EP2574742A1 - Device and method for condensation of steam from ORC systems - Google Patents

Abstract

The device has a module for condensation, where the module has an inlet and one or multiple pipelines (12), such as horizontally disposed pipes. A liquid separator is provided for separating the condensed liquid. A liquid collector is provided for collecting the separated condensed liquid. The liquid separator is provided before or at the inlet or after the pipeline. The liquid collector has a branch pipe, which is formed to divert a part of the separated condensed liquid from the condensation device. An independent claim is included for a method for condensation of vapor expanded in an expansion machine of a thermal power plant to a condensed liquid, particularly oily liquid.

Description

Field of the invention

The present invention relates to an apparatus and a method for the condensation of expanded in an expansion machine of a thermal power plant steam to a condensed, especially oily liquid

State of the art

The operation of expansion machines, such as steam turbines or positive displacement machines, such as reciprocating engines, using the Organic Rankine Cycle (ORC) process to produce electrical energy through the use of organic media, such as low evaporation temperature organic media, at the same temperatures as compared to water As a working medium in general have higher evaporation pressures, is known in the art. ORC systems represent a realization of the Rankine cycle in which, for example, electric energy is obtained in principle via adiabatic and isobaric changes in the state of a working medium. About evaporation, expansion and subsequent condensation of the working medium in this case mechanical energy is recovered and converted into electrical energy. In principle, the working medium is brought to a working pressure by a feed pump, and it is supplied to it in a heat exchanger energy in the form of heat, which is provided by a combustion or a waste heat flow available. From the evaporator, the working medium flows via a pressure pipe to an expansion machine or expansion machine of an ORC system, where it is expanded to a lower pressure. Subsequently, the expanded working medium vapor flows through a condenser, in which a heat exchange between the vaporous working medium and a cooling medium takes place, after which the condensed working medium is returned by a feed pump to the evaporator in a cyclic process.

The advantageousness of the use of Organic Rankine Cycle systems, in particular for the use of low-temperature heat, is well known. Especially in the field of relatively small power of the systems, for example in the range of 1 kW to about 50 kW, displacement machines are often used. These positive displacement machines may be piston engines. These machines require a certain amount of oil as lubricant in the machine. In the machine cycle, the oil in the circulation usually with the working medium with. In this case, the oil in particular also passes through the condenser of the system, which may result in an increased pressure loss during the condensation.

As state of the art capacitors from refrigeration and air conditioning, so-called condenser, are considered. In refrigeration, steam is condensed after compression at high pressure and relatively high temperature. The vapor has a relatively high density when entering the condenser. In order to obtain sufficiently high flow velocities, the steam volume flow is divided into a few pipe runs, which then pass through the individual levels of the condenser.

The condenser typically has an inlet and an outlet between which the ducts are arranged, in which the majority of the condensation takes place. Often, the tubes of the pipelines are arranged substantially horizontally. In a horizontal arrangement, the condensate further requires a driving force to reach the outlet of the condenser. For this purpose, the steam and the condensate must flow in DC. The condensate is thereby "blown" by the steam through the pipes. Energy is needed to transport the condensate by means of the steam. This manifests itself in a pressure drop within the condenser, whereby the pressure loss between the entry of the vapor into the condenser and the exit of the condensate is measurable. The pressure loss increases quadratically with the flow velocity of the steam at turbulent flow. Furthermore, the pressure loss depends on the viscosity of the liquid. In particular, the pressure loss increases with the viscosity of the liquid.

The above-mentioned oil in the displacement machines is used, for example, for the lubrication of flanks and bearings. In other words, it is about the lubrication of sliding and / or rolling components. The oil participates in the cycle of the machine. It is also possible to speak of a fluid that represents a mixture of the actual working medium of the machine and the oil or an oil-containing liquid.

The oil passes the expansion machine together with the steam and leaves the expander, for example, as an oil-steam spray or oil-vapor mist. It is therefore already present in particular at the entrance of the condenser as a liquid in the vapor. That is, while the greater part of the vapor is still present as vaporous working medium, a part of the vapor is already at least partially interspersed with oil-containing liquid droplets at or even before the inlet / inlet into the condenser. Initially, that is, near the inlet of the condenser little condensate is still deposited, the proportion of oil in this condensate is very high. It's practically almost pure oil. Accordingly, the viscosity of this deposited liquid is very high. As a result, very unfavorable, very high pressure losses can be generated for the capacitor. These pressure losses can in turn affect the performance of the entire plant, especially the Expansion machine, which ultimately reduces the efficiency of the entire process. This can lead to performance losses in the double-digit percentage range.

Compared to the air conditioning technology, the working medium is condensed at lower pressures, especially in ORC systems. So the vapor has a lower density here. It is achieved at similar mass flows and condensation rates a significantly larger volume flow. With the same design of the capacitor, this means a greater velocity of the steam and thus significantly greater pressure losses.

An improvement of the condensation and a reduction of the pressure losses can be aimed at by a more frequent distribution of the steam volume flow. However, the problem of oil or oily or oily liquids in the system and the associated pressure drops remains.

In view of the above outlined problem in the prior art, the present invention seeks to provide an apparatus and a method for condensing expanded in an expansion engine of a thermal power plant steam expansion machine of a thermal power plant, whereby the disadvantages outlined above can be mitigated or even eliminated and whereby the associated performance losses can be reduced or even overcome.

Description of the invention

The above object is achieved by a device for condensation of steam expanded in an expansion machine of a thermal power plant to a condensed, in particular oil-containing liquid, having the features of patent claim 1. Likewise, this object is achieved by a corresponding method for the condensation of expanded in an expansion machine of a thermal power plant steam to a condensed, in particular oil-containing liquid, according to the patent claim 12.

The invention provides an apparatus for condensing steam expanded in an expansion engine of a thermal power plant into a condensed, especially oil-containing, liquid, comprising: a module for condensing, wherein the module for condensing comprises an inlet and one or more pipelines, for example substantially horizontally disposed tubes, comprises; a liquid separator for Separation of the condensed liquid; and a liquid collector for collecting the separated condensed liquid.

The deposition of the particular oil-containing liquid from the expanded steam can thus be done in the device, whereby the oily liquid from the device for condensation can get out and the deposit on the pipe inner walls of the one or more pipe runs can be significantly reduced.

A liquid is to be understood here as meaning a liquid which at least partially comprises fractions of oil and fractions of a working medium of the thermal power plant.

As a pipe train here is at least one substantially horizontally extending pipe to be understood, at the end, for example, a pipe bend sits, which can deflect a fluid flow through the pipe by a fixed angle, for example 180 degrees. But there are also other angles for the elbows possible, for example, 90 degrees. Typically, multiple ducts can be connected together.

In the apparatus as described above, the liquid separator may be provided in particular before or at the inlet and / or after the first pipe run; wherein the liquid receiver comprises a branch pipe, which is designed to branch off at least part of the separated, condensed liquid from the device.

The device for condensation, so the condenser, can be placed at some distance or even spatially separated from the expansion machine. As a result, considerable lengths of connecting pipes of, for example, several meters to tens of meters can occur. It may be possible, even before the inlet of the condenser, that is, for example, immediately before a connecting pipe initiates the expansion of the expansion machine expanded steam into the apparatus for condensation, to provide a liquid separator. That is, this liquid separator may be provided substantially immediately before or at the inlet of the device. The latter can already separate condensed liquid from the connecting tube in the connecting tube so that this liquid or at least part of this liquid does not even enter the device. Accordingly, such a liquid separator can also be provided immediately after the inlet of the device. Additionally or alternatively, a liquid separator may typically be provided after the first pass of the module of the device. As a result, at least part of the oil-containing liquid can also be deposited as early as possible so that as little as possible oil-containing liquid passes through the device or even to the outlet of the device.

In the apparatus as described above, the liquid separator may include a siphon disposed between the branch pipe and the liquid collector.

By using a siphon, ie a U-tube bend, a defined flow direction of the fluid, ie the mixture of vapor and liquid, can be supported within the device. Typically, the liquid is in the siphon. Due to the height difference of the liquid column, essentially only liquid and substantially no vapor flow through the siphon up to a maximum pressure difference.

In the apparatus as described above, the liquid separator may include a steam trap having a pipe and a float disposed between the branch pipe and the liquid collector. The steam trap can in particular derive condensate formed, for example, when the system starts up in the apparatus. This can for example be done by a float, which is provided in the steam trap. The float opens in the presence of condensate, the liquid discharge. This can be derived in the device "stagnant" condensate. After draining the condensate, ie after emptying the trap, the float closes the liquid drain again.

It is also possible that one device comprises a liquid trap with a siphon and another liquid trap with a steam trap. Also, further combinations of several siphons and / or steam traps are possible.

A siphon typically requires no other moving parts. The pressure drop across the siphon should be greater than or equal to the pressure loss across the remaining path through the device.

The apparatus as described above may further comprise a cooling device configured to cool the separated condensed liquid prior to passing it into the liquid receiver.

Where the oily liquid is deposited, the separated liquid may have a temperature exceeding, for example, a desired predetermined value of the temperature of the liquid already collected in the liquid receiver. An entry of this separated, warmer liquid in the liquid collector could therefore cause an undesirable increase in temperature of the liquid in the liquid collector. By cooling the point of the discharge, that is essentially the branch pipe, such a temperature entry into the liquid collector can be avoided become. In this case, for example, in addition to an additional cooling device and a volume of air flow of the device, the capacitor can be used.

In the apparatus as described above, the liquid collector may be a food container or the one or more tubes may additionally be at least partially formed as a liquid collector.

So it can be a separate food container, the liquid that is deposited from the device record. This may, for example, then be connected to a pump, such as a feed pump, to pump liquid back to the circuit.

It is likewise possible, in addition or as an alternative, to provide at least parts of one or more of the pipelines as fluid collectors. As a result, it is possible to dispense with a food container for specific applications or, in addition to a food container, a reservoir of liquid / working medium can be provided, for example if otherwise only a small food container can be provided. The device can thereby be designed so that a sufficiently large amount of liquid / working medium in the lower part of the pipe runs of the device fits. The fluid level in the corresponding pipe trains can vary depending on the load condition. Since heat transfers / transfers can also occur in the area of the supply of liquid / working medium, additional supercooling can take place. As a result, for example, cavitations can be avoided even in dynamic operation.

In the apparatus as described above, the liquid separator may be a first liquid separator; the apparatus may further comprise at least one further pipe train and with at least one further liquid separator corresponding to the first liquid separator, the further liquid separator being arranged after the at least one further pipe train and being formed at least one further part of the separated, condensed liquid from the Branch device.

It is thus possible, in the presence of several pipe trains, after a first liquid separator, which may be provided as described above, for example, before or after a first pipe, to provide further liquid separator for further pipe trains. That is, in or after another or after further pipe runs again another part of liquid can be deposited to further reduce the pressure losses.

In the apparatus as described above, there may further be provided at least one further condensation module corresponding to the module as described above; and further there may be provided a manifold disposed in front of the liquid separator configured to combine the expanded vapor after passage through the one or more passages and to pass it on to the further module for condensation.

For example, a condensation device, capacitor, as described above, may include multiple modules. These modules can also be called levels. The modules are typically similar. Already at the inlet of the device, the steam volume flow for the first module can be divided. Before and / or after the first module, as described above, a liquid separator may be provided. Uncondensed steam may be passed or transported to the next module. For this purpose, a manifold may be provided, which summarizes the expanded steam and forwards to the next module. The collecting line can be arranged before or after the liquid separator.

In the apparatus as described above, the manifold may have a single central port with a conduit for passing the expanded vapor or may have a plurality of separate conduits for passing the expanded vapor.

The manifold can thus, for example, summarize the expanded steam in a single line and forward. From this line, the liquid separation can then take place. Or the manifold may be connected to a plurality of conduits, each of which forwards a portion of the vapor to the next module. The manifold then directs, for example, substantially condensed liquid from the lines for liquid separation.

In the apparatus as described above, the manifold may have a downward slope on the liquid separator.

By a gradient, the gravitational force can be used to achieve a better discharge of the liquid. The inclination may typically be a predefined slope of a few degrees. The value of the inclination can be predetermined so that the liquid can flow independently for liquid separation.

The present invention also provides a thermal power plant with a condensation device as described above.

The device as described above can thus be used in a thermal power plant, for example a plant that uses a Clausius Rankine cycle or an Organic Rankine cycle.

The present invention further provides a method of condensing steam expanded in an expansion engine of a thermal power plant into a condensed, especially oil-containing, liquid having a module for condensation, the module for condensing comprising one or more pipe runs, for example, with substantially horizontally disposed pipes ; and a liquid separator, comprising the steps of: dividing a steam flow rate on the one or more passages; Depositing at least part of the condensed, in particular oil-containing, liquid before and / or after the first pipe run; Discharging the separated, condensed liquid; and collecting the separated, condensed liquid.

For the method according to the invention, what has already been said above applies.

The method as described above may further comprise the step of cooling the separated condensed liquid before it is collected.

The method as described above may further comprise the step of depositing at least one further portion of the condensed, especially oil-containing, liquid after at least one further pipe run.

In the method as described above, at least one further module for condensation corresponding to the module described above may be provided, and the method may further comprise the steps of: combining the expanded steam after passing through the one or more pipe trains; and passing the combined, expanded vapor to the further module for condensation.

Further features and exemplary embodiments and advantages of the present invention will be explained in more detail with reference to the following drawings.

It is understood that these exemplified embodiments do not exhaust the scope of the present invention. It is further understood that some or all of the features described below may be combined with each other in other ways.

Brief description of the figures

• FIG. 1 represents a schematic diagram of a conventional thermal power plant.
• FIG. 2 FIG. 3 illustrates a schematic diagram for a division of a steam volume flow in a conventional condenser of a thermal power plant. FIG.
• FIG. 3 schematically shows the deposition of condensed liquid in a device for condensation according to an embodiment of the present invention.
• FIG. 4 schematically shows the deposition of condensed liquid in a device for condensation according to another embodiment of the present invention.
• FIG. 5 shows a detailed illustration of the deposition of condensed liquid according to the embodiment, which in FIG. 3 is shown.
• FIG. 6 shows a further development of the device for condensation, in FIGS. 3 and 5 is shown.
• FIG. 7 shows a further development of the device for condensation, which on the in FIGS. 3 and 5 shown embodiment.
• FIG. 8 shows schematically the distribution of a vapor volume flow at the entrance of a module of a device according to the present invention.
• FIG. 9 shows schematically a further embodiment of the distribution of a vapor volume flow at the entrance of a module of a device according to the present invention.
• FIG. 10 schematically shows a branch element, as shown in the FIGS. 8 and 9 Application can be found.

Detailed description

The FIG. 1 shows purely schematically a conventional thermal power plant. This can be a Clausius Rankine plant or an Organic Rankine plant. The system can in principle work with direct evaporation or with an intermediate circuit (not shown here).

FIG. 1 shows an evaporator 1, which may be, for example, a heat exchanger or a heat transfer element. Heat from a heat source (not shown) may be supplied to the evaporator 1, for example, by a fluid such as flue gas. The supply of heat is exemplified by the arrow 1 A indicated. In the evaporator 1, the heat is transferred from the fluid to a working fluid / working fluid. The working medium is supplied to the evaporator 1, for example, by a feed pump 2. In the evaporator 1, the working medium, for example, completely evaporated. It can also be vaporized by flash evaporation after the heat transfer element. The now practically completely evaporated working fluid is supplied via a suitable pressure line an expansion machine / relaxation machine 3. In the expansion machine 3, the pressurized steam of the working medium can be expanded. By relaxation, a generator 4 can be suitably driven.

The expansion machine 3 may be a positive displacement machine, for example a piston engine. The relaxed working medium is forwarded to the expansion machine 3 to a capacitor 5. In the condenser 5, the working medium condenses. Resulting heat of condensation can by another heat exchanger, which is provided with the reference numeral 5A, or directly to a cooling medium, for. Air, be discharged. The heat exchanger 5A may also be a cooling element. The now liquefied working fluid is passed to the feed pump 2 and passed from there back to the evaporator 1. It is understood that additional pumps may be used in the system, if not shown here.

The FIG. 2 shows purely schematic a conventional interconnection of steam inlets and pipe trains in air conditioning. In the left half of the FIG. 2 is a vapor stream, or vapor 10, shown at an inlet of a condenser. An inlet line is indicated by the reference numeral 11. By the reference numeral 12, a pipe is indicated. The tube 12 consists of an upper tube 12A and a lower tube 12B. The two tubes 12A and 12B are connected to a pipe manifold 15. By way of example, the pipe bend 15 is designed as a "180-degree pipe bend". That is, the pipe bend 15 diverts the steam flow by 180 degrees. A plurality of ducts 12 are shown before the steam is directed to another module of the condenser or, when already fully condensed, to a manifold (not shown), as indicated by reference numeral 14.

In the right half of the FIG. 2 Another option of interconnection in steam inlets is shown. Here are several divisions shown by a plurality of tubes 16, which forward the flow of steam to another module of the capacitor or already complete condensation to a manifold (not shown here). You can also see the tubes 16 as piping, however, have no elbows.

The FIG. 3 shows an embodiment of the present invention. Here are the same elements already in the Figures 1 or 2 were introduced, provided with the same reference numerals.

In the FIG. 3 For example, a vapor stream 10, for example a vaporous working medium which has been expanded in an expansion engine of a thermal power plant, is passed into a device for condensation. In particular, the expansion machine may be a positive displacement machine. In particular, the vaporous working medium, the steam, 10 contain a proportion of oil, which may be present for example as an oil-vapor spray.

FIG. 3 shows by way of example a tube 12 with an upper tube 12A and a lower tube 12B. The two tubes 12A and 12B are connected to a pipe manifold 15. Behind the pipe bend 15, a branch element 17 is provided. The branch element 17 may be a branch pipe. In essence, condensed liquid can already be branched off in the branching element 17 after the first pipe run 12 or even the first part of the first pass 12A. Vaporous working medium, which is not diverted at the branch element 17, is passed via the line 12 B to a feed container 23 and condensed on the way to the feed container 23. In the food container 23, a supply of liquid 23 F is provided. It is understood that this liquid 23F in turn means a mixture of the oily liquid and the actual working medium of the thermal power plant. The advantage of the shown branching with the branching element 17 is that already condensed liquid can be deposited as early as possible, wherein first separated liquid can contain a high proportion of liquid containing oil.

It is understood that the restriction to essentially only one tube 12 shown is purely schematic and only serves to explain the principle. It is also possible to provide further pipe passages which substantially correspond to the pipe train 12. The FIG. 3 shows after the branch element 17 a siphon 19. In the siphon 19 is due to the height difference of the liquid column up to an upper maximum pressure substantially only liquid and no vapor. That is also in FIG. 5 outlined in more detail.

The FIG. 4 shows a further development of the device for condensation according to the present invention. Again, the illustration is purely exemplary and schematic to understand. Similar to in FIG. 3 For example, the restriction to only one pipe 12 with elements 12A and 12B and pipe elbow 15 is to be understood in order to explain the principle. It is of course possible to provide further passages 12 in the device. In the FIG. 4 is like in the FIG. 3 a branch element 17 is shown. The branching element 17 is designed to be similar to the embodiment shown in FIG FIG. 3 is shown to divert condensed liquid, ie condensate from the pipe train 12. Vapor-like working medium, which is not branched off at the branching element 17, is forwarded via the line / pipe 12 B of the pipe train 12 to the feed container 23. In the food container 23, in turn, a liquid level 23F is drawn.

The FIG. 4 shows a steam trap element / steam trap 21 instead of the siphon 19 as shown in FIG FIG. 3 is used. The steam trap 21 may, for example, have a float element / float (not shown here). The float can be lifted in the presence of condensate in the steam trap, for example by the condensate itself, whereby condensate can be discharged. For example, the different specific gravity of liquid and steam is used to separate the liquid from the steam. In principle, it is also possible to use steam traps based on the Bernoulli principle, that is to say on the different dynamic response to changes in the flow velocity in the case of compressible or incompressible fluids. It is also conceivable to use steam traps based on the Venturi effect.

The FIG. 5 shows a detailed representation of the embodiment, as shown by FIG. 3 already described. The siphon 19 receives from the device, such as a pipe 12, branched, separated liquid. The U-tube-shaped siphon 19 is filled to a height h _F with liquid. The siphon 19 consists essentially of two U-tube-shaped interconnected halves. The right half is designated by the reference numeral 19R. The left half is designated by reference numeral 19L. The two halves of the siphon 19 are arranged substantially vertically. The left half 19L leads to a height H where another tube 19K bends substantially horizontally. The tube 19K carries the liquid 19F from the siphon 19 into the food container 23. In the food container 23, the liquid level 23F is as high as the height H. A pressure difference Δp at the siphon 19, ie on the right half 19 R of the siphon 19, is calculated from the product of the density p of the liquid Gravitational acceleration g and the height difference h of the liquid columns. At usual pressure differences, for example, height differences of a few 10 cm up to about 1 m arise. But it can also be larger or smaller height differences possible. Above the height h _F , that is to say in the region of the height h, essentially only steam is located in the right half 19R of the siphon 19; below the height h _F there is essentially only liquid.

The FIG. 6 shows a further development of the basis of FIGS. 3 and 5 sketched embodiment. The same elements are provided with the same reference numerals. After the branch element 17 shows the FIG. 6 a further pipe 18, before the liquid branched off at the branch element 17 to the siphon 19 is passed. The further pipe train 18 is substantially flowed through with branched liquid. Furthermore, a cooling device for cooling the liquid can be used in this area. In FIG. 6 is a cooling flow, for example, an air flow, indicated by the arrows 18F. Due to the condensation heat occurring in the device for condensation, the device is often provided with a cooling. Also, a heat exchanger may be used to warm up another liquid / fluid by means of the heat from the condensing apparatus. Analog can be moved here for the separated, branched liquid. It is also possible (not shown here) to integrate the pipeline after the branching element 17 into a heat transfer packet (not shown here) of the device, that is to say, for example, the heat exchanger already mentioned above. Thus, it is possible, on the one hand to control the temperature of the branched liquid and in particular to lower. On the other hand, this heat can also, instead of dissipatively discharged into the environment, be used for heat transfer to other fluids.

The FIG. 7 shows a further development of the basis of FIGS. 3 and 5 or 6 outlined embodiments. In the FIG. 7 is again a device similar to the device in FIG FIG. 5 shown. In particular, the device has in FIG. 7 in turn, a branch element 17 and a siphon 19. However, the guided in the siphon 19 liquid is now not passed into a food container, but in another pipe 32. The considerations for the pressure differences, which are based on FIG. 5 were discussed, analogously.

The further pipe 32 is connected to a further pipe bend 15 with the pipe 12. Again, it should be understood that purely by way of example two ducts 12 and 32 have been chosen for illustration, and that it is also possible to use a larger number of ducts. The pipe 32 consists of the pipes 32A and 32B and a pipe bend 35. At a junction 37, the siphon 19, that is, the left half 19L of the siphon, opens into the pipe 32B at the end of the pipe bend 35. The tube 32 is substantially filled with liquid, that is, the tube 32 as part of the device for condensation serves as a liquid collector. In the pipe 32, a supply of liquid 32 F is stored. The liquid can be transported further from the pipe train 32 via a further pipe bend 37, which diverts substantially by 90 degrees. Thus, the tubing 32 replaces a food container or may be used in addition to a food container (not shown). During operation, a sufficiently large quantity can be stored in the typically lower region of the device, in this case the pipe train 32. Depending on the load condition, this stock can vary. At high live steam pressures, high density steam fills the evaporator as well as the piping and piping. In low load operation more liquid is needed, which can be removed from the supply, for example, from the pipe 32.

The FIG. 8 shows a breakdown of the vapor flow rate at the inlet of the device according to the present invention. The vapor stream, steam, 10 is conducted in a conduit 11. The guided in the line 11 steam is split on lines 16. In this case, the number of eight lines 16 shown is by no means to be understood as limiting, but should be understood purely by way of example. The steam conducted through the lines 16, which in turn, as already described above, may be a mixture of the actual working medium and an oil-containing fluid, for example an oil-containing liquid, is combined by means of a common manifold 25. The line 25 directs the combined vapor to a branch element / branch 27. From there, at least a portion of the vapor can be passed via the line 29 to another module (not shown here) of the condensation device. The further module can have a distribution of the steam volume flow, as exemplified by the module in FIG FIG. 8 is shown.

In the FIG. 8 For example, condensate / condensed liquid can be passed via line 28 to a liquid separator (not shown here). It is also possible that the line 29 is also provided with a liquid separator (not shown here). The liquid separator may in both cases be of the type as described of the FIGS. 3 to 7 discussed. The in the FIG. 8 selected representation shows the relationships of the elements shown in a plane. That is, a spatial arrangement of the elements is not shown. In particular, a liquid separator can also spatially behind the plane shown in the FIG. 8 be arranged.

The FIG. 9 shows a further development of the distribution of the steam flow rate at the inlet of the device for condensation, as described above. Similar to in FIG. 8 a vapor stream 10 is directed into a conduit 11 which divides the vapor stream into similar conduits 16. Again, it should be understood that there must be no restriction to only eight lines, 16. There may be more as well as fewer lines. In contrast to the embodiment, which in FIG. 6 is shown, each of the lines 16 has a branch element / a branch 27.1, 27.2, 27.3, 27.4, 27.5, 27.6, 27.7, and 27.8. Each line 16 is connected via its respective branch element 27.1, 27.2, 27.3, 27.4, 27.5, 27.6, 27.7, and 27.8 with a manifold 25. The branch elements 27.1 - 27.8 are illustrative in FIG FIG. 10 as discussed below. About the manifold 25 can, similar to the in FIG. 8 shown embodiment, condensed liquid are deposited, approximately in the direction as indicated by the arrow 28 A. This liquid can in turn be directed to a liquid separator (not shown here). The liquid separator may be of the type described with reference to FIGS. 3 to 7 explained.

Each of the lines 16 has behind the respective branch element 27.1, 27.2, 27.3, 27.4, 27.5, 27.6, 27.7, and 27.8 corresponding further lines 29.1, 29.2, 29.3, 29.4, 29.5, 29.6, 29.7 and 29.8. Via these corresponding further lines 29.1, 29.2, 29.3, 29.4, 29.5, 29.6, 29.7 and 29.8, steam which has not yet condensed in the lines 16 can be conducted into a further module (not shown here) of the device. In this case, the further module again correspond to the module shown here. As already on the basis of FIG. 8 mentioned, also shows the illustration in FIG. 9 the relationships of the elements shown in a plane. In other words, one can speak of a projection on the drawing plane. A possible spatial arrangement of the elements is not shown. In particular, a liquid separator, as in the FIGS. 3 to 7 is shown, also spatially behind the plane shown in the FIG. 9 be arranged.

In the FIG. 10 By way of example, a branch element 27 is shown, which in the FIGS. 8 or 9 is shown. This in FIG. 10 shown branch element can in the FIGS. 8 and 9 shown elements 27, 27.1-27.8 correspond. Here, by way of example, a pipeline is shown, the pipe 16 in the FIGS. 8 and 9 can correspond. In the pipeline 16, a vapor stream is passed. The direction of flow of the vapor stream is indicated by the arrow 16R. The steam flow is in the range 27R in FIG. 10 curved by 180 degrees and passed through the pipe 29 on. The pipe 29, the lines 29 and 29.1-29.8 of FIGS. 8 and 9 correspond. Here, the curvature is selected by 180 degrees by way of example, it could also be a curvature of 90 degrees or another angle can be selected. At this point it should be mentioned again that in the FIGS. 8 and 9 selected projection does not show this curvature. The continuous flow of steam after the bend is indicated by the arrow 29R. Due to the inertia of the liquid entrained in the vapor stream 16R, this liquid follows the sharp curvature, here 180 degrees, not or at least not completely and can pass through the pipeline 25, for example by gravity. The corresponding flow direction of the liquid is represented by the arrow 25R. The pipe 25 then leads to a separator, as in the FIGS. 3 to 7 is shown.

Claims (15)

Apparatus for condensing steam expanded in an expansion machine of a thermal power plant into a condensed, in particular oil-containing liquid, comprising: a module for condensation, wherein the module for condensation comprises an inlet, and one or more pipe runs, for example, with substantially horizontally arranged pipes; a liquid separator for separating the condensed liquid; and a liquid collector for collecting the separated, condensed liquid. Apparatus according to claim 1, wherein the liquid separator is provided before or at the inlet and / or after the first pipe run; wherein the liquid receiver comprises a branch pipe, which is designed to branch off at least part of the separated, condensed liquid from the device. The apparatus of claim 2, wherein the liquid separator comprises a siphon disposed between the branch pipe and the liquid collector. The apparatus of claim 2, wherein the liquid separator comprises a steam trap having a conduit and a float disposed between the branch pipe and the liquid collector. The apparatus of at least one of claims 1-4 further comprising a cooling device configured to cool the separated condensed liquid prior to passing it into the liquid receiver. Device according to at least one of claims 1-5, wherein the liquid collector is a food container or wherein the one or more pipe trains are additionally formed as a liquid collector. Apparatus according to any one of claims 2 to 6, wherein the liquid separator is a first liquid separator; with at least one further pipe run and with at least one further liquid separator which corresponds to the first liquid separator, wherein the further liquid separator is arranged after the at least one further pipe run and is designed to branch off at least one further part of the separated, condensed liquid from the device. Device according to one of claims 1 - 7, comprising at least one further module for condensation, which corresponds to the module according to claim 1; and further comprising a manifold disposed in front of the liquid separator configured to combine the expanded vapor after passage through the one or more passages and to pass it on to the further module for condensation. The apparatus of claim 8, wherein the manifold has a single central port with a conduit for passing the expanded vapor or has a plurality of separate conduits for carrying the expanded vapor. Apparatus according to at least one of claims 8 or 9, wherein the manifold has a slope on the liquid separator. Thermal power plant with a device for condensation according to at least one of claims 1-10. A method of condensing expanded steam in an expansion engine of a thermal power plant into a condensed, especially oil-containing, liquid, comprising a module for condensation, wherein the module for condensing comprises one or more pipelines, for example with substantially horizontally arranged pipes; and a liquid separator, with the steps: Dividing a steam volume flow onto the one or more pipe trains; Depositing at least part of the condensed, in particular oil-containing, liquid before and / or after the first pipe run; Discharging the separated, condensed liquid; Collecting the separated, condensed liquid. The method of claim 12, further comprising the step of cooling the separated condensed liquid before it is collected. The method of claim 12, further comprising the step of separating at least one further portion of the condensed, in particular oil-containing liquid, after at least one further pipe run. Method according to at least one of claims 12-14, comprising at least one further module for condensation, which corresponds to the module according to claim 12, with the steps: Combining the expanded steam after passing through the one or more pipe passes; and Forwarding the combined, expanded steam to the further module for condensation.

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