CN104711040A - System and method for continuous slag handling with direct cooling - Google Patents
System and method for continuous slag handling with direct cooling Download PDFInfo
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- CN104711040A CN104711040A CN201410755219.2A CN201410755219A CN104711040A CN 104711040 A CN104711040 A CN 104711040A CN 201410755219 A CN201410755219 A CN 201410755219A CN 104711040 A CN104711040 A CN 104711040A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
- C10J3/845—Quench rings
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/485—Entrained flow gasifiers
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/52—Ash-removing devices
- C10J3/526—Ash-removing devices for entrained flow gasifiers
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- Engineering & Computer Science (AREA)
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Abstract
The invention relates to a system and a method for continuous slag handling with direct cooling. A system includes a quench chamber configured to continuously receive a mixture of a gas and slag, and a downstream end portion coupled to the quench chamber. The quench chamber includes a quench sump configured to continuously separate the gas from the slag in the mixture via a quench liquid. The downstream end portion is configured to continuously convey a slag slurry to a depressurization system. The downstream end portion includes a cooling system configured to directly cool the slag slurry with a cooling fluid, and the slag slurry includes the separated slag and at least a portion of the cooling fluid.
Description
About the statement of the research and development that federal government subsidizes
The present invention is that the contract DE-FE0007859 authorized according to USDOE carries out under the support of government.Government has some right to the present invention.
Technical field
Theme disclosed herein relates to slag disposal system, and more specifically, relates to lasting slag disposal system.
Background technology
Commercial run can use the fluid mixture of the solid particulate starched or be suspended in liquid (such as, water) that solid particulate is transported through corresponding process.Such as, part oxidizing system partly can be oxidized carbonaceous component in an oxygen-containing environment, to produce multi-products and by product.Such as, carbonaceous material can be changed into the useful mixture of carbon monoxide and hydrogen by gasifier, and this mixture is called synthesis gas or synthetic gas.When the carbonaceous material containing ash, the synthetic gas obtained also can comprise so not desirable composition, such as heavy ash or slag, and they can remove together with the useful synthetic gas of generation from gasifier.Therefore, the slag by product produced in gasifier reaction can be directed in gasifier quench liquid, with solidified slag and generation slurry.Substantially, this slurry is discharged at an elevated temperature and pressure from gasifier.The slurry of discharging from gasifier, by step-down, to make it possible to dispose slurry, or processes slurry further.It's a pity can have complicated flow path at slurry from the heat exchanger reducing the temperature of slurry after gasifier is discharged, larger floor space can be had and/or can be easy to corrode because slag gathers or block.
Summary of the invention
Be summarized in some embodiment suitable with originally claimed the present invention in scope below.These embodiments are not intended to limit claimed scope of the present invention, but these embodiments are only intended to the brief overview providing possible form of the present invention.In fact, the present invention can comprise the various ways that can be similar to or be different from the embodiment set forth below.
In a first embodiment, a kind of system comprises the quenching chamber of the mixture being configured to receiver gases and slag constantly, and is connected to the downstream end portion on quenching chamber.Quenching chamber comprises quench tank, and it is configured by the gas of quench liquid constantly in separating mixture and slag.Downstream end portion is configured to constantly slag slurry is transferred to depressurizing system.Downstream end portion comprises cooling system, and it is configured to utilize cooling fluid directly to cool slag slurry, and slag slurry comprises isolated slag and cooling fluid at least partially.
In a second embodiment, a kind of system comprises gasifier, and it is configured to make carbon containing feed be reacted into the mixture of gas and slag.Gasifier comprises quench tank, and it is configured by the gas of quench liquid constantly in separating mixture and slag, and quench liquid is configured to flow through quench tank with the first flow rate.Gasifier also comprises the downstream end portion with cooling system of gasifier, and controller.Downstream end portion is configured to, with the 3rd flow rate, slag slurry is transferred to depressurizing system constantly, 3rd flow rate is about 15% or less of the first flow rate, downstream end portion is configured to add cooling fluid to cool slag slurry with the second speed, and slag slurry comprises slag and cooling fluid.
In the third embodiment, a kind of method comprises separation slag and gas; Cooling fluid is assigned in the downstream end portion of gasifier; The slag slurry through cooling is formed with slag and cooling fluid; And the slag of net cooling slurry is conveyed through substantially constantly the outlet of downstream end portion.The temperature of slag is higher than about 175 DEG C, and cooling fluid is configured to the temperature of slag to be reduced to lower than about 70 DEG C.
Technical scheme 1. 1 kinds of systems, comprising:
Quenching chamber, it is configured to the mixture of receiver gases and slag constantly, and wherein said quenching chamber comprises quench tank, and it is configured by quench liquid and is separated gas in described mixture and slag constantly; And
Downstream end portion, it is connected on described quenching chamber, wherein said downstream end portion is configured to constantly slag slurry is transferred to depressurizing system, described downstream end portion comprises cooling system, it is configured to utilize cooling fluid directly to cool described slag slurry, and described slag slurry comprises isolated slag and cooling fluid at least partially.
The system of technical scheme 2. according to technical scheme 1, is characterized in that, comprises one or more slag grating device, and it is configured to receive described slag slurry.
The system of technical scheme 3. according to technical scheme 2, is characterized in that, described cooling system is at least partially disposed between the first slag grating device in described one or more slag grating device and the second slag grating device in described one or more slag grating device.
The system of technical scheme 4. according to technical scheme 2, is characterized in that, described cooling system is at least partially disposed on described one or more slag grating device upstream.
The system of technical scheme 5. according to technical scheme 1, is characterized in that, comprises the slag grating device be connected in described downstream end portion.
The system of technical scheme 6. according to technical scheme 1, is characterized in that, comprise reactor, and it is connected on described quenching chamber, and wherein said reactor structure becomes to make carbon containing feed react and produce gas and slag.
The system of technical scheme 7. according to technical scheme 1, is characterized in that, described cooling system comprises one or more nozzle, and it is configured to directly be assigned to by described cooling fluid in described slag slurry.
The system of technical scheme 8. according to technical scheme 1, it is characterized in that, described cooling system comprises multiple set of nozzles, it is configured to distribute described cooling fluid, wherein each set of nozzles comprises one or more nozzle, and each in described one or more nozzle be configured to from another the different angle in described one or more nozzle of corresponding set of nozzles, from another the different axial positions in described one or more nozzle of corresponding set of nozzles, described cooling fluid is being distributed from another the different circumferential position in described one or more nozzle of corresponding set of nozzles or in any mode that it combines.
The system of technical scheme 9. according to technical scheme 1, is characterized in that, described cooling system is configured to described slag to be cooled to lower than about 70 DEG C.
Technical scheme 10. 1 kinds of systems, comprising:
Gasifier, it is configured to make carbon containing feed be reacted into the mixture of gas and slag, and wherein said gasifier comprises:
Quench tank, it is configured by quench liquid and is separated gas in described mixture and slag constantly, and wherein said quench liquid is configured to flow through described quench tank with the first flow rate; And
The downstream end portion of described gasifier comprises cooling system, wherein said downstream end portion is configured to constantly slag slurry is transferred to depressurizing system with the 3rd flow rate, described 3rd flow rate is about 15% or less of described first flow rate, described downstream end portion is configured to add cooling fluid to cool described slag slurry with the second flow rate, and described slag slurry comprises described slag and described cooling fluid; And
Controller, it is configured to control described second flow rate.
The system of technical scheme 11. according to technical scheme 10, is characterized in that, comprises one or more slag grating device, and it is configured to receive described slag slurry constantly.
The system of technical scheme 12. according to technical scheme 10, it is characterized in that, comprise the described depressurizing system be connected in described downstream end portion, wherein said depressurizing system comprises one or more orifice plate, one or more dump valve, one or more expansion turbine, one or more impeller pump, or its combination any.
The system of technical scheme 13. according to technical scheme 12, is characterized in that, described controller be configured at least in part based on the expectation of described depressurizing system flow rate and control described second flow rate.
The system of technical scheme 14. according to technical scheme 10, is characterized in that, described cooling system is configured to the described slag slurry of directly cooling, to reduce the evaporation of described slag slurry in described depressurizing system during step-down.
The system of technical scheme 15. according to technical scheme 10, it is characterized in that, comprise multiple sensor, it is configured to provide feedback to described controller, wherein said feedback comprises temperature data, pressure data, data on flows or viscosity data, or its combination any.
The system of technical scheme 16. according to technical scheme 10, is characterized in that, described cinder ladle draws together the described quench liquid being less than about 5%.
Technical scheme 17. 1 kinds of methods, comprising:
Be separated slag and gas, the temperature of wherein said slag is higher than about 175 DEG C;
Be assigned to by cooling fluid in the downstream end portion of gasifier, wherein said cooling fluid is configured to the temperature of described slag be reduced to lower than about 70 DEG C;
The slag slurry through cooling is formed with described slag and described cooling fluid; And
The described slurry of the slag through cooling is conveyed through substantially constantly the outlet of described downstream end portion.
The method of technical scheme 18. according to technical scheme 17, is characterized in that, forms the described slag through cooling slurry and comprises and utilize one or more slag grating device that described slag is crushed to multiple particle.
The method of technical scheme 19. according to technical scheme 18, is characterized in that, in the upstream of described one or more slag grating device, the downstream of described one or more slag grating device or distribute described cooling fluid between described one or more slag grating device.
The method of technical scheme 20. according to technical scheme 18, it is characterized in that, be separated described slag and described gas and comprise and supply quench liquid with the first flow rate, wherein, described cooling fluid distributes with the second flow rate, and described second flow rate is lower than about 15% of described first flow rate.
Accompanying drawing explanation
When reading following detailed description in detail with reference to accompanying drawing, these and other feature of the present invention, aspect and advantage will become better understood, and in the accompanying drawings, same-sign represents same parts in all figure, wherein:
Fig. 1 is the schematic diagram of the embodiment of lasting slag removal system;
Fig. 2 is the schematic diagram of the embodiment of the gasifier with direct cooling system;
Fig. 3 is the cross section obtained along the line 3-3 of Fig. 2 of the embodiment of direct cooling system; And
Fig. 4 is the schema of the technique for processing slurry constantly illustrated according to embodiment.
Embodiment
To be described one or more specific embodiment of the present invention below.In order to be devoted to provide the concise and to the point description to these embodiments, may all features that reality realizes be described in the description.Should be realized, in the exploitation that any this reality realizes, as in any engineering or design project, many decision-makings specific to realizing must be made to reach the specific purposes of developer, the constraint that system of such as obeying is correlated with and the constraint that business is correlated with, these specific purposes can change with different realizations.In addition, should be realized, this development may be complicated and consuming time, but concerning benefiting from those of ordinary skill of the present disclosure, and this development will be only design, produce and the routine mission of manufacture.
When introducing the key element of various embodiments of the present invention, article " ", " being somebody's turn to do " and " described " are intended to represent the meaning that there is this key element one or more.Term " comprises ", " comprising " and " having " be intended to be comprising property, and represent the meaning that can to there is other key element except the key element listed.
Multiple industrial technology relates to process slurry.Slurry can comprise the granular solids be dispersed in fluid (such as water).In some cases, starch and be transported to the second position from first location or container.Slurry can through step-down and/or cooling during being transported to the second position from first location.Such as, part oxidizing system (such as, gasifier) reaction chamber can receive carbon containing feed (such as, the slurry of the carbonaceous particles solid of such as coal or biomass, the granular solids stream of pneumatic conveying, liquid, gas or its combination any) and oxygenant (such as, high purity oxygen).In certain embodiments, reaction chamber can receive water (such as, water spray or steam) to help to produce slurry.The partial oxidation of feed, oxygenant and (in some cases) water can produce useful gaseous product and grey or slag by product.Such as, gasifier can receive feed, oxygen and water, to produce synthesis gas or synthetic gas and slag.In some cases, slag flows in quench liquid (such as water) by gasifier, to produce slag slurry.The slag of discharging from gasifier starches high gauge pressure (gage) pressure that can be in about 1000 to 10000 kPas (kpa).The temperature of the slag slurry in gasifier can be between about 80 to 250 DEG C (such as, between 175 to 475 ℉), between about 100 to 225 DEG C (such as, between 212 to 440 ℉) or between about 150 to 200 DEG C (such as, between 300 to 400 ℉) or higher.Before slag slurry processes further or disposes, slag slurry can be depressured to lower pressure (such as, barometric point).The step-down at elevated temperatures of slag slurry can produce steam flash distillation, liquid at least partially (such as, the water) evaporation wherein in slag slurry.Slag slurry is cooled to significantly reduce starch by the temperature of the steam flash distillation occurred during step-down at slag by the disclosed embodiment discussed below.Such as, slag slurry can be cooled to the temperature lower than about 70 DEG C (such as, 160 ℉) by disclosed embodiment.Slag slurry can be cooled when gasifier downstream does not have heat exchanger or water cooler.Slag slurry to be cooled in the upstream of depressurizing system fluid (such as, water) cooling.The gauge that cooling fluid can be greater than or be substantially equal to the gauge of slag slurry is ejected in slag slurry.
Disclosed embodiment is with lasting technique but not batch process transmits slag slurry.As can be appreciated, continue the comparable batch process of technique (such as, lock hopper) and occupy less vertical direction spatial, and comparable batch process has lower cost.In certain embodiments, continue the comparable batch process of technique and use less water.In addition, as discussed in more detail below, the embodiment continuing technique can increase the control of the amount to the water (such as, cooling fluid) in slag slurry relative to batch process.Thus, disclosed embodiment adopts depressurizing system (such as, liquid expansion system), to remove slag slurry constantly and to reduce pressure, also consumes less space simultaneously.In certain embodiments, depressurizing system such as produces power by expansion turbine.Therefore, some embodiment can be described as slag slurry depressurizing system, or is more generally called slag slurry treatment system.
Consider foregoing teachings, Fig. 1 is the schematic diagram of the embodiment of lasting slag removal system 10.As shown in Fig. 1, continue slag removal system 10 and can comprise part oxidizing system (such as gasifier 12), slag slurry 14, depressurizing system 16 (such as, liquid expansion system, one or more expansion turbine, one or more impeller pump, one or more reciprocating apparatus, one or more orifice plate or one or more dump valve) and controller 18.
Part oxidizing system or gasifier 12 can comprise reaction chamber 20, quenching chamber 22 and downstream end portion 62 further.Protective barrier 24 can closed reaction chamber 20, and can be used as physical barrier, heat rejection, chemical barrier or its combination any.The example that can be used for the material of protective barrier 24 includes but not limited to refractory materials, non-metallic material, pottery, the oxide compound of Yi Jige, aluminium, silicon, magnesium, iron, titanium, zirconium and calcium.In addition, the material for the protection of property obstruct 24 can be brick, the refractory materials that can cast, coating, metallic walls or any form that it combines.Substantially, reaction chamber 20 can provide in check environment, to carry out the chemical reaction of partial oxidation.The chemical reaction of partial oxidation can appear at fuel or hydrocarbon when mixing with oxygen in heat release technique and produce gaseous product and by product.Such as, carbon containing feed 26 can be incorporated into reaction chamber 20 together with oxygen 28, to produce untreated synthetic gas 30 and slag 32.Carbon containing feed 26 can comprise the material of such as biofuel or fossil oil, and can be solid, liquid, gas, slurry or any form that it combines.The oxygen 28 being incorporated into reaction chamber 20 can be replaced by air or oxygen-rich air or supplement.In certain embodiments, optional slag slurry reagent 34 also can add reaction chamber 20 to.Slag slurry reagent 34 can be used to the viscosity of slag slurry 14 to remain in suitable scope, and slag slurry 14 thus can be assisted to be carried through lasting slag removal system 10.In other other embodiment, optional negative catalyst 36 (such as, water or steam) also can be incorporated in reaction chamber 20.Chemical reaction in reaction chamber 20 is by making carbon containing feed 26 at the gauge raised (such as, about 2000 to 10000kpa, or 3000 to 8500kpa) and raise temperature (such as, about 1100 DEG C to 1500 DEG C) under experience steam and oxygen realizes, pressure and temperature depends on the type of the gasifier 12 of use.Under these conditions, and depend on the ash composition in carbon containing feed 26, ash can be in melted state, and this is called molten ash or slag 32.
The quenching chamber 22 of part oxidizing system or gasifier 12 can receive untreated synthetic gas 30 and slag 32 when untreated synthetic gas 30 and slag 32 leave reaction chamber 20 by the bottom end 38 (or throat) of protective barrier 24.Untreated synthetic gas 30 and slag 32 enter quenching chamber 22 under high pressure and high-temperature.Substantially, quenching chamber 22 can be used to the temperature reducing untreated synthetic gas 30, and slag 32 is separated with untreated synthetic gas 30, and quenching chamber 22 can be used to make slag 32 quenching, with solidified slag 32 at least in part.In certain embodiments, the quench ring 40 being arranged in bottom end 38 place of protective barrier 24 is configured to quench liquid 42 (such as water) to be supplied to quenching chamber 22.Quench liquid 42 can be conducted through quench inlet 44 and enter quench ring 40 by pipeline 46.Substantially, quench liquid 42 can flow through quench ring 40 and internal surface along dipping tube 47 flows in quenching chamber groove 48 downwards.Controller 18 can control the flow rate of quench liquid 42 by quench inlet 44.Such as, the flow rate of quench liquid 42 can to control between about 4000 to 10000 liters/min (LPM) (such as by controller 18, between about 1050 to 2640 gallon per minute (GPM)), between about 5000 to 9000LPM (such as, between about 1320 to 2375GPM), or between roughly 6000 to 8000LPM (such as, between about 1585 to 2110GPM).
Untreated synthetic gas 30 and slag 32 also can flow through the bottom end 38 of protective barrier 24, and enter in quenching chamber groove 48 along the internal surface of dipping tube 47.When untreated synthetic gas 30 transports through the pond of the quench liquid 42 in quenching chamber groove 48, slag 32 is cured and is separated with synthetic gas, cooled and the quenching of synthetic gas, and synthetic gas leaves quenching chamber 22 subsequently through syngas outlet 50, as shown in arrow 52 go out.Synthetic gas 54 is left by syngas outlet 50, and to process further in gas treating system 56, there, it can process further, to remove sour gas, particle etc., to form treated synthetic gas.Solidification slag 58 can accumulate in the bottom place of quenching chamber groove 48, and can be used as slag slurry 14 and remove from gasifier 12 constantly.In certain embodiments, the part of quench liquid 42 is also removed from quenching chamber groove 48 by Chilling OUT port 60 sustainably, to process.Such as, particle, incrustation, slag and other material can remove from quench liquid 42 in black water treatment system, and treated quench liquid 42 turns back to quenching chamber groove 48 by quench inlet 44.In such embodiments, the quench liquid 42 be removed can have the attribute being similar to slag slurry 14, and thus, liquid expansion system can be used transport and step-down, this liquid expansion system and the depressurizing system 16 starching 14 for slag be separate or shared by depressurizing system 16.
Slag slurry 14 can have the solid of the Multiple components be suspended in quench liquid 42, includes but not limited to, fuel (such as, coal), dry coke, catalyzer, plastics, chemical, mineral and/or other product.The slag slurry 14 entering the downstream end portion 62 of gasifier 12 can have high pressure and high-temperature.Such as, the gauge of slag slurry 14 can between about 1000 to 10000kpa, between 2000 to 9000kpa, or between 3000 to 8000kpa, and the temperature of slag slurry 14 can between about 150 to 350 DEG C (such as, between 300 to 660 ℉), between 200 to 300 DEG C (such as, between 390 to 570 ℉), or between 225 to 275 DEG C (such as, between 435 to 525 ℉) or higher.In certain embodiments, downstream end portion 62 is narrower than quenching chamber 22.
Cooling system 64 controls by one or more nozzle 68 (such as, 1,2,3,4,5,6,7,8,9,10 or more a nozzle) flow entering the cooling fluid 66 of downstream end portion 62.In certain embodiments, cooling system 64 comprises heat exchanger, vapo(u)rization system or refrigeration system, to be cooled between about 10 to 70 DEG C by cooling fluid.Cooling fluid 66 can be in high gauge, it is between about 1000 to 10000kpa, between 2000 to 9000kpa, or between 3000 to 8000kpa, and the flow rate of cooling fluid 66 can between about 1 to 760LPM (such as, between 0.25 to 200GPM), between 100 to 475 LPM (such as, between 26 to 125 GPM), or between 190 to 380 LPM (such as, between 50 to 100 GPM).The flow rate of cooling fluid 66 can lower than about 15% (such as, 3 to 10%) of the flow rate of the quench liquid 42 entered in quenching chamber 22.Such as, the flow rate of quench liquid 42 can be about 75 to 70LPM, the flow rate of cooling fluid 66 can be about 300LPM, slag 58 flow rate of about 75LPM can flow through the downstream end portion 62 of gasifier 12, and slag slurry 14 (such as, cooling fluid 66 and slags 58) flow rate of about 375LPM can flow through downstream end portion 62.The flow rate of slag slurry 14 can be about 2 to 15% of the flow rate of the quench liquid 42 entered in quenching chamber 22.In certain embodiments, the temperature of cooling fluid 66 can between about 10 to 60 DEG C (such as, between 50 to 140 ℉), between 20 to 50 DEG C (such as, between 70 to 125 ℉), or between 30 to 40 DEG C (such as, between 85 to 105 ℉).Cooling fluid 66 can include but not limited to buck, oiler feed, original make up water, condensation product, other current or its combination any.
Cooling fluid 66 is assigned in downstream end portion 62 by cooling system 64, directly to cool the slag slurry 14 of will discharge from gasifier 12.The slag 58 that one or more streams (such as, jet) and the slag of cooling fluid 66 are starched in 14 interacts, thus reduces the temperature of slag slurry 14.At quench liquid 42 cooling syngas 30 with when entering the slag 32 of quenching chamber 22 from reaction chamber 20, cooling fluid 66 mainly cooling slag starches the solidification slag 58 in 14.Cooling system 64 can be integrated and/or be directly connected in the downstream end portion 62 of gasifier 12 with the downstream end portion 62 of gasifier 12.In certain embodiments, the nozzle 68 of cooling system 64 can be arranged between one or more slag grating device 70 and/or upstream, and slag grating device 70 receives the slag slurry 14 from downstream end portion 62.
As can be appreciated, some design continuing slag removal system 10 can comprise starches the water cooler 72 of 14 (such as slag, heat exchanger), and/or cold water 74 can be assigned between gasifier 12 and depressurizing system 16 (such as, one or more bleeder) in slag slurry 14.Slag slurry 14 can be cooled to the temperature lower than about 70 DEG C (such as, about 160 ℉) when the water cooler 72 of not display in the dotted line box 78 in gasifier 12 downstream or water coolant 74 spray by the embodiment of the lasting slag removal system 10 of current imagination.In addition, cooling fluid 66 is direct cooling curing slag 58 and slag slurry 14 in the downstream end portion 62 of gasifier 12, but not indirectly cools, when the water cooler 72 (such as heat exchanger) being such as vaporized device 12 downstream when slag slurry 14 cools.Height and/or the floor space that water cooler 72 can reduce lasting slag removal system 10 is removed from lasting slag removal system 10.In addition, remove water cooler 72 from lasting slag removal system 10 and can reduce operation and/or installation cost.The pipe of water cooler 72 can be easy to gather solid impurity particle, and this can limit slag slurry stream, and/or slag starches the pipe that can wear and tear or corrode in water cooler 72.
Controller 18 can receive the signal from being arranged on lasting slag removal system 10 multiple sensors everywhere.Such as, flow rate sensor 80 measures the flow rate of quench liquid 42, cooling fluid 66 and slag slurry 14.One or more pressure transmitter 82 and/or temperature sensor 83 can provide the information about the temperature of the characteristic of slag slurry 14, the operation conditions continuing slag removal system 10, slag slurry 14, the pressure etc. of slag slurry 14 throughout.In certain embodiments, controller 18 can receive about the extra sensor information of slag slurry 14 when leaving gasifier 12, such as, but not limited to viscosity, granularity etc.In addition, controller 18 can regulate the operation conditions of lasting slag removal system 10 in response to the sensor information received, as being described below in detail.
In certain embodiments, be connected to one or more slag grating devices 70 on slag grating device driving mechanism 84 (such as, steam turbine, depressurizing system 16, motor or other power source) can slag starch 14 be conducted through depressurizing system 16 before receive slag slurry 14 alternatively.One or more slag grating device 70 can roll the solidification slag 58 in grinding residue-pulp 14, to obtain the size-grade distribution of expectation or the mean particle size of expectation in slag slurry 14.One or more slag grating device 70 can be arranged to one or more level, and one or more slag grating device 70 can be one another in series or be arranged in parallel.One or more slag grating device 70 can include but not limited to rotary screw grating device and tooth-shape rotor slag grating device.Set up suitable size-grade distribution to can be used for making slag to starch 14 flowing, to strengthen the effect of cooling system 64, or make expectation flow through depressurizing system 16, or any its combines.In addition, the mean particle size of solid be suspended in the quench liquid 42 of slag slurry 14 and cooling fluid 66 can be reduced to suitable scope by one or more slag grating device 70.In certain embodiments, one or more slag grating device 70 can reduce granularity, make mean particle size between about 0.5 to 26mm (such as, between 0.02 to 1.0 inch), between 2 to 8mm (such as, between 0.08 to 0.31 inch), or between 4 to 6mm (between 0.16 to 0.24 inch).In one embodiment, mean particle size can lower than 2,3,4,5 or 6mm.In certain embodiments, single slag grating device 70 can be enough to set up this mean particle size, and in other embodiments, two or more slag grating devices 70 can concur (such as, series connection and/or parallel connection), to set up this mean particle size.Such as, the first slag grating device can starch 14 to slag provides roughing broken, and the second slag grating device can starch 14 grating providing thinner to slag.In one embodiment, controller 18 controls slag grating device 70 by controlling slag grating device motor 84.Controller 18 can regulate slag grating device motor 84 based on the information being received from other sensor.In certain embodiments, flowrate control valve 86 can be arranged on slag grating device 70 downstream, to regulate the flow rate of the slag slurry 14 flowing to liquid expansion system 16.In one embodiment, controller 18 can receive the information of the flow rate about slag slurry 14 from flow rate sensor 80.In response to the information that flow sensor 80 receives, controller 18 controls the flow rate of slag slurry 14 by adjust flux control valve 86.In other embodiments, controller 18 can regulate slag to starch the flow rate of 14 based on the signal from other sensor 82,83.
Slag slurry 14 can be fed in depressurizing system 16, to reduce the pressure of slag slurry 14.In certain embodiments, depressurizing system 16 is turbine or decompressor, such as, but not limited to, the impeller pump of expansion turbine, positive displacement meter amount (posimetric) pump, rotary screw pump, improvement, reciprocating apparatus, metering hole, dump valve or its combination any.Pressure transmitter " P2 " 82 can provide the information of the pressure about the slag slurry 14 leaving depressurizing system 16.In certain embodiments, depressurizing system 16 (such as, turbine) can produce power (such as, driving generator), makes slag slurry 14 from the pressure step-down of pressure transmitter " P1 " 82 simultaneously.Such as, the first gauge of the slag slurry 14 of the first pressure transmitter " P1 " 82 measurement between about 1000 to 10000kpa, between 2000 to 9000kpa, or between 3000 to 8000kpa, or can be roughly the high operating pressure of gasifier 12.On the contrary, the second gauge of slag indicated by the second pressure transmitter " P2 " 82 slurry 14 can between barometric point (0kpa) to 100kpa, between 20 to 80kpa, or between 40 to 60kpa.In certain embodiments, the second pressure is substantially equal to barometric point.After leaving depressurizing system 16, slag slurry 14 can enter slag disposal system 88 to downstream further, such as to dewater to slag slurry 14 before disposal slag slurry 14.
Fig. 2 illustrates the embodiment of the downstream end portion 62 of gasifier 12 and the embodiment of cooling system 64.Slag 58 through quenching and solidification can be deposited to downstream end portion 62 from quenching chamber 22.In downstream end portion 62, solidification slag 58 forms slag with quench liquid 42 and cooling fluid 66 and starches 14.Cooling system 64 can have one or more set of nozzles 100 (such as, 1,2,3,4,5,6,7,8,9,10 or more) with by cooling fluid 66 (such as, water) be assigned in downstream end portion 62, and each set of nozzles 100 can have one or more nozzle 68 (such as, 1,2,3,4,5,6,7,8,9,10 or more).Such as, first jet group 102 can have 2 nozzles 68, and second nozzle group 104 and the 3rd set of nozzles 106 can have 4 nozzles 68 separately.
Fig. 3 illustrates the cross-sectional view obtained along the line 3-3 of Fig. 2 of the embodiment of first jet group 102.The nozzle 68 of each set of nozzles 100 can extend through the wall 108 of the downstream end portion 62 of gasifier 12.Each nozzle 68 can, towards the center 110 of downstream end portion 62, along the first tangential direction 112 or along the second tangential direction 114, or combine directed with any its.Such as, first jet 116 can be directed towards center 110, and second nozzle 118 can be directed along the first tangential direction 112.In certain embodiments, one or more nozzles 68 of set of nozzles 100 extend to center 110 by wall 108, and can be radially 120 directed towards wall 108 from center 110, to cause counterclockwise swirl, and the 3rd nozzle 116 can be directed along the second tangential direction 114, to cause clockwise whirlpool.Each in one or more nozzle 68 can penetrate the jet of stream of slag slurry 14 or the mode of stream distributes cooling fluid 66, thus makes that cooling fluid 66 can directly the slag 58 starched in 14 interacts and contacts with slag.In certain embodiments, cooling fluid 66 can be assigned in slag slurry 14 as stream (such as, jet), sheet (such as, vertical sheet, horizontal plate, oblique plate) or cone or its combination any by one or more nozzle 68.
The one or more set of nozzles 100 described in Fig. 2 and 3 can have one or more nozzles 68 of multiple layout.In certain embodiments, the layout of the nozzle 68 in each set of nozzles 100 can around center 110 Rotational Symmetry, thus make cooling system 64 slag can be starched 14 to be cooled to basic uniform temperature (such as, lower than about 50 to 95 DEG C, lower than about 60 to 80 DEG C, or lower than about 70 DEG C).Such as, second nozzle 118 can with first jet 116 spaced apart about 180 °, as shown in Fig. 3.As can be appreciated, be used for herein describe nozzle 68 layout term " approximately " can 10 ° or less in.Other layout of one or more set of nozzles 100 can include but not limited to nozzle 68 be spaced apart from each other about 90 ° (such as, first jet 116, the 3rd nozzle 120, second nozzle 118, the 4th nozzle 122) or about 60 ° (such as, 4th nozzle 122, the 5th nozzle 124 and the 6th nozzle 126) layout, as shown in Fig. 3.In certain embodiments, multiple set of nozzles 100 can be arranged on wall 108, and nozzle 68 is circumferentially offseted around center 110, makes nozzle 68 can distribute cooling fluid 66, to cool the distinct portions of slag slurry 14.Such as, first jet group 102 can have four nozzles 68, and they are spaced apart from each other about 90 ° from 1: 128, and second group 104 can have four nozzles 68, and they are spaced apart from each other about 90 ° from second point 130.
With reference to Fig. 2, cooling fluid 66 (such as, water) distributes by each set of nozzles 100 (such as, spraying) in downstream end portion 62.Cooling fluid 66 can higher gauge (such as, between about 1000 to 10000kpa) distribute, its higher than or be substantially equal to (such as, 10% or less in) slag slurry 14 gauge, thus make cooling fluid 66 can easily flow to slag slurry 14 in.In certain embodiments, substantially all (such as, being greater than 75%) cooling fluids 66 can cool slag slurry 14, and flow through the outlet 132 of downstream end portion 62, but not by syngas outlet 50 or quench liquid outlet 60.Therefore, cooling fluid 66 mainly cools the slag slurry 14 in quenching chamber 22 downstream.
In certain embodiments, downstream end portion 62 can comprise one or more slag grating device 70, to set up the mean particle size of expectation.As above discuss, the first slag grating device 134 can starch 14 to slag provides roughing broken, and the second slag grating device 136 can starch 14 grating providing thinner to slag.Each slag grating device 70 can comprise one or more element 138, and to roll the solidification slag 58 in grinding residue-pulp 14, but other type slag grating device can be used alone or combines use with the slag grating device 70 with element 138.In addition, or in the alternatives of one or more slag grating devices 70 of downstream end portion 62, some embodiments can be included in one or more slag grating devices 70 in outlet 132 downstream.
One or more set of nozzles 100 can be arranged between one or more slag grating devices 70 of downstream end portion 62.In certain embodiments, set of nozzles 100 (such as, second nozzle group 104) is arranged between the first and second slag grating devices 134,136.In addition or in alternatives, set of nozzles 100 (such as, first jet group 102) can be arranged in slag grating device 70 upstream, and/or set of nozzles 100 (such as, the 3rd set of nozzles 106) can be arranged in slag grating device 70 downstream.Cooling system 64 can comprise one or more flowrate control valve and/or manifold, with the distribution of controlled cooling model fluid to one or more set of nozzles 100.Cooling system 64 differently can control the flow of the cooling fluid 66 leading to each set of nozzles 100.Such as, more cooling fluid 66 can be directed to second or the 3rd set of nozzles 104,106 by cooling system 64, less cooling fluid 66 is directed to first jet group 102 simultaneously.In certain embodiments, cooling system 64 differently can control the flow of the cooling fluid 66 of each nozzle 68 leading to corresponding set of nozzles 100.Such as, more cooling fluid 66 can be directed to the nozzle 68 near the warm component of lasting slag removal system 10 by cooling system 64, and less cooling fluid 66 is directed to the nozzle 68 near colder surroundings outside.
In certain embodiments, depressurizing system 16 can comprise one or more bleeder, and it includes but not limited to one or more orifice plate 140, one or more dump valve 142, one or more expansion turbine 144 or one or more acting in opposition impeller pump or its combination any.One or more bleeder can starch 14 step-downs based on the granularity of solidification slag 58 in the flow rate of slag slurry 14 and/or slag slurry 14 to slag at least in part.Such as, one or more orifice plate 140 and/or one or more dump valve 142 can make slag starch 14 at slag slurry 14 with the first flow rate (such as, about 380LPM) amount larger than the step-down when slag slurry 14 flows with the second flow rate (such as, about 300LPM) reduced when flowing.Therefore, controller 18 can control the flow rate of slag slurry 14, to control the step-down of slag slurry 14.In certain embodiments, controller 18 is by controlling the flow rate controlling slag slurry 14 from the flow rate of the cooling fluid 66 of cooling system 64.Such as, the flow rate increasing cooling fluid 66 can increase the flow rate of slag slurry 14 and increase the pressure drop striding across depressurizing system 16.On the contrary, the flow rate reducing cooling fluid 66 can reduce the flow rate of slag slurry 14 and reduce the pressure drop striding across depressurizing system 16.The flow rate of controlled cooling model fluid 66 can make controller 18 can apply precise controlling to the flow rate that slag starch 14, and any minimum flow rate controlled about the flow rate of quench liquid 42 to meet depressurizing system 16 specifies.Such as, regulate the flow rate of cooling fluid 66 to reach about 10% (such as, from 380LPM to 340LPM) and about 10% (such as, from 7570 to 6800LPM) can be reached lower than regulating the flow rate of quench liquid 42 to the impact of the flow rate of slag slurry 14.In addition, or in alternatives, controller 18 controls the flow rate of slag slurry 14 by direct control flow check control valve 86.
Cooling system 64 can be made can to adapt to the flow rate regulation of depressurizing system 16 by controlling to regulate flow rate slag to starch 14 from the flow rate of the cooling fluid 66 of cooling system 64, and between downstream end portion 62 and depressurizing system 16, not add fluid.In certain embodiments, controller 18 can at least in part based on the pressure transmitter 82 in the downstream from depressurizing system 16 feedback and control the slag slurry flow rate of the 14 and/or flow rate of cooling fluid 66.Controller 18 also can be starched the temperature of 14 based on slag at least in part and control the slag slurry flow rate of 14 and/or the flow rate of cooling fluid 66.Such as, controller 18 can control slag slurry 14 and/or the flow rate of cooling fluid 66, to be cooled to lower than about 50 to 95 DEG C by slag slurry, lower than about 60 to 80 DEG C, or lower than the temperature of about 70 DEG C.As can be appreciated, the treater 146 of controller 18 can perform the instruction (such as, code) be stored in the storer 148 of controller 18, starches the flow rate of 14 with the flow rate of controlled cooling model fluid 66 and/or slag.Therefore, the cooling system 64 be connected in downstream end portion 62 can reduce slag slurry 14 from gasifier 12 to the complicacy of the flow path of depressurizing system 16.Thus, cooling fluid 66 can be used to the flow rate cooling slag slurry 14 and control slag slurry 14, to starch 14 step-downs to slag fully, and does not have steam flash distillation.
Fig. 4 is the schema of the technique 180 illustrated for processing slag slurry 14 constantly.In certain embodiments, technique 180 is reacted (frame 182) time at carbonaceous fuel and is started in gasifier 12.As described above, carbonaceous fuel can react with oxygenant and optionally extra water.In gasifier 12 during reaction, quench liquid is added to the quenching chamber 22 in (frame 184) gasifier 12 by lasting slag removal system 10 with the first flow rate, and makes reaction product (such as gaseous product and slag by product) quenching (frame 186).Then gasifier 12 is separated (frame 188) gas and slag, and by gas transmission (frame 190) to gas treating system.As described above, continue cooling fluid is added to (frame 192) gasifier 12 by slag removal system 10 downstream end portion 62 with the second flow rate, thus cool (frame 194) slag and form (frame 196) slag slurry.Slag slurry can be cooled to lower than about 50 to 95 DEG C, lower than about 60 to 80 DEG C, or lower than about 70 DEG C.In certain embodiments, one or more slag grating device 70 can grating slag and form slag slurry, and slag slurry can comprise the quench liquid of slag, the cooling fluid of first part and the interpolation of second section.In certain embodiments, the second flow rate of cooling fluid can be the first flow rate of quench liquid about 2 to 15% between, between about 3 to 10%, or between about 3 to 7%.Continue slag removal system 10 and slag slurry is transmitted (frame 198) to depressurizing system 16 with the 3rd flow rate, depressurizing system 16 makes slag starch step-down (frame 200).3rd flow rate is at least in part based on the second flow rate.Continue slag removal system 10 and can control the 3rd flow rate, to make slag starch step-down (frame 200) to the pressure expected, such as about barometric point.
Technique effect of the present invention comprises realization and continues slag removal system, and between the downstream end portion and depressurizing system of gasifier, does not add water cooler and/or water.Cooling system distributes the cooling fluid of high gauge, with in the downstream end portion of gasifier by slag slurry be reduced to lower than about 50 to 95 DEG C (such as, 120 to 200 ℉), lower than about 60 to 80 DEG C (such as, 140 to 175 ℉), or lower than about 70 DEG C (such as, 160 ℉), thus be reduced in the possibility of the steam flash distillation in depressurizing system.Except cooling slag slurry, cooling fluid can be used to the flow rate controlling to starch towards the slag of depressurizing system.The pressure drop striding across depressurizing system can at least in part based on the flow rate that the slag by depressurizing system is starched.Therefore, the flow rate being controlled slag slurry by the flow rate of controlled cooling model fluid can control to stride across the pressure drop of depressurizing system.
This written description uses the open the present invention of example, comprises optimal mode, and enables any person skilled in the art put into practice the present invention, comprise and manufacture and use any device or system, and carry out the method for any combination.Patentable scope of the present invention is defined by the claims, and can comprise other example that those skilled in the art expect.If other such example has the textural element of the literal language not differing from claim, if or they comprise and the equivalent structural elements of the literal language of claim without substantial differences, then within the scope that they are intended to be in claim.
Claims (10)
1. a system, comprising:
Quenching chamber, it is configured to the mixture of receiver gases and slag constantly, and wherein said quenching chamber comprises quench tank, and it is configured by quench liquid and is separated gas in described mixture and slag constantly; And
Downstream end portion, it is connected on described quenching chamber, wherein said downstream end portion is configured to constantly slag slurry is transferred to depressurizing system, described downstream end portion comprises cooling system, it is configured to utilize cooling fluid directly to cool described slag slurry, and described slag slurry comprises isolated slag and cooling fluid at least partially.
2. system according to claim 1, is characterized in that, comprises one or more slag grating device, and it is configured to receive described slag slurry.
3. system according to claim 2, is characterized in that, described cooling system is at least partially disposed between the first slag grating device in described one or more slag grating device and the second slag grating device in described one or more slag grating device.
4. system according to claim 2, is characterized in that, described cooling system is at least partially disposed on described one or more slag grating device upstream.
5. system according to claim 1, is characterized in that, comprises the slag grating device be connected in described downstream end portion.
6. system according to claim 1, is characterized in that, comprises reactor, and it is connected on described quenching chamber, and wherein said reactor structure becomes to make carbon containing feed react and produce gas and slag.
7. system according to claim 1, is characterized in that, described cooling system comprises one or more nozzle, and it is configured to directly be assigned to by described cooling fluid in described slag slurry.
8. system according to claim 1, it is characterized in that, described cooling system comprises multiple set of nozzles, it is configured to distribute described cooling fluid, wherein each set of nozzles comprises one or more nozzle, and each in described one or more nozzle be configured to from another the different angle in described one or more nozzle of corresponding set of nozzles, from another the different axial positions in described one or more nozzle of corresponding set of nozzles, described cooling fluid is being distributed from another the different circumferential position in described one or more nozzle of corresponding set of nozzles or in any mode that it combines.
9. system according to claim 1, is characterized in that, described cooling system is configured to described slag to be cooled to lower than about 70 DEG C.
10. a system, comprising:
Gasifier, it is configured to make carbon containing feed be reacted into the mixture of gas and slag, and wherein said gasifier comprises:
Quench tank, it is configured by quench liquid and is separated gas in described mixture and slag constantly, and wherein said quench liquid is configured to flow through described quench tank with the first flow rate; And
The downstream end portion of described gasifier comprises cooling system, wherein said downstream end portion is configured to constantly slag slurry is transferred to depressurizing system with the 3rd flow rate, described 3rd flow rate is about 15% or less of described first flow rate, described downstream end portion is configured to add cooling fluid to cool described slag slurry with the second flow rate, and described slag slurry comprises described slag and described cooling fluid; And
Controller, it is configured to control described second flow rate.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US14/103,714 US20150159097A1 (en) | 2013-12-11 | 2013-12-11 | System and method for continuous slag handling with direct cooling |
| US14/103714 | 2013-12-11 |
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| Publication Number | Publication Date |
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| CN104711040A true CN104711040A (en) | 2015-06-17 |
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| CN201410755219.2A Pending CN104711040A (en) | 2013-12-11 | 2014-12-11 | System and method for continuous slag handling with direct cooling |
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| US (1) | US20150159097A1 (en) |
| KR (1) | KR20150068318A (en) |
| CN (1) | CN104711040A (en) |
| AU (1) | AU2014271262A1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US10018416B2 (en) | 2012-12-04 | 2018-07-10 | General Electric Company | System and method for removal of liquid from a solids flow |
| US9228747B2 (en) * | 2013-03-12 | 2016-01-05 | Pratt & Whitney Canada Corp. | Combustor for gas turbine engine |
| US9784121B2 (en) | 2013-12-11 | 2017-10-10 | General Electric Company | System and method for continuous solids slurry depressurization |
| US9464244B2 (en) * | 2014-02-26 | 2016-10-11 | General Electric Company | System and method for black water removal |
| KR20200022423A (en) * | 2017-07-24 | 2020-03-03 | 페스툴 게엠베하 | Method for identifying power tools and their events and / or states |
| CN108676584B (en) * | 2018-06-19 | 2024-01-09 | 中国矿业大学 | Coal tar removal device and method based on paddle bed coupling |
| KR102564464B1 (en) * | 2021-11-19 | 2023-08-09 | 한국에너지기술연구원 | Gasfication system for preventing overheating of gasfier |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1122443A (en) * | 1994-06-27 | 1996-05-15 | 德士古发展公司 | Slag handling system |
| CN101945978A (en) * | 2008-02-13 | 2011-01-12 | 通用电气公司 | Be used to cool off and wash the device and the assembly method of synthetic air |
| PL404251A1 (en) * | 2012-06-07 | 2013-12-09 | Gen Electric | System and method for handling the sludge |
Family Cites Families (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3971639A (en) * | 1974-12-23 | 1976-07-27 | Gulf Oil Corporation | Fluid bed coal gasification |
| US4979964A (en) * | 1989-06-22 | 1990-12-25 | Shell Oil Company | Apparatus for preventing slag tap blockage |
| WO1994016038A1 (en) * | 1992-12-30 | 1994-07-21 | Combustion Engineering, Inc. | Circular slag tap for a gasifier |
| US5554202A (en) * | 1993-09-02 | 1996-09-10 | Texaco Inc. | Gasifier monitoring apparatus |
| US5647876A (en) * | 1995-09-26 | 1997-07-15 | Texaco Inc. | Method of removing volatile metals from slag using an acid wash |
| US20060165582A1 (en) * | 2005-01-27 | 2006-07-27 | Brooker Donald D | Production of synthesis gas |
| DE202006020602U1 (en) * | 2006-08-28 | 2009-04-23 | Siemens Aktiengesellschaft | Apparatus for discharging slag from gasification reactors |
| US20100325954A1 (en) * | 2009-06-30 | 2010-12-30 | General Electric Company | Quench chamber assembly for a gasifier |
| DE102009034870A1 (en) * | 2009-07-27 | 2011-02-03 | Uhde Gmbh | Gasification reactor for the production of CO or H2-containing raw gas |
| DE102010062769B4 (en) * | 2010-12-09 | 2017-02-23 | Siemens Aktiengesellschaft | Soot water purification by means of continuous pressure filtration |
| DE102011088628B4 (en) * | 2011-12-14 | 2015-11-05 | Technische Universität Bergakademie Freiberg | Method and apparatus for entrained flow gasification of solid fuels under pressure |
| US9410097B2 (en) * | 2013-03-15 | 2016-08-09 | General Electric Company | Methods and systems of producing a particulate free, cooled syngas product |
-
2013
- 2013-12-11 US US14/103,714 patent/US20150159097A1/en not_active Abandoned
-
2014
- 2014-12-03 AU AU2014271262A patent/AU2014271262A1/en not_active Abandoned
- 2014-12-10 KR KR1020140177295A patent/KR20150068318A/en not_active Application Discontinuation
- 2014-12-11 CN CN201410755219.2A patent/CN104711040A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1122443A (en) * | 1994-06-27 | 1996-05-15 | 德士古发展公司 | Slag handling system |
| CN101945978A (en) * | 2008-02-13 | 2011-01-12 | 通用电气公司 | Be used to cool off and wash the device and the assembly method of synthetic air |
| PL404251A1 (en) * | 2012-06-07 | 2013-12-09 | Gen Electric | System and method for handling the sludge |
Non-Patent Citations (1)
| Title |
|---|
| 吴德荣主编: "《化工装置工艺设计 下》", 31 August 2014, 华东理工大学出版社 * |
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| AU2014271262A1 (en) | 2015-06-25 |
| US20150159097A1 (en) | 2015-06-11 |
| KR20150068318A (en) | 2015-06-19 |
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