WO2010057919A1 - Vorrichtung zur erzeugung von brennbarem produktgas aus kohlenstoffhaltigen einsatzstoffen - Google Patents
Vorrichtung zur erzeugung von brennbarem produktgas aus kohlenstoffhaltigen einsatzstoffen Download PDFInfo
- Publication number
- WO2010057919A1 WO2010057919A1 PCT/EP2009/065389 EP2009065389W WO2010057919A1 WO 2010057919 A1 WO2010057919 A1 WO 2010057919A1 EP 2009065389 W EP2009065389 W EP 2009065389W WO 2010057919 A1 WO2010057919 A1 WO 2010057919A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- heat
- heat pipe
- transfer medium
- loop
- liquid
- Prior art date
Links
- 238000012546 transfer Methods 0.000 claims abstract description 70
- 239000007788 liquid Substances 0.000 claims abstract description 58
- 238000002485 combustion reaction Methods 0.000 claims abstract description 35
- 238000002309 gasification Methods 0.000 claims abstract description 21
- 229910052739 hydrogen Inorganic materials 0.000 claims description 27
- 239000001257 hydrogen Substances 0.000 claims description 27
- 238000000926 separation method Methods 0.000 claims description 17
- 239000007789 gas Substances 0.000 claims description 16
- 238000000197 pyrolysis Methods 0.000 claims description 8
- 241001124144 Dermaptera Species 0.000 claims 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 1
- 239000000446 fuel Substances 0.000 abstract description 11
- 239000012530 fluid Substances 0.000 abstract description 8
- 238000010276 construction Methods 0.000 abstract description 4
- 238000007789 sealing Methods 0.000 abstract description 2
- 150000002431 hydrogen Chemical class 0.000 description 16
- 238000007872 degassing Methods 0.000 description 14
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 10
- 239000003990 capacitor Substances 0.000 description 9
- 239000011261 inert gas Substances 0.000 description 9
- 229910052783 alkali metal Inorganic materials 0.000 description 7
- 150000001340 alkali metals Chemical class 0.000 description 7
- 238000013461 design Methods 0.000 description 5
- 238000007654 immersion Methods 0.000 description 5
- 238000011049 filling Methods 0.000 description 4
- 238000009825 accumulation Methods 0.000 description 3
- 230000035508 accumulation Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 229910000574 NaK Inorganic materials 0.000 description 2
- 229910045601 alloy Inorganic materials 0.000 description 2
- 239000000956 alloy Substances 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 239000013529 heat transfer fluid Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910052700 potassium Inorganic materials 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 230000008023 solidification Effects 0.000 description 2
- 239000006200 vaporizer Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 230000003313 weakening effect Effects 0.000 description 2
- 229920002943 EPDM rubber Polymers 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 229910001854 alkali hydroxide Inorganic materials 0.000 description 1
- 150000008044 alkali metal hydroxides Chemical class 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000004020 conductor Substances 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 230000002706 hydrostatic effect Effects 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 238000007726 management method Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000035515 penetration Effects 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 230000035945 sensitivity Effects 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000013517 stratification Methods 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D15/00—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies
- F28D15/02—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes
- F28D15/0266—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes with separate evaporating and condensing chambers connected by at least one conduit; Loop-type heat pipes; with multiple or common evaporating or condensing chambers
-
- 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
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/06—Continuous processes
- C10J3/10—Continuous processes using external heating
-
- 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
- C10J3/482—Gasifiers with stationary fluidised bed
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D15/00—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies
- F28D15/02—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes
- F28D15/04—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes with tubes having a capillary structure
- F28D15/043—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes with tubes having a capillary structure forming loops, e.g. capillary pumped loops
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/12—Heating the gasifier
- C10J2300/1246—Heating the gasifier by external or indirect heating
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
- C10J2300/1606—Combustion processes
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
- C10J2300/1637—Char combustion
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1853—Steam reforming, i.e. injection of steam only
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1861—Heat exchange between at least two process streams
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1861—Heat exchange between at least two process streams
- C10J2300/1892—Heat exchange between at least two process streams with one stream being water/steam
Definitions
- the invention relates to a device for producing combustible product gas from carbonaceous feedstocks by allothermic steam gasification according to the preamble of claim 1.
- the pressure-charged allothermal steam gasification of carbonaceous fuels requires heat input into the gasification chamber at a temperature level of about 800-900 ° C.
- heat pipe reformer as known from EP 1 187 892 B1 fuel gas is produced from the carbonaceous feedstocks to be gasified by allothermic steam gasification in a pressure-charged fluidized-bed gasification chamber. The necessary heat is passed from a fluidized bed by means of a skilletleitrohranssen in the carburetor or reformer. Due to the straight and tubular construction of heat pipes are in the known from EP 1 187 892 B1 heat pipe reformer combustion chamber and
- Reformer / gasification chamber arranged one above the other.
- the pressure vessel bottom is exposed to special loads due to the high temperatures in the combustion chamber.
- the soil is weakened by a large number of heat pipe penetrations.
- the sealing of the bushings is also a problem.
- both the line for liquid heat transfer medium and for vaporous heat transfer medium in the common tube shell is arranged.
- the number of feedthroughs can be reduced to two, namely a liquid line and a steam line. If a plurality of such loop heat pipes is used, their separate running steam and liquid lines can be summarized in the carburetor pressure vessel to a common vapor or liquid line, which then enforce the gasification pressure vessel. Outside the carburetor pressure vessel then the two common lines can be split again.
- the number of feedthroughs from or into the carburetor pressure vessel can be significantly reduced to a minimum of two.
- claims 3 and 4 relate to different designs for loop heat pipes with separate running steam and liquid line.
- Heat transfer from the external heat source to the gasifier through two physically separate series-connected heat transfer circuits can be optimized with regard to the heat absorption in the heat source, while the second heat carrier circuit or the associated heat pipe can be optimized in terms of heat dissipation in the gasifier.
- the pyrolysis residues are thermally utilized from the gasifier and on the other hand, the complete fuel supply into the fluidized bed combustion chamber can take place. An additional supply of fuel in the fluidized bed combustion chamber, with the exception of the startup is no longer necessary.
- alkali metals and their alloys eg. B. Na, K, NaK, as a heat transfer medium in the loop heat pipes.
- Fig. 1 shows the basic structure of a high-temperature reformer according to the present invention
- FIG. 2 shows a schematic illustration of a first embodiment of the invention in the high-temperature reformer
- FIG 3 shows a first embodiment of the high-temperature heat transfer circuit in the high-temperature reformer in the form of a loop heat pipe pulsed by capillary structure, CPL;
- FIG. 4 shows a second embodiment of the high-temperature heat transfer circuit in the form of a loop heat pipe, LHP;
- Fig. 5 is the pressure-temperature state diagram for the LHP of Fig. 4;
- FIG. 6 shows a second embodiment of the high-temperature reformer according to the present invention with two physically separate heat transfer fluid circuits
- FIG. 7 shows a pulsed loop heat pipe, CLPHP, as used in the high-temperature reformer of FIG. 7 as the second heat carrier circuit;
- Fig. 10 shows a third embodiment of the high-temperature heat transfer circuit in the form of submerged loop heat pipes.
- Fig. 1 shows the basic structure of a high-end reforming according to the present invention.
- the high-temperature refomer comprises a pressurized carburetor or reformer 2 and an external heat source in the form of a combustion chamber 4.
- the carburetor 2 comprises a carburetor pressure vessel 6, a fuel supply 8, a water supply 10 and a product gas discharge 12 at one temperature from 800 ° C to 900 ° C is produced by allothermic steam gasification of carbonaceous fuels in a known manner product gas.
- the carburetor 2 and the external heat source 4 are connected to each other via a heat carrier circuit or a loop heat pipe 14.
- the heat carrier circuit or the loop heat pipe 14 comprise a heat receiving side 16 and a heat-emitting side 18, which are connected to each other via a steam line 20 for vaporous heat transfer medium and a liquid line 22 for liquid heat transfer medium.
- a lock 24 of the carburetor 2 is connected to the heat source 4.
- About the lock 24 pyrolysis residues from the carburetor 2 of the combustion chamber 4 are supplied as fuel.
- the combustion chamber 4 still has an air supply 26 and a flue gas outlet 28.
- a hydrogen separation device 30 is arranged in the liquid line 22 between the carburetor 2 and the combustion chamber 4.
- the hydrogen separation device 30 By the hydrogen separation device 30, the hydrogen and other foreign matter is separated from the liquid heat transfer medium and the remaining liquid heat transfer medium is fed back to the combustion chamber 4, so that the heat carrier circuit is closed. Due to the high temperatures alkali metals or alloys thereof, z. As Na, K or NaK used.
- Fig. 2 shows schematically a first, concrete embodiment of the invention, wherein for components corresponding to each other, the same reference numerals are used.
- the combustion chamber 4 is a fluidized bed combustion chamber with circulating fluidized bed 32.
- the combustion chamber 4 comprises a riser 34, a cyclone 36 and a lock 38 and a fluidized bed 40, which lead back into the riser 34.
- the heat receiving side 16 of the loop heat pipe 14 comprises a first and a second shell and tube heat exchangers 42 and 44, which are connected in series and in which the liquid heat transfer medium is vaporized by absorbing heat.
- the heat-emitting side 18 includes a third shell-and-tube heat exchanger 46 in which the vaporous heat exchange medium is recondensed by release of the previously received heat.
- the combustion chamber 4 in comparison to the so-called heat pipe reformer according to EP 1 187 892 B1 no restriction in the design and operation.
- all design and operational parameters can be optimally adapted to the requirements of high-temperature heat supply.
- the use of the circulating fluidized bed 32 has the advantage of optimum combustion in riser 34 and optimum and material-conserving heat extraction from the fluidized bed 40 - first shell and tube heat exchanger 42 - and membrane walls - second shell and tube heat exchanger 44 - in the turbulent bottom zone of the riser 34 detailed construction of the circulating fluidized bed combustion chamber 4 is referred to "Handbook of Fluxation and Fluid Particle Systems", by Wen-Ching Yang, ISBN: 0-8247-0259-X.
- the reformer or carburetor 2 can be designed without restrictions with respect to the combustion chamber 4, since combustion chamber 4 and carburetor 2 are not arranged as in the heat pipe reformer in a common container.
- the implementation of the high-temperature steam and liquid line 20, 22 is moved to structurally favorable locations carburetor pressure vessel 6.
- the liquid line 22 and the steam line 20 are guided laterally from the barrel-shaped carburetor 2.
- Cover and bottom of the carburetor pressure vessel 6 are free of the large number of heat pipe feedthroughs, as they are known from the heat pipe reformer. There are only weakenings through the steam supply 10 and the fuel supply 8, as well as product gas discharge 12 and lock 24 for discharging pyrolysis residues.
- the reaction temperature in the gasifier can be substantially higher than the temperatures on the wall of the carburetor pressure vessel. As a result, stable constructions are achieved even when using less expensive materials with smaller wall thicknesses.
- the pyrolysis residues of the carburettor 2 can be utilized directly in the combustion chamber 4 via the lock 24. With favorable process control, the pyrolysis residues are sufficient to cover the fuel requirement of the combustion chamber 4. Product gas leakage flows through the lock 24 can be safely and completely burned in the combustion chamber 4.
- the CPL 500 includes a heat receiving side or evaporator 516 and a heat releasing side and a condenser 518, respectively.
- Vaporizer 516 and condenser 518 are interconnected through a vaporous vapor vapor manifold 520 and a liquid heat transfer medium liquid manifold 522. Steam manifold 520 and liquid manifold 522 are spaced apart from each other.
- Both the evaporator 516 and the condenser 518 consist of a plurality of identical evaporator 524 or condenser elements 526 connected in parallel.
- the evaporator elements 524 have a capillary structure 528 through which the liquid heat transfer medium is vaporized by absorbing heat.
- the Capacitor elements 526 recombine the heat transfer medium while releasing heat.
- the liquid manifold 522 is connected to a surge tank 532 via a surge line 530.
- the expansion tank 532 ensures a steady level in the liquid collecting line 522.
- the liquid flows back into the liquid collecting line 522 due to a small temperature gradient and thus also a pressure gradient.
- the evaporation enthalpy recorded in the evaporator 516 (combustion chamber 4) is thus released again in the condenser 518 (carburettor 2).
- the hydrogen separation device 522 is integrated into the liquid collection line 522 (not shown in FIG. 3).
- the LHP 600 includes a heat receiving side or evaporator 616 and a heat releasing side and a condenser 618, respectively.
- Vaporizer 616 and condenser 618 are connected to each other via a steam line 620 for vaporous heat transfer medium and a liquid line 622 for liquid heat transfer medium. Steam line 620 and liquid line 622 are spaced apart from each other.
- a capillary structure 628 is arranged, is vaporized by the liquid heat transfer medium by absorbing heat.
- the condenser 618 the heat transfer medium condenses again with the release of heat.
- Fig. 5 - is the heat transfer medium in the liquid-vapor equilibrium (fd-GGW) and is overheated in state 2 in the evaporator 616. From state 2 to 3, the pressure drops due to flow losses. Condition 3 via 4 to 5 shows the complete condensation incl. Subcooling of the condensate (condition 5). In state 6, the heat transfer medium is in the upper region of the evaporator 616 and is heated by the evaporator 616 to state 7 (fd- GGW) and then overheated to the temperature 8 in the lower region of the evaporator 616.
- fd- GGW liquid-vapor equilibrium
- the capillary pressure differential in the capillary structure 628 be greater than the sum of the pressure losses from the vapor and liquid flow, the capillary structure 628, and the hydrostatic pressure. Ie. it must apply:
- Such a loop heat pipe is also known from WO / 2003/054469.
- the high-temperature heat transfer circuit 700 comprises a primary heat transfer circuit 701 and a secondary heat transfer circuit 702.
- the primary heat transfer circuit 701 comprises a heat-receiving side 716 and a heat-emitting side 718.
- the heat-receiving side 716 and the heat-emitting side 718 are connected to each other via a steam line 720 for vaporous heat transfer medium and via a liquid line 722 for liquid heat transfer medium.
- Steam line 720 and liquid line 722 are spatially separated.
- the heat releasing side 716 is disposed in the combustion chamber and the heat releasing side 718 is disposed in the carburetor.
- the primary heat carrier circuit 701 can be realized by the loop heat pipes 500 and / or 600 in FIGS. 3 and 4.
- the secondary heat carrier circuit 702 is replaced by a pulsed loop
- the CLPHP 702 has a heat receiving side 736 and a heat releasing side 738.
- the heat receiving side 736 and the heat releasing side 738 are interconnected via a closed meandering vapor / liquid conduit 740.
- Both the heat releasing side 736 and the heat releasing side of the CLPHP 702 are disposed in the gas pressure vessel 706.
- the heat receiving side 736 of the CLPHP 702 is integrated into the heat-emitting side 718 of the primary heat transfer circuit 701.
- the heat transfer medium is alternately via the steam / liquid line 740 from the evaporator 736 in the
- Conductor 738 passed.
- a temperature difference creates a pressure difference that causes the whole system to pulsate. This makes it possible to transport off hydrogen cushions and other inert gases convective and at a suitable location, eg. B. at the top of the condenser 738 via a degassing 730 deduct.
- An advantage of the double heat carrier circuit is that can escape through the decoupling of the pulsating secondary heat transfer medium from the combustion chamber 4 in case of leaks less heat transfer medium.
- inert gas can be present in the alkali-liquid-steam cycle. During operation, hydrogen diffuses into the circuit.
- CPL, LHP, 7-9 the circulatory system
- inert gas accumulations in pipe bends lead to the interruption of the flow and thus to the interruption of the heat transfer.
- a local overheating in the evaporator section could be the result.
- the degassing device or hydrogen separation device 30 for an alkali metal liquid-steam cycle must therefore fulfill the following boundary conditions:
- the media wetted valves must be resistant to alkali metals, hydrogen and possibly alkali hydroxides (lyes). Furthermore, the fittings must be temperature resistant. 2. Shut-off valves and (overpressure) valves must have a large
- the degassing device must ensure that no heat transfer medium (alkali metal) is discharged. Therefore, a reliable gas-liquid separation must be ensured. Consequently, a condensate drainage must be provided.
- Fig. 8 shows an exemplary structure of the hydrogen separation device 30 as it can be used in the various embodiments of the high-temperature reformer.
- the hydrogen separation device 30 in the liquid line 22, 522, 622, 722 comprises a collection container 300 in which a liquid level is set.
- the collecting container 300 has a gas dome 302 in which vaporous heat transfer medium is located and in which hydrogen and other inert gases collect. From this gas dome 302 branches off a stub 304, which leads to a region with lower temperatures ends in a lock device 306.
- materials such as EPDM (up to about 150 ° C.), etc. can be used for the valves 308, 310, 312, 314.
- the temperature of the stub line 304 is decisive for the vapor pressure of the heat transfer medium.
- a long stub 304 therefore results in an inert gas heat transfer separation.
- the temperature of the stub line 304 may not be below the solidification temperature of the heat transfer medium to prevent clogging of the stub 304.
- the degassing device 306 for degassing consists of 4 valves 308, 310,
- each of the first and second valves 308, 310 and the third and fourth valve, 312, 314 in series and the two pairs of rows 308, 310 and 312, 314 are connected in parallel.
- the parallel connection results in a redundant lock system.
- the degassing system or the hydrogen separation device 30 should be installed as possible at the coolest point of the heat transfer circuit.
- a vacuum pump - not shown - creates a vacuum with valve 308 or 312 closed and valve 310 or 314 open, then valve 310 or 314 is closed and valve 308 or 312 is opened and closed again. Then this cycle starts again. In this way, hydrogen and other inert gases are eliminated from the heat transfer circuit.
- FIG. 9 shows a third embodiment of the high-temperature reformer with a fluidized bed combustor 804 and a carburetor or reformer 802.
- the carburetor 802 includes a gasifier pressure vessel 806 that is co-located with the fluidized bed combustor 804 in a common reactor vessel 805.
- a loop heat pipe device 814 having a plurality of loop heat pipes as shown in Figs. 3 and 4 is used.
- the plurality of loop heat pipes are assembled into an evaporator battery 816 and a capacitor battery 818.
- Capacitor battery 818 and evaporator battery 816 are interconnected via a single steam line 820 and via a single fluid line 822.
- the evaporator battery 816 is disposed in the fluidized bed combustor 804, and the capacitor battery 818 is disposed in the gasifier pressurized container 805.
- a degassing and filling tube 830 which leads out of the condenser battery 818 from the carburetor pressure vessel 806 and the common reactor vessel 805, hydrogen and other inert gases are withdrawn.
- the degassing and filling tube 830 the filling of the loop heat pipe device 814 with heat transfer medium.
- the immersion heat pipe 900 shows an alternative embodiment of a heat pipe in the form of a so-called immersion heat pipe 900.
- the immersion heat pipe 900 consists of an outer pipe 902 having an open end 904 and a closed end 906.
- the outer pipe 902 is an inner pipe 908 open on both sides disposed having a first open end 910 and a second open end 912.
- Via the open end 904 of the outer tube 902 flows vaporous heat transfer medium and condenses on the way down to the closed end 906 of the outer tube 902.
- the condensed heat transfer fluid flows through the first open end 910 of the inner tube 908 back up and is on the second open end 912 of the inner tube 908 discharged from the immersion heat pipe 900.
- a corresponding pressure gradient is necessary to promote the heat transfer medium condensate back up.
- the supply of vaporous heat transfer medium via the open end 904 of the outer tube 902 and the discharge of the liquid heat transfer medium via the second open end 912 of the inner tube takes place transversely to the longitudinal extent of the outer and inner tubes 902, 908.
- Meander-shaped heat exchanger pipe guides which are problematic in fluidized beds, in particular in the gasifier, can be avoided by the immersion heat pipe 900 described above since they disturb the structure and the stratification of the fluidized bed.
- 600 loop heat pipe, LHP 616 heat receiving side or evaporator of 600
- 628 capillary structure of 616
- 702 secondary heat transfer circuit, pulsed loop heat pipe, CLPHP 706 gasifier pressure vessel 716 heat receiving side of 701
- Degassing device 736 Heat receiving side or evaporator of 702
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Solid Fuels And Fuel-Associated Substances (AREA)
Abstract
Description
Claims
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA2743075A CA2743075C (en) | 2008-11-18 | 2009-11-18 | Device for generating combustible product gas from carbonaceous feedstocks |
EP09763905A EP2207616B1 (de) | 2008-11-18 | 2009-11-18 | Vorrichtung zur erzeugung von brennbarem produktgas aus kohlenstoffhaltigen einsatzstoffen |
CN200980145945XA CN102215948A (zh) | 2008-11-18 | 2009-11-18 | 用于从含碳原料产生可燃产物气体的装置 |
AT09763905T ATE518589T1 (de) | 2008-11-18 | 2009-11-18 | Vorrichtung zur erzeugung von brennbarem produktgas aus kohlenstoffhaltigen einsatzstoffen |
BRPI0921897A BRPI0921897A2 (pt) | 2008-11-18 | 2009-11-18 | dispositivo para a geração de produto combustível a partir de matérias-primas contendo carbono |
US13/129,387 US20110259556A1 (en) | 2008-11-18 | 2009-11-18 | Device for generating combustible product gas from carbonaceous feedstocks |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE202008015273 | 2008-11-18 | ||
DE202008015273.9 | 2008-11-18 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2010057919A1 true WO2010057919A1 (de) | 2010-05-27 |
Family
ID=41571782
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2009/065389 WO2010057919A1 (de) | 2008-11-18 | 2009-11-18 | Vorrichtung zur erzeugung von brennbarem produktgas aus kohlenstoffhaltigen einsatzstoffen |
Country Status (7)
Country | Link |
---|---|
US (1) | US20110259556A1 (de) |
EP (1) | EP2207616B1 (de) |
CN (1) | CN102215948A (de) |
AT (1) | ATE518589T1 (de) |
BR (1) | BRPI0921897A2 (de) |
CA (1) | CA2743075C (de) |
WO (1) | WO2010057919A1 (de) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2010119139A3 (de) * | 2009-04-17 | 2011-09-29 | Highterm Research Gmbh | Vorrichtung zur erzeugung von produktgas aus kohlenstoffhaltigen einsatzstoffen mit wärmerohren |
DE102010043851A1 (de) | 2010-11-12 | 2012-05-16 | Highterm Research Gmbh | Hochtemperatur-Wärmetransportvorrichtung |
JP2015522669A (ja) * | 2012-05-22 | 2015-08-06 | キャボット マイクロエレクトロニクス コーポレイション | ジルコニア粒子を含むcmp組成物および使用方法 |
FR3124585A1 (fr) * | 2021-06-24 | 2022-12-30 | Thales | Dispositif et procédé de contrôle passif du débit d’un fluide dans une boucle fluide diphasique à pompage mécanique |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
TWI580921B (zh) * | 2014-05-09 | 2017-05-01 | 財團法人工業技術研究院 | 脈衝型多管式熱管 |
CN108458614A (zh) * | 2018-04-13 | 2018-08-28 | 中国科学院理化技术研究所 | 一种回路热管 |
US11051428B2 (en) * | 2019-10-31 | 2021-06-29 | Hamilton Sunstrand Corporation | Oscillating heat pipe integrated thermal management system for power electronics |
CN114214091B (zh) * | 2021-12-20 | 2022-08-30 | 南京林业大学 | 生物质挥发分、水蒸气及生物质半焦三元气化反应制氢装置 |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0415231A2 (de) | 1989-09-01 | 1991-03-06 | DEUTSCHE FORSCHUNGSANSTALT FÜR LUFT- UND RAUMFAHRT e.V. | Wärmerohr |
EP1187892A1 (de) * | 1999-06-09 | 2002-03-20 | Technische Universität München Lehrstuhl für Thermische Kraftanlagen | Vorrichtung zur vergasung kohlenstoffhaltiger einsatzstoffe |
WO2003054469A1 (en) | 2001-12-21 | 2003-07-03 | Tth Research, Inc. | Loop heat pipe |
DE102006016005A1 (de) | 2006-04-05 | 2007-10-11 | Bioage Gmbh | Wärmerohr, Heatpipe-Reformer mit einem solchen Wärmerohr und Verfahren zum Betreiben eines solchen Heatpipe-Reformers |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4474230A (en) * | 1982-08-31 | 1984-10-02 | Foster Wheeler Energy Corporation | Fluidized bed reactor system |
-
2009
- 2009-11-18 EP EP09763905A patent/EP2207616B1/de not_active Not-in-force
- 2009-11-18 CA CA2743075A patent/CA2743075C/en not_active Expired - Fee Related
- 2009-11-18 AT AT09763905T patent/ATE518589T1/de active
- 2009-11-18 US US13/129,387 patent/US20110259556A1/en not_active Abandoned
- 2009-11-18 CN CN200980145945XA patent/CN102215948A/zh active Pending
- 2009-11-18 BR BRPI0921897A patent/BRPI0921897A2/pt not_active IP Right Cessation
- 2009-11-18 WO PCT/EP2009/065389 patent/WO2010057919A1/de active Application Filing
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0415231A2 (de) | 1989-09-01 | 1991-03-06 | DEUTSCHE FORSCHUNGSANSTALT FÜR LUFT- UND RAUMFAHRT e.V. | Wärmerohr |
EP1187892A1 (de) * | 1999-06-09 | 2002-03-20 | Technische Universität München Lehrstuhl für Thermische Kraftanlagen | Vorrichtung zur vergasung kohlenstoffhaltiger einsatzstoffe |
EP1187892B1 (de) | 1999-06-09 | 2004-12-29 | Technische Universität München Lehrstuhl für Thermische Kraftanlagen | Vorrichtung zur vergasung kohlenstoffhaltiger einsatzstoffe |
WO2003054469A1 (en) | 2001-12-21 | 2003-07-03 | Tth Research, Inc. | Loop heat pipe |
DE102006016005A1 (de) | 2006-04-05 | 2007-10-11 | Bioage Gmbh | Wärmerohr, Heatpipe-Reformer mit einem solchen Wärmerohr und Verfahren zum Betreiben eines solchen Heatpipe-Reformers |
Non-Patent Citations (2)
Title |
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AMIR FAHGRI, HEAT PIPE SCIENCE AND TECHNOLOGY, 1995, pages 583 |
AMIR FAHGRI, HEAT PIPE SCIENCE AND TECHNOLOGY, 1995, pages 586 |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2010119139A3 (de) * | 2009-04-17 | 2011-09-29 | Highterm Research Gmbh | Vorrichtung zur erzeugung von produktgas aus kohlenstoffhaltigen einsatzstoffen mit wärmerohren |
DE102010043851A1 (de) | 2010-11-12 | 2012-05-16 | Highterm Research Gmbh | Hochtemperatur-Wärmetransportvorrichtung |
JP2015522669A (ja) * | 2012-05-22 | 2015-08-06 | キャボット マイクロエレクトロニクス コーポレイション | ジルコニア粒子を含むcmp組成物および使用方法 |
FR3124585A1 (fr) * | 2021-06-24 | 2022-12-30 | Thales | Dispositif et procédé de contrôle passif du débit d’un fluide dans une boucle fluide diphasique à pompage mécanique |
Also Published As
Publication number | Publication date |
---|---|
EP2207616A1 (de) | 2010-07-21 |
BRPI0921897A2 (pt) | 2015-12-29 |
CN102215948A (zh) | 2011-10-12 |
ATE518589T1 (de) | 2011-08-15 |
CA2743075C (en) | 2014-05-06 |
CA2743075A1 (en) | 2010-05-27 |
EP2207616B1 (de) | 2011-08-03 |
US20110259556A1 (en) | 2011-10-27 |
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