require 34.62 kW for this compression.
  • the compressed synthesis gas (Stream 106) is passed through a heat exchanger (HX1 ) to reach a temperature of 200 °C.
  • the preheated synthesis gas (Stream 107) is fed to the Fischer - Tropsch Synthesis reactor to form a product stream (Stream 108) comprising of hydrocarbons, oxygenates and water.
  • a wax stream (Stream 109) is separated from the product mixture in a separator maintained at 200 °C. The remaining product stream
  • Stream 1 10 is passed through HX1 and then a chiller to cool the product to 25 °C.
  • the cooled product stream (Stream 1 12) contains a mixture of gas and liquid phases, and is sent to a separator to split the stream into three parts - an aqueous phase containing oxygenates and water (Stream 1 13), a hydrocarbon rich liquid phase (Stream 1 14) and tail gas containing unreacted synthesis gas and short chain hydrocarbons (Stream 1 15).
  • the mechanical power generated by the engine reformer is 15.22 kW, while the power required for the compression of Stream 105 to 106 is 34.62 kW.
  • the compression can be split into 2 stages with a cooling stage in the middle.
  • the first compressor would increase the pressure of the stream by 5.5 bar, while the second stage compressing the gas to 30 barg.
  • the power required for Stage 1 and 2 compressors would be 15.14 kW and 21 .94 kW respectively.
  • the engine reformer could be coupled with the Stage 1 compressor to offset the power requirement of the gas loop.
  • This example illustrates a modeled process involving a 1 .3L rotary engine with one combustion chamber operating under complete combustion conditions and the second chamber operating under partial oxidation conditions, with both chambers using natural gas with 98% CH and 2% C0 2 as a fuel.
  • the engine operates with a coupled turbocharger compressing the gas by a factor of 2.
  • the exhaust from the chamber running partial oxidation is utilized downstream for methanol synthesis reaction.
  • the exit pressure of the exhaust gas from the partial oxidation chamber of the reformer engine is set at a pressure of 30 barg. Air is used as the oxidant.
  • a Selexol® solvent based gas cleanup system is applied
  • the mechanical efficiency of the engine is considered to be 85%.
  • the engine is operating at 7500 rpm and has a compression ratio of 7.65.
  • FIG. 3 A schematic diagram for such a process is provided in Figure 3.
  • a mixture of 36.42 sLps (standard litres per second) of natural gas and 1 10.43 sLps of oxidant (Stream 101 ) is fed to one chamber of the rotary engine reformer to generate a synthesis gas mixture (Stream 103) containing CH , C0 2 , CO, H 2 , H 2 0 and N 2 flowing at 189.95 sLps at an exit pressure of 30 bar.
  • a mixture of Natural gas and air (Stream 102) is passed through the second chamber of the engine reformer to undergo complete combustion.
  • the combustion reaction in this chamber powers the rotation of the rotor in the partial oxidation chamber.
  • Stream 104 is the exhaust gas from the combustion chamber and contains C0 2 , N 2 , H 2 0 and unreacted 0 2 .
  • the synthesis gas mixture from the partial oxidation chamber (Stream 103) is exhausted at 30 barg and allowed to cool to 350°C in a chiller and the cooled synthesis gas (Stream 105) pass through a water gas shift reactor.
  • the water gas shift reactor increases the H 2 :CO ratio of the synthesis gas to 2.1 and the gas (Stream 106) is then sent to a chiller to cool to 25°C.
  • the compositions of the gas streams 101 , 103 and 106 are presented in Table 3.
  • the cooled and compressed gas (Stream 107) is sent to a gas - liquid separator to remove the condensed water (109).
  • the dehydrated synthesis gas stream (Stream 108) undergoes sulfur removal using a Selexol® based absorption bed system.
  • the clean gas (Stream 1 10) is preheated to 180°C (Stream 1 1 1 ) and fed to the Methanol Synthesis reactor.
  • the product coming out of the reactor (Stream 1 12) is a mixture of unreacted synthesis gas and methanol product.
  • Stream 1 12 is cooled in the heat exchanger (Stream 1 13) and a chiller in sequence to cool the product to 25°C (Stream 1 14).
  • Stream 1 14 is passed through a Gas - Liquid Separator to separate the methanol as a liquid product (1 15) from the unreacted synthesis gas product (Stream 1 16).
  • This example illustrates a modeled process involving A 1 .3L rotary engine with one combustion chamber operating under complete combustion condition and the second chamber operating in partial oxidation condition.
  • Gasoline is utilized as a fuel for the chamber having complete combustion
  • landfill gas is utilized as the fuel for the chamber having partial oxidation condition.
  • the composition of the landfill gas is CH : C0 2 : N 2 53:35: 12, along with sulfur based impurities.
  • the engine operates with a coupled turbocharger compressing the gas by a factor of 2.
  • the exit pressure of the exhaust gas from the partial oxidation chamber of the reformer engine is set at a pressure of 30 bar. Oxygen enriched air is used as the oxidant.
  • a dual stage gas cleanup system based on Selexol® solvent is applied downstream of the engine reformer to remove C0 2 in one stage and sulfur compounds in the other.
  • the remaining gas is passed through a membrane based separation system to obtain a clean H 2 stream.
  • the engine is operating at 7500 rpm and has a compression ratio of 7.65.
  • FIG. 3 A schematic diagram for such a case has been presented in Figure 3.
  • 148.64 sLps of air (Stream 101 ) is compressed to 30 barg (Stream 102) and passed through an oxygen selective membrane.
  • the retentate (Stream 103) is 80.69 sLps of 95 % N 2 and the permeate (Stream 104) contains 40% 0 2 and 60% N 2 .
  • the oxygen enriched air stream is mixed with 78.89 sLps of landfill gas along with some amount of moisture (Stream 105).
  • the mixture of landfill gas and oxidant (Stream 106) is fed to one chamber of the rotary engine reformer to generate a synthesis gas mixture (Stream 108) containing CH , C0 2 , CO, H 2 , H 2 0 and N 2 flowing at 169.07 sLps at an exit pressure of 30 bar.
  • a synthesis gas mixture (Stream 108) containing CH , C0 2 , CO, H 2 , H 2 0 and N 2 flowing at 169.07 sLps at an exit pressure of 30 bar.
  • gasoline (Stream 107) is passed into the second chamber of the engine reformer through the fuel mixer along with air to undergo complete combustion.
  • the combustion reaction in this chamber powers the rotation of the rotor in the partial oxidation chamber.
  • Stream 109 is the exhaust gas from the combustion chamber and contains C0 2 , N 2 , H 2 0 and unreacted 0 2 .
  • the synthesis gas mixture (Stream 108) is cooled by quenching with water (Stream 1 10) and the mixture (Stream 1 1 1 ) is sent to a water gas shift reactor to obtain an H 2 :CO ratio of 10 (Stream 1 12).
  • the composition of Stream 106, 108 and 1 12 is provided in Table 5.
  • Stream 1 12 is cooled in a chiller to 25°C (Stream 1 13) and passed through a vapor liquid separator to remove the moisture (Stream 1 14).
  • the remaining gas (Stream 1 13) is compressed to 30 barg and made to undergo a dual stage Selexol® based separation system to remove 23.90 sLps of C0 2 (Stream 1 15) and H s S impurities (Stream 1 16).
  • the remaining synthesis gas mixture (Stream 1 17) is made to pass through a H 2 selective membrane to obtain 62.26 sLps of pure H 2 (Stream 1 18) along with the retentate stream (Stream 1 19).

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
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  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un procédé de production de gaz de synthèse (CO + H2) à partir d'un combustible hydrocarboné à l'aide d'un système moteur à piston rotatif. Les combustibles hydrocarbonés peuvent comprendre, par exemple, du méthane, de l'éthène, de l'éthane, du propène ou du propane. De l'oxygène est alimenté pour la combustion, par exemple sous forme d'air ou de gaz enrichi en oxygène. Le combustible hydrocarboné subit une oxydation partielle afin de produire un gaz de synthèse (gaz synthétique). L'énergie produite par le moteur à piston rotatif peut être utilisée extérieurement pour une variété d'applications. Le gaz de synthèse peut être utilisé directement pour la production de combustibles hydrocarbonés, par exemple pour la production de méthanol ou d'autres produits liquides par l'intermédiaire d'un procédé de synthèse Fischer-Tropsch. Le gaz de synthèse peut être également utilisé pour la production d'hydrogène à l'aide d'une réaction de conversion à la vapeur d'eau.
PCT/CA2018/051190 2017-09-22 2018-09-21 Reformeur rotatif WO2019056119A1 (fr)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113374572A (zh) * 2021-06-29 2021-09-10 北京工业大学 一种结合egr的纯氢燃料转子机控制方法

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3754534A (en) * 1971-12-23 1973-08-28 Gen Motors Corp Rotary combustion engine ignition
GB2148385A (en) * 1983-10-19 1985-05-30 Peter Spencer Production of synthesis gas using an I.C. engine
US6174460B1 (en) * 1996-08-13 2001-01-16 Experimentalny Komplex “Novye Energeticheskie Tekhnologii” (EK “Net”) Obiedinennogo Instituta Vysokikh Temperatur Rossiiskoi Akademii Nauk Method for producing synthesis gas
US6502533B1 (en) * 2001-09-29 2003-01-07 George Beuan Kirby Meacham Internal combustion fuel reforming
US20050004834A1 (en) * 2003-05-07 2005-01-06 The Salamander Organization Limited Method and system for performance analysis for a function or service provided to or in an organization

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3754534A (en) * 1971-12-23 1973-08-28 Gen Motors Corp Rotary combustion engine ignition
GB2148385A (en) * 1983-10-19 1985-05-30 Peter Spencer Production of synthesis gas using an I.C. engine
US6174460B1 (en) * 1996-08-13 2001-01-16 Experimentalny Komplex “Novye Energeticheskie Tekhnologii” (EK “Net”) Obiedinennogo Instituta Vysokikh Temperatur Rossiiskoi Akademii Nauk Method for producing synthesis gas
US6502533B1 (en) * 2001-09-29 2003-01-07 George Beuan Kirby Meacham Internal combustion fuel reforming
US20050004834A1 (en) * 2003-05-07 2005-01-06 The Salamander Organization Limited Method and system for performance analysis for a function or service provided to or in an organization

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113374572A (zh) * 2021-06-29 2021-09-10 北京工业大学 一种结合egr的纯氢燃料转子机控制方法
CN113374572B (zh) * 2021-06-29 2022-08-09 北京工业大学 一种结合egr的纯氢燃料转子机控制方法

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