EP2207616B1 - Device for generating combustible product gas from carbonaceous feedstocks - Google Patents

Abstract

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

Description

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. In the so-called heat pipe reformer, as from the EP 1 187 892 B1 is known to be produced in a pressurized fluidized bed gasification chamber by allothermic steam gasification fuel gas from the carbonaceous feedstocks to be gasified. The necessary heat is passed from a fluidized bed by means of a Wärmeleitrohranordnung in the carburetor or reformer. Due to the straight and tubular construction of heat pipes are in the from the EP 1 187 892 B1 known heat pipe reformer combustion chamber and reformer / gasification chamber arranged one above the other. The pressure vessel bottom is exposed to special stresses due to the high temperatures in the combustion chamber. Moreover, the soil is weakened by a variety of heat pipe bushings. The sealing of the bushings is also a problem.

In the above operating conditions, hydrogen diffuses through the metal jacket of the heat pipes into the interior of the heat pipe and collects in the region of the condenser or the heat-emitting side. In the area of this hydrogen cushion, no heat transfer takes place, so that the heat output transmitted through the heat pipe is reduced. In order to avoid these hydrogen cushions, it is known that the diffusion of hydrogen through coatings of the heat pipes or by separation of the gasification and heat transfer zone in Prevent or reduce carburetor. According to another approach, the outdiffusion of hydrogen is increased by increased internal pressure and purge caps. This is on the DE 102006016005 A1 directed.

From the EP 415231 A2 is a heat pipe with a cylindrical outer shell known in which concentrically inside the cylindrical outer shell, a riser for steam-shaped working fluid is arranged. Due to the nesting of riser and outer shell, can not be prevented that also flows in the actual condensate line steam-shaped working fluid.

Starting from the EP 1 187 892 B1 It is an object of the present invention to reduce the weakening of the carburetor pressure vessel by the plurality of heat pipe bushings.

The solution of this object is achieved by the features of claim 1.

In conventional tubular heat pipes, as for example from the EP 415231 A2 are known, both the line for liquid heat transfer medium and for vaporous heat transfer medium in the common tube shell is arranged. Characterized in that in the present invention loop heat pipes are used in which the liquid heat transfer medium is spatially separated from the vaporous heat transfer medium, 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. Thus, the number of feedthroughs from or into the carburetor pressure vessel can be significantly reduced to a minimum of two.

Another advantage of the invention is that the spatial separation of the steam and liquid line of the loop heat pipes a larger Design freedom arises. Carburetor or reformer and external heat source can be arranged and optimized completely independently.

Due to the separate management of steam and liquid line the course of the steam line with regard to the arrangement of a hydrogen separation device can be optimized - claim 2.

The advantageous embodiments of claims 3 and 4 relate to different designs for loop heat pipes with separate running steam and liquid line.

According to the advantageous embodiment of the invention according to claim 5, the heat transfer from the external heat source into the carburetor by two physically separate series-connected heat carrier circuits with phase change. In this way, the first heat carrier circuit or the associated heat pipe 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.

As a particularly suitable combination have exposed loop heat pipes with separate running steam and liquid line for receiving the heat in the heat source and pulsed loop heat pipes with common steam / liquid line for the release of heat in the carburetor - claim 6 and 7 ,

Due to the advantageous embodiment of the invention according to claim 10, on the one hand 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.

Due to the high operating temperatures are particularly suitable alkali metals and their alloys, eg. B. Na, K, NaK, as a heat transfer medium in the loop heat pipes.

The remaining subclaims relate to further advantageous embodiments of the invention.

Further details, features and advantages resulted from the following description of preferred embodiments with reference to the drawing.

• Fig. 1 zeigt den prinzipiellen Aufbau eines Highterm-Reformers gemäß der vorliegenden Erfindung;
• Fig. 2 eine schematisch Darstellung einer ersten Ausführungsform der Erfindung im Highterm-Reformer;
• Fig. 3 eine erste Ausführungsform des Hochtemperatur-Wärmeträgerkreislaufes im Highterm-Reformer in Form eines mittels Kapillarstruktur gepulsten Loop-Wärmerohrs, CPL;
• Fig. 4 eine zweite Ausführungsform des Hochtemperatur-Wärmeträgerkreislaufes in Form eines Loop-Wärmerohrs, LHP;
• Fig. 5 das Druck-Temperatur-Zustandsdiagramm zu dem LHP nach Fig. 4;
• Fig. 6 eine zweite Ausführungsform des Highterm-Reformers gemäß der vorliegenden Erfindung mit zwei physikalisch getrennten Wärmeträgerkreisläufen;
• Fig. 7 ein gepulstes Loop-Wärmerohr, CLPHP, wie es in dem Highterm-Reformer nach Fig. 7 als zweiter Wärmeträgerkreislauf verwendet wird;
• Fig. 8 eine beispielhafte Ausgestaltung der Wasserstoff-Abscheideeinrichtung Highterm-Reformers;
• Fig. 9 eine dritte Ausführungsform des Highterm-Reformers gemäß der vorliegenden Erfindung mit Vergaser und Brennkammer in einem gemeinsamen Behälter; und
• Fig. 10 eine dritte Ausführungsform des Hochtemperatur-Wärmeträgerkreislaufes in Form von Tauch-Loop-Wärmerohren.

It shows

• Fig. 1 shows the basic structure of a high-term reformer according to the present invention;
• Fig. 2 a schematic representation of a first embodiment of the invention in the high-temperature reformer;
• Fig. 3 a first embodiment of the high-temperature heat transfer circuit in Highterm reformer in the form of a loop heat pipe pulsed by capillary, CPL;
• Fig. 4 a second embodiment of the high-temperature heat transfer circuit in the form of a loop heat pipe, LHP;
• Fig. 5 the pressure-temperature state diagram to the LHP after Fig. 4 ;
• Fig. 6 a second embodiment of the high-temperature reformer according to the present invention with two physically separate heat transfer circuits;
• Fig. 7 a pulsed loop heat pipe, CLPHP, as found in the Highterm Reformer Fig. 7 is used as a second heat carrier circuit;
• Fig. 8 an exemplary embodiment of the hydrogen separator Highterm reformer;
• Fig. 9 a third embodiment of the high-temperature reformer according to the present invention with carburetor and combustion chamber in a common container; and
• Fig. 10 a third embodiment of the high-temperature heat transfer circuit in the form of dip-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. About 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. In the liquid line 22 between the carburetor 2 and the combustion chamber 4, a hydrogen separation device 30 is arranged.

By combustion of the pyrolysis residues from the carburetor 2 and / or by combustion of additional fuel 4 heat is generated in the combustion chamber, which is absorbed by the heat receiving side 16 of the loop heat pipe 14 characterized in that the supplied via the liquid line 22 liquid Heat transfer medium evaporates. The vaporous heat transfer medium flows via the steam line 20 into the gasifier, condenses in the heat-emitting side 18 of the loop heat pipe 14 and thereby provides the necessary for the allothermal Dampfdgsung high-temperature heat heat. The liquefied heat transfer medium is supplied to the hydrogen separation device 30 via the liquid line 22 together with hydrogen which has diffused into the heat transfer circuit 14 in the gasifier. 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 returned 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 schematically shows 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.

In the embodiment according to Fig. 2 has the combustion chamber 4 compared to the so-called heat pipe reformer after EP 1 187 892 B1 no limitation in the construction and operation. Thus, 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 the riser 34 and the optimal 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 Soil zone of the riser 34. With regard to the exact structure of the combustion chamber 4 with circulating fluidized bed 32 is on " Handbook of Fludization and Fluid Particle Systems, "by Wen-Ching Yang, ISBN: 0-8247-0259-X , referenced.

Also, 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. In the embodiment according to Fig. 2 the liquid line 22 and the steam line 20 are guided laterally out of the barrel-shaped carburetor 2. The lid 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.

Due to an internal thermal insulation of the carburetor pressure vessel 6, 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.

Fig. 3 shows a first embodiment of the high-temperature heat transfer circuit in Highterm reformer in the form of a pumped by capillary loop heat pipe 500 (Capillary Pumped Loop CPL), as shown in Publication, Heat Pipe Science and Technology, Amir Fahgri, 1995, page 583 is known. The CPL 500 includes a heat receiving side Evaporator 516 and a heat-releasing side and a condenser 518, respectively. Vaporizer 516 and condenser 518 are connected to each other via 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. In the capacitor elements 526, the heat transfer medium condenses again with the release of 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).

In the liquid collecting line 522, the hydrogen separation device is integrated (in Fig. 3 not shown).

Fig. 4 shows a second embodiment of the high-temperature heat transfer circuit in Highterm reformer in the form of a loop heat pipe 600 (Loop Heat Pipe LHP), as it is known from Publication, Heat Pipe Science and Technology, Amir Fahgri, 1995, page 586 is known. 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. In the evaporator 616, a capillary structure 628 is arranged, through which liquid Heat transfer medium is vaporized by absorption of heat. In the condenser 618, the heat transfer medium condenses again with the release of heat.

In state 1 - 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. For the intended function of the LHP 600, it is necessary that 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: $$\left(\mathrm{\Delta }{p}_{\mathrm{cap}}\right){}_{\mathrm{Max}}\ge \mathrm{\Delta }{p}_{\upsilon }+\mathrm{\Delta }{p}_{\ell }+\mathrm{\Delta }{p}_{\omega }+\mathrm{\Delta }{p}_G\mathrm{,}$$

Such a loop heat pipe is also from the WO / 2003/054469 known.

Fig. 6 shows a second embodiment of the high-temperature reformer according to the present invention with a two-stage high-temperature heat transfer circuit 700. The high-temperature heat transfer circuit 700 includes a primary heat transfer circuit 701 and a secondary heat transfer circuit 702. The primary heat transfer circuit 701 includes a heat receiving side 716 and a heat-releasing 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 transfer circuit 701 may be through the loop heat pipes 500 and / or 600 in Fig. 3 and 4 will be realized.

The secondary heat transfer circuit 702 is implemented by a pulsed loop heat pipe (CLPHP), as shown in FIG Fig. 7 is shown. 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.

With closed pulsed loop heat pipe 702, the heat transfer medium is passed alternately via the vapor / liquid line 740 from the evaporator 736 in the condenser 738. 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.

The following is based on Fig. 8 an exemplary embodiment of hydrogen separation device or degassing 30, 730, 830 describe. 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.

• Ansammlungen von Inertgasen können zur Beeinträchtigung des bestimmungsgemäßen Betriebs führen. Beispielsweise führen Inertgasansammlungen in Rohrkrümmungen zur Unterbrechung der Strömung und damit zur Unterbrechung der Wärmeübertragung. Eine lokale Überhitzung im Verdampferteil könnte die Folge sein.
• Eine permanente Eindiffusion von Wasserstoff führt zu einem steigenden Gesamtdruck im System. Dadurch kann, je nach System, auch der Dampfdruck von Alkali-Metall beeinflusst werden und damit auch die Verdampfungstemperatur. Mit Hilfe einer Entgasungsvorrichtung könnte es möglich sein die Verdampfungstemperatur des Alkali-Metall-Kreislaufs zu beeinflussen.

For reasons of production technology, inert gas can be present in the alkali-liquid-steam cycle. During operation, hydrogen diffuses into the circuit. The consequences of an accumulation of inert gases in the system are manifold and have different effects depending on the circulatory system (CPL, LHP, ...):

• Accumulation of inert gases can impair the intended operation. For example, inert gas accumulations in pipe bends lead to the interruption of the flow and thus to interrupt the heat transfer. A local overheating in the evaporator section could be the result.
• A permanent diffusion of hydrogen leads to an increasing total pressure in the system. Thus, depending on the system, the vapor pressure of alkali metal and thus also the evaporation temperature can be influenced. With the aid of a degassing device, it might be possible to influence the evaporation temperature of the alkali metal circuit.

1. 1. Die Medienberührenden Armaturen müssen beständig gegen Alkalimetalle, Wasserstoff und ggf. Alkalihydroxide (Laugen) sein. Desweiteren müssen die Armaturen Temperaturbeständig sein.
2. 2. Absperr-Armaturen und (Überdruck-)Ventile müssen über einen großen Temperaturbereich vakuumdicht sein.
3. 3. Die Entgasungsvorrichtung muss gewährleisten, dass kein Wärmeträgermedium (Alkalimetall) ausgeschleust wird. Daher muss eine zuverlässige Gas-Flüssig-Trennung gesichert sein. Folglich muss auch eine Kondensatableitung vorgesehen werden.
4. 4. Je nach eingesetztem Wärmeübertragermedium muss dessen Erstarrung im Entgasungsbereich vermieden werden.

The degassing device or hydrogen separation device 30 for an alkali metal liquid-steam cycle must therefore fulfill the following boundary conditions:

1. 1. The media wetted valves must be resistant to alkali metals, hydrogen and possibly alkali hydroxides (lyes). Furthermore, the fittings must be temperature resistant.
2. 2. Shut-off valves and (overpressure) valves must be vacuum tight over a wide temperature range.
3. 3. 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.
4. 4. Depending on the heat transfer medium used, its solidification in the degassing area must be avoided.

Fig. 8 shows an exemplary structure of the hydrogen separation device 30 as 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. As a result, for example, 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.
By degassing a pressure and thus a temperature control is possible. The pressure sensitivity of the system is, as already mentioned, strongly dependent on the circulatory system.

The degassing device 306 for degassing consists of 4 valves 308, 310, 312, 314, wherein in each case 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 in parallel are switched. 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 - generates a vacuum when valve 308 or 312 is closed and valve 310 or 314 is 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 carburetor pressure vessel 806 which is co-located with the fluidized bed combustor 804 in a common reactor vessel 805. As a high-temperature heat cycle for transferring the heat from the fluidized bed combustor 802 into the carburetor 804, a loop heat pipe device 814 having a plurality of loop heat pipes according to FIGS Figures 3 and 4 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 in the fluidized bed combustor 804 and the condenser battery 818 are disposed in the gasifier pressure vessel 805. Via 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. At the same time via the degassing and filling tube 830, the filling of the loop heat pipe device 814 with heat transfer medium. The advantage of this third embodiment of the invention is that the loop heat pipe device 814 can be integrated into an existing reactor design.

Fig. 10 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 tube 902 with an open end 904 and a closed end 906. Inn the outer tube 902 is an open on both sides inner tube 908 is arranged 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 medium 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.

LIST OF REFERENCE NUMBERS

2

druckaufgelandener carburetor or reformer

4

Heat source or combustion chamber

6

Gasifier pressure vessel

8th

Feed device for fuel

10

Water or steam supply

12

Product gas outlet

14

High-temperature heat transfer circuit or loop heat pipe

16

Heat absorbing side of 14

18

Heat-emitting side of 14

20

steam line

22

liquid line

24

Lock for pyrolysis residues

26

air supply

28

Flue gas exhaust.

30

Hydrogen separation device

32

circulating fluidized bed

34

riser

36

cyclone

38

lock

40

fluidized bed

42

first shell and tube heat exchanger

44

second shell and tube heat exchanger

46

third tube bundle heat exchanger

300

Collecting container of 30

302

gas dome

304

stub

306

lock device

308

first valve

310

second valve

312

third valve

314

fourth valve

500

Capillary structure pumped loop heat pipe

516

Heat absorbing side or evaporator of 500

518

Heat-emitting side or capacitor of 500

520

Steam manifold

522

Fluid manifold

524

evaporator element

526

capacitor element

528

Capillary structure of 524

530

compensation line

532

surge tank

600

Loop heat pipe, LHP

616

Heat absorbing side or evaporator of 600

618

Heat-emitting side or capacitor of 600

620

steam line

622

liquid line

628

Capillary structure of 616

700

two-stage high-temperature heat transfer circuit

701

primary heat transfer circuit

702

secondary heat transfer circuit, pulsed loop heat pipe, CLPHP

706

Gasifier pressure vessel

716

Heat absorbing side of 701

718

Heat-emitting side of 701

720

steam line

722

liquid line

730

degassing

736

Heat absorbing side or evaporator of 702

738

Heat-emitting side or condenser of 702

740

Vapor / liquid line

802

Carburetor or reformer

804

Fluidized bed combustor

805

common reactor vessel

806

Vergaserdruckbeälter

814

Loop heat pipe device

816

Evaporator battery

818

Condenser battery

820

steam line

822

condensate line

830

Degassing and filling pipe

900

Diving heat pipe

902

outer tube

904

open end of 902

906

closed end of 902

908

inner tube

910

first open end of 908

912

second open end of 908

Claims (11)

1. A device for generating combustible product gas from carbonaceous feedstocks through allothermal steam gasification, comprising

   - a pressurized gasifier (2) including a gasifier pressure vessel (6), a supply means (8) for the carbonaceous feedstocks, a steam supply (10), and a product gas extracting line (12),

   - an external heat source (4), and

   - a heat transport means (14) comprising a plurality of heat pipes whereby heat is transported, with the aid of a heat transfer medium undergoing a phase change, from the external heat source (4) into the gasifier (2),

   wherein the heat pipes (14) have a heat-releasing side (18) disposed inside the gasifier (2) and a heat-absorbing side (16) disposed inside the external heat source (4),
   characterized in that
   the plurality of heat pipes (14) are loop heat pipes (500; 600; 701, 702; 814), the heat-absorbing side (16; 516; 616; 716; 816) and the heat-releasing side (18; 518; 618; 738; 818) of which are connected to each other via a liquid line (22; 522; 622; 722; 822) for liquid heat transfer medium and via a steam line (20; 520; 620; 720; 820) for vaporous heat transfer medium,
   the liquid and steam lines of individual loop heat pipes (500; 600; 701, 702; 814) are combined into common liquid and steam lines (22; 522; 622; 722; 822; 20; 520; 620; 720; 820) and
   the common liquid lines (22; 522; 622; 722; 822) and the common steam lines (20; 520; 620; 720; 820) are physically separate lines.
2. The device according to claim 1, characterized in that a hydrogen separating means (30; 532; 730; 830) is disposed in the liquid lines (22; 522; 622; 722; 822) of the loop heat pipes (500; 600; 701, 702; 814).
3. The device according to any one of the preceding claims, characterized in that the heat transport means (14) includes at least one loop heat pipe (500; 600; 701) pumped by means of a capillary structure (528; 628).
4. The device according to any one of the preceding claims, characterized in that the heat transport means (14) includes at least one immersed loop heat pipe (900).
5. The device according to any one of the preceding claims, characterized in that
   the heat transport means (14) includes at least one first loop heat pipe (701) comprising a steam line (720) for vaporous heat transfer medium and a liquid line (722) for liquid heat transfer medium, wherein steam line and liquid line are disposed in a physically separate manner,
   the heat transport means (14) includes at least one second heat pipe (702),
   the two heat pipes (701, 702) each have a heat-releasing side (718, 738) and a heat-absorbing side (716, 736),
   the heat-absorbing side (716) of the at least one first loop heat pipe (701) is disposed inside the external heat source (4), and
   the heat-releasing side (718) of the at least one first loop heat pipe (701) is thermally integrated into the heat-absorbing side (736) of the at least one second heat pipe (702), and
   the heat-releasing side (738) of the at least one second heat pipe (702) is disposed inside the gasifier pressure vessel (706).
6. The device according to claim 5, characterized in that the at least one second heat pipe (702) is a pulsed loop heat pipe which comprises a common steam/liquid line (740) and which is disposed inside the gasifier pressure vessel (706).
7. The device according to claim 6, characterized in that the common steam/liquid line (740) has a meander-type shape, in that the heat-releasing side (738) of the pulsed loop heat pipe (702) is disposed in the upper range of the gasifier pressure vessel (706), and in that the heat-absorbing side (736) is disposed in the base area of the gasifier pressure vessel (706).
8. The device according to any one of the preceding claims, characterized in that the external heat source (4) is a fluidized bed combustion chamber.
9. The device according to any one of the preceding claims, characterized in that the gasifier (2) is configured as a fluidized bed gasifier.
10. The device according to claim 8 or 9, characterized in that the gasifier pressure vessel (6) is connected to the fluidized bed combustion chamber (4) via a material lock (24) for pyrolysis residues.
11. The device according to claim 9 or 10, characterized in that fluidized bed gasifier (802) and fluidized bed combustion chamber (804) are disposed inside a common vessel (805).

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