DEVICE FOR GENERATING COMBUSTIBLE PRODUCT GAS FROM CARBONACEOUS FEEDSTOCKS
A device is provided for generating combustible product gas from carbonaceous feedstocks through allothermal steam gasification in a pressurized gasification vessel. The pressurized allothermal steam gasification of carbonaceous fuels requires that heat be supplied to the gasification chamber at a temperature level of approximately 800-900° C. In a heat pipe reformer, as is known from EP 1 187 892 B1, combustible gas is generated from the carbonaceous feedstocks to be gasified through allothermal steam gasification in a pressurized fluidized bed gasification chamber. The heat needed for this is fed to the gasifier or reformer from a fluidized bed combustion system through a heat pipe arrangement. Due to the straight and tubular construction of heat pipes, the combustion chamber and reformer/gasification chamber are disposed one above the other in the known heat pipe reformer from EP 1 187 892 B1. The pressure vessel base is under particular stresses due to the high temperatures in the combustion chamber. In addition, the base is weakened by a plurality of heat pipe feedthroughs. The sealing of the feedthroughs also presents a problem. In conventional tubular heat pipes, the line for liquid heat transfer medium and for gaseous heat transfer medium are both disposed in the common tubular shell. The fact that the present invention uses loop heat pipes in which the liquid heat transfer medium is conveyed spatially separated from the gaseous heat transfer medium allows the number of feedthroughs to be reduced to two, namely a liquid line and a vapor line. When a plurality of such loop heat pipes is used, the separate vapor and fluid lines thereof can be combined in the
The invention relates to a device for generating combustible product gas from carbonaceous feedstocks through allothermal steam gasification in accordance with the preamble of claim 1.
The pressurized allothermal steam gasification of carbonaceous fuels requires to supply heat on a temperature level of approx. 800-900° C. into the gasification chamber. In the so-called heat pipe reformer as known from EP 1 187 892 B1, fuel gas is produced from the carbonaceous feedstocks to be gasified in a pressurized fluidized bed gasification chamber through allothermal steam gasification. The heat required for this purpose is conducted from a fluidized bed combustion system into the gasifier or reformer by means of a thermoconducting pipe arrangement. Due to the straight and tubular construction of heat pipes, the combustion chamber and the reformer/gasification chamber are disposed one above the other in the heat pipe reformer known from EP 1 187 892 B1. The pressure vessel base is subject to particular stresses due to the high temperatures in the combustion chamber. In addition, the base is weakened by a plurality of heat pipe feedthroughs. Sealing of the feedthroughs also presents a problem.
Under the named operating conditions, hydrogen diffuses through the metal jacket of the heat pipes to the inside of the heat pipe and gathers in the area of the condenser, or heat-releasing side. Heat transfer ceases to take place in the area of this hydrogen pocket, whereby the thermal energy transferred by the heat pipe is reduced. In order to avoid such hydrogen pockets, it is known to prevent or reduce the diffusion of hydrogen with the aid of coatings of the heat pipes or by separating gasification and heat transition zones inside the gasifier. In accordance with a different approach, the outward diffusion of hydrogen is intensified by an increased internal pressure and flushing caps. In this regard, reference is made to DE 102006016005 A1.
Starting out from EP 1 187 892 A1 it is the object of the present invention to reduce the weakening of the gasifier pressure vessel through the heat pipe feedthroughs.
This object is achieved through the features of claim 1.
In traditional, tubular heat pipes the lines for both the liquid heat transfer medium and also for the vaporous heat transfer medium are disposed in the common tube shell. Due to the fact that the present invention employs loop heat pipes where the liquid heat transfer medium is conducted in physical separation from the vaporous heat transfer medium, the number of feedthroughs may be reduced to two, namely, a liquid line and a steam line. When a plurality of such loop heat pipes is employed, their separately routed steam and liquid lines may be combined inside the gasifier pressure vessel into one common steam line and liquid line which are then passed through the gasifier pressure vessel. Outside of the gasifier pressure vessel the two common lines may then be split again. The number of feedthroughs from and into the gasifier pressure vessel may thus be reduced considerably, to a minimum of two.
Another advantage of the invention resides in the fact that the physical separation of steam and liquid lines of loop heat pipes allows for a higher freedom of design. Gasifier or reformer, respectively, and external heat source may be disposed and optimized entirely independently of each other.
Due to the separate routing of steam and liquid line, the course of the steam line may be optimized with a view to the arrangement of a hydrogen separating means—claim 2.
The advantageous aspects of claims 3 and 4 relate to different construction forms for loop heat pipes with a separately realized steam and liquid line.
In accordance with the advantageous aspect of the invention according to claim 5, the heat transfer from the external heat source into the gasifier takes place through two physically separated heat medium circuits with phase change which are connected in series. In this way the first heat medium circuit or the associated heat pipe, respectively, may be optimized with regard to heat absorption inside the heat source, while the second heat medium circuit or the associated heat pipe, respectively, may be optimized with regard to heat release inside the gasifier.
Loop heat pipes with separately configured steam and liquid lines for the first stage for absorbing the heat in the heat source and pulsed loop heat pipes having common steam/liquid lines have been found to be a particularly suitable combination for releasing the heat in the gasifier—claims 6 and 7.
Due to the advantageous aspect of the invention according to claim 10, on the one hand the pyrolysis residues from the gasifier are utilized thermally, and on the other hand the entire fuel supply may thus take place in the fluidized bed combustion chamber. An additional supply of fuel into the fluidized bed combustion chamber is not necessary any more, with the exception of the start-up.
Due to the high operation temperatures, alkali metals and their alloys, e.g. Na, K, NaK, are particularly well suited as a heat transfer medium in the loop heat pipes.
The remaining subclaims relate to further advantageous aspects of the invention.
Further details, features and advantages result from the following description of preferred embodiments making reference to the drawings, wherein:
As a result of the combustion of the pyrolysis residues from the gasifier 2 and/or through combustion of additional fuel, heat is generated in the combustion chamber 4 which is absorbed through the heat-absorbing side 16 of the loop heat pipe 14 due to that the fact that the liquid heat transfer medium supplied via the liquid line 22 evaporates. The vaporous heat transfer medium flows into the gasifier via the steam line 20, condenses in the heat-releasing side 18 of the loop heat pipe 14, and thus furnishes the high-temperature heat required for the allothermal steam gasification. The liquefied heat transfer medium is supplied via the liquid line 22, together with the hydrogen having diffused into heat medium circuit 14 in the gasifier, to the hydrogen separating means 30. By means of the hydrogen separating means 30 the hydrogen as well as other foreign matter is separated from the liquid heat transfer medium while the remaining liquid heat transfer medium is resupplied to the combustion chamber 4, whereby the heat transfer medium circuit is closed. Owing to the high temperatures, alkali metals or alloys of these, e.g. Na, K, or NaK, are used.
In the embodiment according to
The reformer or gasifier 2 may equally be designed without any restrictions in terms of the combustion chamber 4 because combustion chamber 4 and gasifier 2 are not disposed in a common vessel as in the heat pipe reformer. The feedthrough of high-temperature steam line and liquid line 20, 22 is placed in constructively favorable locations of the gasifier pressure vessel 6. In the embodiment according to
Owing to an internal thermal insulation of the gasifier pressure vessel 6, the reaction temperature in the gasifier may be substantially higher than the temperatures at the wall of the gasifier pressure vessel. As a result, stable constructions are realized even with the use of lower-cost materials having lower wall thicknesses.
The pyrolysis residues of the gasifier 2 may be utilized directly in the combustion chamber 4 via the material lock 24. At a favorable process management, the pyrolysis residues are sufficient to cover the fuel demand of the combustion chamber 4. Product gas leakage flows via the material lock 24 may be burnt off safely and completely in the combustion chamber 4.
The liquid collection line 522 is connected to a compensation vessel 532 via a compensation line 530. The compensation vessel 532 ensures a uniform filling level in the liquid collection line 522. As a result of a slight temperature gradient and thus also a pressure gradient, the liquid heat transfer medium flows back into the liquid collection line 522. The evaporation enthalpy absorbed in the evaporator 516 (combustion chamber 4) thus is released again in the condenser 518 (gasifier 2).
The hydrogen separating means is integrated into the liquid collection line 522 (not represented in
In state 1—FIG. 5—the heat transfer medium is in liquid/steam equilibrium (f-d-GGW), and in state 2 it is superheated in the evaporator 616. From state 2 to 3 the pressure drops owing to flow losses. State 3 via 4 to 5 shows the complete condensation, including supercooling, of the condensate (state 5). In state 6 the heat transfer medium is located in the upper range of the evaporator 616 and is heated to state 7 by the evaporator 616 (f-d-GGW), to then be superheated to the temperature 8 in the lower range of the evaporator 616. In order for the LHP 600 to function in accordance with its intended purpose, it is necessary that the capillary pressure difference in the capillary structure 628 is greater than the sum of pressure losses of the steam and liquid flows, the capillary structure 628, and the hydrostatic pressure. I.e., the required condition is:
(Δpcap)max≧Δpu+Δpe+Δpw+Δpg
Such a loop heat pipe is also known from WO/2003/054469.
The secondary heat medium circuit 702 is realized with the aid of a pulsed loop heat pipe (Closed Loop Pulsating Heat Pipe, CLPHP) as represented in
In the closed condition of the pulsed loop heat pipe 702, the heat transfer medium is alternately conducted via the steam/liquid line 740 from the evaporator 736 into the condenser 738. A temperature difference brings about a pressure difference causing a pulsed flow in the whole system. As a result it is possible to transport off hydrogen pockets and other inert gases by convection, to withdraw these in a suitable location, e.g. at the top of the condenser 738 via a gas vent 730.
In the following, an exemplary embodiment of a hydrogen separating means or gas venting means 30, 730, 830 is described with reference to
Due to manufacturing conditions, inert gas may be present in the alkali-liquid-steam circuit. During operation, hydrogen diffuses into the circuit. The consequences of an accumulation of inert gases in the system are manifold and have varying degrees of effect depending on the circuit system (CPL, LHP, . . . ):
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- Accumulations of inert gases may detract from operation in accordance with the intended purpose. For example, inert gas accumulations in tube bends cause an interruption of flow and thus an interruption in heat transfer. Local overheating in the evaporator part might ensue.
- Permanent inward diffusion of hydrogen results in a rising overall pressure in the system. Depending on the type of system, this might also influence the vapor pressure of alkali metal and thus the evaporation temperature. It might be possible to influence the evaporation temperature of the alkali metal circuit with the aid of a gas venting device.
The gas venting device or hydrogen separating means 30 for an alkali metal liquid-steam circuit accordingly has to satisfy the following marginal conditions:
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- 1. Mountings that are in contact with the media must be resistant against alkali metals, hydrogen, and in a given case alkali hydroxide (lyes). Moreover the mountings must be temperature-resistant.
- 2. Cutoff mountings and (pressure reducing) valves must be vacuum-tight over a large temperature range.
- 3. The gas venting device must safely prevent outward transfer of heat transfer medium (alkali metal). A reliable gas-liquid separation must therefore be ensured. Accordingly it is also necessary to provide a condensate discharge line.
- 4. Solidification of the heat transfer medium in the gas venting area must be avoided in accordance with the type of heat transfer medium used.
Gas venting allows for pressure regulation and thus also temperature regulation. As was already mentioned, the pressure sensitivity of the system is highly dependent on the circuit system.
The lock means 306 leading to the gas vent consists of four valves 308, 310, 312, 314 with respective serial arrangement of the first and second valves 308, 310 and of the third and fourth valves 312, 314, and parallel arrangement of the two serial pairs 308, 310 and 312, 314. The parallel connection results in a redundancy lock system. If possible, the gas vent system or the hydrogen separating means 30 should be installed in the coolest location of the heat medium circuit. While valve 308 or 312 is closed and valve 310 or 314 is open, a vacuum pump—not represented—creates a vacuum, after which valve 310 or 314 is closed and valve 308 or 312 is opened and closed again.
Subsequently this cycle begins anew. In this way, hydrogen and other inert gases are discharged from the heat medium circuit.
The immersed heat pipe 900 described in the foregoing allows to avoid meander-type heat transfer medium pipe layouts which constitute a problem in fluidized beds, in particular in the gasifier, as they interfere with build-up and layer formation of the fluidized bed.
LIST OF REFERENCE NUMERALS2 pressurized gasifier or reformer
4 heat source or combustion chamber
6 gasifier pressure vessel
8 fuel supply means
10 water or steam supply
12 product gas extracting line
14 high-temperature heat medium circuit or loop heat pipe
16 heat-absorbing side of 14
18 heat-releasing side of 14
20 steam line
22 liquid line
24 material lock for pyrolysis residues
26 air supply
28 flue gas outlet
30 hydrogen separating means
32 circulating fluidized bed
34 ascending pipe
36 cyclone
38 material lock
40 fluidized bed
42 first pipe bundle heat exchanger
44 second pipe bundle heat exchanger
46 third pipe bundle heat exchanger
300 collecting vessel of 30
302 gas dome
304 tap line
306 lock means
308 first valve
310 second valve
312 third valve
314 fourth valve
500 capillary pumped loop heat pipe
516 heat-absorbing side or evaporator of 500
518 heat-releasing side or condenser of 500
520 steam collection line
522 liquid collection line
524 evaporator element
526 condenser element
528 capillary structure of 524
530 compensation line
532 compensation vessel
600 loop heat pipe, LHP
616 heat-absorbing side or evaporator of 600
618 heat-releasing side or condenser of 600
620 steam line
622 liquid line
628 capillary structure of 616
700 two-stage high-temperature heat medium circuit
701 primary heat medium circuit
702 secondary heat medium circuit, pulsed loop heat pipe, CLPHP
706 gasifier pressure vessel
716 heat-absorbing side of 701
718 heat-releasing side of 701
720 steam line
722 liquid line
730 gas venting means
736 heat-absorbing side or evaporator of 702
738 heat-releasing side or condenser of 702
740 steam/liquid line
802 gasifier or reformer
804 fluidized bed combustion chamber
805 common reactor vessel
806 gasifier pressure vessel
814 loop heat pipe means
816 evaporator group
818 condenser group
820 steam line
822 condensate line
830 gas venting and charging pipe
900 immersed heat pipe
902 outer pipe
904 open end of 902
906 closed end of 902
908 inner pipe
910 first open end of 908
912 second open end of 908
Claims
1. A device for generating combustible product gas from carbonaceous feedstocks through allothermal steam gasification, comprising:
- a pressurized gasifier including a gasifier pressure vessel, a supply means for the carbonaceous feedstocks, a steam supply, and a product gas extracting line,
- an external heat source, and
- a heat transport means comprising at least one heat pipe whereby heat is transported, with the aid of a heat transfer medium undergoing a phase change, from the external heat source into the gasifier,
- wherein the at least one heat pipe has a heat-releasing side disposed inside the gasifier and a heat-absorbing side disposed inside the external heat source, and
- wherein the at least one heat pipe is a loop heat pipe, the heat-absorbing and the heat-releasing side of which are connected to each other via a liquid line for liquid heat transfer medium and via a steam line for vaporous heat transfer medium, and in that the liquid line and the steam line are physically separate lines.
2. The device according to claim 1, wherein a hydrogen separating means is disposed in the liquid line of the at least one loop heat pipe.
3. The device according to claim 1, wherein the heat transport means includes at least one loop heat pipe pumped by means of a capillary structure.
4. The device according to claim 1, wherein the heat transport means includes at least one immersed loop heat pipe.
5. The device according to claim 1, wherein the heat transport means includes at least one first loop heat pipe comprising a steam line for vaporous heat transfer medium and a liquid line for liquid heat transfer medium, wherein the steam line and the liquid line are disposed in a physically separate manner, the heat transport means includes at least one second heat pipe, the two heat pipes each have a heat-releasing side and a heat-absorbing side, the heat-absorbing side of the at least one first loop heat pipe is disposed inside the external heat source, and the heat-releasing side of the at least one first loop heat pipe is thermally integrated into the heat-absorbing side of the at least one second heat pipe, and the heat-releasing side of the at least one second heat pipe is disposed inside the gasifier pressure vessel.
6. The device according to claim 5, wherein the at least one second heat pipe is a pulsed loop heat pipe which comprises a common steam/liquid line and which is disposed inside the gasifier pressure vessel.
7. The device according to claim 6, wherein the common steam/liquid line has a meander-type shape, in that the heat-releasing side of the pulsed loop heat pipe is disposed in the upper range of the gasifier pressure vessel, and in that the heat-absorbing side is disposed in the base area of the gasifier pressure vessel.
8. The device according to claim 1, wherein the external heat source is a fluidized bed combustion chamber.
9. The device according to claim 1, wherein the gasifier is configured as a fluidized bed gasifier.
10. The device according to either claim 8 or 9, wherein the gasifier pressure vessel is connected to the fluidized bed combustion chamber via a material lock for pyrolysis residues.
11. The device according to claim 9, wherein the fluidized bed gasifier and the fluidized bed combustion chamber are disposed inside a common vessel.
Type: Application
Filed: Nov 18, 2009
Publication Date: Oct 27, 2011
Inventors: Georg Gallmetzer (Munchen), Felix Nelles (Pfaffenhofen), Martin Kröner (Munchen)
Application Number: 13/129,387
International Classification: F28D 15/04 (20060101);