阅读说明：本技术 蒸发干燥器和其运行方法 (Evaporative dryer and method for operating the same ) 是由 G·卡斯佩斯 H·哈费曼 于 2018-05-14 设计创作，主要内容包括：本发明涉及一种用于干燥颗粒的蒸发干燥器(1),具有：过程室(10)过程室具有至少一个产品入口(11)用于将待干燥的颗粒供送到过程室(10)中并且具有产品出口(12)用于将经干燥的颗粒从过程室(10)导出；布置在该过程室(10)内的换热器(20),具有用于加压蒸气作为热蒸气进入到换热器(20)中的至少一个入口(21、211)和从换热器(20)离开的至少一个冷凝物出口(22、222),其中,所述至少一个冷凝物出口(22、222)与卸压容器(30)连接,其中,在该卸压容器(30)上附接有至少一个泵(40),该泵将卸压蒸气从卸压容器(30)泵出并且导送至热蒸气。(The invention relates to an evaporation dryer (1) for drying particles, comprising: process chamber (10) the process chamber has at least one product inlet (11) for feeding particles to be dried into the process chamber (10) and a product outlet (12) for leading the dried particles out of the process chamber (10); a heat exchanger (20) arranged in the process chamber (10), having at least one inlet (21, 211) for the pressurized steam to enter the heat exchanger (20) as hot steam and at least one condensate outlet (22, 222) from the heat exchanger (20), wherein the at least one condensate outlet (22, 222) is connected to a pressure relief container (30), wherein at least one pump (40) is attached to the pressure relief container (30), pumps the pressure relief steam out of the pressure relief container (30) and conducts it to the hot steam.)

1. An evaporation dryer (1) for drying particles, having

-a process chamber (10) having at least one product inlet (11) for feeding particles to be dried into the process chamber (10) and a product outlet (12) for leading dried particles out of the process chamber (10),

a heat exchanger (20) arranged in the process chamber (10),

-the heat exchanger has at least one inlet (21, 211) for pressurized vapour as hot vapour in the heat exchanger (20) and at least one condensate outlet (22, 222) from the heat exchanger (20), wherein,

-the at least one condensate outlet (22, 222) is connected with a pressure relief vessel (30),

characterized in that at least one pump (40) is attached to the pressure relief container (30), which pump pumps pressure relief vapor out of the pressure relief container (30) and leads it to the hot vapor.

2. The evaporative dryer according to claim 1, characterized in that the pump (40) is configured as a steam jet pump with an operating steam connection (41) and at least one partial flow of the hot steam is applied on the operating steam connection (41).

3. The evaporative dryer according to claim 1 or 2, wherein the pump (40) is configured as a mechanical suction pump.

4. The evaporative dryer according to any of the preceding claims, wherein the pressure in the pressure relief vessel (30) is set to a pressure below the pressure of the hot vapour.

5. The evaporative dryer according to one of the preceding claims, characterized in that the heat exchanger (20) is configured in multiple stages and the first stage (23) of the heat exchanger (20) can be supplied with a mixed vapor of hot vapor and pressure-relief vapor and the second stage (25) can be supplied with hot vapor.

6. Evaporative dryer according to claim 5, characterized in that the two above stages (23, 25) are provided with separate condensate containers (33, 35) which are coupled with the pressure relief container (30).

7. The evaporative dryer according to claim 6, wherein the condensate container (33, 35) is coupled with the pressure relief container (30) via a regulating valve (53, 55).

8. An evaporative dryer according to any preceding claim, wherein the condensate container (33, 35) has a pressure level that is at or lower than the magnitude of the pressure of the hot vapour.

9. The evaporative dryer according to any of the preceding claims, characterized in that it is configured as a fluidized-bed evaporative dryer with an annular process chamber (10) and is provided with a conveyor (16) for feeding fluidizing medium into the process chamber (10) from below, wherein a plurality of cells extending in the vertical direction are configured in the process chamber (10), of which cells one cell constitutes an outfeed cell which is not or less penetrated by fluidizing medium from below, on the lower end of which outfeed cell the product outlet (12) is arranged, and which cells are open at their upper end.

10. An evaporative dryer according to any preceding claim, wherein a plurality of pumps (40) are connected in parallel with one another.

11. The evaporative dryer according to any of the preceding claims, wherein an overpressure exists in the process chamber (10).

12. Evaporative dryer according to one of the preceding claims, characterized in that a connecting line (42) leads from the pressure relief vessel (30) to a mixing point (3) which is connected downstream of the steam generating device (2) and at which the hot steam is mixed with condensate from the pressure relief vessel (30) and/or from the condensate vessels (33, 35, 36).

13. The evaporative dryer according to any one of the preceding claims, wherein a regulating valve (54) is arranged between the pump (40) and the steam generating device (2).

14. The evaporative dryer according to any one of the preceding claims, characterized in that the condensate of a heating plate (28) or of a heating device is conducted from the process chamber (10) or outside the process chamber (10) directly to or via a condensate container (33, 35, 36) or a condensate drain (37) to the pressure relief container (30).

15. A method for operating an evaporation dryer (1), the evaporation dryer (1) being used for drying particles, the evaporation dryer having

-a process chamber (10) having at least one product inlet (11) through which particles to be dried are introduced into the process chamber (10) and a product outlet (12) through which dried particles are conducted out of the process chamber (10),

-a heat exchanger (20) into which pressurized vapor as hot vapor is conducted through at least one inlet (21, 211) and from which condensate is conducted out through at least one condensate outlet (22, 222) and to a pressure relief vessel (30), characterized in that pressure relief vapor is pumped out of the pressure relief vessel (30) through at least one pump (40) and conducted to the hot vapor.

16. Method according to claim 15, characterized in that the evaporation dryer (1) is supplied with hot vapour from different vapour generating devices (2) with different vapour qualities.

Technical Field

The invention relates to an evaporation dryer for drying particles, comprising: a process chamber having at least one product inlet for feeding particles to be dried into the process chamber and a product outlet for leading the dried particles out of the process chamber; a heat exchanger arranged in the process chamber, having at least one inlet for the pressurized vapor, in particular from the vapor generation device, as hot vapor, into the heat exchanger and a condensate outlet from the heat exchanger, wherein the condensate outlet is connected to the pressure relief vessel. The invention also relates to a method for operating such an evaporative dryer. Evaporative dryers are used in particular for drying fluidizable granules, such as crumbs in the production of sugar from sugar beets, but can also be used for drying other granules or granular-like products. Evaporative dryers can be used in the food industry and in the drying of semi-finished or intermediate products or for drying slurries.

Background

In the context of industrial production, the following are often the case: it is responsible for generating the required electrical energy. For this purpose, pressurized hot steam is generated in its own steam generator and is conducted to a turbine in order to generate the electrical current required by the plant, for example a sugar refinery, by means of an electrical generator. Pressurized steam is understood to be steam at high overpressure. In addition to the generation of electrical energy, the drying of the products or granules also requires hot steam as a heat source, for example for evaporative dryers, in particular fluidized-bed evaporative dryers. A balance is to be found here in order to give the consumer, i.e. the turbine and the evaporation dryer, the required amount of steam with the required quality. To ensure this, the pressure can be increased in the steam generator or in the boiler room, but this cannot be done at will. The increased steam pressure is often premised on the construction of a new boiler house, which entails extremely high costs. Another possibility is to better utilize the thermal potential of the hot steam condensate, which is the condensate formed from the steam which has passed through the heat exchanger in the evaporation dryer and has cooled down when heating the product to be dried.

A method and a system for drying particles are known from EP 2801779a1, in which hot vapor is conducted to a heat exchanger in an evaporative dryer for drying wet particles in a closed container. The heat exchanger is arranged within the closed container. The container has an upper cylindrical portion and a lower cylindrical portion. The heat exchanger also has channels that enable the steam formed by the water evaporated from the product to be heated. The heat exchanger is of two-stage construction, wherein the first heat exchanger section is arranged above the second heat exchanger section and the passage for steam passes through the first and second heat exchangers. The heating of the steam takes place indirectly in the lower heat exchanger by condensation of the hot vapour. The condensate formed here is conducted through an upper heat exchanger, the so-called recuperator, is cooled there and indirectly gives a portion of its heat to the steam in the process chamber. An additional pump is required here. The heat transfer between the condensate and the tubes in the recuperator is strongly dependent on the flow velocity of the condensate. Furthermore, this design requires higher expenditure in terms of pumping power. Furthermore, the division into a vapor heat exchanger and a condensate heat exchanger greatly limits the flexibility of the installation.

If the turbine and also the evaporator dryer are operated with steam from only one steam-generating device, the steam pressure fed to the turbine in the steam-generating device or in the boiler room is usually kept constant, since the turbine is usually sensitive to pressure fluctuations. The changing steam demand of the evaporative dryer is thus achieved by a reduction in the steam pressure, but the drying potential is destroyed.

Disclosure of Invention

The aim of the invention is to reduce the steam requirement of an evaporative dryer.

According to the invention, this object is achieved by a device having the features of the independent claim. Advantageous embodiments and embodiments of the invention are disclosed in the dependent claims, the description and the drawings.

The steam dryer according to the invention for drying particles, in particular fluidizable particles such as wood chips or sugar beet extraction chips, has: a process chamber having at least one product inlet for feeding particles to be dried into the process chamber and a product outlet for leading the dried particles out of the process chamber; a heat exchanger arranged within the process chamber, the heat exchanger having at least one inlet for the pressurized vapor, in particular from a vapor generation device, as hot vapor into the heat exchanger and at least one condensate outlet from the heat exchanger, wherein the condensate outlet is connected to a pressure relief vessel, the evaporative dryer being provided for: attached to the pressure relief vessel is at least one pump that pumps pressure relief vapor out of the pressure relief vessel, compresses it, and conducts it to a heat exchanger. The pressurized steam used in drying the particles condenses on the basis of a relatively high pressure at a relatively high temperature level and the condensate formed is collected in a container.

In the case of a single-stage heat exchanger, a pressure corresponding to the hot vapor pressure in the heat exchanger acts on the condensate container. In order to generate the pressure-relieved steam, the condensate container is followed by a control valve for reducing the pressure and a pressure relief container. The formed pressure relief vapor is pumped out of the pressure relief vessel by a pump and fed to a heat exchanger. The suction effect by the pump makes it possible to obtain relatively large quantities of pressure-relieved steam from the outflowing condensate of the heat exchanger and to supply it back to the dryer heating device at increased pressure. By reducing the pressure in the pressure relief vessel, the amount of pressure relief vapor increases and the temperature of the condensate decreases there. The pressure increase of the pressure-relieved vapor is effected by means of a pump, for example a vapor jet pump or a mechanical vapor compressor. In the case of using a vapor injection pump, hot vapor is used as the operating medium. By adding pressure relief steam to the hot steam, the amount of hot steam available is increased and the amount of hot steam required by the steam generating device is correspondingly reduced.

In an advantageous embodiment of the invention, the pump is designed as a vapor injection pump with an operating vapor connection, wherein a partial flow of hot vapor is preferably applied to the operating vapor connection. The advantages of using a vapor jet pump are: it works without maintenance and has no movable parts. It is thereby possible to obtain the pressure-relief steam from the condensate of the heat exchanger solely by the hot steam used for drying.

Depending on the desired degree of return of the pressure-relieved vapor, different amounts of hot vapor can be conducted as operating vapor to the vapor injection pump, so that variable mixing and utilization of the energy present in the pressure-relieved vapor can be brought about.

Instead of the suction pump being configured as a vapor injection pump, it is also possible for the pump to be configured as a mechanical suction pump which is driven by a motor drive, in particular by an electric motor drive. The disadvantage here is the increased maintenance costs for the movable components of the mechanical suction pump compared to the vapor injection pump, but the mechanical pump parameters of the pressure relief vapor to be fed can thus be set very precisely.

In a further development of the invention, it is provided that the heat exchanger is designed in multiple stages, in particular in two stages, and that a mixed vapor of hot vapor and pressure-relief vapor is feedable to the first stage or feedable to the first stage and that a hot vapor without mixing in pressure-relief vapor is feedable to the second stage or feedable to the second stage. The combination of a multistage, in particular two-stage heat exchanger with a pump for increasing the pressure of the pressure-relieved vapor makes it possible to utilize the pressure-relieved vapor of all condensate. The configuration of the evaporative dryer with a multi-stage or two-stage heat exchanger has the advantage that the stages can be loaded with different magnitudes of hot vapor pressure. There is also the possibility of operating the heat exchanger stages with unmixed hot vapor to maximize the drying power. By means of this variable, the evaporator-dryer can be operated optimally both in terms of power and in terms of energy.

Advantageously, the heat exchanger is operated in a convection process or an approximately convection process, wherein the first stage is arranged above in the case of a vertical evaporative dryer in mixed-vapor operation, while the second or further stages are loaded with a higher vapor pressure and are arranged below. The second stage of the heat exchanger is preferably charged with a higher hot vapor pressure in the case of a two-stage configuration. Since both stages of the heat exchanger are loaded with vapor, there is the option of: the dryer capacity is increased by the pressure increase of the first stage. This takes place by reducing the pressure-relief steam mixed into the first stage, but the advantage of saving steam can only be achieved to a limited extent. However, the following possibilities exist due to the variation of the feed quantity: the evaporator-drier is adapted with regard to its power and in the case of a boundary, both or all heat exchanger stages are operated at the same pressure.

The following possibilities exist with the evaporative dryer of the present invention: the heat exchanger divided into several parts is operated by only one steam quality from the steam supply device and the change in the drying capacity is achieved by the degree of additional feeding of hot steam into the upper heat exchanger. In the case of the use of a vapor injection pump as a suction pump, the pressure relief vapor is increased in its pressure by the operating vapor, so that the overall size of the first stage of the heat exchanger can be kept relatively small on the basis of the pressure increase of the pressure relief vapor in the vapor injection pump.

When the heat exchanger is operated in two or more stages, condensate accumulates in both or all of the stages. The invention has the following expansion scheme: separate condensate tanks are associated with two or all stages, which condensate tanks are then coupled to the pressure relief tank. The condensate accumulated in the stages can be utilized by combining the condensates, so that multiple utilization of the condensates can be achieved and pressure relief steam is obtained from the mixed-together condensates, which is also available in the event of pressure relief.

The additional condensate can be conducted directly from the heating surface or from a heating device, which is formed by a heating surface located in or outside the process chamber, or via a condensate container to the pressure relief container and the pressure relief vapor formed therefrom is supplied to the upper heat exchanger. For this purpose, a corresponding condensate line is provided from the process chamber to the pressure relief or condensate container.

The condensate container is preferably coupled to the pressure relief container via a regulating valve in order to reduce the pressure level of the pressure relief container. The condensate container has a pressure level at the pressure level of the respective attached heat exchanger. The common pressure relief vessel preferably has a pressure level which is lower than the pressure level of the hot vapour or the heat exchanger, and thus has a lower temperature than the temperature and the pressure level in the condensate vessel or the heat exchanger.

In order to make the use of pressurized vapor more flexible, a plurality of vapor injection pumps can be connected in parallel so that a large amount of pressure relief vapor can be compressed by the hot vapor. In particular during the partial load production phase, it is expedient to switch off the individual vapor injection pumps.

In a preferred embodiment of the evaporation dryer, it is designed as a fluidized-bed evaporation dryer, which forms an annular process chamber. In the case of a heat exchanger of cylindrical configuration and arranged centrally, and in some cases in a substantially circular arrangement of the two-stage heat exchanger, of the outer casing of the evaporation dryer, an annular process chamber is formed, which is provided with a conveying device for feeding fluidizing medium, in particular steam, from below into the process chamber. In the process chamber, the vertically extending cells are preferably formed by vertically or obliquely extending walls, in which the products to be dried and fluidized, such as wood chips or other particles, are located. The wet product to be dried is introduced into the cells, for example by means of cell vane gates or similar conveying devices. The products to be dried are transported from the feed cell through the cells in succession along the annular process chamber. The conveying direction is essentially predetermined here by the pressure drop in the fluidized bed, which pressure drop is established from the inlet cell to the outlet cell, the product outlet being arranged at the lower end of the outlet cell. No or reduced fluidization is achieved in the outlet cells. When the bottom is closed, no fluidization occurs. If reduced fluidization is desired, this is done by means of tiny perforations in the bottom. The cells are open at their upper ends, so that the product is moved from one cell to the other via the respective upper ends of the cell walls until the product, in the dried state, reaches an outlet cell, in which the product falls downward and is discharged there, for example by means of a cell vane gate and/or a corresponding outlet device, such as a screw conveyor. In addition, the cell walls may have lower openings through which a portion of the product is transported from one cell to an adjacent cell. An overpressure can be present in the process chamber, but it is also possible in principle for the evaporation dryer to also operate at atmospheric pressure. The annular process chamber can also be conical and have a constant or varying, in particular upwardly increasing, distance between the outer wall and the inner wall. Fluidized bed evaporative dryers may also be constructed as pure cylindrical structures without a tapered middle section.

A connecting line can lead from the pressure relief vessel for the condensate to a mixing point downstream of the steam generating device. In this connection, the condensate from the pressure relief vessel or condensation vessel is mixed with the hot steam directly from the steam generating device or turbine, whereby an increase in the steam quantity and at the same time a reduction in the temperature and in some cases in the pressure of the hot steam is obtained. By mixing in the condensate in the region of the mixing point, it can be ensured that the quality of the hot steam conducted to the heat exchanger or exchangers and the pump remains unchanged, even in the presence of fluctuations in the steam quality of the pressure generating device. Furthermore, if the drying power must be adaptable to the product to be dried, the respective desired steam quality can be set by the amount to be mixed in.

A regulating valve may be arranged between the pump and the vapour generating device.

The invention also relates to a method for operating an evaporative dryer for drying particles, having: a process chamber having at least one product inlet through which the particles to be dried are introduced into the process chamber, and a product outlet through which the dried particles are discharged from the process chamber; preferably, the heat exchanger is arranged in the process chamber, pressurized steam, in particular from a steam generating device, is introduced into the heat exchanger via at least one inlet as hot steam and condensate is discharged from the heat exchanger via at least one condensate outlet and is conveyed to the pressure relief vessel, wherein the pressure relief steam is pumped out of the pressure relief vessel via at least one pump and is conveyed to the hot steam. The evaporative dryer is constructed essentially as described above, and by conducting the pressure-relieved vapor to the hot vapor, the amount of vapor required by the vapor generation device can be reduced and an adaptation to the required power can be achieved.

The evaporation dryer can be supplied with hot vapors of different quality from different sources. In the case of a multi-stage configuration, different heat exchanger stages may be fed with different vapor qualities. These vapor qualities may be provided by one vapor generation device or by different vapor generation devices. For example, steam from a turbine may also be used.

Drawings

Embodiments of the invention are explained in detail below on the basis of the sole figure. In the drawing, a schematic representation of an evaporative dryer installation in the form of a fluidized-bed evaporative dryer is shown.

Detailed Description

In the figures, the evaporative dryer 1 is shown in a fluidized bed evaporative dryer configuration. The evaporative dryer 1 has a process chamber 10 with a product inlet 11 for feeding particles to be dried, such as chips, shavings, pellets or other fluidizable particles to be reduced in humidity. Upstream of the product inlet 11 there can be connected a device for feeding the granules from the storage chamber 13, which in the embodiment shown is a cell vane gate and a screw conveyor, both of which are driven by a motor. Arranged in reverse order on the product outlet 12 are a motor-driven screw conveyor and a cell vane gate, which convey the finished dried product into a pressure relief cyclone 14. The construction of the fluidized bed evaporative dryer 1 is provided with a substantially cylindrical housing 15 having a heat exchanger 20 centrally arranged therein, which may be constituted by a plurality of heat exchanger elements. Instead of the substantially cylindrical housing 15, it can also be conically widened or be formed from a combination of cylindrical and conical sections. The heat exchanger 20 forms an annular process chamber 10 together with the cylindrical housing 15. As long as the heat exchanger 20 also has a rounded outer contour, the process chamber 10 is annular, but in principle it is also possible: polygonal inner and outer contours of the process chamber 10. Outside the evaporator-dryer 10, a control valve 57 for the dryer pressure is arranged. The fluidizing medium in the form of steam or vapor is conducted from below through the sieve bottom on the underside of the process chamber 10 by means of the conveyor 16. Vertical walls and/or walls inclined in the conveying direction are arranged in the process chamber 10, so that the annular process chamber 10 is divided into individual cells. These walls can extend as far as the sieve bottom and enable a transition to an adjacent cell at their upper end and, if necessary, at additional openings, not shown, so that fluidized product or fluidized particles are transported from the product inlet 11 through the entire process chamber 10 to the product outlet 12. Advantageously, the inlet cells are located directly beside the outlet cells, so that the product has to move through the process chamber 10 around the heat exchanger 20. As soon as the discharge cell is reached, the dried product can be discharged there by a corresponding conveyor. This construction is known in principle, for example from EP 1956326a 1.

The heat exchanger 20 is configured in the illustrated embodiment in two stages and has two inlets 21, 211, via which the hot steam of the steam generating device 2, for example a boiler room, which provides high-pressure hot steam for operating a turbine on the one hand to generate electrical energy and for providing steam for drying the particles on the other hand, is conducted into the heat exchanger 20. Each inlet 21, 211 is arranged in an upper portion of the respective heat exchanger stage or superheater stage. On the respective lower side of the vertically oriented heat exchanger stages 23, 25, a respective condensate outlet 22, 222 is arranged. The condensate outlets 22, 222 lead to separate condensate containers 33, 35, into which condensate from the respective heat exchanger stages 23, 25 at the operating pressure of the heat exchanger is collected. On the outlet side, each condensate tank 33, 35 is assigned a control valve 53, 55, by means of which the condensate to be discharged is controlled with respect to the fill level in the condensate tank 33, 35. From the condensate containers 33, 35, conduits extend to a common pressure relief container 30, in which condensate from the two heat exchanger stages 23, 25 and in some cases from a heating surface, not described in detail, is collected. A lower pressure exists in the pressure relief vessel 30 relative to the operating pressure of the heat exchanger 20. The condensate collected therein has a significantly lower temperature than the condensate in the condensate containers 33, 35 and is likewise lower in temperature compared to the hot steam. The temperature difference causes the formation of pressure-relief vapor.

Also arranged in the process chamber 10 is an internal heating surface 28 or a heating plate, in which condensate can likewise form, which is conducted via a condensate line with a fitted condensate drain 37 to the pressure relief container 30. Instead of direct routing, the condensate from the heating surface 28 can also be conducted to the pressure relief vessel 30 via condensate vessels 33, 35 for the heat exchanger stages 23, 25.

The pressure relief vapor line 34 leads from the pressure relief container 30 to a suction pump 40, which in the illustrated embodiment is configured as a vapor jet pump. At the steam jet pump 40, the hot steam from the steam generating device 2 is applied to the operating steam connection 41, so that the hot steam is conducted as operating steam to the steam jet pump 40. A control valve 54 is connected upstream of the steam injection pump 40 in order to be able to control the operating pressure of the operating steam. Within the vapor jet pump 40, the hot vapor mixes with the pressure relief vapor from the pressure relief vessel 30 such that: the condensate, which in turn becomes vapor, is mixed with the hot vapor as pressure-relief vapor on the basis of the suction process of the vapor jet pump 40. Whereby the amount of vapour fed to the first heat exchanger stage 23 is increased.

The hot vapor line of the vapor providing device 2 branches off from the regulating valve 54. Part of the flow is conducted via a regulating valve via the upper line branch for driving the injector 17 in the process chamber 10. A significantly greater amount of vapor is conducted into the second heat exchanger stage 25, which is arranged below the first heat exchanger stage 23 located above. A higher vapor pressure than in the first heat exchanger stage 23 acts on the second heat exchanger stage 25. By the amount of pressure relief vapor mixed in from the pressure relief container 30, it is possible to: the different pressures for the first heat exchanger stage 23 are set so that adaptation to correspondingly different heat requirements is possible and the dryer capacity can be easily set, in particular in the case of partial load operation. In order to increase the dryer capacity, the amount of pressure relief steam supplied is reduced, so that in the extreme case the two heat exchanger stages 23, 25 can be operated with hot steam that is not mixed.

A condensate line 42 leads from the pressure relief container 30 or alternatively in a variant not shown from the other condensate container to the mixing point 3, where the condensate is mixed into the original hot steam from the steam supply device 2 after the hot steam has passed through the regulating valve 52. It is thereby possible to adjust the quality of the steam fed to the evaporation dryer 1 to the requirements, in particular to reduce the pressure and temperature and to increase the total steam quantity.

An additional reservoir 36 is connected downstream of the pressure relief reservoir 30 for receiving condensate at lower temperatures and pressures, which may also have other uses.

List of reference numerals

1 evaporative dryer

2 steam generating device

3 mixing point

10 Process Chamber

11 product inlet

12 product outlet

13 reserve chamber

14 pressure relief swirler

15 column casing

16 conveying device

17 ejector

20 heat exchanger

21 hot vapor inlet of upper heat exchanger

Condensate outlet of heat exchanger on 22

23 upper heat exchanger

25 lower heat exchanger

28 internal heating surface

30 pressure relief container

Condensate container for a heat exchanger on 33

34 pressure relief steam line

Condensate container for a lower 35 heat exchanger

36 condensate container

40 pump

41 operation steam joint

42 condensate line to mixing point

Regulating valve of 53 upper heat exchanger

54 regulating valve for operating steam

Regulating valve of 55-lower heat exchanger

57 regulating valve for dryer pressure

211 lower heat exchanger hot vapor inlet

Condensate outlet of the lower 222 heat exchanger