DE102014019805B3 - Compressor system for compressing gases - Google Patents

Abstract

Compressor system for compressing gases in a multi-stage compression comprising several compressors (11, 12) connected in series, including at least one compressor (11) penultimate in flow direction and a last compressor (12) which defines the highest compression stage within the multi-stage compression - One or more intercoolers (13) between the penultimate compressor (11) and the last compressor (12) - and an adsorption dryer (16) connected downstream of the last compressor (12), which is designed as a rotary dryer with a rotating adsorption chamber (44) and inside the adsorption chamber comprises a regeneration sector (17) and a drying sector (18), the regeneration sector (17) being connected to the last compressor (12) in such a way that the compressed gas flow emitted by the last compressor (12) goes through the regeneration sector according to the full flow principle (17) of the adsorption dryer (16) is performed, thereby gek indicates that a control device is provided which is in operative connection with the compressors (11, 12) and controls the compressors (11, 12), in particular sets their speed and / or records their operating data, in particular their speed, in order to compress the regeneration inlet temperature Tdes Gas into the regeneration sector (17) is variable, as required, in particular depending on the current status data of the gas to be compressed or the compressed gas, such as the humidity of the air drawn in and / or the humidity of the compressed gas output from the drying sector (18) adjust.

Description

The invention relates to a compressor system for compressing gases in a multi-stage compression according to the preamble of claim 1 and a method for operating a compressor system according to the features of claim 6.

A previously known compressor system for achieving multi-stage compression comprises several compressors connected in series, namely an upstream compressor and a last compressor which defines the highest compressor stage within the multi-stage compression, one or more intercoolers between the upstream compressor and the last compressor and one downstream of the last compressor Adsorption dryer, which is designed as a rotary dryer and comprises a regeneration sector and a drying sector, the regeneration sector being connected to the last compressor in such a way that the gas flow emitted by the last compressor is completely guided through the regeneration sector of the adsorption dryer using the full flow principle.

Such multi-stage compressor systems or multi-stage compression processes, in which or in which the last compressor, which defines the highest compressor stage within the multi-stage compression, an adsorption dryer, which is designed as a rotary dryer and includes a regeneration sector and a drying sector, the regeneration sector at the last Compressor is connected in such a way that the gas flow output by the last compressor is completely guided through the regeneration sector of the adsorption dryer according to the full flow principle, are known per se.

One problem, however, is that a compressed and dried gas flow should be available at the exit of the drying sector, which must be sufficiently dry in relation to a specified limit value. The pressure dew point is generally used as a measure of the dryness of the dried gas and to that extent for the drying result of the drying process. The pressure dew point indicates the maximum temperature to which a compressed gas stream can be cooled without the water vapor contained in it precipitating as condensate or ice. In the drying process here, the gas flow exiting the last compressor is completely guided through the regeneration sector of the adsorption dryer, which is designed as a rotary dryer, so that the heat of compression that is already generated can be used efficiently to desorb the water previously adsorbed in the adsorption material of the rotary dryer. The adsorption material that has been regenerated to the greatest possible extent in the regeneration sector is used again in the drying sector for gas drying after regeneration.

In order to be able to ensure sufficient drying, i.e. compliance with a specified limit value for the pressure dew point, the regeneration sector from the last compressor must be subjected to a sufficiently high temperature with compressed gas. The temperature at which the compressed gas exits the last compressor and enters the regeneration sector is hereinafter referred to as the regeneration entry temperature T _ri and, as mentioned, must be sufficiently high. For the purposes of the following application, the outlet temperature from the last compressor T _Al is assumed to be the same as the regeneration inlet temperature T _Ri (T _Al = T _Ri ). Even if the compressed gas should cool down slightly between the outlet of the last compressor and the inlet into the regeneration sector, this can be neglected in most practical arrangements. In any case, it should be noted that the regeneration _inlet temperature T _Ri correlates directly with the outlet temperature from the last compressor T _Al .

If the regeneration inlet temperature T _{Ri is} too high, this can be associated with various disadvantages. On the one hand, there is the risk that subsequent components in a connected compressed air system will be subjected to excessively high temperatures for which they are not designed, i.e. the permissible operating temperatures of downstream components will be exceeded.

On the other hand, too high a regeneration inlet temperature T _Ri also correlates with a correspondingly higher inlet temperature of the gas in the last compressor. The compression of a hotter gas is, however, significantly more inefficient than the compression of a comparatively cooler gas, with the result that the compression process becomes inefficient.

Since boundary conditions, such as the temperature of the cooling media that are available for cooling the intercooler (s), or the speed and thus the performance of one or more compressors, can change under certain operating conditions, the regeneration inlet temperature T _Ri can thus initially also change to change their value.

To this extent, it has already been proposed in the prior art to regulate the regeneration inlet temperature T _Ri to a fixed value in order to maintain a predetermined degree of dryness of a compressed gas. One such solution is for example in JPS 56152726. Specifically, a two-stage compression comprising an upstream compressor and a last compressor is proposed there, an intercooler being provided between the upstream compressor and the last compressor. The intercooler provided there is subjected to a regulated flow of cooling water in such a way that the outlet temperature of the compressed gas from the last compressor and thus the regeneration inlet temperature T _{Ri is} always kept above a set minimum temperature. In the prior art, drying is effected by a switching dryer that is to be regenerated in phases. By regulating the cooling water flow acting on the intercooler, the regeneration of the adsorption dryer, which is designed there as a switching dryer, is always carried out at at least the specified minimum temperature.

Also the DE 101 117 790 A1 as well as the US 2003/0188542 A1 disclose controls for regeneration of a dryer.

Based on this prior art, the object of the present invention is to propose a compressor system or a method for operating a compressor system in which the overall energy efficiency is improved in a multi-stage compression with subsequent adsorption drying of the compressed gas.

This object is achieved in terms of device technology by the features of claim 1 and in terms of process technology by the features of claim 6.

Specifically, a compressor system for compressing gases in a multi-stage compression is proposed, comprising several compressors connected in series, including at least one compressor penultimate in flow direction and a last compressor which defines the highest compressor stage within the multi-stage compression, one or more intercoolers between the penultimate one Compressor and last compressor and an adsorption dryer downstream of the last compressor, which is designed as a rotary dryer with a rotating adsorption chamber and includes a regeneration sector and a drying sector within the adsorption chamber, the regeneration sector being connected to the last compressor in such a way that that of the last compressor output compressed gas flow is guided in the full flow principle through the regeneration sector of the adsorption dryer, wherein a control device is provided, which with the Kom pressors ( 11 , 12 ) is in operative connection and the compressors ( 11 , 12 ) controls, in particular adjusts their speed and / or records their operating data, in particular their speed, in order to vary the regeneration inlet temperature T _{Ri of} the compressed gas into the regeneration sector, specifically as required, in particular as a function of the current status data of the gas to be compressed or the compressed gas , such as the humidity of the air sucked in and / or the humidity of the compressed gas discharged from the drying sector.

A rotary dryer within the meaning of the invention is an adsorption dryer, comprising a drum-shaped adsorption chamber with a plurality of adsorption channels containing an adsorption material, a first feed line and a first discharge line being arranged at a first end of the adsorption chamber and a first end line of the adsorption chamber A second feed line and a second discharge line are arranged, the drum-shaped adsorption chamber being rotatable with respect to the feed and discharge lines so that the adsorption channels can be fluidically connected to the first feed line and the second discharge line or the first discharge line and the second feed line in alternation over time. If we are talking about a rotating adsorption chamber, it is made clear that it depends on the relative movement between the adsorption material and the drying or regeneration sector, which is achieved either by the fact that the adsorption chamber rotates and the supply and discharge lines are fixed or that the adsorption chamber is fixed and the supply and discharge lines rotate.

The already mentioned drying sector and the already mentioned regeneration sector are defined, the gas being dried in the drying sector and the adsorption material being regenerated in the regeneration sector, the first feed line being designed in such a way that the gas flow to be dried can be fed to the regeneration sector as a full flow, wherein the second discharge line is connected to the second supply line and thus forms a connecting line and wherein the regeneration sector and drying sector are connected one behind the other for serial flow, so that the gas flow fed to the drying sector is essentially completely identical to that from the regeneration sector, possibly including one from a possibly still existing cooling sector corresponds to discharged gas flow.

In the present description, full flow is to be understood as meaning, in particular, a proportion of the gas flow of at least 95%, preferably at least 99%, more preferably (essentially) 100%.

If intermediate coolers are mentioned in the present application, it is made clear that these are fluidly connected to the penultimate compressor and the last compressor and are designed and set up to cool the partially compressed gas flow, in particular using a cooling medium. Overall, the intercooler is to be understood as a functional unit which, in terms of process technology, brings about the process step of intercooling. Structurally, the intercooler can also be designed to be integrated in a common structural unit with a condensate separator, which will be discussed in greater detail below.

From a procedural point of view, a method for operating a compressor system to achieve multi-stage compression is proposed, comprising several compressors connected in series, including one penultimate compressor in the direction of flow and a last compressor that defines the highest compressor stage within the multi-stage compression and one downstream of the last compressor Adsorption dryer, which is designed as a rotary dryer and comprises a regeneration sector as well as a drying sector, the gas flow output by the last compressor being guided through the regeneration sector of the adsorption dryer in accordance with the full flow principle, with control of the compressors and / or recording and taking into account of operating data, in particular a Speed of the compressors, the setting of the regeneration inlet temperature T _Ri in the regeneration sector is variable, specifically as a function of requirements the specific status data of the gas to be compressed or of the compressed gas, such as the humidity of the gas drawn in and / or the humidity of the compressed gas output from the drying sector, takes place during the operation of the compressor system.

If the present application mentions that the adsorption dryer is connected downstream of the last compressor, the aim is to connect it as directly as possible, also in order to be able to use the heat of the compressed gas flow flowing out of the last compressor directly for the regeneration, if possible without major heat losses . The interposition of components such as a pulsation damper, sensors, valves or other such components that do not significantly influence the temperature of the compressed gas can, however, be provided where necessary or sensible.

A key concept of the present invention is based on the consideration that a fixed degree of dryness of the compressed gas can be ensured with a relatively high fixed regeneration inlet temperature T _Ri , but a high regeneration inlet temperature T _Ri can be disadvantageous for energetic reasons. In situations, for example, in which the sucked-in gas to be compressed is relatively dry, the specified degree of dryness can also be maintained with a lower regeneration inlet temperature T _Ri . At the same time, however, the regeneration _entry temperature T _Ri can then be run lower, so that the regeneration _entry temperature T _{Ri is set} variably according to the invention, specifically as required.

A need-based setting is understood to mean the situation-related stipulation for the value T _Ri depending on the requirements for the gas flow to be provided or the optimization point of view. High values for T _Ri lead to an increased efficiency of the drying process, but also mean a more inefficient compression of the gas flow in the last compressor and are associated with a lower overall efficiency of the system. The needs-based setting and thus the determination of the T _Ri value can also depend on a number of technical and external factors, such as the temperature and humidity of the incoming gas flow, the operating temperature limits of the various components of the system, the speed of the compressors, the temperature of the cooling medium or the ambient temperature of the system. The needs-based setting and thus the definition of the regeneration inlet temperature T _Ri can in this respect include current conditions of various media, such as the temperature of the cooling medium, the temperature and / or humidity of the partially compressed or compressed gas to be compressed. In addition to taking into account the currently given values, values from the past - for example up to 30 min. previous - taken into account when setting the regeneration inlet temperature T _{Ri as} required.

The need-based setting of the regeneration _inlet temperature T _Ri , which corresponds to the outlet temperature of the last compressor T _Al or at least correlates with this, includes a variable setting of the outlet temperature T _{Al of} the last compressor. In contrast to the prior art, a fixed outlet temperature of the last compressor T _Al , which corresponds to the inlet temperature into the regeneration sector, is not fixed, but the outlet temperature of the last compressor T _Al or the regeneration inlet temperature into the regeneration sector T _{Ri of} the adsorption dryer is variable according to the invention hazards.

In this respect, the variable setting can directly or indirectly take into account the state conditions of the sucked in gas. For example, with a relatively moist intake gas, the outlet temperature T _{Al of} the last compressor or the regeneration inlet temperature T _Ri in the regeneration sector could be increased, or with relatively dry sucked gas, the outlet temperature T _{Al of} the last compressor or the regeneration _inlet temperature T _{Ri could be} reduced.

Characterized in that the regeneration inlet temperature T _Ri is set as required, in case of need at a lower regeneration inlet temperature T _Ri can be driven and the predetermined degree of drying will still be met, as when the regeneration inlet temperature T _Ri constant to such a value (high value) is determined, that the specified degree of dryness is adhered to in all conceivable cases.

The regeneration inlet temperature T _Ri can be set as required by setting an opening degree of a bypass line which wholly or partially bridges one or more intercoolers provided between the penultimate compressor and the last compressor. In terms of device technology, this setting can be made via an adjusting element.

In this embodiment, the control device is in operative connection with the setting element or an actuator assigned to the setting element in order to, if necessary, in particular depending on the current status data of the gas to be compressed or of the compressed gas, such as the humidity of the sucked in gas and / or the humidity of the compressed gas discharged from the drying sector to act on the adjusting element. The control device can therefore output a control signal to the setting element or the actuator which is operatively connected to the setting element in order to bring the setting element into a specific, desired position.

In a further preferred embodiment, the control device can include one or more signal inputs, in particular a signal input for an outlet temperature at or downstream of the last compressor, a signal input for at least one signal characterizing the drying process, such as the inlet temperature into the drying sector, the pressure dew point from the drying sector output compressed gas and / or for a cooling medium temperature, a signal input for at least one signal characterizing the compression process of the last compressor, such as a gas inlet temperature at this compressor, a gas outlet pressure of this compressor, a gas inlet pressure of this compressor, an operating temperature of this compressor or downstream components and / or a signal input for at least one signal characterizing the compression process of the penultimate compressor, such as a gas outlet temperature of this penultimate Ko mpressors or a gas outlet pressure of this penultimate compressor, a signal input for the speed of one or more compressors, and / or a signal input for the speed of the adsorption chamber. A signal input is a data input via which the signal device can record and / or process unavailable measurement data (raw data), processed measurement data, digitized measurement data or data that correspond to the respective measurement parameters and are obtained directly or indirectly. In some cases, the signal input can also be a “virtual” signal input, in such a way that the data relating to it are available directly or indirectly to the control device.

In one possible embodiment, the compressor system can include a pressure dew point sensor which is designed to detect the pressure dew point of the compressed gas output at the drying sector and is in operative connection with the control device, such that the setting element via the control device is dependent on the pressure dew point of the compressed gas output at the drying sector is set. Such a structure appears to be particularly simple and sensible, since if the degree of dryness deteriorates, the compressed gas discharged at the drying sector reacts and the setting element can be acted upon in such a way that the regeneration inlet temperature is increased. The regeneration inlet temperature can thus be set to an energetically meaningful value based on the degree of dryness of the compressed gas output.

The control device can furthermore be designed such that it is in operative connection with a data memory for the operating data of the adsorption dryer. It is irrelevant whether the data memory for the operating data of the adsorption dryer is completely or partially designed on the adsorption dryer, on a control device for the adsorption dryer, in the present control device, in a higher-level central control device or in some other suitable manner.

In an advantageous embodiment, the method according to the invention provides that the outlet temperature T _{Al of} the last compressor or the regeneration inlet temperature T _Ri in the Regeneration sector is set in such a way or with the aim that the compressed gas exiting the drying sector complies with a specified minimum limit value for the degree of drying or the pressure dew point of the compressed gas removed from the drying sector does not exceed a specified limit value for the pressure dew point. With the definition of a limit value for the pressure dew point, it can nevertheless be possible that the actual pressure dew point of the gas emerging from the drying sector exceeds this limit value in individual cases for a short time, but not permanently.

In a preferred development, the limit value for the pressure dew point can be set or fixed to a constant value by the user, or it can be set as a function of the application.

The setting of the outlet temperature T _Al or the inlet temperature T _Ri in the regeneration sector can preferably also be set in such a way that a degree of dryness of the compressed gas removed from the drying sector is not only maintained with regard to a minimum degree of drying, but that overdrying, which is disadvantageous in terms of energy, is also avoided becomes.

In a further preferred embodiment of the method according to the invention, it is provided that the needs-based setting of the regeneration inlet temperature T _Ri in the regeneration sector as a function of the specific status data of the gas to be compressed or the compressed gas, such as the humidity of the sucked in gas and / or the humidity of the The compressed gas outputted to the drying sector takes place continuously, quasi continuously or at intervals during the operation of the compressor system.

In a further optional embodiment of the method according to the invention, provision can be made for the inlet temperature T _Ri to be set as required as a function of a detected pressure dew point of the compressed gas that is output from the drying sector. This creates a particularly simple and reliable control option.

• Eine wichtige den Trocknungsvorgang charakterisierende Größe ist die Trocknungseintrittstemperatur, d. h. die Temperatur des Gases, mit der das Gas in den Trocknungssektor des Adsorptionstrockners eintritt, bzw. eine dafür charakteristische Temperatur. Diese Temperatur kann an einer beliebigen Stelle zwischen einem Regenerationsgaskühler, der vor Eintritt in den Trocknungssektor zuletzt durchströmt wird, und dem Trocknungssektor gemessen werden.

The following explains the determination of a default value Tv for the regeneration inlet temperature T _Ri :

• An important variable characterizing the drying process is the drying inlet temperature, ie the temperature of the gas at which the gas enters the drying sector of the adsorption dryer, or a temperature which is characteristic of it. This temperature can be measured at any point between a regeneration gas cooler, through which the flow lasts before entering the drying sector, and the drying sector.

Using the drying inlet temperature, the control device determines a default value Tv for the regeneration inlet temperature T _Ri . A possible setting element is controlled in such a way that this default value Tv is not significantly undershot as long as the penultimate compressor and the last compressor compress gas, with the exception of start-up processes in which the compressors first have to warm up until the regeneration inlet temperature T _{Ri reaches} the default value T. _V can reach or exceed. The setting element remains closed if the preset value T _{V is} not undershot even without flow through the bypass line. As a result, the power consumption of the compressor system is only increased as a function of demand, ie only when it is necessary for adequate drying and then only to the extent that it is necessary.

• • die Temperaturen des Kühlmediums des Regenerationsgaskühlers, der vor Eintritt in den Trocknungssektor zuletzt durchströmt wird,
• • die Temperaturen des Gases im und nach dem Austritt aus dem Trocknungssektor und/oder
• • die Temperatur des Adsorptionsmaterials im Trocknungssektor.

The overall system described is therefore very energy-efficient. Instead of the drying entry temperature, other temperatures which influence the drying entry temperature or are influenced by it could also be used, for example

• • the temperatures of the cooling medium of the regeneration gas cooler, which is last flowed through before entering the drying sector,
• • the temperatures of the gas in and after the exit from the drying sector and / or
• • the temperature of the adsorbent material in the drying sector.

Another important variable that characterizes the drying process is the pressure dew point after leaving the drying sector. If this pressure dew point, which can be detected via the already mentioned pressure dew point sensor, is too high, the setting element can be opened further, but if it is significantly lower than necessary, the setting element can be closed further. Alternatively, a default value Tv for the regeneration inlet temperature T _{Ri can} be changed accordingly, ie increased if the pressure dew point is too high and decreased if it is too low. The setting element is then activated in such a way that the default value Tv for the regeneration inlet temperature T _{Ri is} not undershot. Instead of a pressure dew point sensor, another variable that characterizes the water content of the gas flow can also be used.

It should be noted that an increase in the regeneration inlet temperature T _Ri can only affect the pressure dew point when the adsorption material regenerated with this regeneration inlet temperature T _{Ri is used} to dry the gas. A time delay between regeneration and drying must therefore be taken into account. The control device therefore advantageously interacts with the data memory already mentioned in order to store measured values from different times and to use them for controlling the setting element or for establishing the specification for the regeneration inlet temperature T _Ri . Thus, for the adsorption material located in the drying sector at a point in time, which is relevant for the pressure dew point reached at that point in time, the regeneration inlet temperature values that existed during the regeneration of this adsorption material can be taken into account in order to determine the specified temperature TV. This enables a more stable regulation of the pressure dew point.

For an optimal consideration of the temperature and pressure dew point values when determining the default value T _V , it is advantageous to know the length of a cycle after which the adsorption chamber is again in its starting position relative to the regeneration and drying sector. The length of a cycle can be determined if the speed of the relative movement of the adsorption chamber is present as a value in the control device. This is achieved, for example, in that the control device generates a control signal for the motor drive of the adsorption chamber of the adsorption dryer designed as a rotary dryer and / or that the motor drive transmits a corresponding signal regarding the movement to a corresponding signal input of the control device.

A particularly stable regulation can be achieved if signal inputs for the detected current pressure dew point as well as for the drying inlet temperature are available on the control device.

As a result, when the drying inlet temperature is increased, the preset value Tv for the regeneration inlet temperature T _{Ri can} be increased immediately. This means that there is no (or only a slight) increase in the pressure dew point, since the default value Tv can already be changed before the pressure dew point signal delivers a value above the specified limit value for the pressure dew point. When the pressure dew point signal, e.g. B. because of other influences, such as increase in rel. The humidity and temperature of the gas sucked in by the compressor system, despite exceeding the specified limit value for the pressure dew point, only leads to a minor change in the default value Tv. This ensures that the specified limit value for the pressure dew point is not exceeded with a high degree of certainty.

In the case of compressors with a variable suction volume flow (for example compressors with a variable speed), the drying inlet temperature also changes with the suction volume flow. With a low suction volume flow, the drying inlet temperature is low. Therefore, only a low regeneration inlet temperature T _Ri would be required for drying the low intake volume flow. However, if the intake volume flow is increased based on a low intake volume flow and the drying inlet temperature rises as a result, the regeneration inlet temperature T _Ri previously determined on the basis of the drying inlet temperature at a low intake volume flow would be too low for adequate drying.

It can therefore be advantageous to set the default value for the regeneration inlet temperature T _Ri in the case of low intake volume flows which results from the drying inlet temperature that will be reached with a high intake volume flow. This can be approximately calculated by the control device if the information about the current and the maximum intake volume flow is available for the control device. This is achieved in that the drive for the compressors of the compressor system is controlled via a signal output of the control device and / or a signal input is provided which can be used to determine the current intake volume flow. These can, for example, be signals for the frequency of the rotating field generated by a frequency converter with which the drive for the compressors is operated.

• • Regenerationseintrittstemperatur T_Ri bzw. Austrittstemperatur T_Al des Gases aus dem letzten Kompressor
• • Trocknungseintrittstemperatur
• • Trocknungsaustrittstemperatur
• • Drucktaupunkt nach Trocknung
• • Geschwindigkeit der Adsorptionskammer oder ein Maß für die Drehgeschwindigkeit des als Rotationstrockners ausgebildeten Adsorptionstrockners
• • Ansaugvolumenstrom der Kompressoranlage oder eine andere den zu trocknenden Gasmassenstrom charakterisierende Größe
• • Zeit seit letztem Start der Gasförderung

The variables described affect z. T. only with a delay to the pressure dew point. It is therefore advantageous if stored operating data from earlier times can be used to determine the preset value T _V. Operating data of the adsorption dryer, which are stored in the data memory cooperating with the control device and can be used for controlling the actuator of the setting element or for determining the default value for the regeneration inlet temperature T _Ri

• • Regeneration _inlet temperature T _Ri or outlet temperature T _{Al of} the gas from the last compressor
• • Drying inlet temperature
• • Drying outlet temperature
• • Pressure dew point after drying
• • Speed of the adsorption chamber or a measure of the speed of rotation of the adsorption dryer designed as a rotary dryer
• • Intake volume flow of the compressor system or another variable characterizing the gas mass flow to be dried
• • Time since the last start of gas production

A further improvement of the drying process is achieved if a condensate separator and a condensate drain are provided between the gas outlet from the intercooler and the junction with the bypass line.

Because both the gas inlet temperature and the gas outlet temperature of the last compressor are increased by the measures described, the load limits of the penultimate compressor, the last compressor or downstream components could be exceeded. To avoid this, a signal input for the gas inlet temperature of the last compressor and / or signal inputs for the gas pressures before and / or after the last compressor are provided in the control device. On the basis of this signal or these signals, the default value Tv for the regeneration inlet temperature T _{Ri can} be determined in such a way that the load limits of the penultimate compressor, the last compressor and / or downstream components are reliably observed.

If, on the other hand, the regeneration inlet temperature T _{Ri has to be increased} in certain cases, in which, for example, the humidity of the sucked in gas is very high, this could in principle also be done with a switchable heating device that heats the compressed gas before it enters the regeneration sector. Indeed, such a solution is already in the WO 2009 043 123 A1 described. Compared to a specially provided additional heating device, however, the procedure proposed here, namely routing part of the pre-compressed gas upstream of the last compressor past the intercooler via a bypass line and thus ultimately already supplying pre-compressed gas at a higher temperature to the last compressor, is significantly more efficient, both from energetic considerations as well as structural considerations. From a structural point of view, a separate heating device is not necessary. For energetic considerations, the additional energy to be applied to increase the regeneration inlet temperature in the solution via a heating device should be around two to four times as high as the additional energy required to compress the gas with its increased temperature in the last compressor or, above all, in the penultimate compressor . By opening a cross-section in the bypass line, the temperature of the partially compressed gas rises between the merging point and the last compressor. This higher temperature increases the pressure between the penultimate compressor and the last compressor, which can also be referred to as the intermediate pressure between the penultimate compressor and the last compressor. However, this also increases the pressure ratio for the penultimate compressor, ie the penultimate compressor has to compress the gas to the now higher intermediate pressure, so that the energy expenditure for the penultimate compressor increases.

The principle of the action on the regeneration inlet temperature T _Ri by means of an adjusting element provided in a bypass line is already from FIG JP 5106560 known. However, only part of the hot compressed gas is used there to regenerate the adsorption material. However, the bypass line raises the temperature of the entire compressed hot gas and thus also increases the power consumption of the compressor system for compressing the entire gas flow. The increase in temperature due to the increased power consumption of the last compressor is not used for part of the compressed gas, but this part is passed through a cooler without using the heat. This makes this process relatively inefficient. In addition, in none of the above-mentioned documents is there any need-dependent control of the regeneration inlet temperature T _Ri . This leads to an unnecessarily high power consumption of the compressor system. It is often operated with a pressure dew point that is significantly lower than necessary. This also makes the process relatively inefficient.

Finally, a switch dryer is provided in the cited prior art. Due to the large time interval between the regeneration of a container and the drying of compressed gas with this container, it would require an unacceptably long reaction time to act on the regeneration temperature if the humidity of the compressed gas is too high. To this extent, with the system proposed there, a demand-dependent control of the regeneration inlet temperature cannot actually be implemented structurally.

In a preferred embodiment of the present invention, the compressor system is designed to achieve two-stage compression, so that the compressor upstream in the direction of flow defines the lowest compressor stage. Although two-stage compression is a frequent application, it should be pointed out at this point that the invention is of course not limited to use in two-stage compression, but rather the Compressor system can be designed to achieve a three-, four-, five- or higher-stage compression. The method can also be applied to a three-, four-, five- or higher-stage compression. In a four-stage compression, for example, viewed in the direction of flow, the third compressor is the penultimate compressor and the last compressor is the fourth compressor within the meaning of the present invention. In the case of five-stage compression, the penultimate compressor is the fourth compressor and the last compressor is the fifth compressor, viewed in the direction of flow. To clarify, it is mentioned that the last compressor, viewed in the direction of flow, denotes the last compressor of the multi-stage compression before the gas flow is transferred to the adsorption dryer, i.e. before it enters the regeneration sector.

In a further preferred embodiment, the adjusting element is designed for a continuous or steady adjustment of the gas flow. Furthermore, if necessary, the adjusting element can also completely shut off the bypass line and / or completely open a line cross-section of the bypass that is fed to the adjusting element. In all of the aforementioned refinements, it is conceivable to allow a setting in discrete steps or continuously or steadily. A release of the cross-section in discrete steps for the flow through the bypass line could also be achieved by connecting several shut-off valves in parallel. The setting element could also be located directly at the branching point 24 or at the junction 21st the bypass line 14th be installed in the form of a distribution or mixing valve. In a specifically possible embodiment, the setting element can be a proportional valve.

In a particularly preferred embodiment, the setting element is coupled to an actuator which is designed for electrical, pneumatic or hydraulic actuation of the setting element.

In a specifically conceivable embodiment, the actuator is driven by a motor, for example.

In a further, preferred embodiment, an already mentioned condensate separator is provided, which is arranged downstream of the intercooler (s) upstream of a merging point at which the gas flow passed through the bypass line is combined with the gas flow passed over the intercooler (s) before it enters the last compressor . The condensate separator can also be designed to be integrated with the intercooler in a common structural unit. Although configurations are also conceivable in which intercoolers between an upstream and a downstream compressor or a penultimate compressor and a last compressor only cool the compressed gas and the compressed gas supplied to the downstream or last compressor, the provision of a condensate separator appears to be sensible when the compressed gas is cooled down to such an extent that the moisture or water vapor it contains can partially condense out and be separated. This makes it possible to remove some of the water contained in the gas sucked in by the penultimate compressor from the gas flow before this gas flow is used to regenerate the adsorption material. As a result, a better drying result can be achieved, or the desired drying result can be achieved with a lower regeneration inlet temperature T _Ri and thus lower power consumption, in particular of the last compressor. To clarify, it is added that the condensate separator is arranged in a connecting line between the intercooler and the junction point, that is, the gas flow, which is also passed through the intercooler, flows through it.

The invention is explained in more detail below with regard to further features and advantages using the description of exemplary embodiments and with reference to the accompanying drawings.

• 1a eine erste Ausführungsform einer Kompressoranlage zur Komprimierung von Gasen in einer zweistufigen Verdichtung nach der vorliegenden Erfindung,
• 1b eine zweite Ausführungsform einer Kompressoranlage zur Komprimierung von Gasen in einer zweistufigen Verdichtung nach der vorliegenden Erfindung,
• 1c eine dritte Ausführungsform einer Kompressoranlage zur Komprimierung von Gasen in einer zweistufigen Verdichtung nach der vorliegenden Erfindung,
• 2 eine weitere Ausführungsform einer Kompressoranlage zur Komprimierung von Gasen in einer zweistufigen Verdichtung,
• 3 eine Ausführungsform einer Kompressoranlage zur Komprimierung von Gasen in einer dreistufige Verdichtung,
• 4a ein Diagramm zur Erläuterung der Zusammenhänge zwischen Temperaturen und Taupunkten im Vergleich zwischen einer erfindungsgemäßen Anlage bzw. einem erfindungsgemäßen Verfahren und einer Anlage bzw. einem Verfahren nach dem Stand der Technik,
• 4b eine Veranschaulichung der Zusatzleistungsaufnahmen für die beiden Gesamtsysteme B und C des anhand von 4a veranschaulichten Beispiels.

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• 1a a first embodiment of a compressor system for compressing gases in a two-stage compression according to the present invention,
• 1b a second embodiment of a compressor system for compressing gases in a two-stage compression according to the present invention,
• 1c a third embodiment of a compressor system for compressing gases in a two-stage compression according to the present invention,
• 2 another embodiment of a compressor system for compressing gases in a two-stage compression,
• 3 an embodiment of a compressor system for compressing gases in a three-stage compression,
• 4a a diagram to explain the relationships between temperatures and dew points in comparison between a system according to the invention or a method according to the invention and a system or a method according to the prior art,
• 4b an illustration of the additional service consumptions for the two overall systems B and C of the based on 4a illustrated example.

In 1a a first embodiment of a compressor system for compressing gases in a two-stage compression according to the present invention is shown. The compressor system includes an upstream (penultimate) compressor 11 , which in the present embodiment represents the lowest compressor stage and a last compressor 12 , which represents the highest compressor stage in the present embodiment. Overall, as mentioned, the present embodiment is a compressor system with two-stage compression.

In general, the compressor system according to the invention or the method according to the invention can be operated with different gases. In many applications, however, the gas to be compressed is air or the compressed gas is compressed air. The exemplary embodiments are described below with reference to FIG 1 to 3 also explained with reference to the example case in which the gas to be compressed is air.

Between the upstream compressor 11 and last compressor 12 is an intercooler 13 and downstream of the intercooler 13 a condensate trap 20th and a steam trap 45 arranged. The intercooler 13 can be exposed to cold, in particular a cold fluid such as cold water or ambient air, and so that of the upstream compressor 11 cool the supplied compressed compressed air.

The cooling of the upstream compressor 11 Compressed compressed air may be required for several reasons. On the one hand, it should be prevented that in downstream compressor stages, specifically in the last compressor here 12 is heated to a temperature which is above an operating temperature that is beneficial for the last compressor or for connected components. On the other hand, cooler air has a higher density and can therefore be compressed more energy-efficiently than heated air. With regard to energy efficiency, it can also make sense to use the upstream stage here specifically in the upstream compressor 11 to cool compressed air.

Will the compressed air in the intercooler 13 Cooled above its pressure dew point, the moisture contained in it condenses out. Via the condensate separator already mentioned 20th and the condensate drain 45 this moisture, in particular the water contained in the compressed air, can be removed. In this respect, through the intercooler 13 and the condensate trap 20th in the case of cooling above the dew point, the one in the upstream compressor 11 compressed air can also be dried.

It's an intercooler 13 bridging bypass line 14th intended. The bypass line 14th insofar runs between a branch point 24 between the upstream compressor 11 and the intercooler 13 and a union point 21st between the condensate trap 20th and the last compressor 12 is arranged. Inside the bypass line 14th is an adjusting device 15th provided here specifically as a via an actuator 19th actuatable proportional valve is formed. The - for example electrically driven - actuator 19th can from a control device 22nd be controlled, so that a stepless adjustment of the setting member 15th , specifically the proportional valve at the instigation of the control device 22nd is possible.

Downstream of the last compressor 12 is an adsorption dryer 16 , which is designed here as a rotary dryer, arranged. The adsorption dryer designed as a rotary dryer includes a regeneration sector 17th as well as a drying sector 18th . The rotary dryer embodied as an adsorption dryer can, however, also comprise further sectors, for example a cooling sector or also several regeneration sectors or several drying sectors.

The adsorption dryer 16 is via a connecting line 37 like this to the last compressor 12 connected that the entire compressed gas flow initially to an inlet 30th of the regeneration sector 17th , then through the regeneration sector 17th and from an exit 31 of the regeneration sector 17th then to the drying sector 18th is led. In the drying sector 18th the compressed air comes from an inlet 28 of the drying sector 18th through this and will come to an exit 29 of the drying sector. All of the hot compressed air from the last compressor 12 flows through a connecting line 37 to the regeneration sector 17th of the adsorption dryer 16 .

Inside a housing section of the adsorption dryer 16 in which the regeneration sector 17th and the drying sector 18th are defined is a first dryer-side condensate separator 25th with a first condensate drain on the dryer side 47 arranged in order to discharge water that occurs at the inlet of the drying sector, for example by cooling the moist air when the compressor system is not running. In the direction of flow of the compressed gas is between the regeneration sector 17th and the drying sector 18th also a regeneration gas cooler 26th provided, to which a second dryer-side condensate trap 27 with a second condensate drain on the dryer side 48 connects. To an equal or preferably higher pressure at the entrance of the drying sector 18th than at the exit of the regeneration sector 17th can also be provided with a pressure booster 36 between the second dryer-side condensate trap 27 and the entrance 28 in the drying sector 18th be provided.

The control device 22nd still stands with a motor drive 32 of the adsorption dryer 16 as well as with several sensors that provide information about the condition of the compressed air in the compressed air system in operative connection, specifically with a first temperature sensor 33 , a second temperature sensor 34 and a third temperature sensor 35 in operative connection. The first temperature sensor 33 is downstream of the junction point 21st and upstream of the last compressor 12 provided and thus records the temperature of the compressed air before entering the last compressor 12 . The second temperature sensor 34 is between the last compressor 12 and the entrance 30th in the regeneration sector 17th arranged and thus records the temperature of the compressed air after the last compressor 12 . The third temperature sensor 35 is after the second condensate trap on the dryer side 27 and in front of the pressure booster 36 , so at the same time in front of the entrance 28 in the drying sector 18th intended.

By recording the temperatures in front of the entrance 28 in the drying sector 18th or in front of the entrance 30th in the regeneration sector 17th and before the entrance to the last compressor 12 can be adjusted using the setting element 15th control the temperature so that an optimal regeneration inlet temperature T _ri given is. This is with the second temperature sensor 34 monitored simultaneously.

Alternatively or in addition to the first temperature sensor 33 , second temperature sensor 34 or to the third temperature sensor 35 can also be a pressure dew point sensor 43 at the exit 29 of the drying sector 18th of the adsorption dryer 16 be provided. The pressure dew point sensor 43 determines a current pressure dew point at the drying sector 18th compressed air output. If the pressure dew point of the output compressed air approaches the specified limit value for the pressure dew point, measures are taken immediately, specifically the setting element 15th acted in such a way that a previously established limit value GWT for the pressure dew point is adhered to with sufficient reliability. Specifically, it can be provided that if the current pressure dew point is that of the drying sector 18th Compressed air output increases in the direction of the limit value of the pressure dew point, the bypass line 14th via the setting element 15th is opened in such a way that the regeneration inlet temperature rises and, while accepting additional energy consumption through higher regeneration inlet temperatures, improved drying of the compressed air is achieved, so that exceeding the specified pressure dew point is prevented with sufficient reliability.

In 1b a second embodiment of a compressor system for compressing gases in a two-stage compression according to the present invention is shown. This second embodiment of a compressor system largely corresponds to the structure of FIG 1a Illustrated embodiment of a compressor system, which differs from the based on 1a illustrated embodiment differs only in that the adjusting member 15th at the end of the bypass line 14th at the union point 21st is designed as a mixing valve. The adjusting element designed as a mixing valve 15th can in this respect via the bypass line 14th and the one via the intercooler 13 Adjust the guided partial flow and, on the one hand, the flow via the bypass line 14th guided partial flow and on the other hand that via the intercooler 13 Completely shut off the guided partial flow. The adjusting element designed as a mixing valve 15th is also here via an actuator 19th can be actuated so that the actuator, which is, for example, electrically driven by the control device 22nd can be controlled.

In 1c A third embodiment of a compressor system for compressing gases in a double compression is illustrated, which differs from that based on FIG 1b Embodiment illustrated differs in that between the penultimate compressor 11 and last compressor 12 the already mentioned intercooler 13 as the last intercooler and an upstream intercooler as the penultimate intercooler 13 ' is trained. The bypass line 14th In the present embodiment, however, it only bridges the one between the penultimate compressor when viewed in the direction of flow 11 and last compressor 12 last intercooler 13 but not the one between the penultimate compressor 11 and last compressor 12 penultimate intercooler 13 ' . Here too - according to the embodiment 1b - the setting element 15th designed as a mixing valve, the point of union 21st is provided and in this respect an adjustment of the bypass line 14th or the intercooler 13 caused partial flows. In particular, via the intercooler 13 conducted partial flow or that via the bypass line 14th guided partial flow are completely shut off. Trained as a mixing valve Setting element 15th can by means of an actuator 19th be actuated, for example by the control device 22nd can be controlled.

In 2 shows a modified embodiment of a compressor system for compressing gases in a two-stage compression. This compressor system largely corresponds to the structure of the 1a Illustrated embodiment of a compressor system, which differs from the based on 1a illustrated embodiment differs only in that instead of the first temperature sensor 33 in the embodiment according to 1a a first pressure measuring sensor 38 and a second pressure measuring sensor 39 are provided. The first pressure measuring sensor 38 is between the penultimate compressor 11 and the last compressor 12 , especially between the junction point 21st and the last compressor 12 arranged and detects the inlet pressure of the last compressor 12 . The second pressure measuring sensor 39 is on the output side of the last compressor 12 provided upstream or downstream of the second temperature sensor 34 or in the same position as the second temperature sensor 34 . First pressure measuring sensor 38 and second pressure measuring sensor 39 stand with the control device 22nd in operative connection and transfer the recorded pressure values to the control device 22nd .

From the pressure ratio between the inlet pressure of the last compressor 12 and discharge pressure of the last compressor 12 and the one via the second temperature sensor 34 recorded outlet temperature of the last compressor 12 can then be the inlet temperature of the last compressor 12 can be determined approximately.

In 3 an embodiment of a compressor system for compressing gases in a triple compression is illustrated. The flow sheet in the embodiment according to 3 The illustrated embodiment differs from the flow diagram of the embodiment as presented with reference to FIG 1 was illustrated only by the fact that in front of the upstream compressor 11 an additional lower compressor stage as an input compressor 40 and between the input compressor 40 and the upstream compressor 11 a second intercooler 41 , a second condensate trap 42 and a second condensate drain 46 is provided.

In 4a is a diagram to explain the relationships between temperatures and dew points in comparison between a system according to the invention or a method according to the invention and a system or a method according to the prior art. Specifically, gas temperatures and pressure dew points at the exit of the drying sector (y-axis) are shown as a function of the cooling medium temperature (x-axis).

In this based on the 4a In the illustrated example, the cooling medium temperature is the temperature at which the cooling medium enters the overall system. The cooling medium enters the intercooler at this temperature in parallel 13 and the regeneration gas cooler 26th a. However, the qualitative statements also apply if the cooling medium has the intercooler 13 and the regeneration gas cooler 26th flows through sequentially, since in this case too an increase in the cooling medium temperature with which the cooling medium enters the overall system, an increase in the gas outlet temperature of these two coolers, that is to say the intercooler 13 and the regeneration gas cooler 26th , entails.

For the examples shown, gas pressures, intake gas flow of the compressors, relative humidity of the intake gas are assumed to be constant. An overall system A, in which no measures are taken to influence the regeneration entry temperature T _Ri , an overall system B, in which the regeneration entry temperature T _Ri is regulated to a constant, sufficiently high value, and an overall system C with the inventive regulation of the regeneration entry temperature T _Ri considered. The curve 51 represents the course of the drying inlet temperature (can be recorded by the third temperature sensor 35 ). This curve is identical in all three cases A, B and C considered and increases with the cooling medium temperature.

The curve 50A indicates the temperature profile of the regeneration inlet temperature T _Ri for the entire system A. It runs roughly parallel to the drying inlet temperature. The pressure dew point curve 52A of overall system A increases continuously and in this example exceeds a limit temperature GT the limit value GWT for the pressure dew point.

For overall system B, in which the regeneration inlet temperature T _Ri according to curve 50B is kept at a constant high value, the pressure dew point becomes 52B kept below the limit value GWT. However, it is lowered over the entire temperature interval of the cooling medium under consideration, so that unnecessarily low pressure dew points are reached. For this, there is a considerable difference between the constant regeneration entry temperature B and the regeneration entry temperature T _Ri 50A of the overall system A in the entire operating area. For higher regeneration inlet temperatures, a higher power consumption of the overall system is required. Overall system B with constant regeneration inlet temperature therefore has a significantly higher power consumption than the entire system A.

At total system C according to the invention with the demand-dependent regulation of the regeneration inlet temperature T _Ri regeneration inlet temperature T _Ri (line is 50C ) only for coolant temperatures above the limit temperature GT Compared to the overall system A, it is higher and only so much higher that the limit value GWT for the pressure dew point is not exceeded here. The history 50C the regeneration entry temperature T _Ri in the overall system C is significantly below the curve 50B with constant regulation. As a result, the overall power requirement is lower and the process is considerably more energy efficient.

For the in 4a considered example are in 4b the additional power consumption (y-axis) of the two overall systems B and C based on the overall system A as a function of the cooling medium temperature (x-axis), i.e. the difference between the power consumption of the overall system B or C and the power consumption, system A has the same operating conditions.

The line 53B shows the additional power consumption ΔP _{BA of} the overall system B, the line 53C the additional power consumption ΔP _{CA of} the overall system C. In the operating range under consideration, for the overall systems B and C, as in 4a shown the limit GW _T for the pressure dew point are not exceeded. The constant predetermined value for the regeneration inlet temperature T _Ri was therefore set so high that the limit value GWT is just reached at the highest cooling medium temperature of the operating range under consideration and thus in the worst case. At this point, systems B and C, as in 4a shown, the same regeneration inlet temperature T _Ri and the same pressure dew point and thus the same additional power consumption.

In the case of overall system B, however, the additional power consumption is higher the lower the cooling medium temperature. This is due to the fact that in overall system B the energetic advantages that these lower cooling medium temperatures bring about in overall system A are not used. At low cooling medium temperatures, an energetically advantageous low gas inlet temperature of the highest compressor stage is brought about in comparison system A; B. the gas inlet temperature is artificially increased by the regulation, so that no energetic improvement is achieved through lower cooling medium temperatures.

When overall system C of the auxiliary power requirement .DELTA.P _CA is the lower, the lower the coolant temperature, as the default value for the regeneration inlet temperature T _Ri is lowered depending on demand at lower regeneration inlet temperatures T _Ri. Below the limit temperature GT If the overall system A falls below the limit value GWT for the pressure dew point (cf. 4a) . It is therefore not necessary in this area for the regeneration entry temperature T _{Ri to be} increased. With the demand-dependent regulation of the overall system C, the temperature is below the limit GT no higher regeneration entry temperature T _Ri than that which is present in the overall system A, determined as the default value, ie the setting element 15th holds the bypass line 14th locked. Therefore takes place below the limit temperature GT with overall system C no additional power consumption.

List of reference symbols

11

penultimate compressor

12

last compressor

13, 13 '

Intercooler

14th

Bypass line

15th

Setting element

16

Adsorption dryer

17th

Regeneration sector

18th

Drying sector

19th

Actuator

20th

Condensate separator

21st

Union point

22nd

Control device

23

Data storage

24

Branching point

25th

first dryer-side condensate separator

26th

Regeneration gas cooler

27

second condensate separator on the dryer side

28

Entrance (drying sector)

29

Exit (drying sector)

30th

Input (regeneration sector)

31

Output (regeneration sector)

32

motor drive

33

first temperature sensor

34

second temperature sensor

35

third temperature sensor

36

Pressure booster

37

Connecting line

38

first pressure measuring sensor

39

second pressure measuring sensor

40

Input compressor

41

(second) intercooler

42

(second) condensate separator

43

Pressure dew point sensor

44

Adsorption chamber

45

Condensate drain

46

(second) condensate drain

47

first condensate drain on the dryer side

48

second condensate drain on the dryer side

T _ri

Regeneration inlet temperature

T _Al

Outlet temperature from the last compressor

GW _T

Limit value for the pressure dew point

GT

Limit temperature

Claims (8)

Compressor system for compressing gases in a multistage compression comprising - several compressors (11, 12) connected in series, comprising at least one compressor (11) penultimate in flow direction and a last compressor (12) which defines the highest compression stage within the multistage compression - One or more intercoolers (13) between the penultimate compressor (11) and the last compressor (12) - and an adsorption dryer (16) connected downstream of the last compressor (12), which is designed as a rotary dryer with a rotating adsorption chamber (44) and inside the adsorption chamber comprises a regeneration sector (17) and a drying sector (18), the regeneration sector (17) being connected to the last compressor (12) in such a way that the compressed gas flow emitted by the last compressor (12) goes through the regeneration sector in the full flow principle (17) of the adsorption dryer (16) is performed, thereby characterized in that a control device is provided which is in operative connection with the compressors (11, 12) and controls the compressors (11, 12), in particular sets their speed and / or records their operating data, in particular their speed, in order to reach the regeneration inlet temperature T. _{Ri of} the compressed gas in the regeneration sector (17) is variable, as required, in particular depending on the current status data of the gas to be compressed or the compressed gas, such as the humidity of the air drawn in and / or the humidity of the air from the drying sector (18) compressed gas output. Compressor system after Claim 1 , characterized in that the control device (22) comprises one or more signal inputs, in particular - a signal input for an outlet temperature at or downstream of the last compressor (12), - a signal input for at least one signal characterizing the drying process, such as the inlet temperature in the drying sector (18), the pressure dew point of the compressed gas output from the drying sector (18) and / or for a cooling medium temperature, - a signal input for at least one signal characterizing the compression process of the last compressor (12), - such as a gas inlet temperature at this compressor, - a Gas outlet pressure of this compressor, - a gas inlet pressure of this compressor, - an operating temperature of this compressor or downstream components, - a signal input for at least one signal characterizing the compression process of the penultimate compressor, - such as a gas outlet temperature of the penultimate compressor (11), or - a gas outlet pressure of the penultimate compressor (11), - a signal input for the speed of one or more compressors (11, 12), and / or - a signal input for the speed of the adsorption chamber (44). Compressor system after Claim 1 or 2 , characterized in that a pressure dew point sensor (43) is provided which is designed to detect the pressure dew point of the compressed gas output at the drying sector (18) and is in operative connection with the control device (22) such that the regeneration inlet temperature T _{Ri of} the compressed gas can be set in the regeneration sector (17) via the control device (22) as a function of the pressure dew point of the compressed gas output at the drying sector (18). Compressor system according to one of the Claims 1 to 3 , characterized in that the control device (22) is in operative connection with a data memory (23) for operating data of the adsorption dryer (16). A method for operating a compressor system to achieve multi-stage compression, comprising several compressors (11, 12) connected in series, including a penultimate compressor (11) in the flow direction and a last compressor (12) which defines the highest compression stage within the multi-stage compression and one the last compressor (12) downstream adsorption dryer (16), which is designed as a rotary dryer and comprises a regeneration sector (17) and a drying sector (18), the gas flow emitted by the last compressor (12) through the regeneration sector (17) of the Adsorption dryer (16) is performed, characterized in that via a control of the compressors (11,12) and / or a detection and consideration of operating data, in particular a speed of the compressors (11,12), the setting of the regeneration inlet temperature T _Ri in the Regeneration sector (17) variable, namely cond is done appropriately in particular as a function of the specific status data of the gas to be compressed or the compressed gas, such as the humidity of the sucked in gas and / or the humidity of the compressed gas output from the drying sector (18) during operation of the compressor system. Method according to one of the Claim 5 , characterized in that the regeneration inlet temperature T _Ri in the regeneration sector (17) is set in such a way that the compressed gas emerging from the drying sector (18) complies with a specified minimum limit value for the degree of dryness or the pressure dew point of the compressed gas taken from the drying sector (18) Gas does not exceed a specified limit value GWT for the pressure dew point. Procedure according to Claim 5 , characterized in that the limit value GWT for the pressure dew point is set to a constant value by the user or is determined or set as a function of the application. Method according to one of the Claims 5 to 7th , characterized in that the inlet temperature T _{Ri is set} as a function of a detected pressure dew point of the compressed gas at the outlet from the drying sector (18).

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