EA043218B1 - TWO-STAGE METHOD FOR EXTRACTION OF FLUORINE-CONTAINING INHALATING ANESTHETICS - Google Patents

Description

Prerequisites for the creation of the invention

Inhalation anesthetics are administered to patients to induce or maintain anesthesia in the patient. Administered inhalation anesthetics are predominantly vented back into the environment with the air exhaled by the patient, so they are constantly released in operating rooms and vented through the roof, damaging the environment. This is because flurane-class inhalational anesthetics are composed of halogenated hydrocarbons. They are potent greenhouse gases and deplete the ozone layer. Therefore, the recovery of inhalational anesthetics from the air exhaled by patients is important to protect the health of hospital staff in areas without ventilation for environmental protection, as well as from an economic point of view.

Devices and methods by which inhalation anesthetics can be adsorbed and desorbed from patient exhaled air onto filter materials are already known.

EP 15166625 describes a filter system for a building, in particular for a hospital, which is designed to filter anesthetic gases from the gas mixture passing through the filter system.

EP 15162339 discloses a device for recovering anesthetic gases, in particular halogenated hydrocarbons, which is adapted to desorb halogenated hydrocarbons adsorbed on filter materials with steam.

Documents EP 08701206 and EP 07787403 describe a process and a filter for adsorbing halogenated hydrocarbons and then desorbing them from the filter.

WO 2007093640 describes a filter cartridge capable of adsorbing and desorbing halogenated hydrocarbons.

Inhalation anesthetics must be sterilized to reuse recovered volatile anesthetics for patient anesthesia. So far, the prior art does not know methods and devices designed to extract and sterilize inhalation anesthetics in one way.

Purpose of the invention

Therefore, it is an object of the present invention to provide a method and apparatus for improved recovery of inhalation anesthetics. This goal is achieved by the method of extracting fluorine-containing inhalation anesthetics according to claim 1. Preferred embodiments of the method are presented in paragraphs 2-9. This problem is further solved with the device according to claim 10. Preferred embodiments of the device are presented in paragraphs 11-13.

Definitions

The term adsorbent or sorbent in the context of the present description means a material that can adsorb gases on its surface. The adsorbent and sorbent are used interchangeably in the present invention.

The term sorbate means an adsorbent with gases adsorbed on it.

The term desorbate means desorbed gases.

The term sorbent refers to the gases to be adsorbed.

The term halogenated hydrocarbons is to be understood herein as meaning fluorine-containing inhalation anesthetics.

Detailed description of the present invention

The first aspect of the present invention relates to a process for recovering halogenated hydrocarbons. In this method, in the desorption step, a bulk stream consisting mainly of dry water vapor at elevated temperature is passed through the adsorbent containing adsorbed halogenated hydrocarbons (in particular, water vapor flows through the adsorbent containing adsorbed halogenated hydrocarbons). As a result, the adsorbed halogenated hydrocarbons are desorbed by the adsorbent and absorbed into the bulk stream, resulting in a secondary bulk stream containing halogenated hydrocarbons and steam. This secondary volume stream is converted by cooling into a condensate containing halogenated hydrocarbons and water. The halogenated hydrocarbons are separated from the condensate. At this stage, the temperature is in particular equal to or higher than 100°C. In various embodiments of the method, this step is carried out, in particular at a temperature of from 100 to 150°C, in particular at a temperature of from 120°C to 150°C.

According to the invention, the desorption step is preceded by a sterilization step. Thus, in particular, the sorbate is exposed to the water vapor of the hot water vapor atmosphere before flowing. The inventors have determined the parameters of this step that are necessary and sufficient to process active ingredients derived from sorbates potentially contaminated by pathogenic organisms in such a way that they comply with the regulatory requirements of European drug regulatory authorities and similar regulatory requirements in other countries. In particular, the desorption step and the sterilization step are performed in direct sequence in order to increase the efficiency of the process. However, it is also possible to provide a pause between the desorption step and the sterilization step. In addition, the desorption step and the sterilization step can in particular be carried out in the same plant or in different plants. For example, a desorption tank

- 1 043218 can be connected first to the sterilization unit and then to the desorption unit.

According to the invention, during the sterilization step, the adsorbent containing adsorbed halogenated hydrocarbons is brought into contact, in particular with dry steam for at least 10 minutes, in particular for 10 minutes to 60 minutes, at a temperature of more than 120°C, in particular at a temperature of 121° C. to 150° C., and at a pressure of 0.15 MPa to 0.4 MPa, in particular at a pressure of 0.15 MPa to 0.3 MPa.

In an embodiment, the adsorbent containing adsorbed halogenated hydrocarbons is brought into contact with, in particular, dry steam for 20 minutes to 40 minutes, in particular for about 30 minutes, at a temperature of from 135°C to 145°C and pressure from 0.24 MPa to 0.26 MPa.

By combining the sterilization parameters, namely time, temperature and pressure, conditions are created in which complete inactivation of all pathogens present in the sorbate is ensured.

At the same time, the above-mentioned sterilization parameters, namely time, temperature and pressure, are chosen so that the adsorbed halogenated hydrocarbons do not decompose or undergo chemical reactions under the prevailing conditions, so that the sterilized halogenated hydrocarbons can be reused after desorption.

According to an embodiment, water vapor does not flow through the adsorbent during the sterilization step. According to an embodiment, water vapor flows through the adsorbent only once, during the introduction of water vapor, and then remains in a positive pressure vapor atmosphere. In particular, only after the sterilization step is completed, steam is passed through the adsorbent to desorb the halogenated hydrocarbons.

The pressure increase in the sterilization step and the flow of water vapor through the adsorbent in the desorption step can be controlled, for example, by opening and closing a valve in the desorption tank. Alternatively, other manual means may be provided to carry out the steps of the method. For example, the desorption tank can be manually connected in series to the pipelines of the sterilization plant and the desorption plant, the pressure in the tank is built up by the sterilization plant, and then the volume flow in the tank is generated using the desorption plant.

According to a further embodiment, the sterilization step and the desorption step are performed in direct sequence in the desorption tank in the same plant.

For desorption, water vapor is passed through the sorbate, in particular so that a steady flow of water vapor through the sorbate allows the halogenated hydrocarbons to be taken up by the water vapor and thus removed. A mixture of water vapor and halogenated hydrocarbons is formed.

This mixture, in accordance with an embodiment of the method, is purified from trapped impurities and brought to a temperature below 30°C. A two-phase mixture of liquids is formed, i.e. condensate. The halogenated hydrocarbons are separated from this condensate and further processed. Water can be returned to the way.

According to a further embodiment, the mixture of steam and halogenated hydrocarbons is brought to a temperature below 70°C, in particular below 65°C, further in particular below 60°C, further in particular below 55°C, further in particular below 50°C, further in particular below 45°C, to form a two-phase mixture of liquids (or condensate), additionally in particular below 40°C, additionally in particular below 35°C, additionally in particular below 30°C, additionally in particular below 25°C, additionally in particular below 20° C., furthermore in particular below 15° C., furthermore in particular below 10° C., furthermore in particular below 5° C., wherein the mixture is previously purified from trapped impurities. In particular, a two-phase mixture of liquids, i.e. a condensate, is thereby formed, wherein the halogenated hydrocarbons are separated and further processed. In particular, it can be returned to the way.

The temperature to which the mixture is brought to form a condensate may be selected depending on the boiling point of the halogenated hydrocarbon to be desorbed. In this case, the temperature must be below the boiling point of the corresponding hydrocarbon. Additionally, the temperature can be optimized to minimize the gas fraction over the mixture of desorbate and water that typically forms when the heavier phase sinks in order to minimize losses through the gas phase. In addition to the boiling point of the corresponding halogenated hydrocarbon, process control parameters are also taken into account when choosing the temperature to which the condensate is brought. For example, temperatures that are too low can cause coolers or pipelines to freeze, which adversely affects the process. For example, the boiling points of some common inhalational anesthetics are as follows: sevoflurane: 58.5°C, isoflurane: 48.5°C, desflurane: 22.5°C, enflurane: 56.5°C, halothane: 50.2°C .

After desorption of the halogenated hydrocarbons, the sorbent is in particular cooled. Now the sorbent, devoid of the adsorbed substance, can be used for further adsorption/desorption cycles.

- 2 043218

According to a further embodiment, the adsorbent on which the halogenated hydrocarbons are adsorbed is an activated carbon, in particular a hydrophobic activated carbon, and/or a zeolite, in particular a hydrophobic zeolite, in particular a modified hydrophobic zeolite. The adsorbent is in particular porous and contains pores, in particular in the micrometer and/or nanometer range. You can also use a mixture of adsorbents.

According to a further embodiment of the invention, the adsorbent is characterized in that it has a water content of <5% (wt.%), in particular a water content of <2% (wt.%) before adsorption or after the whole process cycle and before being used for adsorption of anesthetics. This water content may change during the course of the process.

Adsorbents can be either hydrophilic or hydrophobic. In particular, hydrophobic adsorbents are used in the present method. Hydrophobic adsorbents can also absorb large amounts of water. Adsorption is possible only in areas of the adsorbent that are not occupied by water. Thus, the adsorbent used according to the invention should in particular have the lowest possible water content in order to be able to absorb as many halogenated hydrocarbons as possible. After desorption of halogenated hydrocarbons, the adsorbent may, for example, have a water content of more than 30% (wt.%). Once most of the water has been removed, the adsorbent can be reused.

According to a further embodiment, the steam used in the desorption step is substantially free of liquid water, in particular contains less than 0.1 weight percent liquid water, additionally in particular does not contain liquid water.

Distinguish between wet steam and superheated steam. Superheated steam is steam that has a temperature above the boiling point of water at a given pressure.

Therefore, superheated steam no longer contains liquid water. In the case of wet steam, there is always a portion of water droplets in the steam.

According to a further embodiment, the steam used is clean steam. Pure steam is obtained by evaporating fully demineralized water.

In a further embodiment, the halogenated hydrocarbons include fluorinated anesthetics or are fluorine-containing anesthetics, in particular sevoflurane, isoflurane, enflurane, halothane, desflurane, or mixtures thereof.

According to a further embodiment, the adsorbent containing halogenated hydrocarbons was obtained by filtering the exhaled air from the treatment of patients who were anesthetized with halogenated hydrocarbons.

According to a further embodiment of the method, the sterilization step and the desorption step are carried out in a desorption vessel resistant to a pressure of up to 0.4 MPa. The desorption tank contains, in particular, at least one steam inlet and at least one steam outlet. In particular, steam is supplied to the desorption tank through a steam inlet and exits the desorption tank, in particular through a steam outlet. The adsorbent containing the adsorbed halogenated hydrocarbons is positioned between the steam inlet and the steam outlet in the desorption tank such that steam entering the desorption tank through the vapor inlet must pass through the adsorbent before it exits the desorption tank through steam outlet. Thus, each point of the adsorbent containing the adsorbed halogenated hydrocarbons comes into contact with the vapor. As steam flows through the adsorbent, in particular, a temperature gradient is formed from the steam inlet to the steam outlet. Thus, the coldest point of the desorption vessel, in particular, is at the steam outlet. A temperature sensor is installed at this location.

According to an embodiment of the invention, the desorption tank comprises a valve downstream of the steam outlet, the valve being closed during the sterilization step and open during the desorption step. Thus, the required pressure in the desorption tank can be set during the sterilization step. During the sterilization step, the valve is in particular open so that the secondary volume flow can exit the desorption tank through the steam outlet.

The adsorbent containing halogenated hydrocarbons may, according to an embodiment, be contained in the desorption tank in an adsorbent container operable to be removed from the desorption tank.

The desorption vessel according to an embodiment comprises an annular wall and a bottom terminating in an annular wall, the bottom being in particular a curved bottom, in particular a convex bottom according to DIN 28011. In particular, due to its curvature, the bottom forms a cavity under the adsorbent container inserted into the desorption tank and configured to accommodate condensate. The condensate contains, in particular, condensed gases. The condensate may contain water vapor as well as halogenated hydrocarbons. The bottom is not necessarily in the form of a convex bottom, but is advantageous for the method according to the present invention, since the mixture of desorbate and water can thus pass through

- 3 043218 exhaust valve without leaving any residue.

The bottom according to an embodiment is designed to absorb as much condensate as possible under operating conditions. The amount of absorbed condensate depends on the temperature difference in the desorption tank. In certain embodiments, it is still contemplated to preheat the bottom of the tank in order to keep the amount of condensate as low as possible. In most operating conditions, it is difficult to avoid residual condensate because once some condensate has formed, it cannot be completely converted to the gas phase by subsequent steam due to the small heat transfer surface.

According to a further embodiment, the bottom of the desorption tank comprises a first shell and a second shell, wherein a space is formed between the first shell and the second shell, and steam is introduced into the space, in particular during the sterilization step, whereby the bottom is heated.

The temperature prevailing in the desorption tank is measured and controlled, in particular, by a temperature sensor. The temperature sensor is located below the adsorbent container inserted into the desorption tank, in particular between the steam outlet and the adsorbent container inserted into the desorption tank, in particular directly below the adsorbent container inserted into the desorption tank.

The temperature sensor according to the embodiment is located directly below the desiccant container. The temperature sensor is thus positioned in such a way that the sensing element is positioned exactly under the bottom of the adsorbent container. Thus, the temperature sensor always measures the temperature of the vapor phase and not the temperature of the condensate that may accumulate in the area of the bottom of the desorption tank.

According to an embodiment, the temperature sensor is configured to control the method. Once the predetermined sterilization temperature has been reached during the sterilization step, the set sterilization time is measured. After the sterilization time has elapsed, the sterilization step is terminated. This can be done by opening the valve and thus initiating the desorption step.

According to a further embodiment, a controller is provided to control the method, the controller being designed to control the method based on the temperature measured by the temperature sensor, in particular the vapor phase.

According to an embodiment, a temperature sensor is used to monitor and control the method according to the invention, but only in cases where the sterilization process is restarted when the temperature falls below the set temperature. In particular, there is no communication with the steam generator in the method. In these embodiments, the process itself, in particular, is controlled only according to a pressure above the set operating pressure.

According to an embodiment, a temperature sensor is used to monitor and control the process according to the invention by directly controlling the steam generator and, if applicable, the associated valves.

According to an embodiment, the desorption tank comprises two adsorbent containers arranged one above the other. The adsorbent containers are in particular supplied with steam through two steam inlets respectively located above or upstream of the adsorbent containers. By arranging two adsorbent containers, each with its own steam inlet, the temperature gradient in the adsorbent is reduced. Thus, sterilization is feasible even at a lower steam temperature compared to a device with only one steam inlet at any point in the adsorbent. Of course, the desorption tank may also comprise three or more adsorbent containers arranged one above the other in a similar manner.

The adsorbent container comprises, according to an embodiment, an annular wall, a bottom and/or a lid terminating in an annular wall. According to a further embodiment, the bottom and/or the lid comprise or consist of a gas-permeable filter cloth.

According to an embodiment, the filter cloth contains pores in the range of 10-100 µm, in particular in the region of 20-50 µm, in particular 40 µm.

According to a further embodiment, the filter fabric contains pores with a pore size in the range from 10 nm to 100 µm, in particular from 100 nm to 100 µm, additionally in particular from 1 µm to 100 µm, while the pores, in particular, can have different sizes. .

The adsorbent container(s) may be inserted(s) into the desorption tank.

The wall of the adsorbent container, in particular, is not in contact with the wall of the desorption tank, forming a space between the wall of the desorption tank and the wall of the adsorbent container.

In order to prevent steam from flowing in the space between the adsorbent container and the desorption tank, an adsorbent container cover according to the embodiment is provided with a seal so that steam must pass through the adsorbent container. This seal

- 4 043218 is an inflatable gland seal.

According to a further embodiment, a seal, in particular an annular seal, is provided between the desorption reservoir and the adsorbent container (or each adsorbent container in the case of multiple adsorbent containers) which closes the space between the desorption reservoir and the adsorbent container, in particular in a gas-tight manner. In particular, the seal is located at the top edge of the adsorbent container (or corresponding adsorbent container) when the (respective) adsorbent container is inserted into the desorption tank. In particular, the seal is deformed by an excess pressure (for example, an inert gas, for example, up to 0.12 MPa above the process pressure prevailing in the desorption tank), so that the seal closes the space, in particular in a gas-tight manner (in particular, the seal is pressed against to the outer wall of the desiccant container or to the inner wall of the desorption tank). According to one embodiment, the seal is only deformed during the overpressure desorption step. During the sterilization step, the seal is in particular not subjected to excess pressure so that a stable vapor atmosphere can be formed (also in the space between the adsorbent container and the desorption tank).

Another aspect of the process is the recovery of halogenated hydrocarbons in the recovery step. To this end, the secondary volume stream which exits the desorption tank according to the embodiment through the steam outlet is emptied of entrained impurities via a collection line by means of in particular a washable pre-filter and in particular a washable post-filter. . According to an embodiment, the secondary bulk flow is brought to a temperature below 30° C. by subsequent coolers, in particular three such coolers downstream.

According to a further embodiment, the secondary volume flow is brought to a temperature below 70°C, in particular below 65°C, further in particular below 60°C, further in particular below 55°C, further in particular below 50°C, further in particular below 45°C, further in particular below 40°C, further in particular below 35°C, further in particular below 30°C, further in particular below 25°C, further in particular below 20°C, further in particular below 15° C, additionally in particular below 10° C., additionally in particular below 5° C., aftercoolers, in particular three such aftercoolers.

After the last cooler, the mixture of condensate and water thus formed is sent, in particular, to a container for collecting condensate. A two-phase mixture of liquids is formed. In particular, halogenated hydrocarbons are separated from this condensate and further processed. Water can be returned to the evaporation process.

A further aspect of the present invention includes an apparatus for performing the illustrated two-stage process for recovering halogenated hydrocarbons. This device contains a pressure-resistant desorption tank. This desorption vessel comprises a steam inlet adapted to receive steam into the desorption vessel, in particular to be connected to a steam generator, a steam outlet adapted to discharge steam from the desorption vessel, the outlet being located downstream of the outlet for steam in the steam outlet direction, a valve with which the outlet can be closed, a space in particular between the steam inlet and the steam outlet, which is intended to accommodate bulk material, such as an adsorbent containing halogenated hydrocarbons.

The steam required for the process can be generated, in particular, by a steam generator which is part of the device according to the present invention. Alternatively, a separate external steam generator can also be connected to the appliance's steam inlet.

The formation of condensate according to the method according to the present invention can take place in particular in a desorption tank or in a separate condensing section or in a condensate tank.

The valve is particularly pressure resistant up to a pressure of at least 0.4 MPa. The valve is particularly configured to control the pressure in the desorption tank. When the valve is closed, it is in particular designed to allow the pressure in the desorption tank to increase. When the valve is closed, the steam outlet is in particular blocked. When the valve is open, the volume flow can exit the desorption tank, in particular through the steam outlet.

According to an embodiment of the device according to the present invention, the desorption tank comprises at least one removable adsorbent container provided to accommodate the bulk material, and a temperature sensor, which is located on the adsorbent container.

- 5 043218 sorbent or on its side facing the steam outlet, that is, on the side facing away from the steam inlet. The temperature sensor is located, in particular, immediately below the desiccant container. The adsorbent container thus forms in particular at least part of the space, in particular the entire space, which is adapted to receive the bulk material. In the case of a plurality of adsorbent containers, the plurality of adsorbent containers, in particular, jointly form said space for accommodating bulk material.

According to an embodiment of the device, the temperature sensor is connected to the control device, which is designed to open the valve after reaching the target temperature and/or after the expiration of a preselected period of time, in particular from 10 minutes to 60 minutes, during which the target temperature is maintained. The control device may be located outside the desorption tank.

According to a further embodiment, the desorption vessel comprises a curved bottom, in particular a convex bottom according to DIN 28011. The bottom is in particular designed to absorb condensed parts during the sterilization step.

According to a further embodiment, the desorption vessel is pressure resistant up to 0.4 MPa.

According to a further embodiment, the desorption tank is configured to accommodate two adsorbent containers positioned one above the other and with two steam inlets respectively positioned above the adsorbent containers.

According to a further embodiment, the device comprises a steam generator configured to generate, in particular, dry steam, the steam generator being in fluid communication or connected to at least one steam inlet.

According to a further embodiment, the apparatus comprises a dryer downstream of the steam generator, wherein the dryer is configured to generate superheated steam conditions under certain conditions. The dryer may be a mist tower.

The steam generator contains, in particular, lower and upper switching points for level control. The water level can be controlled, in particular by level control, so that the steam generator does not run without water or overflow, and in this way steam of the required quality can be provided.

It can be provided that when the fill level drops below a predetermined fill level, the steam generator, or in particular the individually switchable cartridges, each 5 kW, is automatically switched off to prevent running out of water and glowing.

According to a further embodiment, the apparatus comprises a plurality of desorption tanks, wherein the steam generator is connected to respective steam inlets of the plurality of desorption tanks. In an embodiment, the steam generator is connected to four desorption tanks. The maximum productivity of obtaining pure steam is 60 kg/h, 0.2 MPa (overpressure 1 atmosphere). This is fully exploited, in particular, in the parallel operation of four desorption tanks. In subsequent work, in particular, from about a third to a half of this value is used.

According to an additional embodiment, the device is configured to provide parallel operation of desorption tanks in different quantities with a time delay of 1 to 2 minutes.

According to a further embodiment, the steam generator is configured to produce clean steam from demineralized water.

Fully demineralized water according to an embodiment is provided by a water treatment device upstream of the steam generator. It contains in particular a tap water supply point, in particular a water softener and in particular a downstream reverse osmosis module. The treated water according to the embodiment is stored in a water storage tank connected to a steam generator. In particular, a pre-filter is installed between the tap water supply point and the water softener.

The pre-filter contains, according to an embodiment, pores with a size of 50 µm to a maximum of 100 µm.

According to a further embodiment, the pre-filter contains pores with a pore size in the range from 10 nm to 100 µm, in particular from 100 nm to 100 µm, additionally in particular from 1 µm to 100 µm, whereby, in particular, the pores can be of different size.

In particular, the fine filter is located between the water softener and the reverse osmosis module.

The pores of the fine filter according to the embodiment have a size of 2 µm to 8 µm, and the pore size may vary. In certain embodiments, the average size is 5 microns.

- 6 043218

According to an additional embodiment, the fine filter contains pores with a pore size in the range from 10 nm to 8 µm, in particular from 100 nm to 8 µm, additionally in particular from 1 µm to 8 µm, while, in particular, the pores can be of different size.

According to a further embodiment, the device comprises a condensate section, wherein the desorption tank is connected to the condensate section, and wherein the condensate section is configured to cool the secondary volume stream and produce condensate therefrom. The filter is located, in particular, between the desorption tank and the condensate section. This filter is particularly adapted to filter out all particles entrained in and separated from the secondary bulk flow as they flow through the adsorbent. This filter can, in particular, be washed. You can arrange some of these filters in series.

In an embodiment, a pre-filter, in particular a washable pre-filter, and a post-filter, in particular a washable post-filter, are located between the desorption tank and the condensate section, with the pre-filter located upstream of the post-filter.

According to one embodiment, the pre-filter contains pores with a size of 15 µm to 30 µm, in particular approximately 25 µm.

According to a further embodiment, the pre-filter contains pores with a pore size in the range from 10 nm to 30 µm, in particular from 100 nm to 30 µm, additionally in particular from 1 µm to 30 µm, in particular, the pores can be different sizes.

According to one embodiment, the post-filter contains pores with a size of 1 µm to 5 µm, in particular approximately 5 µm.

According to an additional embodiment, the post-filter contains pores with a pore size in the range from 10 nm to 5 µm, in particular from 100 nm to 5 µm, additionally in particular from 1 µm to 5 µm, while, in particular, the pores can be of different sizes.

According to a further embodiment, the condensate section comprises a pre-cooler, an intercooler, and an aftercooler that are arranged in series. According to an embodiment, the pre-cooler and intercooler are operated using (particularly uncooled) tap water or configured to operate using (particularly uncooled) tap water. The aftercooler is operated, in particular, using chilled tap water or may be operated using chilled tap water. The fine filter, in particular, is located between the intercooler and the aftercooler.

Alternatively, all coolers, ie. pre-cooler, inter-cooler and after-cooler can also be operated using chilled tap water, the temperature of which may vary depending on process control.

According to an embodiment, the fine filter contains pores with a size of 1 µm to 5 µm, in particular approximately 5 µm.

According to an additional embodiment, the fine filter contains pores with a pore size in the range from 10 nm to 5 µm, in particular from 100 nm to 5 µm, additionally in particular from 1 µm to 5 µm, while, in particular, the pores can be of different sizes. size.

According to a further embodiment, the device comprises a filter washing system, wherein the filter washing system is configured to wash the pre-filter, intermediate filter, post-filter and/or fine filter, in particular automatically. According to an additional embodiment, the filter washing system is configured to wash the pre-filter, intermediate filter, post-filter and/or fine filter with different volumes of washing liquid, in particular water (eg, demineralized water, deionized water). According to a further embodiment, the filter washing system is designed to wash the pre-filter, intermediate filter, post-filter and/or fine filter with a time delay. The filter washing system is particularly connected to a storage tank for storing washing liquid, or includes a storage tank for storing washing liquid. In particular, the filter washing system includes a pump for pumping washing liquid from the storage tank through a pre-filter, an intermediate filter, a post-filter and/or a fine filter. The upper limit of the total volume for rinsing the filters is calculated, in particular, from the volume of the storage tank minus the residual amount of filling, the size of which is determined so that the pump does not run without water.

According to a further embodiment, the condensate section is followed by a collection section. It, in particular, contains a container for collecting condensate, a compressed air generator, as well as a buffer container.

The condensate collection container is connected, in particular downstream of the aftercooler. This condensate collection container is particularly adapted to collect o

- 7 043218 well-organized condensate and its separation into its phases.

According to a further embodiment, the device comprises a buffer container, wherein the device is configured to transfer halogenated hydrocarbons, which are capable of separating from water due to their density, into the buffer container via an outlet when an appropriate fill level is reached.

According to a further embodiment, the device comprises a seal, in particular an annular seal, located or configured to be located in the space between the adsorbent container (or each adsorbent container) and the desorption reservoir, which is formed to close the space, in particular in a gas-tight manner, when the adsorbent container is inserted into the desorption tank, and thus, in particular, to prevent vapor flow in the space between the adsorbent container and the desorption tank.

According to a further embodiment, the device is configured to deform the seal by means of excess pressure (e.g. inert gas, e.g. up to 0.12 MPa above the process pressure prevailing in the desorption tank), so that the seal closes the space, in particular in a gas-tight manner (in particular , while the seal is able to press against the outer wall of the container for the adsorbent or against the inner wall of the desorption tank using excess pressure).

According to an embodiment, the device is configured to deform the seal only during the overpressure desorption step.

According to a further embodiment, the lid of the adsorbent container comprises a seal.

According to a further embodiment, the seal is in the form of an inflatable gland seal.

According to an additional embodiment, the desorption tank comprises a bottom, wherein the bottom comprises a first shell and a second shell, wherein a space is made between the first shell and the second shell, and wherein, in particular, the device is configured to supply steam into the space during the sterilization step, so that the bottom is made with the possibility of heating.

Description of figures

In FIG. 1 shows a desorption tank with two removable desiccant containers.

In FIG. 2 shows an adsorbent container.

In FIG. 3 shows a block diagram of the extraction setup.

In FIG. 1 shows a desorption vessel 100 comprising an annular wall 170 and a bottom 130 terminating in an annular wall 170, comprising two steam inlets 110a, 110b and a steam outlet 120 located on the bottom 130 of the desorption vessel. A valve 140 is disposed at the steam outlet. This valve 140 is configured to open or close the outlet pipe 190 downstream of the steam outlet 120. Two removable desiccant containers 200a, 200b are located one above the other in the desorption tank 100. Steam inlets 110a, 100b are located above the removable desiccant containers 200a, 200b. The temperature sensor 150 is disposed between the steam outlet 120 and the lower desiccant container 200b directly below the lower desiccant container 200b. It is connected to the control device 160.

In FIG. 2 shows an adsorbent container 200. It comprises an annular wall 220 terminating in a bottom 230 and a lid 240. The bottom 230 and lid 240 of the adsorbent container are provided with a filter cloth 250. 220 for the adsorbent in a gas-tight manner when the adsorbent container is inserted into the desorption tank.

In FIG. 3 shows a block diagram of the extraction setup. In the desorption tanks 100, a sterilization and desorption process takes place. The dry clean steam required for this purpose is provided in the steam generator 300 with a downstream dryer 310. The dryer 310 may be a mist tower. Clean steam is obtained from demineralized water. The demineralized water is provided in a treatment device upstream of the steam generator 300, which is configured to treat the water from the tap water supply point 410 in the first stage with the water softener 420 and in the second stage with the reverse osmosis module 430. The pre-filter 450 is located between the tap water supply point 410 and the water softener 420. The fine filter 460 is located between the water softener 420 and the reverse osmosis module 430. Behind the reverse osmosis module 430 is a water storage tank 440 for storing purified tap water for use in the steam generator 300 . Desorption tanks 100 are located between the steam generator 300 and the condensate section. The condensate section is configured to cool the gas mixture leaving the

- 8 043218 desorption tank 100, at the stage of desorption with the formation of condensate. The condensate section contains a pre-cooler 520, an intercooler 530, and an aftercooler 540. Upstream of the pre-cooler 520 are a pre-filter 510a and a post-filter 510b. The fine filter 550 is located between the intercooler 530 and aftercooler 540.

The collection section is adjacent to the condensate section. One or more interconnected condensate collection containers 610 are located downstream of the aftercooler 540 and configured to collect the condensate passing through the aftercooler 540 and separate it into its phases.

One or more buffer containers 630 may be connected to the condensate collection container 610 and configured to accommodate the condensate separated into its phases. Alternatively, only one condensate collection container 610 (no additional buffer containers 630) can be provided, which can contain all of the stripping condensate (in particular, an additional certain amount of water required to separate the stripping).

Removal of the desorbate from the desorption tank 100 can be carried out, in particular, by using the potential energy of the desorbate or, for example, by a blow of an inert gas (eg, nitrogen).

Description of Exemplary Embodiments

Example 1

The supply of superheated steam is divided into two phases. In the first phase, superheated steam flows from the steam generator to the desorption tank with the outlet valve closed until a pressure of 0.2 MPa or more is reached. This pressure and the corresponding temperature are maintained for a period of 30 minutes. During this time, autoclave-like conditions prevail in the desorption tank, ensuring complete inactivation of all pathogens present in the sorbate (bacteria, microplasmas, fungi, viruses, viroids, prions and/or parasites).

This inactivation phase is followed by a desorption phase over a period of 120 minutes during which, with the outlet valve open, a uniform flow of superheated vapor through the desorption tank allows the removal of halogenated hydrocarbons from the sorbate, which are absorbed and removed. This mixture of condensate and steam is cleaned of entrained impurities via a collector line with a washable pre-filter (stainless steel filter, 25 microns) and a washable post-filter (stainless steel, 5 microns) and brought to a temperature below 30 degrees using three coolers connected in series. Depending on the halogenated hydrocarbon to be desorbed, in particular the inhalation anesthetic, this temperature difference can be adjusted as described above. After the last cooler, the mixture of condensate and water is sent to a container for collecting condensate.

Example 2

Overview of process data for various sterilization cycles

Experiment t/°s on entrance (+15 K) t / ¹ min ' °C T ¹ max /°C Pressure /bar Time / min Microorganisms 1.1 121.11 (+15 K) 80.6 127.5 6 2.4 28:46 min Microorganisms in all positions 1.2 121.11 (+15 K) 116.62 130.9 3 2.5 28:50 min Microorganisms in one position 1.3 121.11 (+15 K) 124.59 141.4 4 2.4 28:10 min The absence of microorganisms in all positions 1.4 121.11 (+15 K) 125.01 136.5 5 2.35 28:27 min Microorganisms in two positions

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2.1 121.11 (+15 K) 126.30 134.5 7 2.44 32:53 min The absence of microorganisms in all positions 2.2 121.11 (+15 K) 100.40 130.0 7 N/A 34:49 min Microorganisms in two positions 2.3 121.11 (+15 K) 64.03 128.1 6 2.48 30:15 min Microorganisms in six positions 2.4 121.11 (+15 K) 121.68 129.2 9 2.5 28:27 The absence of microorganisms in all positions 2.5 121.11 (+15K) 127.25 131.3 4 2.5 30:22 The absence of microorganisms in all positions 3.1 121.1 (+25 K) 134.08 144.5 7 h, o 33:24 Not indicated 3.2 121.1 (+25 K) 132.15 146.4 6 3.0 37:31 Not indicated 3.3 121.1 (+25 K) 131.0 143.9 6 3.0 36:44 Not indicated 3.4 121.11 (+25 K) 134.89 138.0 8 3.0 29:03 Not indicated

List of reference designations:

100 - desorption tank;

110 - steam inlet;

110a - first steam inlet;

110b - second steam inlet;

120 - steam outlet;

130 - bottom of the desorption tank;

140 - valve;

150 - temperature sensor;

160 - control device;

170 - wall of the desorption tank;

190 - exhaust pipe;

200 - adsorbent container;

210 - seal;

220 - wall of the container for the adsorbent;

230 - the bottom of the container for the adsorbent;

240 - container cover for adsorbent;

250 - filter cloth;

300 - steam generator;

310 - dryer;

410 - tap water supply point;

420 - water softener;

430 - reverse osmosis module;

440 - water storage tank;

450 - pre-filter;

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460 - fine filter;

510 - filter;

510a - pre-filter;

510b - post-filter;

520 - pre-cooler;

530 - intercooler;

540 - aftercooler;

550 - fine filter;

610 - container for collecting condensate;

620 - compressed air generator;

630 - buffer container.

Claims (13)

1. A method for extracting fluorine-containing inhalation anesthetics, wherein at the stage of desorption, water vapor is passed through the adsorbent containing adsorbed fluorine-containing inhalation anesthetics, which leads to the formation of a secondary volume flow containing fluorine-containing inhalation anesthetics, and the secondary volume flow is converted by cooling into condensate , containing fluorine-containing inhalation anesthetics and water, from which fluorine-containing inhalation anesthetics are separated, characterized in that at the sterilization stage preceding the desorption stage, the adsorbent containing adsorbed fluorine-containing inhalation anesthetics is brought into contact with water vapor for at least 10 minutes, at temperature over 120°C and pressure from 0.15 MPa to 0.4 MPa. 2. Method according to claim 1, characterized in that the sterilization step and the desorption step are carried out in direct sequence in the same apparatus. 3. The method according to any of the preceding claims, characterized in that the adsorbent containing adsorbed fluorine-containing inhalation anesthetics was obtained by filtering the air inhaled and exhaled during the treatment of patients. 4. Method according to any one of the preceding claims, characterized in that the sterilization step is carried out for 20 to 40 minutes, in particular for about 30 minutes, at a temperature of 135 to 145°C and a pressure of 0.24 to 0, 26 MPa. 5. Method according to any one of the preceding claims, characterized in that the sterilization step and the desorption step are performed in a desorption tank (100), wherein the desorption tank (100) comprises a steam inlet (110) and a steam outlet (120) , and the adsorbent is located in the desorption tank (100) between the steam inlet (110) and the steam outlet (120), so that the steam entering the desorption tank (100) through the steam inlet (110) must flow through adsorbent before it exits the desorption tank (100) through the steam outlet (120). 6. Method according to claim 5, characterized in that the desorption tank (100) comprises a valve (140) after the steam outlet (120), wherein the valve (140) is closed during the sterilization step and open during the desorption step. 7. The method according to any one of claims 5 or 6, characterized in that the temperature prevailing in the desorption tank (100) is measured by a temperature sensor (150), and the temperature sensor (150) is located under the container (200) for the adsorbent, inserted into the desorption tank (100), in particular between the steam outlet (120) and the adsorbent container (200) inserted into the desorption tank (100), in particular directly below the adsorbent container (200) inserted into the desorption tank ( 100). 8. Method according to any one of claims 5 or 7, characterized in that the desorption tank (100) comprises two adsorbent containers (200a, 200b) positioned one above the other and the adsorbent containers (200a, 200b) can be supplied with steam through two inlets (110a, 110b) for steam, located respectively above the containers (200a, 200b) for the adsorbent. 9. Method according to any one of claims 5 to 8, characterized in that the adsorbent container (200) comprises a bottom (230) and/or a lid (240), wherein the bottom (230) and/or the lid (240) comprise a permeable gas filter cloth (250) or consist of it. 10. Apparatus for carrying out the method according to any one of the preceding claims, comprising a pressure-resistant desorption tank (100), a water vapor inlet (110) configured to receive steam into the desorption - 11 043218 ation tank (100), steam outlet (120), configured to release water vapor from the desorption tank (100), with outlet pipe (190) located downstream of the steam outlet (120) in towards the steam outlet, a valve (140) configured to close the outlet pipe (190), a space for accommodating bulk material; characterized in that the desorption tank (100) comprises an adsorbent container (200) for accommodating bulk material and a temperature sensor (150) located on the side of the adsorbent container (200) facing the steam outlet (120); and the temperature sensor (150) is connected to the control device (160), which is configured to open the valve (140) after reaching the target temperature and/or after a preselected period of time from 10 to 60 minutes has elapsed, during which the target temperature is maintained. 11. Device according to claim 10, characterized in that the desorption tank (100) is pressure resistant up to 0.4 MPa. 12. Device according to any one of claims 10 or 11, characterized in that the desorption tank is adapted to accommodate two containers (200a, 200b) for the adsorbent, located one above the other, and is provided with two inlets (110a, 110b) for steam, located respectively above the containers (200a, 200b) for the adsorbent. 13. The device according to any one of claims 10 or 11, characterized in that it contains a steam generator (300) configured to generate water vapor, while the steam generator (300) is in fluid communication with the inlet (110) for pair.