WO2010012026A1 - Apparatus for liquefaction of carbonaceous material - Google Patents
Apparatus for liquefaction of carbonaceous material Download PDFInfo
- Publication number
- WO2010012026A1 WO2010012026A1 PCT/AU2009/000957 AU2009000957W WO2010012026A1 WO 2010012026 A1 WO2010012026 A1 WO 2010012026A1 AU 2009000957 W AU2009000957 W AU 2009000957W WO 2010012026 A1 WO2010012026 A1 WO 2010012026A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- carbonaceous material
- liquid
- high pressure
- separator
- liquefaction apparatus
- Prior art date
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Classifications
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- E—FIXED CONSTRUCTIONS
- E21—EARTH DRILLING; MINING
- E21B—EARTH DRILLING, e.g. DEEP DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
- E21B43/24—Enhanced recovery methods for obtaining hydrocarbons using heat, e.g. steam injection
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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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
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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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
- C10G1/065—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation in the presence of a solvent
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/24—Stationary reactors without moving elements inside
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4037—In-situ processes
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4081—Recycling aspects
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/80—Additives
- C10G2300/805—Water
Definitions
- This invention relates to apparatus for the recovery of hydrocarbons from carbonaceous material.
- carbonaceous material is intended to refer to refer to an a solid, semi-solid or bituminous organic fossil fuel compound such as coal, including lignite (also Jknown as brown coal), sub-bituminous coal, bituminous coal, anthracite and graphite, as well as oil shale, oil sands (tar sands), heavy or bituminous oil deposits, and other related substances, and combinations thereof whether mined or in situ.
- lignite also Jknown as brown coal
- sub-bituminous coal also Jknown as brown coal
- bituminous coal bituminous coal
- anthracite and graphite as well as oil shale, oil sands (tar sands), heavy or bituminous oil deposits, and other related substances, and combinations thereof whether mined or in situ.
- oil sands oil sands
- heavy or bituminous oil deposits and other related substances, and combinations thereof whether mined or in situ.
- hydrocarbon would be understood by a person skilled in the art to refer to an organic compound consisting of hydrogen and carbon.
- liquid hydrocarbon is intended to refer to the hydrocarbons produced by the method of the invention that are suitable for use as a fuel, either directly or following an appropriate treatment, conversion or upgrade using methods well-known to those persons skilled in the cart.
- the liquid hydrocarbons may also comprise some solid or particulate matter, including oil-soluble solids.
- the liquid hydrocarbon of present invention may also be referred to as “oil”, “coal oil”, “unconventional oil”, “crude oil” or “crude oil substitute” by persons skilled in the art.
- in situ is intended to limit the carbonaceous material as being in its original location, that is, within a geological deposit of carbonaceous material found naturally in the ground.
- an in situ deposit of carbonaceous material frequently comprises various forms of carbonaceous materials including oil shale, oil sands (tar sands), heavy or bituminous oil deposits, lignite (also known as brown coal), sub-bituminous coal, bituminous coal through to anthracite and graphite and combinations thereof.
- reaction reaction is intended to refer to a chemical reaction wherein a solid, semi-solid or bituminous carbonaceous material is reduced to a less solid or liquid form.
- chemical bonds between two atoms in a molecule e.g. double bonds between two carbon atoms in a molecule of a carbonaceous material
- reaction that binds hydrogen atom(s) are generally reduced by a reaction that binds hydrogen atom(s), such that the two carbon molecules previously double bonded together remain joined by a single bond and one or both are now bonded to a hydrogen (or other) atom.
- the liquefaction reaction molecules may be separated from each other and the previous carbon or carbon-carbon bonds may now "capped" or occupied with a hydrogen atom.
- Carbon-carbon (CC) bonds are particularly susceptible to cleavage from OH, that is the hydroxyl radical or the hydroxyl ion or from various other free radicals.
- the hydroxyl radical and other free radicals effective in cleaving carbon bonds in hydrocarbons can be generated from the mobilisation of the volatiles component of the hydrocarbon typically from thermal elevation of the hydrocarbon or can be supplied by application of substances that contain OH to the hydrocarbon.
- Supercritical water or to a lesser degree superheated water are both a source of OH.
- Both supercritical water and to a lesser degree superheated water are able to provide such a hydrogen atom for transfer or capping to the carbonaceous material.
- the source of such a hydrogen from water is typically from a H 3 O ion which will resolve back to H 2 O after transferring one H atom in this example or from a H atom that has been ionised from its partner OH ion for example in supercritical water.
- Superheated water is generally considered to contain 100 times the water ions than are found in ambient water and supercritical water is generally considered to consist of 70% water ions. If such a hydrogen atom is not immediately available for "capping" at the severed carbon bond or the severed carbon-carbon bond than there is a tendency or high likelihood that the severed C or CC bonds will rejoin to other molecules that have undergone similar bond cleavage and the resulting "uncapped " union or rejoining of molecules that have had their carbon bonds severed results in a hydrocarbon molecule that is particularly resistant to further hydrogenation or upgrading.
- Carbonaceous material is liquefied as it is hydrogenated, meaning that a carbonaceous material changes from a more solid state to a more liquid state, that is, a liquid hydrocarbon. Under experimental conditions, hydrogenation of coal may result in up to 96% of coal being liquefied. Hydrogenation is a strongly- exothermic process. The terms “liquefying” or “liquefaction” are also intended to be referring to this process.
- reaction zone is intended to refer to the in situ area in which the liquefaction reaction is occurring.
- aqueous solution is intended to refer to a liquid that is water, or similar to water, or a water- based liquid in which other chemical components may be dissolved or are dissolved. However, it will be appreciated that the liquid can be a superheated or supercritical fluid. It is also to be understood that any of the aqueous solutions of the present invention may alternatively comprise components selected from the group consisting of water, hydrogen peroxide, methanol, ethanol, acetone, propane, ethylene, and propylene. The aqueous solution can further comprise an organic component, diesel fuel, or a liquid hydrocarbon. Alternatively or in addition it may contain a catalyst or a combination of catalysts to assist in the hydrogenation of the carbonaceous material.
- supercritical fluid describes a fluid at a temperature and pressure above its thermodynamic critical point; wherein the term “thermodynamic critical point” refers to the conditions (i.e. temperature and pressure) at which the phase boundary between a liquid and a gaseous phases of the aqueous solution ceases to exist.
- thermodynamic critical point refers to the conditions (i.e. temperature and pressure) at which the phase boundary between a liquid and a gaseous phases of the aqueous solution ceases to exist.
- thermodynamic critical point can be thought of as a "supercritical region” consisting of a range of temperatures and pressures at which the fluid behaves as a "supercritical fluid”, rather than a distinct point, line or distinct combination of pressure and temperature.
- a "supercritical fluid” of the present invention is intended to refer to a fluid with temperatures or pressures in or around the supercritical point that behaves like a supercritical fluid or with properties at least partially of a supercritical fluid or similar to a supercritical fluid.
- a "superheated fluid” is a fluid under pressure greater than atmospheric pressure at temperatures between its usual boiling point (i.e. at atmospheric pressure) and its thermodynamic critical point.
- superheated water may have a pressure range and temperature range between 100 0 C at atmospheric pressure to the point where the fluid is considered to be in the supercritical range.
- superheated water could have a pressure of 15 MPa and a temperature of 350 0 C, a pressure of 10 MPa and a temperature of 350 0 C, a pressure of 0.5 MPa and 10 MPa and a temperature of 150 0 C to 350 0 C, etc.
- a person skilled in the art will appreciated that superheated fluid can exists in a wide range of pressures and temperatures.
- Supercritical water could have a temperature of 385°C and a pressure of 22 MPa, or could have a temperature of 430 0 C and a pressure of 25 MPa .
- a person skilled in the art will similarly recognise that supercritical water can exist in a wide range of pressures and temperatures.
- the invention is said to reside in a carbonaceous material liquefaction apparatus comprising a nozzle assembly to supply a pressurised liquid towards a carbonaceous material as a high velocity liquid, a supply line to supply the high pressure liquid to the nozzle assembly, the high velocity liquid reacting with the carbonaceous material to produce a processed carbonaceous material, a product return line to return the processed carbonaceous material and entrained liquid to a processing plant, the processing plant comprising a heat exchanger to transfer heat from the product return line to the supply line, a high pressure pump to provide the high pressure liquid to the supply line, a separator in the product return line downstream of the heat exchanger to separate gas and oil product from the processed carbonaceous material and entrained liquid, and a recycle line to transfer at least part of the liquid from the separator to the high pressure pump.
- a locating device such as a flow through mandrel or a device similar to a twin port bridge plug or any device which allows return flow back up the annular space between the tubing and the outer well casing can be employed to stabilise the nozzle against and within the casing.
- nozzle and tubing and casing arrangements employed in the oil industry and commonly referred to as "jet pumping".
- jet pumping In these conventional oil field nozzle/casing arrangements the nozzle is always positioned above not below, an isolating and centralising packer assembly.
- the packer In this conventional oilfield arrangement the packer is of an isolating variety such that the fluid that is discharged from the nozzle never makes contact with the carbonaceous geological formation.
- the fluid discharged from the nozzle is never employed for reactions of a chemical nature with the returns flow in the annular space in the geological carbonaceous deposit in the well.
- the apparatus is employed solely to provide a lift mechanism for hydrocarbon that is typically crude oil.
- This conventional recovery of crude oil occurs by sucking the crude oil upwards through a one way port in the isolating packer above the geological deposit, and into the annular space of the well via the reduced pressure existing in the annular space of the well as a consequence of the high velocity discharge of a fluid through a nozzle above the isolating packer.
- the crude oil is then physically entrained in the Liquid flow that has exited the nozzle and is transported physically to surface for recovery from the annulus in a liquid phase.
- the apparatus described enables a reaction or reactions to occur between the supercritical water and the carbonaceous material either in situ in the geological formation or alternately in an above ground surface vessel.
- the recovery stream or the "returns" of the upgraded carbonaceous material are entrained in a vaporous (steam) return stream which so enables large return flow rates with very little restriction of flow for the upgraded (hydrogenated) product return stream.
- the velocity that the supercritical fluid acquires as it is discharged from the nozzle enables the fluid to exist as a liquid or at least liquid droplets even though the surrounding temperature and lower pressure would ordinarily otherwise dictate that the liquid would vaporise.
- This condition of a supercritical high velocity liquid existing in an environment of lower temperature and pressure which would otherwise dictate that the liquid vaporise will continue until the velocity depletes to a lower velocity at which point the supercritical liquid will become sub-critical and so vaporise.
- This condition is reached upon contact of the high velocity supercritical fluid with the carbonaceous material. At that point any of the high velocity supercritical fluid which has not been employed in the upgrading reactions with the carbonaceous material will vaporise into what is essentially steam.
- Any entrained moisture content of the carbonaceous material or surrounding geological formation will similarly vaporise into steam, partly driven by exposure to the high velocity supercritical water and its temperature, partly due to the heat generated by the exothermic hydrogenation reactions and heat generated from exothermic oxidation and redox reactions-, and also by the activation energy imparted to molecules from the transfer of the kinetic energy of velocity into internal activation energy of molecules upon the collision impact of the high velocity supercritical fluid and the stationary carbonaceous material.
- the now upgraded hydrocarbon liquids derived from the carbonaceous material have a higher boiling point than water, typically 300°C to 900°C the coal oil produced from the reactions is entrained in droplet form within the steam vapour. Any gaseous products of reaction are similarly entrained in this vapour phase.
- This composite steam/hydrocarbon droplet vapour is able to be easily transported either from an in situ geological formation or from an above ground vessel for further upgrading or separation and so ease of recovery is much enhanced over existing methods.
- the apparatus so described enables for the intimate contact between the reactants, in this case supercritical water and the carbonaceous material.
- This intimate contact results from the atomised high velocity supercritical water contacting the carbonaceous material.
- This intimate contact between reactants is otherwise typically only enabled by mining or bringing to surface the raw carbonaceous material and then separating impurities from the carbonaceous material, drying or removing any moisture from the carbonaceous material and finally grinding or commutating the carbonaceous material into a smaller particle size before contact with a usually static or low velocity flow reaction fluid. Instead this grinding to a smaller particle size of the carbonaceous material is replaced by the intimate contact afforded by the high velocity contact/impact of the atomised reaction fluid i.e. supercritical water.
- the apparatus further comprises an injection apparatus downstream or upstream of the high pressure pump to supply initiation chemicals and catalysts to the high pressure liquid supply line.
- the apparatus further comprises a reaction vessel, means to supply a charge of the carbonaceous material to the reaction vessel and the product return line being connected to the reaction vessel, the nozzle assembly directing the high velocity liquid towards the charge of the carbonaceous material in the reaction vessel.
- the apparatus further comprises means to withdraw spent residue of the carbonaceous material from the reaction vessel.
- the nozzle assembly comprises a plurality of nozzles.
- the product return line comprises a well casing and the supply line comprises a high pressure tubing within the well casing and preferably the high pressure tubing and the attached nozzle extend beyond the limit of the outer casing and the carbonaceous material is selected from coal, oil shale and tar sands.
- the nozzle or nozzles are attached to a tubing and both are able to be moved within the carbonaceous geological deposit via control of the tubing string movement from surface.
- a moveable tubing string is commonly employed for various oil and gas operations and is commonly referred to as a coil tubing unit.
- the recovery mechanism from the carbonaceous geological deposit in situ remains the same. That is the returns stream is still recovered via the annulus of the well and is in a substantially vapour phase.
- the nozzle assembly is able to be variably directed towards the carbonaceous material in an in-situ reaction zone. This can be achieved by using a nozzle with a defined angle of spray pattern that is less than 360 degrees.
- the angle of the spray pattern of the nozzle may be rotated or advanced by any means familiar to those skilled in the art or alternately the nozzle may be replaced by another nozzle with a different angle of spray pattern to the first nozzle.
- the nozzle assembly comprises a plurality of nozzles radiating the high velocity liquid towards the in-situ carbonaceous material.
- a nozzle with a complete or nearly complete 360 degree angle of spray pattern may be employed.
- the high pressure pump to provide the high pressure liquid to the supply line provides the liquid at pressures of from 15 MPa and 35 MPa.
- the apparatus further comprises a bleed off excess entrained liquid from the separator.
- the separator comprises a multi-stage separator, a first separator comprising a flash separator to separate gases from the processed carbonaceous material and entrained liquid, a second separator comprising an oil-liquid separator to separate oil from the processed carbonaceous material and entrained liquid and a filter to separate particulate material from the processed carbonaceous material and entrained liquid.
- carbonaceous materials such as coal, oil sands and/or oil shale can be efficiently liquefied in situ or in a above ground reactor using an aqueous solution that is capable of liquefying the carbonaceous material in a reaction zone.
- the liquefaction reaction can be initiated by applying to a carbonaceous material an aqueous solution capable of initiating liquefaction, such as an aqueous solution containing water, hydrogen peroxide and/or an alcohol such as methanol, and optionally a catalyst.
- an aqueous solution capable of initiating liquefaction, such as an aqueous solution containing water, hydrogen peroxide and/or an alcohol such as methanol, and optionally a catalyst.
- an aqueous solution initiates a liquefaction reaction that is exothermic. Due to the insulative properties of carbonaceous material in an in situ carbonaceous material formation for instance, the temperature is raised within the reaction zone within the carbonaceous material formation as the liquefaction reaction progresses.
- the heated aqueous solution will be heated to high temperatures and simultaneously be pressurized to above atmospheric pressure, for example, to obtain a superheated fluid or supercritical fluid, that is to say, water with supercritical properties.
- a superheated fluid or supercritical fluid that is to say, water with supercritical properties.
- Such substances may include methanol, hydrogen peroxide, catalysts (that were initially ingrained as impurities in the carbonaceous material), water, hydrogen gas and/or methane gas and various free radicals.
- the aqueous solution can be applied and the produced liquid hydrocarbons recovered using a modified conventional mining technology.
- the aqueous solution is applied using a nozzle apparatus that applies the aqueous solution to the face of the carbonaceous material formation at a high velocity, that is to say, water with supercritical properties.
- the nozzle apparatus may also optionally or alternatively depressurize the aqueous solution immediately prior to application of the aqueous solution to the face of the carbonaceous material formation.
- a second aqueous solution i.e. water with supercritical properties
- the second aqueous solution facilitates a continuing liquefaction reaction that liquefies the carbonaceous material to produce liquid hydrocarbon
- the second aqueous solution comprises components selected from the group consisting of water, hydrogen peroxide at a (w/w) concentration range between 0.1% to 70%, methanol at a (w/w) concentration range between 0.1% to 30%, and a second catalyst
- the second aqueous solution is a fluid selected from the group consisting of a heated fluid, a superheated fluid, a supercritical fluid and a high-velocity superheated fluid.
- reaction zone may be pre-heated by any means known to those skilled in the art.
- liquefying the carbonaceous material to produce liquid hydrocarbons using a high-velocity superheated fluid may provide an efficient means of liquefying a carbonaceous material to liquid hydrocarbon in situ.
- a method of liquefying a carbonaceous material in situ or in a reactor to produce liquid hydrocarbons using a high-velocity superheated fluid comprising the following steps:
- Figure 1 shows a schematic arrangement of a process accordingly to one embodiment of the invention
- Figure 2 shows a schematic view of the apparatus suitable for the in-situ processing embodiment of the present invention
- Figure 3 shows a schematic view of an apparatus suitable for the aboveground liquefaction of carbonaceous materials according to the present invention.
- Figure 4 shows a detail of a portion of the in situ processing apparatus of the present invention.
- schematic apparatus of the present invention includes an input apparatus section 2 and an output apparatus section 4. Between the input apparatus section 2 and the output apparatus section 4 is the liquefaction stage 6.
- high pressure pump arrangement means 10 are provided to supply high pressure liquid such as an aqueous solution at high pressure.
- the high pressure liquid is directed along line 12 and catalysts, initiators and/or other components are added through line 14 from supply 16.
- a heater arrangement 17 is also provided on line 12 to optionally heat the high pressure liquid to a desired temperature.
- Line 18 provides the high pressure liquid such as the aqueous solution at high pressure to a liquefaction stage 6.
- the aqueous solution is directed through a nozzle assembly which may be a single nozzle or multiple nozzles towards the carbonaceous material as a high velocity fluid, for example, a high velocity superheated or supercritical fluid.
- the nozzle is capable of depressurising the aqueous solution.
- the aqueous solution may be delivered to the carbonaceous material as a high velocity superheated fluid with retained supercritical properties.
- the aqueous solution reacts with the carbonaceous material and causes liquefaction of the carbonaceous material to produce an upgraded or liquefied carbonaceous material which is composed of a hydrocarbon liquid and gases along with entrained liquid and particulate residues. These are transferred by line 20 to the output apparatus section 4.
- the high pressure liquid is essentially water but can include other compounds such as initiators, catalysts and the like as required.
- Figure 2 shows the apparatus of the present invention for use with in situ liquefaction of a carbonaceous material such as coal.
- a coal seam 30 is situated below an overburden layer 32.
- a well casing 34 is extended through the overburden 32 into the coal seam 30.
- a high pressure tubing 36 extends with a nozzle 38 which extends below the well casing 34.
- the space between the well casing and the high pressure tubing 36 provides an annular return space 39 for product from the in situ reaction zone 40.
- the reaction product of processed carbonaceous material (such as liquid hydrocarbon) which exits through the annular space 39 is transferred via pipe 42 to a heat exchanger 44.
- heat from the reaction product is transferred to the aqueous solution in the high pressure liquid pipe 46 which directs aqueous solution, optionally at high pressure, into the high pressure tubing 36.
- the high pressure aqueous solution is supplied by high pressure pump 48.
- the aqueous solution can then optionally be heated by a boiler to the j desired temperature.
- Reactant components and catalysts can be provided from supply 50 into the high pressure line 46 to facilitate the liquefaction reaction.
- the nozzle 38 may be capable of depressurising a high pressure fluid to a lower pressure fluid, for example, depressurising as supercritical fluid at 25 MPa to a fluid having a pressure of 0.5 MPa to 10 MPa.
- the nozzle 38 is also capable of delivering the fluid at high velocity, for example 50 to 450 m/sec.
- the nozzle 38 may also be capable of delivering the fluid as a high velocity spray.
- reaction product After the reaction product has been cooled in the heat exchanger 44 it goes to a gas, liquid and oil separator 52 in which gas 54, oil 56 and liquid 58 are separated and solid residue 60 is also filtered out.
- a proportion of the liquid the liquid 58 is transferred by line 64 to the high pressure pump for reuse and the rest goes to waste.
- Carbonaceous material seams often have a high water content and hence there will be excess water to recover or send to waste.
- FIG 3 shows an aboveground apparatus according to the present invention.
- the same reference numerals will be used for corresponding items to those shown in Figure 2.
- a reaction vessel 70 has an input apparatus 72 and a residue withdrawal apparatus 74. These input apparatus 72 and residue withdrawal apparatus 74 are provided with supply vanes 76 to enable continuous charging of carbonaceous material into the reaction vessel without the loss of pressure and desired reaction product. Other forms of charging and removal apparatus may also be used according to the present invention.
- a nozzle assembly 78 provides multiple jets 80 of high pressure liquid to engage with carbonaceous material within the reaction vessel 70. Take off 82 withdraws reacted product from the reaction chamber.
- the reaction product of processed carbonaceous material which exits reaction chamber is transferred via pipe 42 to a heat exchanger 44. In the heat exchanger heat from the reaction product is transferred to the liquid in the high pressure liquid pipe 46 which directs high pressure liquid into reaction chamber 70.
- the high pressure liquid is supplied by high pressure pump 48.
- Initiation chemicals and catalysts are provided from supply 50 into the high pressure line 46.
- reaction product After the reaction product has been cooled in the heat exchanger 44 it goes to a gas, liquid and oil separator 52 in which gas 54, oil 56 and liquid 58 are separated and any solid residue 60 is also filtered out.
- a proportion of the liquid the liquid 58 is transferred by line 64 to the high pressure pump for reuse and the rest goes to waste.
- Carbonaceous material often has a high water content and hence there will be excess water to send to waste.
- FIG. 4 shows detail of the * underground portion of the apparatus suitable for in situ carbonaceous material liquefaction.
- the apparatus includes a well casing 34 through which is directed the high pressure tubing 36 with a nozzle 38 extending below the end of the well casing 34.
- a spacer 90 in the well casing supports the high pressure tubing in the well casing and has apertures 92 for the return of reacted product into the annular space 39.
- the nozzle 38 is directed laterally away from the well casing and means can be provided to rotate the high pressure tubing as indicated by the arrows 94 and move it vertically as indicated by the'arrow 96 so that the region of carbonaceous material which can be treated can be varied.
Abstract
Description
Claims
Priority Applications (10)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA 2732134 CA2732134A1 (en) | 2008-07-28 | 2009-07-28 | Apparatus for liquefaction of carbonaceous material |
AU2009276282A AU2009276282A1 (en) | 2008-07-28 | 2009-07-28 | Apparatus for liquefaction of carbonaceous material |
US13/056,493 US20110211997A1 (en) | 2008-07-28 | 2009-07-28 | Apparatus for liquefaction of carbonaceous material |
NZ59117109A NZ591171A (en) | 2008-07-28 | 2009-07-28 | Liquefaction of carbonaceous material using a pressurised superheated liquid |
CN200980129441.9A CN102105559B (en) | 2008-07-28 | 2009-07-28 | Apparatus for liquefaction of carbonaceous material |
JP2011520277A JP2011529127A (en) | 2008-07-28 | 2009-07-28 | Equipment for liquefaction of carbonaceous materials |
EP09802267A EP2310471A4 (en) | 2008-07-28 | 2009-07-28 | Apparatus for liquefaction of carbonaceous material |
ZA2011/01486A ZA201101486B (en) | 2008-07-28 | 2011-02-24 | Apparatus for liquefaction of carbonaceous material |
US13/874,571 US20130315792A1 (en) | 2008-07-28 | 2013-05-01 | Apparatus for liquefaction of carbonaceous material |
US14/576,587 US20150101792A1 (en) | 2008-07-28 | 2014-12-19 | Apparatus for liquefaction of carbonaceous material |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2008903840 | 2008-07-28 | ||
AU2008903840A AU2008903840A0 (en) | 2008-07-28 | Inventive jet pumping | |
AU2008903845A AU2008903845A0 (en) | 2008-07-28 | Method for in situ liquefaction of coal | |
AU2008903845 | 2008-07-28 |
Related Child Applications (2)
Application Number | Title | Priority Date | Filing Date |
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US13/874,571 Continuation US20130315792A1 (en) | 2008-07-28 | 2013-05-01 | Apparatus for liquefaction of carbonaceous material |
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PCT/AU2009/000958 WO2010012027A1 (en) | 2008-07-28 | 2009-07-28 | Method of liquefaction of carbonaceous material to liquid hydrocarbon |
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EP (2) | EP2310471A4 (en) |
JP (2) | JP2011529128A (en) |
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AU (2) | AU2009276282A1 (en) |
CA (2) | CA2732138A1 (en) |
EA (1) | EA201100292A1 (en) |
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WO2012000033A1 (en) | 2010-07-01 | 2012-01-05 | Ignite Energy Resources Limited | Ballistic heating process |
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Also Published As
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CA2732134A1 (en) | 2010-02-04 |
ZA201101467B (en) | 2011-10-26 |
AU2009276282A1 (en) | 2010-02-04 |
NZ591171A (en) | 2013-05-31 |
CN102105559A (en) | 2011-06-22 |
US20110211997A1 (en) | 2011-09-01 |
EP2310471A4 (en) | 2012-02-01 |
NZ591177A (en) | 2011-08-26 |
US8727000B2 (en) | 2014-05-20 |
WO2010012027A1 (en) | 2010-02-04 |
CN102105559B (en) | 2014-06-25 |
CA2732138A1 (en) | 2010-02-04 |
US20130315792A1 (en) | 2013-11-28 |
CN102165036B (en) | 2015-05-20 |
EP2326696A1 (en) | 2011-06-01 |
US20150101792A1 (en) | 2015-04-16 |
EA201100292A1 (en) | 2011-12-30 |
JP2011529128A (en) | 2011-12-01 |
JP2011529127A (en) | 2011-12-01 |
EP2310471A1 (en) | 2011-04-20 |
US20110180262A1 (en) | 2011-07-28 |
ZA201101486B (en) | 2011-10-26 |
CN102165036A (en) | 2011-08-24 |
AU2009276283A1 (en) | 2010-02-04 |
EP2326696A4 (en) | 2012-02-08 |
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