CH713961A2 - Method of transferring the heat and heat exchanger contained in a gas therefor. - Google Patents

Abstract

A method for heat exchange of heat contained in a fluid, wherein as the fluid, an indirectly heated, infrared radiation emitting gas is used, which is fed via a feed line (2) to the heat exchanger (1) and in this through an absorber space (3), and wherein at least one surface (7) absorbing the heat of the gas whose infrared radiation absorbing surface is provided in the absorber space (3), and further adjusting the mass flow and the temperature of the gas and forming the at least one surface (7) absorbing the heat exchange in that, in operation, the ratio ψ of the heat flow flowing through it through absorption relative to the total heat flow flowing through it is ≥ 0.6. This makes it possible to realize a simple and inexpensive heat exchanger.

Description

Description: The present invention relates to a method according to the preamble of claim 1, a heat exchanger according to the preamble of claim 10 and a method of operating a furnace according to the preamble of claim 16.

Solar power plants such as solar tower power plants operate on an industrial scale, such as. The solar power plant Ivanpah in California, which has a rated output of 392 MW, directly generates steam in the temperature range of over 750 ° K at 170 bar by directing the concentrated solar radiation onto tubes of a tower-mounted heat exchanger in which the steam is generated. Salt heat accumulators allow steam to be used during periods of good sunshine.

For a higher efficiency increasingly solar tower power plants are provided which heat via a volumetric receiver air to over 1000 ° K, up to 1500 ° K and, today tentatively, against 2000 ° K and above. The heated air is then used via heat exchangers to generate steam or process heat. It is also foreseeable that, for example, such solar tower power plants are also designed for a performance range in the manner of Ivanpah.

On the other hand, it is known that with small, local stand-alone arrangements with a dish receiver (but which can also be combined into clusters) also temperatures above 1000 ° K, even beyond 2500 ° K addition with a power in the field of kilowatt hours. The use of such heat sources is also interesting.

The nature of the matter, the heat generated in the receiver of solar systems radiant heat is removed at temperatures of about 1000 ° K in the form of heated air from the receiver. The use of the heat thus transported in turn requires the use of downstream heat exchangers. The central for a heat exchanger, good heat transfer into the medium to be heated causes a significant construction cost, usually associated with a significant flow resistance in the heating medium.

Accordingly, it is the object of the present invention to provide an improved method for transferring the heat contained in a gas and an improved heat exchanger.

This object is achieved by a method according to the characterizing features of claim 1, by a heat exchanger with the characterizing features of claim 11 and an operating method with the characterizing features of claim 14.

By using an infrared radiation emitting gas which is fed into an absorber space of a heat exchanger, its heat can be radiated, i. transmitted via its infrared radiation, with sufficient power to an absorbing surface of the heat exchanger. This eliminates process steps and arrangements for optimized heat transfer by convection, which are expensive to produce due to the largest possible ratio of convective surfaces to the volume of the heat-emitting gas and generate a significant flow resistance.

Characterized in that a heat emitting infrared radiation gas is guided into an absorber space of a heat exchanger, the desired heat transfer can take place predominantly absorptive, which allows to design the heat exchanger according to simple.

Characterized in that an oven is provided with a supply line for indirectly heated, radiating gas in the infrared range, this can in place of radiation via heat-emitting combustion products (gases and especially soot, which also radiates in the visible frequency range and thus makes the flame visible ) are operated with the indirect heated gas, which allows to operate a low-cost retrofitted stove pollutant-free or to spare the operation of pollutants eliminating facilities and to continue to use existing infrastructure with minor modifications.

With respect to, the absorbent surface, the ratio ψ of the heat flow through absorption over the total heat flow flowing through them> 0.6, the advantages shown above are particularly clear.

Infrared radiating gases can be heated in particular by a receiver according to the unpublished CH patent application 00 627/17, which in contrast to the known volumetric receivers a gas absorptively heated. Such gases, which are heatable by blackbody radiation radiation, in turn emit in the infrared region and are then, in addition to conventionally heated infrared emitting gases, ideally available for use in the present invention.

Preferred embodiments have the features of the dependent claims. The invention will be explained in more detail with reference to FIGS. It shows:

1a shows schematically a heat exchanger according to the invention in cross-section,

FIG. 1b shows a schematic view from the outside onto the absorber space of a heat exchanger in the manner of that of FIG. 1a, FIG.

1c schematically shows a modified embodiment of the heat exchanger of FIGS. 1a and 1b in the view of FIG. 1b,

2a shows the scheme of a system with a heat storage and a heat exchanger according to the invention,

2b shows the steps of the inventive method for transferring the heat contained in a gas,

Fig. 3a shows schematically a view of the absorber space of an inventively operated, conventional reformer

3b shows the steps of the inventive operating method, and

4 shows a receiver according to the generation of indirectly heated, infrared radiant gas.

Fig. 1a shows schematically a cross section through an embodiment of a heat exchanger 1 according to the present invention. A heat-emitting, indirectly heated (see below) gas passes via a supply line 2 in accordance with the arrow direction in an absorber chamber 3, flows through this to a discharge line 4, through which the gas leaves the heat exchanger 1 again, wherein in the shown Embodiment, the supply line 2, the absorber chamber 3 and the discharge line 4 form an arrangement for the transport of gas through the heat exchanger 1 therethrough.

An indirectly heated gas according to the present invention has been heated in front of the heat exchanger 1, wherein its heat to be exchanged in the absorber chamber does not originate from its own combustion - in contrast to a flue gas produced in the absorber room, i. a combustion product, the heat to be exchanged is created by a combustion process acting in the absorber space.

Between the supply line 2 and the absorber chamber 3 is a manifold 5 for the gas flowing through the absorber chamber 3, such that it flows through the entire diameter of the absorber chamber 3 through this. A collector 6 for the gas leads this to the absorber chamber 3 in the derivative 4. The manifold 5 and the collector 6 are also components of the arrangement for transporting gas through the heat exchanger 1. Distributor 5 and collector 6 can be made by a person skilled in the specific case be designed suitable.

The absorber chamber 3 is cylindrical in the embodiment shown, the gas passed through is a radiant in the infrared region gas or a gas mixture having radiating gases in the infrared range.

In the absorber chamber 3 are axially extending to this, here designed as tubes 7 lines arranged, which in turn are fed by a manifold 8 for fluids to be heated and open into a collector 9 for the heated fluids. Again, the manifold 8 and the collector 9 can be suitably designed by the skilled person in the concrete case. The surfaces of the tubes 7 form infrared radiation absorbing surfaces. If only one tube 7 is provided, at least one absorbent surface is present, otherwise several, in particular in the case shown here, with a bundle of tubes 7 (see Figures 1b and 1c).

The heat exchanger 1 and thus the absorber chamber 3 by flowing, warm, radiating in the infrared gas radiates accordingly on the surfaces of the tubes 7, heated them, so that a heat exchange between the infrared radiating gas and the absorbent surfaces of the tubes 7 takes place, which in turn they heat the fluid flowing through them. The tubes thus form a surface intended for heat exchange via infrared radiation - in contrast, for example, to the surface of the wall 10 of the absorber chamber 3 which, despite its insulation, causes an undesirable heat loss of the gas which does not serve the intended heat exchange.

In the infrared range radiating gases are, for example, CO2, water vapor, CH4, NH3, CO, SO2, HCl, NO, and NO2.

In general, it is the case that gases emit electromagnetic radiation in the characteristic frequency bands for them, wherein the radiation intensity or the power of the radiation per area in W / m2 depends on the temperature.

For solid bodies, the model of the (ideal) radiating black body ("black body radiation"), whose radiation intensity in W / m2 over the entire frequency spectrum depends on its temperature, with the maximum intensity with higher temperature of the black body against shifts higher frequencies and at the same time increases with the fourth power of the temperature.

Already the real solid body has collapses of the radiation in its frequency spectrum compared to the frequency spectrum of the (ideal) black body - for a certain real solid body, the radiation intensity drops in some of these characteristic frequencies, in some cases considerably.

In this regard, have more extreme properties gases which radiate only in individual frequency bands, which may be in the ultraviolet range, in the visible range or in the infrared range. If a gas radiates at a comparatively low temperature, for example in the ultraviolet range, its radiation intensity, i. the radiated power, small, it radiates at the same temperature in the infrared range, its radiation intensity is high. According to the invention, this property of the gases is utilized in today technically controllable temperature ranges of up to 2500 ° K or above (in the coming years, these temperature ranges will shift upwards) in the

Infrared radiation emitting gases are used, in which case their radiation intensity is considerably and thus efficiently used for heat exchange.

As a result, in addition to the advantages given below a very simple, yet efficient heat exchanger can be formed, which transfers the heat from a radiant in the infrared gas to another medium. Among other things (see below) eliminates the usual design effort for the convective heat transfer, which occurs by contact and correspondingly causes a large heat exchanging area in relation to the volume of the heat-emitting gas.

The Applicant has found that the structural advantages of heat exchange by emission / absorption have an effect above all when the ratio ψ of the heat exchange exchanged by absorption with respect to the total heat flow (exchanged by absorption and convection) is> 0.6, that is, the proportion of absorption to the proportion of convection outweighs. In this case, a heat exchange by convection even with the simplest realization of the heat exchanger is unavoidable and, in the sense of heat exchange, also quite welcome. However, the smaller the proportion of convection, the greater the constructive simplification or less the expense for the production and possibly the maintenance of the heat exchanger itself. The person skilled in the specific case, the determining parameters (the infrared radiant gas or the gas mixture, its temperature, pressure and flow rate, the geometry of the absorber space and the at least one absorbing surface, etc.) to suitably adjust the ratio ψ> 0.6 and realize the advantages of the invention.

At this point it should be noted that the embodiment shown with five tubes 7 in the diameter of the cylindrical absorber chamber 3 is purely exemplary to understand the circumstances. In principle, any number of conduits passing through the absorber space may be provided in any configuration and course (i.e., not axially extending) of any desired configuration, provided that the proportion of absorptive heat input still predominates, i.e., the amount of absorptive heat absorbed. the ratio ψ> 0.6 is realized.

According to the invention there results a heat exchanger with an arrangement for the transport of heat releasing heat in the heat exchanger by infrared radiation, which has an absorber space with at least one surface provided for the heat exchange via infrared radiation, the heat exchanger having a supply line for indirectly heated, Heat releasing gas is formed and the absorber space and the at least one absorbing surface are formed such that in operation at a predetermined mass flow and a predetermined temperature of the heat-releasing gas in the absorbent surface, the ratio ψ of the heat flow flowing through absorption over the whole flowing through heat flow> 0.6.

Fig. 1b shows a view from the outside to the absorber chamber 3 of the heat exchanger 1 of Fig. 1a. Visible are the cylindrical wall 10 of the absorber chamber 3, and the tubes 7, which are arranged in a spatial bundle extending adjacent to each other and so fill the cylindrical absorber space 3 approximately uniformly in the embodiment shown. For procedural reasons, a different arrangement can be provided., The tubes 7 are heated during operation of the heat exchanger 1 (Fig. 1a) of the axially flowing, symbolized by the arrows 15, infrared radiating gas (for example, steam) over its length substantially absorptively become. In the tubes themselves flow here in the same direction, as indicated by the arrows 15, for example, components for the (catalytic) production of syngas or other chemically reacting substances, or simply a fluid which the exchanged heat about in the sense of a secondary circuit can lead to a suitable location, as may be the case with process heat, for example.

In the case of the production of syngas, the arrangement shown in FIGS. 1a and 1b represents a reformer with heat exchange realized according to the invention. High temperatures are required for syngas production, for example an average tube temperature of 1200.degree. In the present case, in the sense of a simple embodiment, an outer pipe diameter of 130 mm, an inner pipe diameter of 100 mm and a pipe length of 12 m here (ie a height of the absorber chamber 3 of 12 m) are assumed, the heat flow q into a pipe 7 100 kW / m2 of the pipe surface (which, of course, depends on the particular process taking place in the pipe). It is further assumed that the distance of the tubes from the center to the center of the six-fold outer diameter of the tubes amount, ie 780 mm, and the distance of an outermost tube to the wall 10 of the absorber chamber 3 the half, so 390 mm. Thus, the absorber space 3 has a diameter of 3.9 m. The partial pressure of the infrared-radiating gas amounts to 1 bar, whereby the water vapor flowing through in the assumed example has the ambient pressure of 1 bar (thus no non-radiating gases are mixed in).

An approximate calculation by the applicant gives, under the above assumptions, the values for the ratio ψ shown in the table below on the basis of two examples, with different temperatures of the available, indirectly heated gas:

Tin (inlet temperature of the gas) 1700 ° K 1580 ° K

Tout (gas outlet temperature) 1340 ° K 1460 ° K V (flow velocity) 7.1m / s 21.1m / s ψ (absorption / absorption + convection ratio) 0.97 0.94

TGas Average gas temperature for the flash estimate 1520 ° K 1520 ° K

Thus, the heat exchange according to the invention by the heat exchanger 1 shown (Fig. 1 a) can be realized. It should be noted that uniform conditions have been assumed in the absorber space 3 under the flashover calculation, ie the effects on the wall 10 and the real temperature profile from the inlet to the outlet of the tubes 7 (ie along the axis of the cylindrical absorber space 3) have been neglected. This does not change the fundamental feasibility.

Depending on the reaction (as mentioned above: for example, a syngas reaction) or the needs of the heat-receiving fluid prevails in the lines (tubes 7), an overpressure of, for example, 40 bar, with a higher pressure of, for example, 100 bar may be desirable , Then, the wall thickness of the corresponding pressure test lines to be formed (pipes 7) increase accordingly, which in turn is detrimental to the heat flow into the line, so for example, the temperature of the infrared radiant gas must be increased to the desired heat flow (in the present example, 100 kW / m2).

According to the inventive concept of the absorber space 3 (or the heat exchanger 1, Fig. La), the guided through the absorber space 3 lines 7 are compactly bundled, for example so that the absorber space 3 is limited by a tubular wall 10. This in turn makes it possible to design the absorber space 3 comparatively easily at higher or high pressure, since then, in a tubular wall area, pressure-related tangential stresses which are substantially simpler to construct occur. If overpressure prevails in the absorber chamber 3, the pressure difference to the internal pressure of the pipes (pipes 7) decreases. Accordingly, the wall thicknesses of the lines can be reduced and thus the heat flow into the lines can be improved.

Resulting in a heat exchanger according to the invention with an arrangement for the transport of heat in the heat exchanger by infrared radiation heat releasing gas having an absorber space with at least one intended for heat exchange via infrared radiation surface, characterized in that the heat exchanger with a supply line for indirectly heated, heat-releasing gas is formed and the absorber space and the at least one absorbing surface are formed such that in operation at a predetermined mass flow and a predetermined temperature of the heat-releasing gas in the absorbent surface, the ratio ψ of the heat flowing therethrough Absorption over the total heat flow flowing through it is> 0.6.

PA 11 It is further apparent that preferably the at least one absorbent surface is formed by a number of lines, preferably pipelines, and wherein the lines are arranged as a bundle extending through the absorber space, and space between the lines operable by-passing, infrared emitting radiant gas is provided.

PA 9/13 It is further shown that preferably the absorber space pressure test, for a pressure of the heat-emitting gas of> 5 bar, preferably> 10 bar, more preferably> 20 bar and very preferably> 50 bar is designed.

A rough estimate under the above assumptions for the dimensions of the tubes 7 and the heat flux of 100 kW / m2 results for an operating pressure in the absorber chamber 3 of 10 bar when water vapor is used as the infrared emitting gas:

Tin (inlet temperature of the gas) 1620 ° K

Tout (outlet temperature of the gas) 1340 ° K V (flow rate) 3.8 m / s ψ (ratio absorption / absorption + convection) 0.9

TGas average temperature of the gas for the rough estimate 1480 ° K

The emissivity s of a gas increases with its pressure p and the thickness L of the radiative gas layer (path length), it holds that ε = f (p, L). The dimensionless curve of the emissivity shows the shape of an inverted hoke-stick, with a steep slope at low path length (L) and a weak slope at a certain distance from the radiation-receiving wall, ie greater path length. With increasing pressure so can the distances from pipe 7 to reduce pipe 7, in the present example to 390 mm, which leads at an operating pressure in the absorber chamber 3 of 10 bar to a diameter of 1.95 m - that is half the diameter of the absorber space 3 opposite the case with an operating pressure of 1 bar. These smaller dimensions support the pressure-resistant design of the absorber space-which in turn facilitates even higher pressures in this. The skilled person can in concrete cases, for example, based on the optimum internal pressure in the lines 7 and the wall thickness (heat transfer) determine an operating pressure in the absorber chamber 3 in consideration of the cost of pressure safety and heat transport into the lines 7 inside.

It should be noted at this point that in the above quantitatively described examples, the ratio ψ in the range of 0.9 and above - among other things, because of the high temperatures of the indirectly heated gas of about 1500 ° K. The inventive ratio of> 0.6 but according to the findings of the applicant also achievable with temperatures of indirectly heated gas of> 1000 ° K, for example 1300 ° K or, according to the above examples of more than 1500 ° K. PA 8/18 It follows that, according to the invention, the indirectly heated gas preferably has a temperature of> 1000 ° K, preferably> 1300 ° K and particularly preferably> 1500 ° K.

Fig. 1c shows a view from the outside to the absorber chamber 3 of another embodiment of the heat exchanger 1 of Fig. 1 a. As can be seen in Fig. 1 b, the cylindrical wall 20 of the absorber chamber 21, and the tubes 7, which are arranged in a spatial bundle extending adjacent to each other and so fill the cylindrical absorber space 21.

Compared to the embodiment of Fig. 1b walls 22 are additionally provided, which are arranged between the tubes 7. During operation, these walls 22, or their surfaces 23, are heated by the infrared radiation gas through its infrared radiation until a temperature equilibrium sets in, since the walls 22 in turn lose energy due to (real) blackbody radiation. It is to be noted that the wall 20 of the absorber space already acts in this sense, but the walls 22 are additional, separate walls with additional surfaces 23 separate from the wall of the absorber space 20 ,

It is mentioned above that the curve of the emissivity e has a first region with a strong increase and a second region with a weak increase, whereby of course the transition is not sharp. This means that the energy radiated into a wall first grows strongly with increasing thickness (path length L) of the radiating gas layer, then becomes increasingly weaker after a thickness dependent on the gas, among other things (but still increases, after all). This can be interpreted as meaning that the gas is self-isolated, in other words, a gas zone away from the wall is less able to deliver energy to the wall through its radiation. If a further wall is now arranged in a suitable area, which likewise heats up and then emits (real) black body radiation, it will reach the wall to be heated virtually unhindered (for these frequencies, at least in the frequency ranges in which the infrared-emitting gas does not absorb eliminates the insulating effect) and thus heat them unimpaired. As a result, this increases the heat flow q flowing through the absorbing surfaces of the conduits. The person skilled in the art can arrange such a further wall in a specific case at a distance here to the absorbing surfaces (here: the row of tubes 7), which lies in the range of the weak increase of the emissivity s of the infrared-radiating gas, and further so that the intensity the black body radiation of the further wall at the absorbing surfaces is greater than the intensity of the infrared radiant gas layer cut off by the further wall (additional intensity due to the cut path length L).

It should be noted at this point that the lines or pipes 7, although in turn emit black body radiation, but at a relatively low temperature, since they are due to the flowing in them, to be heated fluid heat sinks. The above-mentioned further walls reach an equilibrium temperature above the temperature of the lines 7 or the at least one absorbing surface in the absorber space, so that in the mentioned, suitable arrangement, the heat radiation to the at least one absorbing surface can be improved.

PA 12 In summary, a number are arranged in the absorber space in this distributed lines, each with an absorbent surface and at least one in operation by the heat donating gas in turn heatable further surface provided which irradiates the absorbing surfaces in operation by black body radiation, in such the heat flow q is increased by absorption through the absorbing surfaces.

Fig. 2a shows schematically the arrangement of a system 30 for the use of solar energy with a novel heat exchanger 1, a heat storage 31 and a receiver 32 for (concentrated) solar radiation and a photovoltaic receiver 37th

In the receiver 32, a suitable fluid is heated by incident solar radiation 33, for example, to a temperature above 1000 ° K, or to about 2000 ° K, passes via a line 34 into a heat storage 35 and via a line 36 back into the Receiver 32, so that via the corresponding circuit via the lines 34, 36 of the heat accumulator 35 can be loaded with heat. A photovoltaic system or a photovoltaic receiver 37 generated by the incidence of sun rays 33 stream, which provides heat of the desired temperature in the heat storage 31 via power lines 37 and an electric heater 38, in particular, in the heat storage a uniform upper temperature in Areas at, for example, 2000 ° K. By the heat of the heat accumulator 31, an infrared radiant gas is then heated and passed through the lines 39, 40 in the circuit through the heat exchanger 1.

Preferably, however, an infrared radiating gas is already heated by the receiver 32, which is sent via lines 41,42 in the circuit through the heat exchanger 1, i. E. this is optionally supplied directly, depending on whether the heat storage 38 is to be loaded or not.

In the heat exchanger 1, a fluid is heated, which flows through the lines 43, 44 therethrough. It may, as mentioned above, generally to process heat of any kind to educts / products for a chemical

Reaction or to act steam to drive a steam turbine (electricity). An advantage of the system 30 shown is, for example, in a simple temperature control of the heat exchanger 1 supplied infrared radiating gas: for cooling the circuit (directly via receiver 32 or the heat storage 35) such, not heated gas can be mixed, for heating is the electric heater 38 available, which in principle can generate very high temperatures as such, even if the radiation intensity of the sun is below the threshold, which would require the receiver 32 for the desired very high temperature. Another advantage of the system shown is that the infrared-emitting gases can be performed with relatively simple design effort under pressure in the circuit shown, the heat transfer in the heat exchanger 1 is also feasible with little effort.

The system shown can thus be operated with only one heat source for the indirectly heated gas (solar receiver 32 or heat storage 38) or in combination of these heat sources, if desired in addition to the heater 38th

PA 14 It can be seen that in the embodiment shown, the arrangement for transporting the heat-emitting gas is operatively connected (e.g., in a circuit) to a heat source indirectly heating the gas, which preferably has a heat storage. PA 15 Next, the heat source at least one of the heat-producing means solar receiver, heat storage or a preferably electric, particularly preferably powered by pho-voltaic current heating. PA 6/7 For the process according to the invention, it is apparent that the gas emitting infrared rays is preferably conducted in a circuit enclosing the heat exchanger in which the gas is indirectly heated, and more preferably in this circuit before the heat exchanger, a heat storage is provided , In addition, it results that for the indirect heating at least one of the heat sources receiver, heat storage or heating, preferably an electric heater, which is particularly preferably powered photovoltaic is used. The receiver 32 can be designed as a receiver of a solar tower power plant, s. to the description of FIG. 4 below. The heat accumulator 35 can be formed in accordance with WO 2012/027 854, wherein the bulk material can consist of Al 2 O 3 (the salt heat accumulators customary today are not suitable for temperatures according to the present invention, since the salt then decomposes). Photovoltaic solar plants are known in the art.

2b shows the steps of the inventive method for heat exchange. In step 45, a gas is selected as the heat-releasing gas, the heat to be exchanged has not arisen from its combustion, and which has been heated in front of the heat exchanger, that is an indirectly heated gas, and emits the infrared radiation to heat over this radiation to exchange. PA 3 Preferably, such gases are heteropolar gases. Suitable are CO2, water vapor, CH4, NH3, CO, SO2, HCl, NO, and NO2 or a mixture of these gases. Non-radiating gases can be mixed in the specific case, if this is indicated for procedural reasons, but within the limits indicated by the ratio ψ.

In step 46, the gas (or gas mixture) are selected for the specific case, the mass flow (flow velocity and pressure) and its temperature with the respective formation of the absorbent surfaces in the absorber chamber mutually tuned such that the ratio ψ of the exchange serving heat flow through absorption to the total exchanged heat flow> 0.6, ie the absorption over the convection outweighs. Preferably, the absorbent surfaces are formed by the surfaces of conduits 7 passing through the absorber space 3 (Figures 1a to 1c), more preferably a (spatial) bundle of conduits being provided since the gas can flow well around it. In the lines, the fluid to be heated is passed. PA 4 The absorbent surface may also be formed by a wall portion of the absorber space, or by one or more conduits (preferably piping) for a fluid to be heated by the heat exchange. PA 2 The higher the ratio ψ is chosen, e.g. > 0.7, preferably> 0.8 and particularly preferably> 0.9, the easier it is to form the heat exchanger. If the gas is passed through the absorber space under overpressure (PA 9 preferably> 5 bar, preferably> 10 bar, particularly preferably> 20 bar and very preferably> 50 bar), the heat exchanger according to the invention can be made particularly compact.

In step 47, the prepared heat exchange is carried out by the selected gas or gas mixture is passed under the predetermined operating parameters through the absorber space with the suitably formed absorber surfaces.

PA 6 It is apparent that the gas emitting the infrared rays is preferably conducted in a circuit enclosing the heat exchanger, in which the gas is indirectly heated, and wherein a heat accumulator is preferably provided in this circuit upstream of the heat exchanger. In the case of solar heating of the gas, this can thus also be made available outside the times of intense solar radiation. PA 7 Furthermore, at least one of the heat sources receiver, heat storage or heating, preferably an electric heater, which is particularly preferably fed photovoltaic, preferably used for the indirect heating, which results in an advantageous independence of the intensity of each prevailing solar radiation.

3a shows schematically the absorber chamber (or heat chamber) 50 of a conventional reformer operated according to the invention. Reforming is used for chemical transformation in process engineering and is often catalytically carried out as an endothermic process. In particular, "tubular reformers" are known, i. Reforming plants in which the substances to be processed are passed through pipes in a heat chamber, so that the chemical

Process required heat through the tubes can be supplied to the substances. The heat is generated by burners, the combustion products often contain radiating soot in the infrared range and also emitting gases in the infrared range.

The heat chamber, which is an oven, is rectangular - elongated. Along the center line of the heating chamber, the tubes are arranged in a row one behind the other, so that on both sides of the tubes there is an elongate partial chamber into which the flames produced by the burners act. In the "top fired" principle, the flames protrude from above into the subchambers; in the "terraced wall" principle, the burners are arranged on steps on the outer walls of the subchambers, and in the "side fired" principle, the burners are arranged distributed over the outer walls. The disadvantage of this principle is that the temperature over the length of the tubes is difficult to control (high temperatures at the location of the flame, then strong temperature drop) and that sufficient space for the undisturbed development of the flame must be present. Finally, this principle also implies that in a heating chamber, the tubes are arranged in rows to form an efficient relationship between the area of the flames and the area of the absorbent surfaces created by the tubes.

According to the invention, a conventional reformer is now provided with a heating chamber 50, in which tubes 51 are arranged one behind the other, in series, with a supply line for indirectly heated, radiating in the infrared range gas and the combustion device is not used, i. for the intended operation of the furnace, and thus of the reformer, shut down or expanded. The gas flows according to the arrows 52 through the sub-chambers 53, 54 on both sides of the row of tubes 51 (and of course also between the tubes) and heats them by its infrared radiation.

For a rough estimate, it is again assumed that syngas is to be produced in the reformer, for which purpose, for example, an average tube temperature of 1200 ° K is again required. As with Fig. 1b, an outer pipe diameter of 130 mm, an inner pipe diameter of 100 mm and a pipe length of 12 m here (ie a height of the heat chamber 50 of 12 m) is assumed, the heat flow q into a pipe 7 into 100 kW / m2 of the pipe surface should be. The temperature of the outer wall is 350 ° K, the convective heat transfer coefficient h 10 W / (m2K) which at an ambient temperature of 300 K results in a total heat flow q (by convection and heat radiation) of 0.89 kW / m2 due to the insulation.

For example, in the furnace of the conventional reformer, methane is burned in air under ambient pressure (CH 4 + 2 O 2 + 8 N 2 -> CO 2 + 2H 2 O + 8 N 2) and this conventional operation is the operation according to the invention with indirectly heated gas, here water vapor under ambient pressure , compared with, results after a rough estimate of the applicant:

Parameters of conventional furnace indirectly heated gas

Tin (temperature of the flame / inlet temperature of the gas) 2050 ° K 1580 ° K

Tout (outlet temperature of the gas) 1330 ° K 1340 ° K V (flow velocity) 3.6 m / s 11.2 m / s

TGas average temperature of the gas for the 1550 ° K 1460 ° K rough calculation p (partial pressure of the infrared radiating gas - 0.27 bar 1 bar N2 does not emit infrared) ψ (ratio absorption / absorption + convection) 0.95 0.97 [0061] A conventional reformer, which generates the required heat through an oven, can thus be operated via the operating method according to the invention with indirectly heated gas emitting in the infrared range. It is advantageous that the indirectly heated gas in the circuit (with or without heat storage, see Fig. 2a) can be performed, in contrast to the furnace, in which the flue gases are not reusable. In addition, if the indirect heating by a solar receiver takes place, the environmental footprint can be significantly reduced, without the need for major investments on the part of the reformer. Finally, it is also true here that in the absence of a necessarily very hot flame over the length of the tubes a more uniform and therefore more favorable heat distribution is to be expected.

3b shows the steps of the inventive method for operating a furnace. In step 55, a furnace or reformer is selected to operate in place of combustible materials with indirectly heated infrared radiating gas.

In step 56, the combustion assembly is shut down or removed and set up a supply line for indirectly heated, infrared radiating gas.

In step 57, analogous to step 46 of Fig. 2b, the infrared radiating gas or gas mixture is selected and set its operating parameters to achieve a ratio of ψ> 0.6.

In step 58, the intended operation of the furnace is taken up with the passage of the gas. Again, heteropolar gases are preferred. As mentioned above, CO2, water vapor, CH4, NH3, CO, SO2, HCl, NO, and NO2 or a mixture of these gases are suitable. Non-radiating gases can be admixed by the person skilled in the specific case, if this is indicated for procedural reasons, but in the limits indicated by the ratio ψ.

According to the invention there results a method for operating a furnace which has a flow path for gases to be combusted for generating the useful heat, wherein an absorber space is present in the flow path and has at least one surface provided for receiving the heat exchange via infrared radiation and wherein the combustion assembly of the furnace is not used and provided with a supply line for indirectly heated, infrared-radiating gas, such that this gas can be operably carried in and out of the gas-to-be-combusted flow path and the furnace In operation indirectly heated, radiating in the infrared range gas is supplied with a mass flow and a temperature, so that in the at least one absorbing surface, the ratio ψ of the heat flow through absorption to the total heat flow> 0.6. PA 17 Preferably, the furnace is switched into a circuit of indirectly heated gas, which preferably includes a heat storage.

In an embodiment, not shown in the figures, the heat exchange takes place in the inventive heat exchanger not via lines that carry the exchanged heat receiving fluid, but directly to a material present in the absorber space, which is heated by absorption of the infrared radiation, For example, metals for a heat treatment or to produce a molten metal or, for example, for the production of glass by producing a melt consisting of the starting materials. PA 5 This results in a method in which preferably an absorbent surface is formed by a material to be heated.

Fig. 4 shows schematically a receiver 60 according to the still unpublished Swiss patent application CH 00 627/17 for the indirect heating of a radiant in the infrared gas or gas mixture. The receiver 60 has a heating region 61, which has an optical opening 62, for example a quartz window, and an absorber 63, wherein an absorption space 65 is provided between the quartz window 64 and the absorber 63, corresponding to the arrows drawn from the infrared-radiating gas to be heated from right to left, ie against the absorber 63, flows through. For this purpose, the transport device 66 of the receiver 60 has inlet ports 67 for heat-transporting medium, which are arranged around the quartz window 64 and lead into the absorption space 65, and a central outlet port 68 behind the absorber 63.

The absorber 63 is formed as a black body radiation assembly with reduced convection, i. E. it has a radiation absorbing surface 70 arranged in the path of the incident solar radiation 69, which is designed such that it is operatively heated due to the solar radiation 69 incident on the surface 70 and then into the absorber space 65 via its surface 70 in accordance with infrared radiation 71 emits.

Thus, the absorber 63 gives its heat output to a substantial part in the form of infrared radiation in the absorber chamber 65, where the incoming gas to him already absorptively heated before it reaches him.

As mentioned above, real structure only radiates approximately as the ideal black body does. In the present case, a "black body radiation arrangement" is understood to mean that the incident solar radiation 69 is absorbed to the greatest possible extent on the surface of the absorber (ie in principle penetrates only slightly into the absorber, in contrast to the volumetric absorber), so that this surface is high heated and thereby radiates in the manner of a black body with the relevant high temperature in the absorber space 65. The majority of the radiation emitted into the absorber space 65 is at temperatures of the absorber 63 to 2000 ° K (or even higher) in the infrared range, i. in opposite to the visible light lower frequencies.

An elaborate, in particular for volumetric receiver provided, staggered in depth absorber structure that absorbs their depth of incident radiation according to their depth by being at least partially scattered in the interior and is increasingly absorbed after multiple reflection, thus eliminating. This eliminates the often occurring with such absorber structures, complex thermal problems.

In this case, the absorber 63 is formed konvektionsarm, i. easy to flow through without increased convective properties for the heat exchange of importance. It also eliminates the training for maximized convection of the flowing medium, i. the necessary structure for the most efficient heat exchanger structure compared with the volume of heat exchanging medium medium large surface, which is expensive to produce at high efficiency and has a significant pressure drop of the medium flowing through the result in operation.

At this point it should be noted that a certain convective heat transfer at the absorber 63 is of course inevitable, especially in the embodiment shown in FIG. 4, since this forms a wall section of the absorption space 65 there. The corresponding convective heat transfer to the heat-transporting gas is, of course, desirable in terms of heat transfer - however, the outlet temperature Tout of the heated gas should be based to a significant extent on absorption below, thus allowing a simplified design of the receiver 60.

The simplified structure of the absorber 63 opens, among other things, as mentioned above, the possibility for a more stable operation, for example in thermal terms (temperature distribution over the absorber 63), which leads to an improved industrial suitability of the receiver.

The result is a receiver with a heating area for the heating of a heat-transporting medium having an optical opening for sunlight, and arranged in the path of the incident sunlight, the sunlight-absorbing absorber, with a transport arrangement for the transport of the medium through the heating region, wherein the absorber is designed as a black body radiation assembly with reduced convection and the transport arrangement for the transport of a gas as a heat-transporting medium.

In this case, the absorber designed as a black body radiation arrangement with reduced convection is preferably designed for the flow through of the heat-transporting gas and is also preferably opposite the optical opening 64.

Further, as the heat-transporting medium, an infrared-absorbing gas or gas mixture which absorbs in frequency bands of the infrared region is used. Such gases are, for example, heteropolar gases, preferably CO2; Water vapor, CH4, NH3, CO, SO2, HCl, NO, and NO2. The use of such gases ultimately results in a greenhouse effect that can be utilized or utilized by the receiver 60, since these gases are highly transparent to the visible light, which thus essentially reaches the absorber 63, but little to hardly for the infrared radiation of the absorber are transparent, so that they heat so absorptively before the absorber 63. It should be noted here that real gases do not absorb visible light or infrared radiation uniformly over all frequencies or are transparent, but vary greatly in particular in frequency bands specific for a particular gas. In addition, the absorption decreases with the distance from the radiation source. This is referred to above with regard to the absorption or transparency of radiation from "highly transparent" or from "little to little transparent".

The absorber 63 may be formed as a perforated plate, preferably as a double perforated plate or as a simple, flat lattice structure. In the case of the perforated plate, a hole pattern is distributed over the extent thereof, so that the heat-transporting gas can easily flow through, but enough surface of the perforated plate for the absorption of the incident solar radiation and the infrared reflection is given in the absorber space. The person skilled in the art can easily optimally determine the hole pattern in the specific case. Likewise, in the case of a lattice structure or double perforated plate with two parallel plates, then the holes of one plate relative to those of the other plate are offset from each other, such that despite convective low passage of the heat exchange gas the absorption space a possible continuous, radiant Surface of the absorber is facing. A suitable material for the absorber is silicon carbide SiC.

Since absorbing gases in the infrared range also radiate in the infrared range, the above-mentioned gases for solar heating in the receiver (preferably, but not exclusively) of a solar tower power plant and then be provided for the inventive heat exchange. It is also possible that a receiver according to FIG. 2 is used in Dish concentrators, since temperatures of up to 2000 ° K and above can be reached there, too, because of the two-dimensional concentration of solar radiation.

Claims (18)

claims 1. A method for heat exchange of heat contained in a fluid, characterized in that a indirectly heated, infrared radiation emitting gas is used as the fluid via a feed line (2) to the heat exchanger (1) and in this through an absorber space (3) therethrough wherein in the absorber space (3) at least one surface for absorbing the heat of the gas whose infrared radiation absorbing surface is provided, and wherein the mass flow and the temperature of the gas adjusted and the at least one heat exchange absorbing surface is formed such that in Operation is the ratio ψ of the heat flow flowing through them by absorption against the total heat flow flowing through it> 0.6. 2. The method of claim 1, wherein the ratio ψ> 0.7, preferably> 0.8 and more preferably> 0, 9 is. 3. The method of claim 1, wherein the gas comprises a heteropolar gas, preferably CO2, water vapor, CH4, NH3, CO, SO2, HCl, NO, and NO2 or a mixture of these gases. 4. The method of claim 1, wherein the at least one surface is formed by lines for a medium to be heated, preferably pipes (7) or by at least one wall portion of the absorber space. 5. The method of claim 1, wherein an absorbent surface is formed by a material to be heated. 6. The method of claim 1, wherein the infrared rays emitting gas in a the heat exchanger (1) enclosing circuit is performed, in which the gas is heated indirectly, and preferably provided in this circuit before the heat exchanger (1) a heat storage (31) becomes. 7. The method of claim 1 or 6, wherein for the indirect heating at least one of the heat sources receiver (32), heat storage (35) or heating, preferably an electric heater (38), which is particularly preferably photovoltaic powered is used. 8. The method of claim 1, wherein as a fluid indirectly to a temperature of> 1OOO ° K, preferably> 1300 ° K and more preferably> 1500 ° K heated gas is used. 9. The method of claim 1, wherein the infrared radiation emitting gas is conducted under a pressure greater than the ambient pressure through the absorber space (3), preferably> 5 bar, preferably> 10 bar, more preferably> 20 bar and more preferably> 50 bar. 10. Heat exchanger for carrying out the method according to claim 1, with an arrangement for the transport of heat in the heat exchanger by infrared radiation heat releasing gas having an absorber space (3) with at least one provided for the heat exchange via infrared radiation surface, characterized in that the heat exchanger ( 1) with a feed line (2) for indirectly heated, heat-releasing gas is formed and the absorber space (3) and the at least one absorbing surface are formed such that in operation at a predetermined mass flow and a predetermined temperature of the heat-releasing gas in the absorbing surface, the ratio ψ of the heat flow flowing through it by absorption against the total heat flow flowing through it> 0.6. 11. A heat exchanger according to claim 10, wherein the at least one absorbing surface by a number of lines, preferably pipes (7), is formed, and wherein the lines (7) are arranged as a bundle, which extends through the absorber space (3), and space is provided between the conduits for operable, inflowing, radiant infrared emitting gas. 12. A heat exchanger according to claim 10, wherein in the absorber space (3) a number in this distributed lines are arranged, each having an absorbent surface and at least one in operation by the heat donating gas in turn heatable further surface (23) is provided, which in operation by Blackbody radiation irradiated the absorbing surfaces, such that the heat flow is increased by absorption by the absorbent surfaces. 13. Heat exchanger according to claim 10, wherein the absorber chamber (3) pressure test, for a pressure of the heat-emitting gas> 5 bar, preferably> 10 bar, more preferably> 20 bar and very preferably> 50 bar is designed. 14. Heat exchanger according to claim 10, wherein the arrangement for transporting the heat-emitting gas is operatively connected to a gas indirectly heating the heat source, which preferably has a heat storage (31). 15. Heat exchanger according to claim 14, wherein the heat source of at least one of the heat-producing means solar receiver (32), heat storage (31) or a preferably electric, particularly preferably powered by photovoltaic power heating (38). 16. A method for operating a furnace having a flow path for generating the useful heat to be combusted gases, wherein in the flow path, an absorber space (50) is present which has at least one provided for receiving the heat exchange via infrared radiation surface, characterized in that the furnace combustion device is not used and it is provided with a supply line for indirectly heated infrared radiating gas, such that this gas can be operably carried in and out of the flow path for gases to be combusted, and indirectly to the furnace during operation heated, radiating in the infrared range gas is supplied with a mass flow and a temperature, so that in the at least one absorbing surface, the ratio ψ of the heat flow through absorption to the total heat flow> 0.6. 17. The method of claim 15, wherein the furnace is connected in a circuit of indirectly heated gas, which preferably includes a heat storage (31). 18. The method of claim 16, wherein the indirectly heated gas has a temperature of> 1000 ° K, preferably> 1300 ° K and more preferably> 1500 ° K.