CN107261755B - Vacuum pressure swing adsorption oxygen generation system with product gas transition tank and oxygen generation method thereof - Google Patents
Vacuum pressure swing adsorption oxygen generation system with product gas transition tank and oxygen generation method thereof Download PDFInfo
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- CN107261755B CN107261755B CN201710659126.3A CN201710659126A CN107261755B CN 107261755 B CN107261755 B CN 107261755B CN 201710659126 A CN201710659126 A CN 201710659126A CN 107261755 B CN107261755 B CN 107261755B
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- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
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- B01D2259/40028—Depressurization
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Abstract
The invention discloses a vacuum pressure swing adsorption oxygen generation system with a product gas transition tank, wherein a corresponding product gas transition tank is arranged corresponding to each adsorption tower, the product gas produced by each adsorption tower in the oxygen generation process sequentially passes through the product gas transition tank and then enters the product gas buffer tank, a high oxygen concentration part at the front section of the product gas enters the product gas buffer tank to serve as the product gas of the oxygen generation system, a low oxygen concentration part at the rear section is temporarily stored in the product gas transition tank according to the concentration gradient of the produced oxygen, and when the corresponding adsorption tower is transferred into a vacuumizing flushing regeneration mode and the product gas is boosted, the temporarily stored low oxygen concentration product gas is returned to the adsorption tower to serve as flushing regenerated gas and product gas lifting compressed gas. It also discloses an oxygen production method. The invention has the following effects: the use efficiency of the adsorbent is improved, the oxygen recovery rate of the system is improved, the energy consumption of the system is saved, and the cost of the system is reduced.
Description
Technical Field
The invention relates to a pressure swing adsorption gas separation technology, in particular to a vacuum pressure swing adsorption oxygen generation system with a product gas transition tank and an oxygen generation method thereof.
Background
The vacuum pressure-variable adsorption oxygen-producing system is characterized by that it utilizes air blower to raise pressure of raw material air, and utilizes the different adsorbents filled in the adsorption tower to make high pressure treatment on water (H) in the raw material air 2 O), carbon dioxide (CO) 2 ) And nitrogen (N) 2 ) Selectively adsorbing oxygen (O) 2 ) The product gas produced by the system is formed; when the adsorbent is saturated, vacuum is adoptedThe pump vacuumizes and depressurizes the adsorption tower to make the water (H) 2 O), carbon dioxide (CO) 2 ) And nitrogen (N) 2 ) And (3) obtaining desorption, regenerating the adsorbent, and obtaining an oxygen-enriched gas product with higher oxygen concentration (60-93%) by using multi-tower circulation.
The existing vacuum pressure swing adsorption oxygen generation system is generally composed of a blower, a vacuum pump, a switching valve, two identical adsorption towers (A, B), a product gas buffer tank, a control device, a pipeline and the like. The adsorption tower is filled with adsorption water (H) from bottom to top 2 The adsorbent of O) (such as activated alumina, silica gel, zeolite), adsorbing carbon dioxide (CO) 2 ) Adsorbent (such as activated carbon, silica gel, zeolite) and adsorbent nitrogen (N) 2 ) Such as lithium-based molecular sieves Li-X).
In order to make the raw material air uniformly enter the adsorption bed layer and the adsorbent filled in the bed layer uniformly transfer and adsorb oxygen (O) which is not adsorbed in the bed layer 2 ) Uniformly flowing out of the adsorption bed layer, wherein in the structure of an adsorption tower (A, B), gas distributors are arranged at the bottom and the top of the adsorption tower, and the corresponding gas distributors occupy a certain empty volume; when the adsorbent is packed in the adsorption tower, a certain empty volume exists among the adsorbent particles.
Raw material air from the atmosphere is subjected to air filter to remove solid particles such as dust, and then enters a blower to be boosted, the boosted raw material air is respectively circulated and sent into an adsorption tower (A, B) by a switching valve, and water (H) 2 O), carbon dioxide (CO) 2 ) And nitrogen (N) 2 ) The oxygen (O) in the raw material air is absorbed by the corresponding adsorbent in the adsorption tower (A, B) 2 ) And the non-adsorption component flows out of the top of the adsorption tower (A, B) and enters a product gas buffer tank through a switching valve to become product gas produced by the system, and the process is an adsorption oxygen production process.
When the adsorbent in the adsorption tower gradually reaches adsorption saturation, the adsorption tower is in the highest adsorption pressure state, the pressure in the adsorption tower is usually 120-160 kpa.A, and the oxygen concentration gradient in the adsorption tower is as follows: the oxygen concentration of the air at the bottom of the tower is about 21 percent and gradually transits to 60-90 percent (the oxygen concentration of the adsorption end product) of the top of the tower. In order to improve the adsorption efficiency and the oxygen production capacity of the system, the high-pressure gas at the adsorption tail end in the adsorption tower after adsorption saturation is used as uniform pressure gas, and the uniform pressure gas is uniformly fed into another adsorption tower in the system at the end of vacuumizing through a switching valve for recovery, so that the pressure of the adsorption tower is reduced in the forward direction, and the process is a uniform pressure reduction process.
After the adsorption towers are depressurized, the adsorption towers are vacuumized by a vacuum pump, the pressure of the adsorption towers is continuously reduced, and water (H) adsorbed in the adsorbent 2 O), carbon dioxide (CO) 2 ) And nitrogen (N) 2 ) Gradually desorbing, pumping out the adsorbent to the atmosphere through a switching valve, and gradually regenerating the adsorbent, wherein the process is a vacuum regeneration process.
In the middle and later stage of the vacuum pumping of the adsorption tower, in order to strengthen the regeneration of the adsorbent, a small amount of product gas stored in the product gas buffer tank is used for flushing the adsorbent from the top of the adsorption tower to the back flow adsorption tower through a switching valve, so that the adsorbent is thoroughly regenerated, and the process is a vacuum flushing regeneration process.
And at the end of vacuumizing the adsorption tower, the high-pressure gas at the adsorption end in the other adsorption tower at the adsorption end in the system is used as uniform pressure gas, the uniform pressure gas is uniformly fed into the adsorption tower through a switching valve, part of the uniform pressure gas is recovered, and the part of the uniform pressure gas is used for replacing low-oxygen concentrated waste gas at the lower part of the adsorption tower, and the process is a uniform feeding recovery process.
After passing through the adsorption towers which are all in the recovery process, before the adsorption tower is switched into the adsorption oxygen production process, the product gas stored in the product gas buffer tank is required to be used for carrying out product gas boosting on the adsorption tower from the reflux adsorption tower at the top of the adsorption tower through the switching valve, and when the pressure of the adsorption tower is boosted to the adsorption oxygen production pressure, the adsorption tower can be switched into the adsorption oxygen production process, and the process is a product gas boosting process.
In summary, each adsorption column in a vacuum pressure swing adsorption oxygen generation system undergoes the following process within one oxygen generation system oxygen generation cycle: raw material air adsorption oxygen production, uniform depressurization, vacuumizing regeneration, uniform recovery, product gas pressure boosting, and multi-tower continuous phase staggering operation. Under the control of a programmable controller, the automatic circulation operation is realized through a switching valve system.
The existing vacuum pressure swing adsorption oxygen generation system has the following defects:
and in the adsorption oxygen production process, the raw material air blower starts to supply air to the adsorption tower from the raw material air blower to the end of adsorption saturation of the adsorbent in the adsorption tower, and the whole adsorption oxygen production process is that the raw material air after pressurization is continuously fed into the adsorption tower from the bottom of the adsorption tower by the air blower. Water (H) in the raw material air continuously fed into the adsorption column 2 O), carbon dioxide (CO) 2 ) And nitrogen (N) 2 ) The oxygen (O) in the raw material air continuously entering the adsorption tower is continuously adsorbed by the adsorbent in the adsorption tower and gradually accumulated from the bottom layer to the top layer of the adsorbent until the adsorption is saturated 2 ) And the product gas flows out from the top of the adsorption tower to be directly fed into a product gas buffer tank, and is buffered and stored in the product gas buffer tank and then is used as the final product gas produced by the vacuum pressure swing adsorption oxygen production system for the subsequent users. Because the adsorbent in the adsorption tower is a process from gradual adsorption accumulation to adsorption saturation in the whole adsorption process, the oxygen concentration of the product gas flowing out of the adsorption tower is gradually reduced from high to low, the product gas oxygen concentration range of the process is generally determined by the final product gas oxygen concentration output by the whole vacuum pressure swing adsorption oxygen production system, namely, the high oxygen concentration product gas in the early stage of oxygen production by adsorption and the low oxygen concentration product gas when the adsorbent is close to saturation in the final stage of oxygen production by adsorption are mixed in a product gas buffer tank to obtain the product gas with average oxygen concentration, and the mixed product gas with the average oxygen concentration becomes the final product gas produced by the whole vacuum pressure swing adsorption oxygen production system, so that the final product gas oxygen concentration is reduced.
In the vacuum flushing regeneration process, a small amount of final product gas stored in the product gas buffer tank is used as flushing gas to flow back into the adsorption tower from the top of the adsorption tower in order to strengthen the regeneration of the adsorbent. The part of flushing gas is completely pumped by a vacuum pump to be discharged to the atmosphere after flushing the adsorbent, thereby wasting the high-oxygen concentration product gas and reducing the oxygen recovery rate.
And in the product gas pressure rising process, the final product gas stored in the product gas buffer tank is used as product gas pressure rising gas to flow back into the adsorption tower from the top of the adsorption tower, and the partial product gas pressure rising gas is not wasted, but is distributed in the adsorption tower in average oxygen concentration, so that the adsorption operation is not facilitated, the adsorption efficiency cannot be fully exerted, and the oxygen recovery rate is reduced.
In the existing vacuum pressure swing adsorption oxygen generation system, the pressure reduction process is carried out, so that when the high-pressure raw material air stored in the empty volume occupied by the gas distributor at the bottom of the adsorption tower at the tail end of the adsorption tower and the empty volume occupied by the corresponding pipeline is uniformly compressed at the top of the adsorption tower, the high-pressure raw material air enters the adsorption bed layer of the adsorption tower, and at the moment, the adsorption bed layer is in the pressure reduction process, and water (H 2 O), carbon dioxide (CO) 2 ) And nitrogen (N) 2 ) The gas is not adsorbed by the adsorbent in the adsorption bed layer, becomes invalid gas and resides in the adsorption tower, the pressure energy is wasted, and when the adsorption tower is switched into a vacuumizing state, part of the gas is pumped by a vacuum pump after the volume of the gas is enlarged in the vacuum state. Not only increases the energy consumption of the vacuum pump of the oxygen production system, but also causes pollution to the adsorbent in the adsorption bed.
In the existing vacuum pressure swing adsorption oxygen production system, after the adsorption tower is subjected to the uniform recovery process, the pressure of the adsorption tower is still lower than the ambient atmospheric pressure, and before the adsorption tower is transferred into the adsorption oxygen production process, only product gas can be used for boosting the pressure of the adsorption tower, so that the vacuum energy of the adsorption tower cannot be effectively utilized, and the energy consumption of the system is increased.
In the existing vacuum pressure swing adsorption oxygen generation system, due to the processes of uniform depressurization and uniform recovery, the raw material air blower is necessarily vented twice through the blower venting switching valve in an adsorption regeneration cycle process, so that the running stability of the raw material air blower is reduced, the energy consumption of the oxygen generation system is increased, and the venting noise is generated.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a method for improving the utilization method according to the characteristic of the change of the gas-oxygen concentration of the product in the adsorption oxygen production process, thereby reducing the oxygen loss of the product, and improving the utilization rate of the adsorbent and the oxygen recovery rate of the system; the vacuum pressure swing adsorption oxygen generating system with the product gas transition tank and the oxygen generating method thereof utilize partial pressure and vacuum energy in the adsorption process of the adsorption tower to automatically empty and self-suck the atmosphere at the bottom of the adsorption tower, reduce the load of a blower and a vacuum pump, reduce the energy consumption of the system and realize the continuous air supply of the blower.
The aim of the invention is achieved by the following technical scheme: a vacuum pressure swing adsorption oxygen generation system with a product gas transition tank comprises an adsorption tower A, an adsorption tower B, an adsorption tower C, an atmospheric suction main pipe P1, an atmospheric discharge main pipe P3, a blower AC, a vacuum pump VP, a product buffer tank VS1, a product gas transition tank VS2A, a product gas transition tank VS2B and a product gas transition tank VS2C, wherein the product gas transition tank VS2A, the product gas transition tank VS2B and the product gas transition tank VS2C are used for keeping one-dimensional flowing of product gas in and out; the outlet end of the atmosphere suction main pipe P1 is connected with a self-suction switching valve V1A, a self-suction switching valve V1B and a self-suction switching valve V1C in parallel, and the other ends of the self-suction switching valve V1A, the self-suction switching valve V1B and the self-suction switching valve V1C are respectively connected with the bottoms of an adsorption tower A, an adsorption tower B and an adsorption tower C; an outlet end of the blower AC is connected with an air inlet main pipe P2, the other end of the air inlet main pipe P2 is connected with an air inlet switching valve V2A, an air inlet switching valve V2B and an air inlet switching valve V2C in parallel, and the other ends of the air inlet switching valve V2A, the air inlet switching valve V2B and the air inlet switching valve V2C are respectively connected with the bottoms of the adsorption tower A, the adsorption tower B and the adsorption tower C; the inlet end of the emptying main pipe P3 is connected with an emptying switching valve V3A, an emptying switching valve V3B and an emptying switching valve V3C in parallel, and the other ends of the emptying switching valve V3A, the emptying switching valve V3B and the emptying switching valve V3C are respectively connected with the bottoms of the adsorption tower A, the adsorption tower B and the adsorption tower C; the inlet end of the vacuum pump VP is connected with a vacuum main pipe P4, the other end of the vacuum main pipe P4 is connected with a vacuum switching valve V4A, a vacuum switching valve V4B and a vacuum switching valve V4C in parallel, and the other ends of the vacuum switching valve V4A, the vacuum switching valve V4B and the vacuum switching valve V4C are respectively connected with the bottoms of the adsorption tower A, the adsorption tower B and the adsorption tower C; the inlet end of the product buffer tank VS1 is connected with a product gas main valve V8, the other end of the product gas main valve V8 is connected with a product gas main pipe P5, the other end of the product gas main pipe P5 is connected with a product gas transition switching valve V7A, a product gas transition switching valve V7B and a product gas transition switching valve V7C in parallel, the other ends of the product gas transition switching valve V7A, the product gas transition switching valve V7B and the product gas transition switching valve V7C are respectively connected with the outlets of the product gas transition tank VS2A, the product gas transition tank VS2B and the product gas transition tank VS2C, and the inlets of the product gas transition tank VS2A, the product gas transition tank VS2B and the product gas transition tank VS2C are respectively connected with a product gas switching valve V5A, a product gas switching valve V5B and a product gas switching valve V5C, and the other ends of the product gas switching valve V5C are respectively connected with the tops of the adsorption towers A, B and C; the top of adsorption tower A, adsorption tower B, adsorption tower C is connected with pressure equalizing switching valve V6A, pressure equalizing switching valve V6B and pressure equalizing switching valve V6C respectively, and pressure equalizing switching valve V6A, pressure equalizing switching valve V6B and pressure equalizing switching valve V6C's the other end communicates each other.
The product gas transition tanks comprise tank bodies, gas flow distributors A, gas flow distributors B and vertically distributed bundling pipes, wherein the gas flow distributors A are arranged in the tank bodies, the gas flow distributors A are arranged between an inlet of the product gas transition tank and the bundling pipes, the gas flow distributors B are arranged between an outlet of the product gas transition tank and the bundling pipes, and gas flow channels A are formed in the inner space of the bundling pipes; an air flow channel B is formed between the outer wall of the bundling pipe and the inner wall of the tank body; an air flow channel C is formed between the outer walls of adjacent pipelines in the bundling pipe.
The oxygen production method of the vacuum pressure swing adsorption oxygen production system with the product gas transition tank comprises the following steps:
s1, feeding raw material air into an adsorption tower A by a blower AC, and discharging product gas from the adsorption tower A: opening an air inlet switching valve V2A, a product gas switching valve V5A, a product gas transition switching valve V7A and a product gas main valve V8, closing a self-priming switching valve V1A, an emptying switching valve V3A, a vacuum switching valve V4A and a pressure equalizing switching valve V6A, boosting raw material air by a blower AC, conveying the raw material air to an adsorption tower A through the air inlet switching valve V2A, sequentially adsorbing water, carbon dioxide and nitrogen in the raw material air by activated alumina, zeolite and lithium-based molecular sieves filled in the adsorption tower A respectively, and enabling oxygen-enriched gas to flow out of the top of the adsorption tower A as product gas and sequentially flow into a product buffer tank VS1 through the product gas switching valve V5A, the product gas transition tank VS2A, the product gas transition switching valve V7A and the product gas main valve V8;
s2, reducing pressure in the adsorption tower A: when the adsorbent filled in the adsorption tower A reaches adsorption saturation, an air inlet switching valve V2A is closed, an air blower AC is switched to the air inlet of the adsorption tower B, a product gas switching valve V5A and a product gas transition switching valve V7A are closed, the adsorption tower A stops producing product gas, a pressure equalizing switching valve V6A and a pressure equalizing switching valve V6C are opened, at the moment, the adsorption tower C is at the end of vacuumizing, the high-pressure air at the adsorption tail end in the adsorption tower A is taken as pressure equalizing air, and sequentially passes through the pressure equalizing switching valve V6A and the pressure equalizing switching valve V6C and enters the adsorption tower C at the end of vacuumizing, so that the pressure of the adsorption tower A is reduced in a forward direction, and the high-pressure air at the adsorption tail end of the adsorption tower A is recovered by the adsorption tower C;
s3, emptying the bottom of the adsorption tower A: 2-4S before the step S2 is finished, the pressure of the adsorption tower A is still higher than the ambient atmospheric pressure, the pressure equalizing switching valve V6A and the pressure equalizing switching valve V6C are kept in an opened state, the emptying switching valve V3A is opened, and air at the bottom of the adsorption tower A is emptied from the bottom of the adsorption tower A through the emptying switching valve V3A;
s4, vacuumizing an adsorption tower A: after the step S3 is finished, the pressure of the adsorption tower A is close to the ambient atmospheric pressure, the emptying switching valve V3A, the equalizing switching valve V6A and the equalizing switching valve V6C are closed, the vacuum switching valve V4A is opened, the vacuum pump VP vacuumizes the adsorption tower A, the pressure of the adsorption tower A gradually reaches the vacuum regeneration pressure of the adsorbent, the water, the carbon dioxide and the nitrogen adsorbed by the adsorbent are gradually desorbed, and the adsorbent is gradually regenerated;
s5, flushing the product gas of the adsorption tower A: when the step S4 is finished for 4-8 seconds, keeping the vacuum switching valve V4A in an opened state, continuously vacuumizing the adsorption tower A by the vacuum pump VP, opening the product gas switching valve V5A, refluxing the product gas in the product gas transition tank VS2A to the adsorption tower A through the product gas switching valve V5A, flushing the product gas in the adsorption tower A, reinforcing the regeneration of the adsorbent in the adsorption tower A, and keeping the pressure of the adsorption tower A unchanged basically in the whole flushing process;
s6, recycling the adsorption tower A: after the step S5 is finished, and 2-4S before the step S4 is finished, keeping a vacuum switching valve V4A in an opening state, continuously vacuumizing an adsorption tower A by a vacuum pump VP, closing a product gas switching valve V5A, opening a pressure equalizing switching valve V6A and a pressure equalizing switching valve V6B, wherein the adsorption tower B is positioned at the tail end of the adsorption, the high-pressure gas at the tail end of the adsorption in the adsorption tower B is used as pressure equalizing gas, sequentially enters the adsorption tower A through the pressure equalizing switching valve V6B and the pressure equalizing switching valve V6A, the high-pressure gas at the tail end of the adsorption tower B is recovered, and the low-oxygen concentrated waste gas at the lower part of the adsorption tower A is replaced by the partial gas;
s7, product gas pressure in the first stage of the adsorption tower A is increased: after the step S6 is finished, closing a vacuum switching valve V4A, a pressure equalizing switching valve V6A and a pressure equalizing switching valve V6B, opening a product gas switching valve V5A, and enabling product gas in a product gas transition tank VS2A to flow back to an adsorption tower A through the product gas switching valve V5A so as to boost the product gas in the first stage of the adsorption tower A;
s8, product gas pressure in the second stage of the adsorption tower A is increased, and the bottom of the adsorption tower A is self-sucking with the atmosphere: the product gas switching valve V5A is still kept in an open state, the pressure of the adsorption tower A is still lower than the ambient atmospheric pressure at the moment, the self-priming switching valve V1A is opened, and the air is self-priming through the self-priming switching valve V1A and enters the bottom of the adsorption tower A, so that the pressure of the adsorption tower A is gradually increased to the ambient atmospheric pressure;
s9, product gas pressure in the third stage of the adsorption tower A is increased: when the pressure of the adsorption tower A reaches the ambient atmospheric pressure, the opening state of the product gas switching valve V5A is still maintained, the self-priming switching valve V1A is closed, the product gas transition switching valve V7A is opened, the product gas in the product buffer tank VS1 flows back to the product gas transition tank VS2A through the product gas transition switching valve V7A, the product gas in the product gas transition tank VS2A flows back to the adsorption tower A through the product gas switching valve V5A, the pressure of the adsorption tower A is continuously increased until the adsorption pressure is reached, and the product gas pressure increase is completed.
The invention has the following advantages: according to the characteristic of gas-oxygen concentration change of the product in the adsorption oxygen production process, the invention improves the utilization method, and increases the air-oxygen yield of raw materials by about 5% on the existing vacuum pressure swing adsorption oxygen production system; the bottom of the adsorption tower is deflated in the residual pressure state, so that the pumping speed of the vacuum pump is reduced, and the energy consumption of the system can be reduced by about 5%; the adsorption tower is continuously supplied with air by self-priming air in a negative pressure state of the adsorption tower and the blower in a circulating way, so that the air supply flow and the emptying loss of the blower are reduced, and the energy consumption of the system is reduced by about 5%. Meanwhile, the raw material air blower circularly and continuously supplies air to the adsorption tower, so that the running stability of the raw material air blower is improved, and the emptying noise is avoided.
Drawings
FIG. 1 is a schematic diagram of the structure of the present invention;
FIG. 2 is a schematic diagram of the product gas transition tank structure of the present invention;
FIG. 3 is a cross-sectional view A-A of FIG. 2;
FIG. 4 is a timing diagram of an oxygen generation cycle of the present invention;
FIG. 5 is a schematic diagram of a system structure according to a second embodiment;
in the figure, a 1-product gas transition tank outlet, a 2-gas distributor B, a 3-tank body, a 4-bundling pipe, a 5-gas distributor A, a 6-product gas transition tank inlet, a 7-gas channel A, an 8-gas channel B and a 9-gas channel C.
Detailed Description
The invention is further described below with reference to the accompanying drawings, the scope of the invention not being limited to the following:
embodiment one: as shown in fig. 1, a vacuum pressure swing adsorption oxygen generating system with a product gas transition tank comprises an adsorption tower a, an adsorption tower B, an adsorption tower C, an atmospheric suction main pipe P1, an atmospheric discharging main pipe P3, a blower AC, a vacuum pump VP, a product buffer tank VS1, a product gas transition tank VS2A for keeping product gas flowing in and out one-dimensional, a product gas transition tank VS2B and a product gas transition tank VS2C.
As shown in fig. 1, the outlet end of the atmospheric suction main pipe P1 is connected in parallel with a self-suction switching valve V1A, a self-suction switching valve V1B and a self-suction switching valve V1C, and the other ends of the self-suction switching valve V1A, the self-suction switching valve V1B and the self-suction switching valve V1C are respectively connected with the bottoms of the adsorption tower a, the adsorption tower B and the adsorption tower C.
As shown in fig. 1, an outlet end of the blower AC is connected with an intake manifold P2, and the other end of the intake manifold P2 is connected with an intake switching valve V2A, an intake switching valve V2B and an intake switching valve V2C in parallel, and the other ends of the intake switching valve V2A, the intake switching valve V2B and the intake switching valve V2C are respectively connected with bottoms of the adsorption tower a, the adsorption tower B and the adsorption tower C.
As shown in fig. 1, the inlet end of the blowdown header P3 is connected in parallel with a blowdown switch valve V3A, a blowdown switch valve V3B and a blowdown switch valve V3C, and the other ends of the blowdown switch valve V3A, the blowdown switch valve V3B and the blowdown switch valve V3C are respectively connected with the bottoms of the adsorption tower a, the adsorption tower B and the adsorption tower C.
As shown in fig. 1, the inlet end of the vacuum pump VP is connected with a vacuum main pipe P4, the other end of the vacuum main pipe P4 is connected with a vacuum switching valve V4A, a vacuum switching valve V4B and a vacuum switching valve V4C in parallel, and the other ends of the vacuum switching valve V4A, the vacuum switching valve V4B and the vacuum switching valve V4C are respectively connected with the bottoms of the adsorption tower a, the adsorption tower B and the adsorption tower C.
As shown in fig. 1, the inlet end of the product buffer tank VS1 is connected with a product gas main valve V8, the other end of the product gas main valve V8 is connected with a product gas main pipe P5, the other end of the product gas main pipe P5 is connected with a product gas transition switching valve V7A, a product gas transition switching valve V7B and a product gas transition switching valve V7C in parallel, the other ends of the product gas transition switching valve V7A, the product gas transition switching valve V7B and the product gas transition switching valve V7C are respectively connected with a product gas transition tank VS2A, a product gas transition tank VS2B and a product gas transition tank VS2C, the other ends of the product gas transition tank VS2A, the product gas transition tank VS2B and the product gas transition tank VS2C are respectively connected with a product gas switching valve V5A, a product gas switching valve V5B and a product gas switching valve V5C, and the other ends of the product gas switching valve V5C are respectively connected with the tops of the adsorption towers a, B and C.
As shown in fig. 1, the tops of the adsorption tower a, the adsorption tower B and the adsorption tower C are respectively connected with a pressure equalizing switching valve V6A, a pressure equalizing switching valve V6B and a pressure equalizing switching valve V6C, and the other ends of the pressure equalizing switching valve V6A, the pressure equalizing switching valve V6B and the pressure equalizing switching valve V6C are mutually communicated.
As shown in fig. 1, 2 and 3, the product gas transition tank comprises a tank body 3, an air flow distributor A5, an air flow distributor B2 and a vertically distributed bundling pipe 4 which are arranged in the tank body 3, wherein the air flow distributor A5 is arranged between an inlet 6 of the product gas transition tank and the bundling pipe 4, the air flow distributor B2 is arranged between an outlet 1 of the product gas transition tank and the bundling pipe 4, and an air flow channel A7 is formed in the inner space of the bundling pipe 4; an air flow channel B8 is formed between the outer wall of the bundling pipe 4 and the inner wall of the tank body 3; an air flow channel C9 is formed between the outer walls of adjacent pipelines in the bundling pipe 4.
As shown in fig. 1, the bottoms of the adsorption tower a, the adsorption tower B and the adsorption tower C are respectively connected with a vent switching valve V3A, V3B, V C for venting the bottom of the residual pressure state of the adsorption tower.
As shown in fig. 1, the bottoms of the adsorption tower a, the adsorption tower B and the adsorption tower C are respectively connected with a self-priming switching valve V1A, V1B, V C for self-priming air at the bottom of the adsorption tower in a negative pressure state.
As shown in FIG. 1, the nitrogen-adsorbing gas (N) filled in the adsorption tower A, the adsorption tower B and the adsorption tower C 2 ) The molecular sieve is a high-efficiency Li-X type lithium-based molecular sieve.
As shown in fig. 1 to 4, the oxygen production method of the vacuum pressure swing adsorption oxygen production system with the product gas transition tank comprises the following steps:
the single tower of the adsorption tower A comprises the following working steps:
s1, feeding raw material air into an adsorption tower A by a blower AC, and discharging product gas from the adsorption tower A: opening an air inlet switching valve V2A, a product gas switching valve V5A, a product gas transition switching valve V7A and a product gas main valve V8, closing a self-priming switching valve V1A, an emptying switching valve V3A, a vacuum switching valve V4A and a pressure equalizing switching valve V6A, boosting raw material air by a blower AC, continuously conveying the raw material air to an adsorption tower A through the air inlet switching valve V2A, and continuously feeding water (H in the raw material air of the adsorption tower A 2 O), carbon dioxide (CO) 2 ) And nitrogen (N) 2 ) Sequentially and respectively adsorbed by activated alumina, zeolite and lithium-based molecular sieve filled in the adsorption tower A, and water (H 2 O), carbon dioxide (CO) 2 ) And nitrogen (N) 2 ) Gradually accumulating from bottom to top of the adsorbent in the adsorption tower until the adsorption is saturated, and continuously introducing oxygen (O 2 ) The product gas flows out from the top of the adsorption tower A, and the adsorbent in the adsorption tower A is gradually adsorbed and accumulated until the adsorption is saturated in the whole adsorption oxygen production process, so that the oxygen concentration of the product gas flowing out of the adsorption tower A in the adsorption oxygen production process is gradually reduced from high to low. Oxygen-enriched gas with gradient change of oxygen concentration is taken as product gas to flow out from the top of the adsorption tower A and sequentially passes through the product gas switching valve V5A to produceThe product gas transition tank inlet 6 and the gas flow distributor A5 enter a gas flow channel A7, a gas flow channel B8 and a gas flow channel C9 in the product gas transition tank. Because the air flow distributor A5, the air flow channel A7, the air flow channel B8, the air flow channel C9 and the air flow distributor B2 arranged in the product air transition tank VS2A have the functions that the product air entering the air flow channel A7, the air flow channel B8 and the air flow channel C9 in the product air transition tank VS2 flows in one dimension in the air flow channel, the phenomenon that the front-stage gas resides and the rear-stage gas is mixed can not occur, the product air entering the air flow channel A7, the air flow channel B8 and the air flow channel C9 can necessarily keep the oxygen concentration gradient, and the product air entering the product air buffer tank VS1 from the air flow channel A7, the air flow channel B8 and the air flow channel C9 through the air flow distributor B2, the product air transition tank outlet 1, the product air transition switching valve V7A and the product air total valve V8 enters the product air buffer tank VS1, so that the high-oxygen concentrated product air at the front stage in the adsorption oxygen production process enters the product air buffer tank VS1 as the final product air of the adsorption oxygen production system, and the low-oxygen concentration product air at the rear stage in the adsorption oxygen production process keeps the oxygen concentration gradient and remains the oxygen concentration gradient in the air flow channel A7, the air flow channel C9 as the product air in the product air transition tank VS1, and the product air is flushed by the product air step of the gas flushing step.
S2, reducing pressure in the adsorption tower A: when the adsorbent filled in the adsorption tower A reaches adsorption saturation, an air inlet switching valve V2A is closed, an air blower AC is switched to the adsorption tower B for air inlet, a product gas switching valve V5A and a product gas transition switching valve V7A are closed, the adsorption tower A stops producing product gas, a pressure equalizing switching valve V6A and a pressure equalizing switching valve V6C are opened, at the moment, the adsorption tower C is at the end of vacuumizing, the high-pressure air at the adsorption tail end in the adsorption tower A is taken as pressure equalizing air, and sequentially passes through the pressure equalizing switching valve V6A and the pressure equalizing switching valve V6C and enters the adsorption tower C at the end of vacuumizing, so that the pressure of the adsorption tower A is reduced in a forward direction, and the high-pressure air at the adsorption tail end of the adsorption tower A is recovered by the adsorption tower C.
S3, emptying the bottom of the adsorption tower A: and 2-4S before the step S2 is finished, the pressure of the adsorption tower A is still higher than the ambient atmospheric pressure and is about 110-115 kpa.A, the adsorption tower A is still in the pressure reducing process, the next step-like adsorption tower A is shifted into vacuumizing regeneration to continuously reduce the pressure, and if part of raw material air at the bottom of the adsorption tower A, which is higher than the ambient atmospheric pressure, diffuses towards the top of the adsorption tower A, the part of raw material air cannot be adsorbed and utilized by the adsorbent in the adsorption bed layer, and pollutes the adsorbent in the adsorption bed layer, so that invalid gas resides in the adsorption tower. The pressure equalizing switching valve V6A and the pressure equalizing switching valve V6C are kept in the opening state, the emptying switching valve V3A is opened, so that part of raw material air at the bottom of the adsorption tower A is directly emptied from the bottom of the adsorption tower A through the emptying switching valve V3A, the pressure of the adsorption tower A is reduced to be close to the ambient atmospheric pressure, meanwhile, the pumping air flow of a vacuum pump is reduced, and the energy consumption of an oxygen production system is reduced.
S4, vacuumizing an adsorption tower A: after the end of step S3, the pressure of the adsorption tower a approaches the ambient atmospheric pressure, the emptying switching valve V3A, the equalizing switching valve V6A and the equalizing switching valve V6C are closed, the vacuum switching valve V4A is opened, the vacuum pump VP vacuumizes the adsorption tower a, the pressure of the adsorption tower a gradually reaches the vacuum regeneration pressure of the adsorbent, and the water (H 2 O), carbon dioxide (CO) 2 ) Nitrogen (N) 2 ) Desorbing and regenerating the adsorbent.
S5, flushing the product gas of the adsorption tower A: and (2) when the step S4 is finished and the time is 4-8 seconds later, keeping the vacuum switching valve V4A in an opened state, continuously vacuumizing the adsorption tower A by the vacuum pump VP, opening the product gas switching valve V5A, and enabling the low-oxygen concentrated product gas in the gas flow channel A7, the gas flow channel B8 and the gas flow channel C9 in the product gas transition tank VS2A to be used as flushing gas of the adsorption tower A, and enabling the flushing gas to flow back into the adsorption tower A through the inlet gas flow distributor A5, the product gas transition tank inlet 6 and the product gas switching valve V5A under the pressure effect. Because of the functions of the air flow distributor A5, the air flow channel A7, the air flow channel B8 and the air flow channel C9 arranged in the product gas transition tank VS2A, the product gas flowing out of the air flow channel A7, the air flow channel B8 and the air flow channel C9 in the product gas transition tank VS2 can flow in one dimension in the air flow channel, and the phenomenon of residence of the front-stage gas and mixing of the rear-stage gas can not be generated. The reflux sequence of the flushing gas is as follows: the adsorption column a is continuously purged from a low oxygen concentration to a high oxygen concentration in accordance with an oxygen concentration gradient. The adsorption tower A is still vacuumized during flushing, and the pressure of the adsorption tower A is basically kept unchanged in the whole flushing process, so that the lowest oxygen concentration part in the low oxygen concentration product gas at the later stage of the adsorption oxygen production process is used as the product gas flushing gas of the adsorption tower A, the high oxygen concentration product gas is saved, and the oxygen recovery rate is improved.
S6, recycling the adsorption tower A: after the step S5 is finished, and 2-4S before the step S4 is finished, the vacuum switching valve V4A is kept in an open state, the vacuum pump VP continues to vacuumize the adsorption tower A, the product gas switching valve V5A is closed, the pressure equalizing switching valve V6A and the pressure equalizing switching valve V6B are opened, at the moment, the adsorption tower B is at the tail end of the adsorption, the high-pressure gas at the tail end of the adsorption in the adsorption tower B is used as pressure equalizing gas, and sequentially passes through the pressure equalizing switching valve V6B and the pressure equalizing switching valve V6A to enter the adsorption tower A, the high-pressure gas at the tail end of the adsorption tower B is recovered, and the low-oxygen concentrated waste gas at the lower part of the adsorption tower A is replaced by the partial gas.
S7, product gas pressure in the first stage of the adsorption tower A is increased: after the step S6 is finished, the vacuum switching valve V4A, the pressure equalizing switching valve V6A and the pressure equalizing switching valve V6B are closed, the product gas switching valve V5A is opened, and the low-oxygen concentrated product gas at the later stage of the adsorption oxygen production process residing in the product gas transition tank VS2A, the gas flow channel B8 and the gas flow channel C9 are used as rising compressed gas of the adsorption tower A and flow back into the adsorption tower A through the inlet gas flow distributor A5, the product gas transition tank inlet 6 and the product gas switching valve V5A in sequence under the pressure effect of the rising compressed gas. Because of the functions of the air flow distributor A5, the air flow channel A7, the air flow channel B8 and the air flow channel C9 arranged in the product gas transition tank VS2A, the product gas flowing out of the air flow channel A7, the air flow channel B8 and the air flow channel C9 in the product gas transition tank VS2 can flow in one dimension in the air flow channel, and the phenomenon of residence of the front-stage gas and mixing of the rear-stage gas can not be generated. The reflux sequence of the rising compressed air is as follows: the adsorption tower A is continuously refluxed from low oxygen concentration to high oxygen concentration according to the oxygen concentration gradient, and the first-stage product gas pressure of the adsorption tower A is increased.
S8, product gas pressure in the second stage of the adsorption tower A is increased, and the bottom of the adsorption tower A is self-sucking with the atmosphere: still keep the product gas switching valve V5A open state, adsorption tower A pressure still is less than ambient atmospheric pressure this moment, opens self-priming switching valve V1A, and the atmosphere is from inhaling the bottom entering adsorption tower A through self-priming switching valve V1A self-priming, carries out product gas and self-priming atmosphere and boost jointly to adsorption tower A, makes adsorption tower A pressure rise gradually to ambient atmospheric pressure.
S9, product gas pressure in the third stage of the adsorption tower A is increased: when the pressure of the adsorption tower A reaches the ambient atmospheric pressure, the opening state of the product gas switching valve V5A is still kept, the self-priming switching valve V1A is closed, the product gas transition switching valve V7A is opened, and the product gas in the product buffer tank VS1 flows back to the air flow channel A7, the air flow channel B8 and the air flow channel C9 through the product gas transition switching valve V7A, the product gas transition tank outlet 1, the air flow distributor B2 and the reflux flow, and the residual low-oxygen concentrated product gas in the air flow channel A7, the air flow channel B8 and the air flow channel C9 at the rear stage of the adsorption oxygen production process flows back into the adsorption tower A through the air flow distributor A5, the product gas transition tank inlet 6 and the product gas switching valve V5A in sequence under the pushing of the reflux product gas of the product buffer tank VS 1. Because of the functions of the air flow distributor A5, the air flow channel A7, the air flow channel B8, the air flow channel C9 and the air flow distributor B2 which are arranged in the product gas transition tank VS2A, the residual product gas of the air flow channel A7, the air flow channel B8 and the air flow channel C9 can flow in one dimension in the air flow channel, and the phenomenon of residence of the front-stage gas and the mixing of the rear-stage gas can not be generated. The reflux sequence of the rising compressed air is as follows: and continuously refluxing the adsorption tower A from low oxygen concentration to high oxygen concentration according to an oxygen concentration gradient, and boosting the product gas in the third stage of the adsorption tower A until the adsorption pressure is reached, so that the product gas boosting pressure is completed, the higher oxygen concentration part in the low oxygen concentration product gas in the later stage of the adsorption oxygen production process is used as the product gas boosting pressure of the adsorption tower A, the continuously refluxing the adsorption tower A from low oxygen concentration to high oxygen concentration according to an oxygen concentration gradient is kept, and the boosted gas of the refluxing adsorption tower A is continuously distributed from bottom to top in the adsorption tower A. Saving the product gas with high oxygen concentration and improving the oxygen recovery rate.
(II) the working steps of oxygen production circulation of the oxygen production system are as follows:
as shown in FIG. 4, the working principle and the single tower working steps of the adsorption tower B and the adsorption tower C are identical to those of the single tower working step of the adsorption tower A, raw material air is supplied to adsorb and produce air by using a blower AC, product air with low oxygen concentration at the rear section of the adsorption and oxygen production process of the corresponding adsorption tower is respectively resided by using a product air transition tank VS2B and a product air transition tank VS2C, the resided product air is used as product air flushing air of the corresponding adsorption tower product air flushing step and product air lifting and compressing air of the product air lifting and compressing process, vacuumizing is performed by using a vacuum pump VP, residual pressure at the bottom of the adsorption tower is automatically discharged after the adsorption tower is depressurized by using the product air at the first stage of the adsorption tower, and the vacuum state at the bottom of the adsorption tower is used for self-sucking the atmosphere after the product air is pressurized.
As shown in FIG. 4, the adsorption towers A, B and C are operated in a continuous misorientation mode, so that the oxygen production system can circularly work to continuously produce oxygen.
As shown in fig. 4, the blower AC supplies air to the adsorption columns a, B, and C in successive staggered steps, respectively.
As shown in fig. 4, the vacuum pump VP vacuum-pumps the sequential misdirection steps of the adsorption columns a, B, and C, respectively.
Embodiment two: the difference between this embodiment and the first embodiment is that: as shown in fig. 5, there are no product gas transition switching valve V7A, product gas transition switching valve V7B, and product gas transition switching valve V7C between the product gas main valve V8 and the tops of the product gas transition tanks VS2A, VS2B, VS2C.
Claims (2)
1. A vacuum pressure swing adsorption oxygen generation system with a product gas transition tank is characterized in that: the device comprises an adsorption tower A, an adsorption tower B, an adsorption tower C, an atmosphere suction main pipe P1, an air discharging main pipe P3, a blower AC, a vacuum pump VP, a product buffer tank VS1, a product gas transition tank VS2A, a product gas transition tank VS2B and a product gas transition tank VS2C, wherein the product gas transition tank VS2A, the product gas transition tank VS2B and the product gas transition tank VS2C are used for keeping one-dimensional flowing of product gas in and out; the outlet end of the atmosphere suction main pipe P1 is connected with a self-suction switching valve V1A, a self-suction switching valve V1B and a self-suction switching valve V1C in parallel, and the other ends of the self-suction switching valve V1A, the self-suction switching valve V1B and the self-suction switching valve V1C are respectively connected with the bottoms of an adsorption tower A, an adsorption tower B and an adsorption tower C; the outlet end of the blower AC is connected with an air inlet header pipe P2, the other end of the air inlet header pipe P2 is connected with an air inlet switching valve V2A, an air inlet switching valve V2B and an air inlet switching valve V2C in parallel, and the other ends of the air inlet switching valve V2A, the air inlet switching valve V2B and the air inlet switching valve V2C are respectively connected with an adsorption tower A, an adsorption tower B and an adsorption towerThe bottom of the C is connected; the inlet end of the emptying main pipe P3 is connected with an emptying switching valve V3A, an emptying switching valve V3B and an emptying switching valve V3C in parallel, and the other ends of the emptying switching valve V3A, the emptying switching valve V3B and the emptying switching valve V3C are respectively connected with the bottoms of the adsorption tower A, the adsorption tower B and the adsorption tower C; the inlet end of the vacuum pump VP is connected with a vacuum main pipe P4, the other end of the vacuum main pipe P4 is connected with a vacuum switching valve V4A, a vacuum switching valve V4B and a vacuum switching valve V4C in parallel, and the other ends of the vacuum switching valve V4A, the vacuum switching valve V4B and the vacuum switching valve V4C are respectively connected with the bottoms of the adsorption tower A, the adsorption tower B and the adsorption tower C; the inlet end of the product buffer tank VS1 is connected with a product gas main valve V8, the other end of the product gas main valve V8 is connected with a product gas main pipe P5, the other end of the product gas main pipe P5 is connected with a product gas transition switching valve V7A, a product gas transition switching valve V7B and a product gas transition switching valve V7C in parallel, the other ends of the product gas transition switching valve V7A, the product gas transition switching valve V7B and the product gas transition switching valve V7C are respectively connected with the outlets of the product gas transition tank VS2A, the product gas transition tank VS2B and the product gas transition tank VS2C, and the inlets of the product gas transition tank VS2A, the product gas transition tank VS2B and the product gas transition tank VS2C are respectively connected with a product gas switching valve V5A, a product gas switching valve V5B and a product gas switching valve V5C, and the other ends of the product gas switching valve V5C are respectively connected with the tops of the adsorption towers A, B and C; the top of the adsorption tower A, the adsorption tower B and the adsorption tower C are respectively connected with a pressure equalizing switching valve V6A, a pressure equalizing switching valve V6B and a pressure equalizing switching valve V6C, the other ends of the pressure equalizing switching valve V6A, the pressure equalizing switching valve V6B and the pressure equalizing switching valve V6C are mutually communicated, and the adsorption tower A, the adsorption tower B and the adsorption tower C are filled with nitrogen (N) 2 ) The molecular sieve is a high-efficiency Li-X type lithium-based molecular sieve, the product gas transition tank comprises a tank body, an air flow distributor A, an air flow distributor B and a vertically distributed bundling pipe, wherein the air flow distributor A is arranged between an inlet of the product gas transition tank and the bundling pipe, the air flow distributor B is arranged between an outlet of the product gas transition tank and the bundling pipe, and an air flow channel A is formed in the inner space of the bundling pipe; an air flow channel B is formed between the outer wall of the bundling pipe and the inner wall of the tank body; the said processAn air flow channel C is formed between the outer walls of adjacent pipelines in the bundling pipe.
2. The method for producing oxygen for a vacuum pressure swing adsorption oxygen production system having a product gas transition tank as claimed in claim 1, wherein: it comprises the following steps:
s1, feeding raw material air into an adsorption tower A by a blower AC, and discharging product gas from the adsorption tower A: opening an air inlet switching valve V2A, a product gas switching valve V5A, a product gas transition switching valve V7A and a product gas main valve V8, closing a self-priming switching valve V1A, an emptying switching valve V3A, a vacuum switching valve V4A and a pressure equalizing switching valve V6A, boosting raw material air by a blower AC, conveying the raw material air to an adsorption tower A through the air inlet switching valve V2A, sequentially adsorbing water, carbon dioxide and nitrogen in the raw material air by activated alumina, zeolite and lithium-based molecular sieves filled in the adsorption tower A respectively, and enabling oxygen-enriched gas to flow out of the top of the adsorption tower A as product gas and sequentially flow into a product buffer tank VS1 through the product gas switching valve V5A, the product gas transition tank VS2A, the product gas transition switching valve V7A and the product gas main valve V8;
s2, reducing pressure in the adsorption tower A: when the adsorbent filled in the adsorption tower A reaches adsorption saturation, an air inlet switching valve V2A is closed, an air blower AC is switched to the air inlet of the adsorption tower B, a product gas switching valve V5A and a product gas transition switching valve V7A are closed, the adsorption tower A stops producing product gas, a pressure equalizing switching valve V6A and a pressure equalizing switching valve V6C are opened, at the moment, the adsorption tower C is at the end of vacuumizing, the high-pressure air at the adsorption tail end in the adsorption tower A is taken as pressure equalizing air, and sequentially passes through the pressure equalizing switching valve V6A and the pressure equalizing switching valve V6C and enters the adsorption tower C at the end of vacuumizing, so that the pressure of the adsorption tower A is reduced in a forward direction, and the high-pressure air at the adsorption tail end of the adsorption tower A is recovered by the adsorption tower C;
s3, emptying the bottom of the adsorption tower A: 2-4S before the step S2 is finished, the pressure of the adsorption tower A is still higher than the ambient atmospheric pressure, the pressure equalizing switching valve V6A and the pressure equalizing switching valve V6C are kept in an opened state, the emptying switching valve V3A is opened, and air at the bottom of the adsorption tower A is emptied from the bottom of the adsorption tower A through the emptying switching valve V3A;
s4, vacuumizing an adsorption tower A: after the step S3 is finished, the pressure of the adsorption tower A is close to the ambient atmospheric pressure, the emptying switching valve V3A, the equalizing switching valve V6A and the equalizing switching valve V6C are closed, the vacuum switching valve V4A is opened, the vacuum pump VP vacuumizes the adsorption tower A, the pressure of the adsorption tower A gradually reaches the vacuum regeneration pressure of the adsorbent, the water, the carbon dioxide and the nitrogen adsorbed by the adsorbent are gradually desorbed, and the adsorbent is gradually regenerated;
s5, flushing the product gas of the adsorption tower A: when the step S4 is finished for 4-8 seconds, keeping the vacuum switching valve V4A in an opened state, continuously vacuumizing the adsorption tower A by the vacuum pump VP, opening the product gas switching valve V5A, refluxing the product gas in the product gas transition tank VS2A to the adsorption tower A through the product gas switching valve V5A, flushing the product gas in the adsorption tower A, reinforcing the regeneration of the adsorbent in the adsorption tower A, and keeping the pressure of the adsorption tower A unchanged basically in the whole flushing process;
s6, recycling the adsorption tower A: after the step S5 is finished, and 2-4S before the step S4 is finished, keeping a vacuum switching valve V4A in an opening state, continuously vacuumizing an adsorption tower A by a vacuum pump VP, closing a product gas switching valve V5A, opening a pressure equalizing switching valve V6A and a pressure equalizing switching valve V6B, wherein the adsorption tower B is positioned at the tail end of the adsorption, the high-pressure gas at the tail end of the adsorption in the adsorption tower B is used as pressure equalizing gas, sequentially enters the adsorption tower A through the pressure equalizing switching valve V6B and the pressure equalizing switching valve V6A, the high-pressure gas at the tail end of the adsorption tower B is recovered, and the low-oxygen concentrated waste gas at the lower part of the adsorption tower A is replaced by the partial gas;
s7, product gas pressure in the first stage of the adsorption tower A is increased: after the step S6 is finished, closing a vacuum switching valve V4A, a pressure equalizing switching valve V6A and a pressure equalizing switching valve V6B, opening a product gas switching valve V5A, and enabling product gas in a product gas transition tank VS2A to flow back to an adsorption tower A through the product gas switching valve V5A so as to boost the product gas in the first stage of the adsorption tower A;
s8, product gas pressure in the second stage of the adsorption tower A is increased, and the bottom of the adsorption tower A is self-sucking with the atmosphere: the product gas switching valve V5A is still kept in an open state, the pressure of the adsorption tower A is still lower than the ambient atmospheric pressure at the moment, the self-priming switching valve V1A is opened, and the air is self-priming through the self-priming switching valve V1A and enters the bottom of the adsorption tower A, so that the pressure of the adsorption tower A is gradually increased to the ambient atmospheric pressure;
s9, product gas pressure in the third stage of the adsorption tower A is increased: when the pressure of the adsorption tower A reaches the ambient atmospheric pressure, the opening state of the product gas switching valve V5A is still maintained, the self-priming switching valve V1A is closed, the product gas transition switching valve V7A is opened, the product gas in the product buffer tank VS1 flows back to the product gas transition tank VS2A through the product gas transition switching valve V7A, the product gas in the product gas transition tank VS2A flows back to the adsorption tower A through the product gas switching valve V5A, the pressure of the adsorption tower A is continuously increased until the adsorption pressure is reached, and the product gas pressure increase is completed.
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| CN110627022B (en) * | 2019-10-22 | 2023-09-19 | 湖南泰瑞医疗科技有限公司 | Three-tower oxygen generation system |
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| CN106698357A (en) * | 2016-12-28 | 2017-05-24 | 北京金大万翔环保科技有限公司 | Device and method for preparing oxygen through three-tower low pressure adsorption and vacuum desorption |
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| CN207324434U (en) * | 2017-07-25 | 2018-05-08 | 杨炯良 | A kind of vacuum pressure swing adsorption system for oxygen production with product gas transition tank |
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| CN107261755A (en) | 2017-10-20 |
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