CN221244562U

CN221244562U - Gas-liquid separation equipment and water electrolysis hydrogen production processing system

Info

Publication number: CN221244562U
Application number: CN202323054989.8U
Authority: CN
Inventors: 郑联欢; 焦庆生; 邵长娜; 姜超
Original assignee: Wuxi Longji Hydrogen Energy Technology Co ltd
Current assignee: Wuxi Longji Hydrogen Energy Technology Co ltd
Priority date: 2023-11-10
Filing date: 2023-11-10
Publication date: 2024-07-02
Anticipated expiration: 2033-11-10

Abstract

The utility model belongs to the technical field of hydrogen production by water electrolysis, and discloses gas-liquid separation equipment and a water electrolysis hydrogen production treatment system. The gas-liquid separation equipment comprises at least one first gas-liquid separator, wherein the first gas-liquid separator is used for separating gas-liquid mixed liquid to obtain crude gas and liquid with gas; and the flash separator is used for separating the liquid with the entrained gas obtained by the first gas-liquid separator so as to separate the liquid from the entrained gas. The gas-liquid separation equipment can realize the rapid separation of gas and liquid, ensure the complete separation of liquid discharge and exhaust, prevent the gas-liquid entrainment phenomenon possibly occurring in the pollution discharge process, reduce the liquid discharge noise, reduce the risk of gas entering a collecting system, reduce the action frequency of a discharge control valve, save energy and reduce the failure rate of the gas-liquid separation equipment.

Description

Gas-liquid separation equipment and water electrolysis hydrogen production processing system

Technical Field

The utility model belongs to the technical field of hydrogen production by water electrolysis, and particularly relates to gas-liquid separation equipment and a water electrolysis hydrogen production treatment system.

Background

The alkaline water electrolysis hydrogen production is one of the methods which are widely applied and mature at present. The hydrogen production process using water as raw material is the reverse process of producing water by burning hydrogen and oxygen, and the hydrogen and oxygen in the hydrogen/alkali gas-liquid mixed flow produced by decomposing in the electrolytic tank can be separated from alkali liquor by gas-liquid separation process. In the existing separation process, due to factors such as equipment layout restriction, process sequence and the like, the liquid of hydrogen/oxygen after cooling and gas-water separation is generally collected by a buffer tank and then discharged.

The volume of the existing buffer tank is smaller, so that the liquid discharge frequency is high, the gas-liquid separation efficiency in the buffer tank is poor, the gas-liquid entrainment condition exists, the discharge noise is large, and the risk that the sewage collecting system is channeling into hydrogen/oxygen gas can be increased.

Disclosure of utility model

In view of the foregoing drawbacks or shortcomings in the prior art, it is desirable to provide a gas-liquid separation apparatus and a water electrolysis hydrogen production processing system.

In a first aspect of the present utility model, there is provided a gas-liquid separation apparatus comprising:

At least one first gas-liquid separator for separating the gas-liquid mixture to obtain crude gas and gas-entrained liquid;

And the flash separator is used for separating the liquid with the entrained gas obtained by the first gas-liquid separator so as to separate the liquid from the entrained gas.

According to the gas-liquid separation equipment provided by the utility model, the gas and the liquid can be rapidly separated, the complete separation of liquid discharge and exhaust is ensured, the gas-liquid entrainment phenomenon possibly occurring in the pollution discharge process is avoided, the liquid discharge noise is low, the risk of gas channeling of a collecting system is reduced, the action frequency of a discharge control valve is reduced, and the failure rate of the gas-liquid separation equipment is reduced while the energy is saved.

In addition, the gas-liquid separation equipment of the utility model can also have the following additional technical characteristics:

Preferably, the flash separator comprises a flash separation tank, wherein the top of the flash separation tank is provided with an emptying port, a first emptying pipe is arranged at the emptying port, and an emptying control valve is arranged on the first emptying pipe;

A pressure transmitter is arranged on the flash separation tank and is used for acquiring pressure information in the flash separation tank;

The emptying control valve is used for controlling the connection or disconnection of the first emptying pipe based on the pressure information acquired by the pressure transmitter.

Preferably, the evacuation control valve is used for controlling the first evacuation pipe to be conducted when the pressure in the flash separation tank is a first pressure value, and controlling the first evacuation pipe to be closed when the pressure in the flash separation tank is a second pressure value; wherein the first pressure value is greater than the second pressure value.

Preferably, a first mechanical drain valve is disposed on the first drain pipe between the drain port and the drain control valve.

Preferably, a second blow-down pipe is arranged at the blow-down port, and a second mechanical blow-down valve is arranged on the second blow-down pipe.

Preferably, a liquid outlet is formed in the side wall of the flash separation tank, a liquid outlet pipe is arranged at the liquid outlet, and a liquid outlet control valve is arranged on the liquid outlet pipe;

A liquid level transmitter is arranged on the flash separation tank and is used for detecting liquid level information in the flash separation tank;

The liquid discharge control valve is used for controlling the connection or disconnection of the liquid discharge pipe based on the liquid level information detected by the liquid level transmitter.

Preferably, the drain control valve is used for controlling the drain pipe to be conducted when the liquid in the flash separation tank is at a first liquid level, and used for controlling the drain pipe to be closed when the liquid in the flash separation tank is at a second liquid level; wherein the first liquid level is higher than the second liquid level.

Preferably, a mechanical drain valve is arranged on the drain pipe between the drain port and the drain control valve.

Preferably, a sedimentation port is arranged at the bottom of the flash separation tank, and a trash discharge valve is arranged at the sedimentation port.

Preferably, the sedimentation port is funnel-shaped.

Preferably, the flash separator comprises an atmospheric flash tank, wherein the top of the atmospheric flash tank is provided with an air vent, the side wall of the atmospheric flash tank is provided with a liquid outlet, the liquid outlet is provided with a liquid discharge pipe, and the liquid discharge pipe is provided with a liquid discharge pump;

A liquid level meter is arranged in the normal pressure flash tank and is used for acquiring liquid level information in the normal pressure flash tank;

The liquid discharge pump is used for controlling the starting and stopping of the liquid discharge pump based on the liquid level information acquired by the liquid level meter.

Preferably, the liquid discharge pump is used for controlling the liquid discharge pump to be started when the liquid in the normal pressure flash tank is at a third liquid level, and controlling the liquid discharge pump to be stopped when the liquid in the normal pressure flash tank is at a fourth liquid level; wherein the third liquid level is higher than the fourth liquid level.

In a second aspect of the embodiment of the application, a water electrolysis hydrogen production treatment system is provided, and the water electrolysis hydrogen production treatment system comprises the gas-liquid separation equipment according to any embodiment of the application.

Preferably, the water electrolysis hydrogen production processing system further comprises:

The second gas-liquid separator is used for separating gas-liquid mixed liquid generated by the decomposition of the electrolytic tank to obtain gas and liquid with liquid carried by the gas-liquid mixed liquid; the gas-liquid mixed solution comprises a mixed solution of hydrogen and alkali liquor or a mixed solution of oxygen and alkali liquor;

The scrubber is used for scrubbing the gas with the liquid to obtain scrubbed gas;

And the cooler is used for cooling the washed gas to obtain gas carrying liquid, and sending the gas carrying liquid into the first gas-liquid separator.

Additional aspects and advantages of the utility model will be set forth in part in the description which follows, and in part will be obvious from the description, or may be learned by practice of the utility model.

Drawings

Other features, objects and advantages of the present application will become more apparent upon reading of the detailed description of non-limiting embodiments, made with reference to the accompanying drawings in which:

FIG. 1 is an exemplary block diagram of a prior art hydro-electrolytic hydrogen production processing system;

FIG. 2 is an exemplary block diagram of a water electrolysis hydrogen production processing system provided in an embodiment of the present application;

FIG. 3 is an exemplary block diagram of a flash separator provided in an embodiment of the present application.

In the above figures: 10a first gas-liquid separator; a flash separator 20; 210 flash separation tank; 220 a first blow-down pipe; 221 an evacuation control valve; 222 a first mechanical drain valve; 230 pressure transmitter; 240 a second blow-down tube; 241 a second mechanical drain valve; 250 drain pipes; 251 drain control valve; 252 mechanical drain valve; 260 a level transmitter; 270 precipitation ports; 280 liquid inlet pipe; 281 first shut-off valve; 290 branch pipes; 291 second shut-off valve; a second gas-liquid separator 30; a 40 scrubber; a 50 cooler; 60 buffer tanks.

Detailed Description

The utility model is described in further detail below with reference to the drawings and examples. It is to be understood that the specific embodiments described herein are merely illustrative of the utility model and are not limiting of the utility model. It should be further noted that, for convenience of description, only a portion related to the present utility model is shown in the drawings.

It should be noted that, without conflict, the embodiments of the present application and features of the embodiments may be combined with each other. The application will be described in detail below with reference to the drawings in connection with embodiments.

The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the application. As used in this specification and the appended claims, the singular forms "a," "an," and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise. It should also be understood that the term "and/or" as used herein refers to and encompasses any or all possible combinations of one or more of the associated listed items.

Throughout the specification and claims, the term "comprising" is to be interpreted as an open, inclusive meaning, i.e. "comprising, but not limited to, unless the context requires otherwise.

In the description of the present specification, the terms "one embodiment," "some embodiments," "example embodiments," "examples," "particular examples," or "some examples," etc., are intended to indicate that a particular feature, structure, material, or characteristic associated with the embodiment or example is included in at least one embodiment or example of the present disclosure. The schematic representations of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics may be combined in any suitable manner in any one or more embodiments or examples.

The terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the embodiments of the present disclosure, unless otherwise indicated, the meaning of "a plurality" is two or more.

In the existing alkaline water electrolysis hydrogen production system, water is decomposed through an electrolytic tank to generate a gas-liquid mixed solution of hydrogen and alkali liquor and a gas-liquid mixed solution of oxygen and alkali liquor, the two types of gas-liquid mixed solutions are subjected to a gas-liquid separation process to separate the hydrogen from the alkali liquor and the oxygen from the alkali liquor, the separation processes of the two types of gas-liquid mixed solutions are the same, and the existing gas-liquid separation and pollution discharge process is exemplified by a gas-liquid mixed solution separation process of the hydrogen and the alkali liquor, and is as follows:

As shown in fig. 1, for the gas-liquid mixed solution of hydrogen side, a second gas-liquid separator 30, such as a hydrogen-liquid separator, is firstly adopted to carry out gas-liquid separation on the gas-liquid mixed solution of hydrogen and alkali liquor, the separated hydrogen is provided with a small amount of alkali liquor, the hydrogen is fed into a hydrogen scrubber 40 to be washed, the washed gas is fed into a hydrogen cooler 50 to be cooled, water in the hydrogen gradually condenses and separates out in the cooling process, a small amount of condensate is entrained with the hydrogen to a first gas-liquid separator 10, such as a gas-water separator, the liquid phase separated by the gas-water separator automatically flows to a buffer tank 60 from a bottom outlet, and when the liquid in the buffer tank 60 is collected to a certain liquid level, the part of liquid is intermittently discharged as process waste liquid at regular time.

According to the above process description, the liquid phase finally separated by the gas-water separator is collected and discharged through the buffer tank 60, and the discharge frequency is high due to the small volume of the buffer tank 60, and the gas-liquid entrainment condition exists during liquid discharge due to the existence of a certain gas phase in the condensate buffer tank 60, so that the discharge noise is high, and the risk of the sewage collecting system channeling hydrogen/oxygen gas is increased.

Since the collection buffer tank 60 is arranged in a timed discharge manner, the collection buffer tank 60 is placed at the lowest point in the layout, and the front and rear shut-off valves of the collection buffer tank 60 are arranged in opposite phases. Firstly, a feed valve is closed, a discharge valve is opened, the collecting liquid buffer tank 60 is depressurized to normal pressure, then the feed valve is opened, the discharge valve is closed, water and air are pressed into the collecting liquid buffer tank 60 under the system pressure, the valve opening and closing process is repeated after the tank is full, and waste liquid is discharged to a sewage collecting pipe network by the pressure in the tank. Meanwhile, in order to meet the process control requirement, a shut-off valve is required to be arranged at the inlet/outlet of the condensate collection buffer tank 60, and automatic valve interlocking control is arranged, so that the condensate is discharged regularly, high-frequency valve action is realized, and the probability of system faults is increased.

To solve the above technical problem, referring to fig. 2 and 3, a first aspect of an embodiment of the present application provides a gas-liquid separation apparatus, including:

at least one first gas-liquid separator 10 for separating the gas-liquid mixture to obtain a crude gas and a gas-entrained liquid;

A flash separator 20 for separating the gas-entrained liquid from the gas-entrained liquid obtained from the first gas-liquid separator 10.

Specifically, the gas-liquid separation device is used for treating gas-liquid mixed liquid so as to realize rapid and thorough separation of gas and liquid, wherein the specific types of the gas and the liquid can be set by one skilled in the art according to actual requirements. In the embodiment of the application, taking the mixed solution of hydrogen and alkali liquor generated in the water electrolysis hydrogen production process as an example, the treatment process of the gas-liquid mixed solution by the gas-liquid separation equipment provided by the embodiment of the application is exemplified, and the treatment principle of other types of gas-liquid mixed solutions of the gas-liquid separation equipment, such as the mixed solution of oxygen and alkali liquor, is the same, and the application is not repeated.

The first gas-liquid separator 10 may be a gas-water separator, the top of the first gas-liquid separator 10 has an air outlet, the bottom of the first gas-liquid separator has a liquid outlet, the first gas-liquid separator 10 is used for separating a mixed liquid of hydrogen and mist, the separated crude gas such as hydrogen is discharged through the air outlet for subsequent process treatment, and a small amount of hydrogen is entrained in the separated liquid such as dilute alkali solution and discharged from the liquid outlet. Because of the different specific gravity of the gas and the liquid, the liquid is subjected to a larger gravity force when flowing together with the gas, a downward speed is generated, the gas still flows towards the original direction, the liquid and the gas have a tendency to be separated in the gravity field, the downward liquid is attached to the wall surface and gathered together, and the downward liquid is discharged through a liquid outlet at the bottom of the first gas-liquid separator 10.

The bottom of the side wall of the flash separator 20 (flash vaporization) is provided with a liquid inlet, the liquid outlet of the first gas-liquid separator 10 is communicated with the liquid inlet of the flash separator 20 through a liquid inlet pipe 280, the liquid inlet pipe 280 is provided with a first cut-off valve 281, and the first cut-off valve 281 can be a pressure reducing valve, a mechanical valve or an electric valve. By controlling the first shut-off valve 281 on the feed pipe 280, the liquid separated by the first gas-liquid separator 10 (or the liquid entrained with the gas) can be discharged into the flash separator 20 at regular intervals.

The liquid with gas discharged from the liquid outlet at the bottom of the first gas-liquid separator 10 flows into the flash separator 20 through the liquid inlet pipe 280, the flash separator 20 utilizes the difference of saturated vapor pressures of substances at different temperatures, and the liquid substances are quickly evaporated by reducing the pressure, so that the conversion of the liquid substances into gaseous substances is realized, the quick separation of gas and liquid is realized, the complete separation of liquid discharge and exhaust is ensured, and the gas-liquid entrainment possibly occurring in the pollution discharge process is avoided.

The plurality of first gas-liquid separators 10 may be in communication with one flash separator 20 to increase the gas-liquid separation efficiency of the flash separator 20.

According to the gas-liquid separation equipment provided by the utility model, the existing gas-liquid separation pollution discharge process is optimized, the flash separator 20 is adopted to replace the existing buffer tank 60, the capacity of the flash separator 20 is 1.5-2 times that of the existing buffer tank 60, the flash separator 20 with larger capacity is utilized to reduce the action frequency of discharge control valves (such as the first cut-off valve 281 on the liquid inlet pipe 280 and the liquid discharge valve on the liquid discharge pipe 250), the failure rate of the gas-liquid separation equipment is reduced while energy is saved, the thorough separation of liquid and gas can be realized, the generation of gas-liquid entrainment phenomenon is avoided, the liquid discharge noise is low, and the risk of the sewage collecting system channeling hydrogen/oxygen gas is reduced.

In some embodiments, as shown in fig. 2 and 3, the flash separator 20 includes a flash separation tank 210, a vent is provided at the top of the flash separation tank 210, a first vent pipe 220 is provided at the vent, and a vent control valve 221 is provided on the first vent pipe 220;

a pressure transmitter 230 is arranged on the flash separation tank 210, and the pressure transmitter 230 is used for acquiring pressure information in the flash separation tank 210;

The evacuation control valve 221 is configured to control the first evacuation pipe 220 to be turned on or off based on pressure information obtained by the pressure transmitter 230.

Specifically, the sewage (such as dilute alkali solution) and entrained gas (such as oxygen or hydrogen) collected by the flash separation tank 210 are subjected to balanced flash separation (flash vaporization equilibrium) in the flash separation tank 210, a pressure-emptying interlocking loop is arranged on the flash separation tank 210, that is, a pressure transmitter 230 (PT) is arranged on the flash separation tank 210, the pressure transmitter 230 can measure pressure information in the flash separation tank 210 in real time, and an emptying control valve 221 is controlled to perform corresponding operation according to the pressure information measured by the pressure transmitter 230 so as to control the on or off of the first emptying pipe 220, so that automatic control of exhaust is realized. The drain control valve 221 may be an electric valve or a pneumatic valve, and the electric valve may be a switch-type electric valve or an adjustment-type electric valve, or may be an electric ball valve or an electric butterfly valve; the pneumatic valve can be a butterfly valve, a ball valve, a stop valve and the like.

For the hydrogen production process, the gas discharged from the vent is typically hydrogen or oxygen. In some embodiments, the vent control valve 221 is configured to control the first vent pipe 220 to conduct when the pressure within the flash separation tank 210 is a first pressure value, and to control the first vent pipe 220 to close when the pressure within the flash separation tank 210 is a second pressure value; wherein the first pressure value is greater than the second pressure value.

Specifically, the pressure in the flash separation tank 210 is derived from the first gas-liquid separator 10, a first shut-off valve 281 on a liquid inlet pipe 280 between the first gas-liquid separator 10 and the flash separation tank 210 is opened, the first gas-liquid separator 10 provides pressure into the flash separation tank 210, the pressure in the flash separation tank 210 is gradually increased, when the pressure is increased to a first pressure value, an emptying control valve 221 controls a first emptying pipe 220 to be communicated, and hydrogen in the flash separation tank 210 is discharged from an emptying port; then the pressure in the flash separation tank 210 is gradually reduced, and when the pressure in the flash separation tank 210 is reduced to the second pressure value, the emptying control valve 221 controls the first emptying pipe 220 to be closed, so that the minimum equilibrium set pressure in the flash separation tank 210 is maintained, and the equilibrium flash separation of the gas and the liquid in the flash separation tank 210 is ensured. The evacuation control valve 221 may also be an electric valve or a pneumatic valve, and the specific type of the evacuation control valve 221 is not described in detail herein.

The first pressure value and the second pressure value can be preset by a person skilled in the art according to actual needs, where the first pressure value is a starting pressure value that needs to be reached when the evacuation control valve 221 controls the first evacuation pipe 220 to be turned on, and the second pressure value is a starting pressure value that needs to be reached when the evacuation control valve 221 controls the first evacuation pipe 220 to be turned off.

In this example, controlling whether to discharge gas based on the magnitude of the pressure in the flash separation tank 210 reduces the operating frequency of the purge control valve 221, saves energy while reducing the failure rate of the purge control valve 221; and the interlocking control mode of the pressure transmitter 230 and the evacuation control valve 221 is adopted, so that the control precision of the evacuation control valve 221 is improved, the intelligent gas emission control is realized, and the operation difficulty and the maintenance strength are reduced. The pressure-emptying interlocking loop is utilized to ensure that the pressure in the balanced flash separation tank 210 is always in a process set interval, and can provide power for automatic liquid discharge, so that the position arrangement of the flash separation tank 210 is more flexible.

In some embodiments, as shown in fig. 2 and 3, a first mechanical purge valve 222 is disposed on the first purge tube 220 between the purge port and the purge control valve 221.

Specifically, when the evacuation control valve 221 fails, the first mechanical evacuation valve 222 may control the first evacuation pipe 220 to be turned on or off, so as to improve the safety of the gas-liquid separation device.

In some embodiments, as shown in fig. 2 and 3, a second blow-down pipe 240 is disposed at the blow-down port, and a second mechanical blow-down valve 241 is disposed on the second blow-down pipe 240.

Specifically, the second mechanical evacuation valve 241 is used to control the second evacuation pipe 240 to be turned on or off, and in practical application, when the flash separation tank 210 needs to be overhauled, the second mechanical evacuation valve 241 is used to control the second evacuation pipe 240 to be turned on, so as to evacuate the gas in the flash separation tank 210, without triggering the interlocking control mode of the pressure transmitter 230 and the evacuation control valve 221.

In some embodiments, as shown in fig. 2 and 3, a liquid outlet is formed on the side wall of the flash separation tank 210, a liquid outlet pipe 250 is disposed at the liquid outlet, and a liquid outlet control valve 251 is disposed on the liquid outlet pipe 250;

A liquid level transmitter 260 is arranged on the flash separation tank 210, and the liquid level transmitter 260 is used for detecting liquid level information in the flash separation tank 210;

The drain control valve 251 is configured to control the on or off of the drain pipe 250 based on the liquid level information detected by the liquid level transmitter 260.

Specifically, a liquid level-liquid draining interlocking loop is arranged on the flash separation tank 210, that is, a liquid level transmitter 260 (LT) is arranged on the flash separation tank 210, the liquid level transmitter 260 can measure liquid level information in the flash separation tank 210 in real time, and a liquid draining control valve 251 is controlled to execute corresponding operation according to the liquid level information measured by the liquid level transmitter 260 so as to control the connection or the disconnection of a liquid draining pipe 250, so that automatic control of liquid draining is realized. For the hydrogen production process, the liquid discharged from the liquid outlet is typically alkali solution such as dilute potassium hydroxide solution.

In some embodiments, the drain control valve 251 is configured to control the drain 250 to be on when the liquid in the flash separation tank 210 is at a first level, and to control the drain 250 to be off when the liquid in the flash separation tank 210 is at a second level; wherein the first liquid level is higher than the second liquid level.

Specifically, a first shut-off valve 281 on a liquid inlet pipe 280 between the first gas-liquid separator 10 and the flash separation tank 210 is opened, liquid in the first gas-liquid separator 10, such as alkali liquor or alkali liquor entrained with hydrogen, flows to the flash separation tank 210, the liquid level in the flash separation tank 210 gradually rises, when the liquid level rises to the first liquid level, a liquid discharge control valve 251 controls a liquid discharge pipe 250 to be conducted, liquid in the flash separation tank 210, such as alkali liquor, is discharged from a liquid discharge port, supernatant (such as alkali liquor) in sewage is discharged by using the pressure in the flash separation tank 210, the alkali liquor has a certain recycling value, and can be collected by a recycling system or a waste water collecting system. Wherein, the liquid outlet can be arranged at the bottom end of the side wall of the flash separation tank 210, so that the liquid in the flash separation tank 210 can flow out from the liquid outlet. During the liquid discharge, the liquid level in the flash separation tank 210 gradually decreases until the liquid level decreases to the second level, and the drain control valve 251 controls the drain pipe 250 to be closed, stopping the drain.

The sizes of the first liquid level and the second liquid level can be preset according to actual demands by a person skilled in the art, the first liquid level is higher than the second liquid level, the first liquid level is a starting liquid level value which needs to be reached when the liquid discharge control valve 251 valve controls the liquid discharge pipe 250 to be conducted, and the second liquid level is a starting liquid level value which needs to be reached when the liquid discharge control valve 251 controls the liquid discharge pipe 250 to be closed.

In this example, controlling whether to drain liquid based on the liquid level condition in flash separation tank 210 reduces the operating frequency of drain control valve 251, saves energy while reducing the failure rate of drain control valve 251; and the liquid level transmitter 260 and the liquid discharge control valve 251 are in an interlocking control mode, so that the control precision of the liquid discharge control valve 251 is improved, intelligent liquid discharge control is realized, and the operation difficulty and maintenance intensity are reduced. The pressure of the flash separation tank 210 can be flexibly set according to the process requirement, and the pressure is matched with an automatic liquid discharge interlocking control loop, so that the installation height limit of the flash separation tank 210 is solved, the flash separation tank can be flexibly arranged according to the field condition, and the layout is more reasonable.

In some embodiments, as shown in fig. 2 and 3, a mechanical drain valve 252 is provided on the drain 250 between the drain port and the drain control valve 251.

Specifically, the mechanical drain valve 252 is used to control the drain 250 to be turned on or off, in practical application, when the flash separation tank 210 needs to be overhauled, the mechanical drain valve 252 can be used to control the drain 250 to be turned on, so as to drain the liquid in the flash separation tank 210, without triggering the interlocking control mode of the liquid level transmitter 260 and the drain control valve 251, so that the operating frequency of the drain control valve 251 is reduced, and the failure rate of the drain control valve 251 is reduced.

In the embodiment of the application, the top of the flash separation tank 210 is exhausted, the bottom is discharged, the gas-liquid two phases are ensured to be completely separated in the discharging process, and the complete gas-liquid equilibrium separation is realized by utilizing the equilibrium flash separation principle. The flash separation tank 210 is provided with a pressure-emptying interlocking loop and a liquid level-liquid discharge interlocking loop, so that the system pressure is ensured, the complete separation of gas/liquid discharged materials is ensured, and the problem of gas-liquid entrainment in the pollution discharge process is avoided.

In some embodiments, as shown in fig. 2 and 3, a settling port 270 is provided at the bottom of the flash separation tank 210, and an electric impurity removal valve is provided at the settling port 270.

Specifically, for the hydrogen production process, impurities such as alkali solution in a crystalline state, e.g., potassium hydroxide in a crystalline state, may be generated in the flash separation tank 210 after separating the hydrogen and the alkali solution, and may be discharged through the precipitation port 270. A trash discharge valve, which may be a pneumatic valve, an electric valve, or a mechanical valve, is provided at the settling port 270; wherein, set up electric or pneumatic trash discharge valve at precipitation port 270, can realize precipitation port 270's automation and open and close, improve intelligent operation degree. The mechanical impurity discharging valve is arranged at the precipitation port 270, and the mechanical impurity discharging valve can be manually controlled, so that the situation that liquid cannot be discharged due to the failure of the electric or pneumatic impurity discharging valve is prevented, and the use safety of the flash separation tank 210 is improved.

In some embodiments, as shown in fig. 2 and 3, the sedimentation port 270 is funnel-shaped in shape.

Specifically, a funnel-shaped settling port 270 is provided at the bottom of the flash separation tank 210, and the funnel-shaped settling port 270 can be used as a collection area for impurities such as potassium hydroxide in a crystalline state. The funnel-shaped settling port 270 includes a conical funnel and a straight cannula communicating with the bottom of the conical funnel. The electric impurity removing valve or/and the mechanical impurity removing valve can be arranged on the straight insertion pipe or on a drain pipe communicated with the straight insertion pipe, and the collected sediment such as impurities is discharged periodically. Wherein the inclination angle between the face of the cone-shaped bucket and the horizontal plane is 25-60 degrees, preferably 30-45 degrees, such as 30 degrees, 35 degrees, 40 degrees, 45 degrees and the like, preferably 30 degrees, which can be set by those skilled in the art according to actual requirements.

In this example, the bottom of the flash separation tank 210 is provided with a dedicated settling and standing collection zone, which ensures a sufficient residence time and a sufficient settling and collecting space for solid residues and the like in the liquid in the flash separation tank 210, and enables the periodic discharge of the collected sediments such as impurities.

It should be noted that, compared to the existing horizontal buffer tank 60, the flash separation tank 210 provided in the embodiment of the present application is a vertical flash separation tank 210, the vertical distance between the liquid inlet at the bottom of the sidewall of the vertical flash separation tank 210 and the precipitation opening 270 provided at the bottom is a preset distance, the preset distance may be set according to actual requirements, and the vertical distance between the liquid inlet and the precipitation opening 270 may be ensured to be set to a larger distance value by the vertical flash separation tank 210, so as to ensure that solid impurities in the flash separation tank 210 can have sufficient time to be precipitated and collected in the funnel region of the precipitation opening 270, thereby improving the solid-liquid separation efficiency.

The flash separation tank 210 provided by the embodiment of the application can realize solid-liquid separation of waste liquid such as alkali liquor, supernatant obtained by separation is discharged from the liquid outlet at the bottom of the side wall of the flash separation tank 210, has recycling value, reduces the discharge of waste water, and the funnel-shaped precipitation port 270 arranged at the bottom can collect solid residues and discharge the solid residues regularly, so that the discharge amount of waste water is reduced, and the environmental friendliness of gas-liquid separation equipment is improved. In addition, the gas-liquid separation equipment provided by the embodiment of the application can realize centralized collection treatment of all pollution discharge (such as alkali liquor), simplify the system, facilitate field management by uniformly arranging the flash separation tanks 210, reduce the complexity of the process and the failure rate of the equipment by the centralized arrangement of the flash separation tanks 210, and reduce the operation difficulty and the maintenance strength.

In some embodiments, as shown in fig. 2 and 3, a branch pipe 290 is disposed on the liquid inlet pipe 280 between the liquid outlet of the first gas-liquid separator 10 and the first cut-off valve 281, and a second cut-off valve 291 is disposed on the branch pipe 290.

Specifically, the branch pipe 290 is communicated with the liquid inlet pipe 280, the second shut-off valve 291 may control the connection or disconnection of the branch pipe 290, and the second shut-off valve 291 may be a mechanical valve or an electric valve. When the flash separator 20 is in failure and requires maintenance or when the flash separator 20 is in regular maintenance, the first cut-off valve 281 may be closed, the second cut-off valve 291 may be opened, and the liquid discharged from the first gas-liquid separator 10 may be directly discharged to an external treatment system without being treated by the flash separator 20.

Illustratively, the first shut-off valve 281 is open and the second shut-off valve 291 is closed, and the liquid within the first gas-liquid separator 10 flows into the flash separation tank 210 for flash separation; the first shut-off valve 281 is closed and the second shut-off valve 291 is opened, and the liquid in the first gas-liquid separator 10 flows into the external processing system.

In other embodiments, the flash separator 20 comprises an atmospheric flash tank, the top of the atmospheric flash tank is provided with a vent, the side wall of the atmospheric flash tank is provided with a liquid outlet, the liquid outlet is provided with a liquid discharge pipe 250, and the liquid discharge pipe 250 is provided with a liquid discharge pump;

Specifically, the top of the normal pressure flash tank is provided with a vent, so that continuous discharge of gases such as hydrogen or oxygen can be realized. The bottom of the side wall of the normal pressure flash tank is provided with a liquid outlet, a liquid discharge pump is arranged at the liquid outlet, and the liquid discharge speed is improved by adopting the liquid discharge pump. The liquid level meter is arranged in the normal pressure separation tank, can acquire liquid level information in the normal pressure separation tank in real time, and controls the start or stop of the liquid discharge pump based on the liquid level information acquired by the liquid level meter. In the example, through the interlocking control of the liquid level meter and the liquid discharge pump, the automatic liquid discharge of the normal pressure separation tank is realized, the intelligent degree is high, and the control precision is high.

Wherein, the middle part of the side wall of the normal pressure separating tank is provided with a liquid inlet, the liquid outlet of the first gas-liquid separator 10 is communicated with the liquid inlet of the normal pressure separating tank through a liquid inlet pipe 280, the liquid inlet pipe 280 is provided with a first cut-off valve 281, and the first cut-off valve 281 can be a pressure reducing valve, a mechanical valve or an electric valve. By controlling the first shut-off valve 281 on the liquid inlet pipe 280, the liquid separated by the first gas-liquid separator 10 (or the liquid with entrained gas) can be discharged into the atmospheric pressure separation tank at regular intervals. The bottom of the side wall of the normal pressure separation tank is provided with a liquid outlet, the liquid outlet is provided with a liquid outlet pipe 250, the liquid outlet pipe 250 is provided with a cut-off valve, and the conduction or the closing of the liquid outlet pipe 250 can be controlled through the cut-off valve.

In other embodiments, the liquid displacement pump is configured to control the liquid displacement pump to start when the liquid in the atmospheric flash tank is at a third level and to control the liquid displacement pump to stop when the liquid in the atmospheric flash tank is at a fourth level; wherein the third liquid level is higher than the fourth liquid level.

Specifically, a first shut-off valve 281 on a liquid inlet pipe 280 between the first gas-liquid separator 10 and the normal pressure separation tank is opened, liquid in the first gas-liquid separator 10, such as alkali liquid or alkali liquid with hydrogen, flows to the normal pressure separation tank, the liquid level in the normal pressure separation tank gradually rises, when the liquid level rises to a third liquid level, a liquid discharge pump is started, a shut-off valve on the liquid discharge pipe 250 is opened, liquid in the normal pressure separation tank, such as alkali liquid, is discharged from a liquid discharge port, and the liquid discharge rate is increased through the liquid discharge pump. In the process of discharging the liquid, the liquid level in the normal pressure separation tank gradually decreases until the liquid level decreases to the fourth liquid level, the liquid discharge pump stops working, and the shut-off valve on the liquid discharge pipe 250 is closed to stop liquid discharge.

In the example, the liquid discharging speed is improved by adopting the liquid discharging pump, and the automatic discharge of the liquid in the normal pressure separation tank is realized in an interlocking control mode of high-start and low-stop of the liquid discharging pump and the liquid level meter, so that the intelligent degree is high.

Specifically, the gas-liquid separation device provided by any embodiment of the application is used for treating the mixed liquid of hydrogen and alkali liquor generated by water electrolysis hydrogen production, or treating the mixed liquid of generated oxygen and alkali liquor, so that the separation efficiency and the separation effect of gas and liquid are improved, the action frequency of a discharge control valve is reduced by using the flash separator 20 with larger volume, the failure rate of the gas-liquid separation device is reduced while energy is saved, the thorough separation of liquid and gas can be realized, the generation of gas-liquid entrainment phenomenon is avoided, the liquid discharge noise is low, and the risk of the sewage collecting system channeling hydrogen/oxygen gas is reduced.

In some embodiments, as shown in fig. 2, the water electrolysis hydrogen production processing system further comprises:

A second gas-liquid separator 30 for separating the gas-liquid mixture generated by the decomposition of the electrolytic cell to obtain a gas and a liquid with entrained liquid; the gas-liquid mixed solution comprises a mixed solution of hydrogen and alkali liquor or a mixed solution of oxygen and alkali liquor;

a scrubber 40 for scrubbing the gas entrained with the liquid to obtain a scrubbed gas;

A cooler 50 for cooling the scrubbed gas to obtain a liquid-carrying gas, and feeding the liquid-carrying gas into the first gas-liquid separator 10.

Specifically, the liquid inlet of the second gas-liquid separator 30 is communicated with at least one electrolytic tank, the hydrogen/alkali liquid mixed solution and the oxygen/alkali liquid mixed solution generated by the electrolytic tank enter the second gas-liquid separator 30 to perform gas-liquid separation, the separated hydrogen or oxygen is sent out from the gas phase outlet at the top of the second gas-liquid separator 30, and the separated alkali liquid is discharged from the liquid outlet at the bottom of the second gas-liquid separator 30 and flows into an alkali liquid circulation system. Wherein the liquid inlet of the second gas-liquid separator 30 may be connected to a plurality of electrolytic cells, thereby improving the separation efficiency of the electrolytic products such as the hydrogen/alkali solution mixture and the oxygen/alkali solution mixture.

The hydrogen or oxygen separated by the second gas-liquid separator 30 is entrained with a small amount of alkali liquor, and is pumped by a pump to be washed by the washer 40, and the washing water is used as system consumption water supplement. The scrubber 40 is provided with an overflow port which is communicated with the liquid inlet of the second gas-liquid separator 30 at the lower part through a pipeline, and can repeatedly separate alkali liquid with gas entrained, so as to improve the separation efficiency of hydrogen or oxygen and the alkali liquid. The gas phase separated by the second gas-liquid separator 30 is discharged through a gas outlet, the gas outlet is inserted below the inner liquid surface of the scrubber 40 through a conduit, the scrubber is performed by bubbling, and the scrubbed hydrogen or oxygen is delivered to the cooler 50 through a gas phase outlet at the upper part of the scrubber 40.

The cooler 50 cools the hydrogen or oxygen, and in the cooling process, the water of the hydrogen or oxygen gradually condenses out, most of condensate flows back to the second gas-liquid separator 30 through the condensate port of the cooler 50, and a small part of condensate is entrained to the first gas-liquid separator 10 along with the hydrogen or oxygen.

The first gas-liquid separator 10 separates the gas-liquid mixture of the entering hydrogen or oxygen carrying the condensate, the separated gas phase is sent to the subsequent treatment unit through a gas phase outlet at the top of the separator, and the liquid phase is sent to the flash separator 20 for gas-liquid separation.

It should be noted that, the gas-liquid separation device and the water electrolysis hydrogen production treatment system provided by the embodiment of the application treat the gas-liquid mixed liquid generated in the hydrogen production process, and the liquid in the field can treat other types of gas-liquid mixed liquid according to actual requirements, for example, the gas-liquid separation process of the pressure system in the industries of traditional fine chemical engineering, petrochemical engineering, semiconductors, new energy sources and the like can all adopt the gas-liquid separation device and the water electrolysis hydrogen production treatment system provided by the embodiment of the application for treatment.

The above description is only illustrative of the preferred embodiments of the present utility model and of the principles of the technology employed. It will be appreciated by persons skilled in the art that the scope of the utility model referred to in the present utility model is not limited to the specific combinations of the technical features described above, but also covers other technical features formed by any combination of the technical features described above or their equivalents without departing from the inventive concept. Such as the above-mentioned features and the technical features disclosed in the present utility model (but not limited to) having similar functions are replaced with each other.

Claims

1. A gas-liquid separation apparatus, characterized by comprising:

The flash separator is used for separating the liquid with the entrained gas obtained by the first gas-liquid separator so as to separate the liquid from the entrained gas;

The flash separator comprises a flash separation tank, wherein the top of the flash separation tank is provided with an emptying port, a first emptying pipe is arranged at the emptying port, and an emptying control valve is arranged on the first emptying pipe;

2. The gas-liquid separation apparatus according to claim 1, wherein the purge control valve is configured to control the first purge pipe to be turned on when the pressure in the flash separation tank is a first pressure value, and to control the first purge pipe to be turned off when the pressure in the flash separation tank is a second pressure value; wherein the first pressure value is greater than the second pressure value.

3. The gas-liquid separation apparatus of claim 2, wherein a first mechanical purge valve is disposed on the first purge line between the purge port and the purge control valve.

4. A gas-liquid separation apparatus according to claim 3, wherein a second blow-down pipe is provided at the blow-down port, and a second mechanical blow-down valve is provided on the second blow-down pipe.

5. The gas-liquid separation equipment according to any one of claims 1 to 4, wherein a liquid discharge port is formed in the side wall of the flash separation tank, a liquid discharge pipe is arranged at the liquid discharge port, and a liquid discharge control valve is arranged on the liquid discharge pipe;

6. The gas-liquid separation apparatus of claim 5, wherein the drain control valve is configured to control the drain to conduct when liquid in the flash separation tank is at a first level and to control the drain to close when liquid in the flash separation tank is at a second level; wherein the first liquid level is higher than the second liquid level.

7. The gas-liquid separation apparatus according to claim 6, wherein a mechanical drain valve is provided on the drain pipe between the drain port and the drain control valve.

8. The gas-liquid separation apparatus according to any one of claims 1 to 4, wherein a settling port is provided at the bottom of the flash separation tank, and a drain valve is provided at the settling port.

9. The gas-liquid separation apparatus according to claim 8, wherein the settling port is funnel-shaped in shape.

10. The gas-liquid separation equipment according to claim 1, wherein the flash separator comprises an atmospheric flash tank, a vent is arranged at the top of the atmospheric flash tank, a liquid outlet is arranged on the side wall of the atmospheric flash tank, a liquid discharge pipe is arranged at the liquid outlet, and a liquid discharge pump is arranged on the liquid discharge pipe;

11. The gas-liquid separation apparatus of claim 10, wherein the liquid displacement pump is configured to control the liquid displacement pump to be activated when the liquid in the atmospheric flash tank is at a third liquid level and to control the liquid displacement pump to be deactivated when the liquid in the atmospheric flash tank is at a fourth liquid level; wherein the third liquid level is higher than the fourth liquid level.

12. A water electrolysis hydrogen production processing system, characterized in that it comprises the gas-liquid separation apparatus according to any one of claims 1 to 11.

13. The hydro-electrolytic hydrogen production processing system of claim 12, further comprising: