CN107200307B - Three-tower vacuum pressure swing adsorption oxygen generation system and oxygen generation method thereof - Google Patents

Three-tower vacuum pressure swing adsorption oxygen generation system and oxygen generation method thereof Download PDF

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CN107200307B
CN107200307B CN201710659064.6A CN201710659064A CN107200307B CN 107200307 B CN107200307 B CN 107200307B CN 201710659064 A CN201710659064 A CN 201710659064A CN 107200307 B CN107200307 B CN 107200307B
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switching valve
adsorption tower
product gas
pressure
adsorption
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CN107200307A (en
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杨炯良
胡学奎
梁勇
李伟
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
    • C01B13/0229—Purification or separation processes
    • C01B13/0248—Physical processing only
    • C01B13/0259—Physical processing only by adsorption on solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • 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
    • B01D53/047—Pressure swing adsorption
    • B01D53/0476—Vacuum pressure swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • 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
    • B01D53/047—Pressure swing adsorption
    • B01D53/053—Pressure swing adsorption with storage or buffer vessel
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
    • C01B13/0229—Purification or separation processes
    • C01B13/0248—Physical processing only
    • C01B13/0259—Physical processing only by adsorption on solids
    • C01B13/0262—Physical processing only by adsorption on solids characterised by the adsorbent
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00—Purification or separation of specific gases
    • C01B2210/0001—Separation or purification processing
    • C01B2210/0009—Physical processing
    • C01B2210/0014—Physical processing by adsorption in solids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00—Purification or separation of specific gases
    • C01B2210/0001—Separation or purification processing
    • C01B2210/0009—Physical processing
    • C01B2210/0014—Physical processing by adsorption in solids
    • C01B2210/0015—Physical processing by adsorption in solids characterised by the adsorbent

Abstract

The invention discloses a three-tower vacuum pressure swing adsorption oxygen generation system, wherein a corresponding product gas transition tank is arranged corresponding to each adsorption tower, a high oxygen concentration part at the front section of the product gas produced in each adsorption oxygen generation process of the adsorption tower enters the product gas buffer tank to serve as product gas of an oxygen generation system, a low oxygen concentration part at the rear section of the product gas resides in the product gas transition tank according to the produced oxygen concentration gradient, and the product gas is taken as a product gas lifting compressed air backflow adsorption tower for boosting when the corresponding adsorption tower is transferred into a product gas boosting step; the invention also discloses an oxygen production method, wherein an independent bundling pipe pressure equalizing tank is arranged, the pressure equalizing gas which is uniformly discharged in the pressure equalizing process of the adsorption tower is temporarily stored in the bundling pipe pressure equalizing tank according to the uniform oxygen concentration gradient, and when the adsorption tower is transferred into a uniform inlet recovery step, the uniform inlet gas is recovered. The invention has the following effects: the method improves the gas-oxygen concentration of the product, the use efficiency of the adsorbent and the oxygen recovery rate of the system, reduces the load of the blower and the vacuum pump, reduces the energy consumption and the investment of the system, and realizes the continuous air supply of the blower.

Description

Three-tower vacuum pressure swing adsorption oxygen generation system and oxygen generation method thereof
Technical Field
The invention relates to a pressure swing adsorption gas separation technology, in particular to a three-tower vacuum pressure swing adsorption oxygen generation system 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, the vacuum pump is used to vacuumize and depressurize the adsorption tower, so that 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.
In order to improve the adsorption efficiency and increase the oxygen production capacity of the system, the existing vacuum pressure swing adsorption oxygen production system uses the high-pressure gas at the adsorption tail end in the adsorption tower as uniform pressure gas after the adsorption tower is saturated, uses the adsorption tower at the vacuumizing tail end to uniformly recycle the high-pressure gas, and recycles the uniform pressure gas to the adsorption tower at the vacuumizing tail end, wherein a small amount of the uniform pressure gas is taken as flushing gas to be pumped by a vacuum pump and discharged to the atmosphere, and the rest of the uniform pressure gas is taken as low-oxygen concentrated waste gas in a displacement gas retention tower to be recycled and discharged out of the lower part of the vacuumizing tower, and the following 3 methods are generally adopted in specific implementation:
(1) The product gas flushing regeneration and pressure equalizing recovery method comprises the following steps: when the vacuumizing of the adsorption tower B is finished for 2-6 s, reversely flushing the adsorption tower B for 2-3 s by using a small amount of product gas generated in a product gas buffer tank or the adsorption tower A to strengthen the regeneration of the adsorbent in the adsorption tower B, and replacing part of low-oxygen concentrated waste gas at the lower part of the adsorption tower B, wherein the pressure of the adsorption tower B is basically kept unchanged, and the process is a product gas flushing regeneration process; when the reverse flushing of the adsorption tower B is finished, the adsorption tower A is in an adsorption saturation state, at the moment, an air inlet of an air blower of the adsorption tower A is closed through an air inlet switching valve, the air blower is in an air-out state through an air blower air-out switching valve (at the moment, the adsorption tower B is still in a vacuum pumping state), the top of the adsorption tower A is directly communicated with the top of the adsorption tower B through a pressure equalizing switching valve, the adsorption tower A equalizes pressure to the adsorption tower B, high-pressure air at the adsorption tail end in the adsorption tower A after the adsorption tower A is adsorbed and saturated is used as equalized air, the adsorption tower B at the vacuumizing tail end is utilized for equalizing and recycling, the equalized air of the adsorption tower B at the vacuumizing tail end is recycled, a small amount of the equalized air is pumped out to the atmosphere as flushing air, the rest of the equalized air is recycled as a replacement air to preserve the adsorption tower B, and the low-oxygen dense exhaust gas at the lower part of the adsorption tower B is replaced, and the equalizing pressure recycling process is adopted.
(2) The pressure equalizing gas flushing regeneration recovery method comprises the following steps: when the adsorption tower B is in an adsorption saturated state 2-6 s before vacuumizing, at the moment, an air inlet of an air blower of the adsorption tower A is closed through an air inlet switching valve, the air blower is in a emptying state (at the moment, the adsorption tower B is still in a vacuum pumping state) through an air blower emptying switching valve, the top of the adsorption tower A is directly communicated with the top of the adsorption tower B through a pressure equalizing switching valve, the adsorption tower A equalizes pressure to the adsorption tower B, high-pressure air at the adsorption tail end in the adsorption tower A after adsorption saturation is taken as pressure equalizing air, the adsorption tower B at the vacuumizing tail end is utilized for carrying out uniform recovery, a small amount of the pressure equalizing air is taken as flushing air to be pumped away to the atmosphere, the rest of the pressure equalizing air is taken as a displacement air to be reserved in the adsorption tower B, and low-oxygen concentrated waste gas at the lower part of the adsorption tower B is displaced, and the process is a pressure equalizing air flushing regeneration recovery process.
(3) Chinese patent CN201310007058.4 discloses a vacuum pressure swing adsorption oxygen generating system and control method thereof: and when the adsorption tower A is saturated, the air inlet of the air blower of the adsorption tower A is closed through the air inlet switching valve, and the air blower is in a venting state through the air blower venting switching valve (at the moment, the adsorption tower B is still in a vacuum pumping state of the vacuum pump). The top of the adsorption tower A is directly communicated with a first pressure equalizing tank through a pressure equalizing switching valve, high-pressure gas at the adsorption tail end in the adsorption tower A is used as pressure equalizing gas after adsorption saturation, and a front-stage high-oxygen concentration part of the pressure equalizing gas is placed in the first pressure equalizing tank forward for temporary storage; and then the top of the adsorption tower A is directly communicated with a second pressure equalizing tank through a pressure equalizing switching valve, and the rear low-oxygen concentration part of the partial pressure equalizing gas is continuously and forward placed into the second pressure equalizing tank for temporary storage. And at the end of vacuumizing the adsorption tower A, the top of the adsorption tower A is directly communicated with a second pressure equalizing tank through a pressure equalizing switching valve, temporary storage pressure equalizing gas (pressure equalizing gas rear section low-oxygen concentrated part) of the adsorption tower A, which is placed in the second pressure equalizing tank in the forward direction, is used for reversely flushing the adsorption tower A, low-oxygen concentrated waste gas at the lower part of the adsorption tower A at the tail end of vacuumizing is replaced, the top of the adsorption tower B is directly communicated with the first pressure equalizing tank through the pressure equalizing switching valve after vacuumizing the adsorption tower B, temporary storage pressure equalizing gas (pressure equalizing gas front section high-oxygen concentrated part) of the adsorption tower A, which is placed in the first pressure equalizing tank in the forward direction, is used for boosting the adsorption tower B, and recovery of the adsorption tail end high-pressure gas high-oxygen concentrated part in the adsorption tower after adsorption saturation of the adsorption tower A is realized.
After the adsorption towers are depressurized, the vacuum pump is used for vacuumizing the adsorption towers, and the suction is continuously reducedWith column pressure, water adsorbed in the adsorbent (H 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.
The product gas flushing regeneration and pressure equalizing recovery method comprises the following steps: because part of product gas is used for flushing the adsorbent in the adsorption tower in the regeneration process, the adsorbent in the adsorption tower is regenerated more thoroughly, and the low-oxygen concentrated waste gas at the lower part of the regeneration adsorption tower is discharged more fully. However, most of the flushing gas can be pumped by the vacuum pump, and part of the product gas for flushing is lost, so that the load of the vacuum pump is increased, the energy consumption of the system is increased, and the gas yield of the device is correspondingly reduced.
The method for regenerating and recovering the uniform pressure gas flushing comprises the following steps: when the adsorption tower A is saturated, the pressure in the adsorption tower A is generally 120-160 kpa.A, and the oxygen concentration gradient in the adsorption tower A 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. At this time, the adsorption tower B is just close to or at the end of vacuumizing, the pressure in the adsorption tower B is generally between 40 and 60kpa.A, and the oxygen concentration gradient in the adsorption tower B is as follows: the tower bottom is 8-11% and gradually transits to the tower top of 60-90% (the oxygen concentration of the adsorption end product). Because the bottom and the top of the adsorption tower are provided with the gas distributors and occupy a certain empty volume; when the adsorbent is packed in the adsorption tower, a certain empty volume exists among the adsorbent particles. When the top of the adsorption tower A is communicated with the top of the adsorption tower B for pressure equalizing (at the moment, the adsorption tower A stops air inlet and the adsorption tower B continues vacuumizing), the pressure equalizing gas, the oxygen concentration and the oxygen concentration gradient flowing into the adsorption tower B from the adsorption tower A are as follows: 60-90% (adsorption end gas oxygen concentration) to about 21% of air oxygen concentration, namely the initial oxygen concentration of the pressure equalizing gas of the adsorption tower A is 60-90% (adsorption end product oxygen concentration), the final oxygen concentration is about 21%, and the initial oxygen concentration of the pressure equalizing gas correspondingly flowing into the adsorption tower B is 60-90% (adsorption end product oxygen concentration), and the final oxygen concentration is about 21%. The result of this pressure equalization process must be: the recovered equalizing gas with high oxygen concentration is filled in the bottom of the adsorption tower to be subjected to next adsorption, and the recovered equalizing gas with low oxygen concentration is filled in the top of the adsorption tower to be subjected to next adsorption. Is unfavorable for adsorption operation, and reduces adsorption efficiency and oxygen recovery rate.
Chinese patent CN201310007058.4 discloses a vacuum pressure swing adsorption oxygen generating system and a control method thereof, which have fully described the drawbacks of the existing process, and the solution provided by the method is: and when the adsorption tower A is saturated, the air inlet of the air blower of the adsorption tower A is closed through the air inlet switching valve, and the air blower is in a venting state through the air blower venting switching valve (at the moment, the adsorption tower B is still in a vacuum pumping state of the vacuum pump). The top of the adsorption tower A is directly communicated with a first pressure equalizing tank through a pressure equalizing switching valve, high-pressure gas at the adsorption tail end in the adsorption tower A is used as pressure equalizing gas after adsorption saturation of the adsorption tower A, and a front-stage high-oxygen concentration part of the pressure equalizing gas is forward placed into the first pressure equalizing tank for temporary storage; and then the top of the adsorption tower A is directly communicated with a second pressure equalizing tank through a pressure equalizing switching valve, and the rear low-oxygen concentration part of the partial pressure equalizing gas is continuously and forward placed into the second pressure equalizing tank for temporary storage. And at the end of vacuumizing the adsorption tower A, the top of the adsorption tower A is directly communicated with a second pressure equalizing tank through a pressure equalizing switching valve, temporary storage pressure equalizing gas (pressure equalizing gas rear section low-oxygen concentrated part) of the adsorption tower A is placed in the second pressure equalizing tank in the forward direction to reversely flush the adsorption tower A, low-oxygen concentrated waste gas at the lower part of the adsorption tower A at the tail end of vacuumizing is replaced, the top of the adsorption tower B is directly communicated with the first pressure equalizing tank through the pressure equalizing switching valve after vacuumizing the adsorption tower B, the temporary storage pressure equalizing gas (pressure equalizing gas front section high-oxygen concentrated part) of the adsorption tower A is placed in the first pressure equalizing tank in the forward direction to boost the adsorption tower B, and recovery of the adsorption tail end high-pressure gas high-oxygen concentrated part in the adsorption tower after adsorption saturation of the adsorption tower A is realized. The method is essentially characterized in that the pressure equalizing gas is divided into two parts, a high oxygen concentration part of a front section of the pressure equalizing gas firstly enters a first pressure equalizing gas tank for temporary storage, a low oxygen concentration part of a rear section of the pressure equalizing gas enters a second pressure equalizing gas tank for temporary storage, the low oxygen concentration part of the rear section of the pressure equalizing gas, which is temporarily stored in the second pressure equalizing gas tank, is used for flushing and regenerating the regenerated adsorption tower, and a high oxygen concentration part of the front section of the pressure equalizing gas, which is temporarily stored in the first pressure equalizing gas tank, is used for recovering the boosted gas of the regenerated adsorption tower. Although the method has a certain technical progress, the following defects still exist: (1) After the partial pressure equalization gas with low oxygen concentration at the rear stage is mixed into the average oxygen concentration in the second pressure equalization tank, the regenerated adsorption tower is washed and replaced, and the oxygen concentration of the washing gas left in the adsorption tower is evenly distributed; (2) The partial pressure equalizing gas with high oxygen concentration in the front stage can be mixed into the average oxygen concentration in the first pressure equalizing gas tank, and then the average oxygen concentration is refilled into the regenerated adsorption tower for recovery, and the oxygen concentration in the regenerated adsorption tower is uniformly distributed. Still be unfavorable for adsorption operation, adsorption efficiency can not fully exert, and oxygen recovery rate improves limitedly.
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 depressurization process can lead the empty space occupied by the gas distributor at the bottom of the adsorption tower at the adsorption end and the empty space occupied by the corresponding pipelineWhen the high-pressure raw material air stored in the storage volume 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 a depressurization 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 provides a method for improving the utilization method according to the characteristics of gas-oxygen concentration of a product in the adsorption oxygen production process and the change of the gas-oxygen concentration in the pressure equalization process, so as to reduce the oxygen loss of the product, improve the utilization rate of an adsorbent and the oxygen recovery rate of a system; the three-tower vacuum pressure swing adsorption oxygen production system and the oxygen production 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 three-tower vacuum pressure swing adsorption oxygen generation system 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, 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 uniform pressure gas to flow in and out one dimension; 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 the bundling pipe equalizing tank VS3 is connected with an equalizing switching valve V10, the other end of the equalizing switching valve V10 is connected with an equalizing gas main pipe P6, the other end of the equalizing gas main pipe P6 is connected with an equalizing switching valve V6A, an equalizing switching valve V6B and an equalizing switching valve V6C in parallel, and the other ends of the equalizing switching valve V6A, the equalizing switching valve V6B and the equalizing switching valve V6C are respectively connected with the tops of the adsorption tower A, the adsorption tower B and the adsorption tower C; the top of the bundling pipe equalizing tank VS3 is also connected with an equalizing switching valve V11, and the other end of the equalizing switching valve V11 is connected with an equalizing gas main pipe P6.
The product gas transition tank comprises a tank body A, an air flow distributor B and a vertically distributed bundling pipe A, wherein the air flow distributor A is arranged between an inlet of the product gas transition tank and the bundling pipe A, the air flow distributor B is arranged between an outlet of the product gas transition tank and the bundling pipe A, and an air flow channel A is formed in the inner space of the bundling pipe A; an air flow channel B is formed between the outer wall of the bundling pipe A and the inner wall of the tank body A; an air flow channel C is formed between the outer walls of adjacent pipelines in the bundling pipe A.
The bundling tube equalizing tank VS3 comprises a tank body B, an air inlet and outlet distributor C and a vertically distributed bundling tube B, wherein the air inlet and outlet distributor C is arranged in the tank body B, the air inlet and outlet distributor C is arranged at the top of the tank body B and is positioned at the inlet and outlet ends of the bundling tube B, and an air flow channel D is formed in the inner space of the bundling tube B; an air flow channel E is formed between the outer wall of the bundling pipe B and the inner wall of the tank body B; an air flow channel F is formed between the outer walls of adjacent pipelines in the bundling pipe B.
The all-out switching valve V11 is a regulating valve.
The oxygen production method of the three-tower vacuum pressure swing adsorption oxygen production system 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, respectively inputting a switching valve V10 and a pressure equalizing switching valve V11, 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, and sequentially adsorbing water, carbon dioxide and nitrogen in the raw material air by activated alumina, zeolite and a lithium-based molecular sieve filled in the adsorption tower A respectively, wherein oxygen-enriched gas flows out from the top of the adsorption tower A as product gas and flows 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 in sequence;
S2, equalizing pressure between the adsorption tower A and a bundling tube equalizing tank VS 3: 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 an equalizing switching valve V10 are opened, high-pressure air at the adsorption tail end in the adsorption tower A is used as pressure equalizing air and sequentially passes through the pressure equalizing switching valve V6A and the equalizing switching valve V10 and is uniformly introduced into a bundling pipe pressure equalizing tank VS3, 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 temporarily stored in the bundling pipe pressure equalizing tank VS 3;
s3, emptying the bottom of the adsorption tower A: after the step S2 is finished, the pressure of the adsorption tower A is still higher than the ambient atmospheric pressure, the equalizing switching valve V6A is closed, the equalizing switching valve V10 is opened, 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 is 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, carbon dioxide and nitrogen adsorbed by the adsorbent are desorbed, and the adsorbent is regenerated;
S5, recycling the adsorption tower A: starting a uniform outlet switching valve V11 and a uniform pressure switching valve V6A 2-4S before the step S4 is finished, enabling uniform pressure gas temporarily stored in a bundling pipe uniform pressure tank VS3 to flow back into an adsorption tower A through the uniform outlet switching valve V11 and the uniform pressure switching valve V6A in sequence under the pressure effect of the uniform pressure gas, recovering high-pressure gas at the adsorption tail end temporarily stored in the bundling pipe uniform pressure tank VS3 in the step S2 of the adsorption tower B, and replacing low-oxygen concentrated waste gas at the lower part of the adsorption tower A by using the partial gas, wherein the adsorption tower A still performs vacuumizing when uniform pressure gas is recovered;
s6, boosting product gas in the first stage of the adsorption tower A: after the step S5 is finished, closing a vacuum switching valve V4A, a pressure equalizing switching valve V6A and a pressure equalizing switching valve V11, 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;
s7, 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;
S8, 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 characteristics of gas-oxygen concentration of a product in the adsorption oxygen production process and uniform pressure gas-oxygen concentration change in the pressure equalizing process, the invention improves the utilization method, and increases the air-oxygen yield of raw materials by about 8 percent 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 schematic structural diagram of a cluster-tube pressure equalizing tank VS3 according to the present invention;
FIG. 5 is a cross-sectional view A-A of FIG. 4;
FIG. 6 is a timing diagram of an oxygen generation cycle of the present invention;
in the figure, a 1-product gas transition tank outlet, a 2-gas distributor B, a 3-tank A, a 4-bundling pipe A, a 5-gas distributor A, a 6-product gas transition tank inlet, a 7-gas channel A, an 8-gas channel B, a 9-gas channel C, a 10-tank B, a 11-gas distributor C, a 12-bundling pipe B, a 13-gas channel D, a 14-gas channel E and a 15-gas channel F are arranged.
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:
as shown in fig. 1, a three-tower vacuum pressure swing adsorption oxygen generation system 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 for keeping one-dimensional flow of product gas in and out, and a bundling pipe equalizing tank VS3 for keeping one-dimensional flow of uniform pressure gas in and out.
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 top of the bundling tube equalizing tank VS3 is connected with an equalizing switching valve V10, the other end of the equalizing switching valve V10 is connected with an equalizing gas main pipe P6, the other end of the equalizing gas main pipe P6 is connected with an equalizing switching valve V6A, an equalizing switching valve V6B and an equalizing switching valve V6C in parallel, and the other ends of the equalizing switching valve V6A, the equalizing switching valve V6B and the equalizing switching valve V6C are respectively connected with the tops of the adsorption tower a, the adsorption tower B and the adsorption tower C.
As shown in fig. 1, the top of the bundling tube equalizing tank VS3 is further connected with an equalizing switching valve V11, and the other end of the equalizing switching valve V11 is connected with the equalizing gas manifold P6.
As shown in fig. 1-3, the product gas transition tank comprises a tank body A3, an air flow distributor A5, an air flow distributor B2 and a vertically distributed bundling pipe A4, wherein the air flow distributor A5 is arranged between an inlet 6 of the product gas transition tank and the bundling pipe A4, the air flow distributor B2 is arranged between an outlet 1 of the product gas transition tank and the bundling pipe A4, and an air flow channel A7 is formed in the inner space of the bundling pipe A4; an air flow channel B8 is formed between the outer wall of the bundling pipe A4 and the inner wall of the tank body A3; an air flow channel C9 is formed between the outer walls of adjacent pipelines in the bundling pipe A4.
As shown in fig. 1, 4 and 5, the bundling tube equalizing tank VS3 includes a tank B10, an in-out airflow distributor C11 disposed in the tank B10, and vertically distributed bundling tubes B12, where the in-out airflow distributor C11 is disposed at the top of the tank B10 and is located at an inlet end and an outlet end of the bundling tubes B12, and an airflow channel D13 is formed in an inner space of the bundling tubes B12; an air flow channel E14 is formed between the outer wall of the bundling pipe B12 and the inner wall of the tank body B10; an air flow channel F15 is formed between the outer walls of adjacent pipelines in the bundling pipe B12.
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 average outlet switching valve V11 is a regulating valve, and is used for regulating flow and pressure parameters of average pressure gas and purge gas of the adsorption tower.
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 6, the oxygen production method of the three-tower vacuum pressure swing adsorption oxygen production system 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 an air blower AC, and producing the adsorption tower AAnd (3) product gas: opening an 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, a pressure equalizing switching valve V6A, a uniform inlet switching valve V10 and a uniform outlet switching valve V11, boosting raw material air by a blower AC, continuously conveying the raw material air to an adsorption tower A through the inlet switching valve V2A, and continuously feeding water (H 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 flows out of the top of the adsorption tower A as product gas and sequentially passes through the product gas switching valve V5A, the product gas transition tank inlet 6 and the gas flow distributor A5, and enters the gas flow channel A7, the gas flow channel B8 and the gas flow channel C9 in the product gas transition tank. Because the gas flow distributor A5, the gas flow channel A7, the gas flow channel B8, the gas flow channel C9 and the gas flow distributor B2 arranged in the product gas transition tank VS2A have the functions that the product gas entering the gas flow channel A7, the gas flow channel B8 and the gas flow channel C9 in the product gas transition tank VS2 flows in one dimension in the gas flow channel without generating the phenomenon that the front-stage gas resides and the rear-stage gas is mixed, the product gas entering the gas flow channel A7, the gas flow channel B8 and the gas flow channel C9 can necessarily keep the oxygen concentration gradient, and enters the product buffer tank VS1 from the gas flow channel A7, the gas flow channel B8 and the gas flow channel C9 through the gas flow distributor B2, the product gas transition tank outlet 1, the product gas transition switching valve V7A and the product gas total valve V8, thereby realizing that the high-oxygen concentrated product gas enters the product gas buffer tank VS1 at the front stage in the adsorption oxygen production process is used as the final product gas of the adsorption oxygen production system and the oxygen production system is adsorbed The low-oxygen concentrated product gas at the later stage of the process keeps the oxygen concentration gradient of the low-oxygen concentrated product gas to stay in the gas flow channel A7, the gas flow channel B8 and the gas flow channel C9 of the product gas transition tank VS1, and is used as the product gas lift compression gas in the product gas lift compression process of the adsorption tower A;
s2, equalizing pressure between the adsorption tower A and a bundling tube equalizing tank VS 3; 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, at the moment, the adsorption tower A is in an adsorption tail end state, the pressure of the adsorption tower A is the highest adsorption pressure, the space occupied by gas distributors at the top and the bottom of the adsorption tower A and the space occupied by corresponding pipelines are equal, and the oxygen concentration gradient of high-pressure gas stored in the space occupied among adsorbent particles 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. Opening a pressure equalizing switching valve V6A and a uniform inlet switching valve V10, wherein high-pressure gas at the adsorption tail end in the adsorption tower A sequentially passes through the pressure equalizing switching valve V6A, the uniform inlet switching valve V10 and the inlet and outlet gas flow distributor C11 as uniform pressure gas and is uniformly introduced into a gas flow channel D13, a gas flow channel E14 and a gas flow channel F15 under the pressure action of the uniform pressure gas, and the uniform pressure gas flow outlet sequence is as follows: continuously flowing out from high-oxygen concentration equalizing gas to low-oxygen concentration equalizing gas according to the oxygen concentration gradient, realizing forward equalizing, reducing the pressure of the adsorption tower A, and temporarily storing the high-pressure gas at the adsorption tail end of the adsorption tower A in the gas flow channels D13, E14 and F15 in the bundling pipe equalizing tank VS 3. Because the in-out airflow distributor C11, the airflow channel D13, the airflow channel E14 and the airflow channel F15 which are arranged in the bundling pipe equalizing tank play a role in that the equalizing gases entering the airflow channel D13, the airflow channel E14 and the airflow channel F15 in the bundling pipe equalizing tank VS3 can flow in one dimension in the airflow channels, and the phenomenon that the front-stage gases stay and the rear-stage gases are mixed can not occur, so that the equalizing gases entering the airflow channel D13, the airflow channel E14 and the airflow channel F15 can necessarily keep the oxygen concentration gradient, the equalizing gases temporarily stored in the airflow channel D13, the airflow channel E14 and the airflow channel F15 in the bundling pipe equalizing tank VS3 are continuously stored temporarily (the adsorption tower A is used for equalizing the equalizing gases temporarily stored in the bundling pipe equalizing tank VS3, and the equalizing gases are used as the equalizing gases in the S5 process of the adsorption tower C in the oxygen production cycle of the oxygen production system of the latter);
S3, emptying the bottom of the adsorption tower A: after 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 of adsorption tower A is carried into vacuumizing regeneration to continuously reduce the pressure, and part of raw material air which is stored in the empty volume occupied by the gas distributor at the bottom of the adsorption tower A and the empty volume occupied by the corresponding pipeline at the inlet at the bottom of the adsorption tower A and is higher than the ambient atmospheric pressure is not adsorbed and utilized by the adsorbent in the adsorption bed layer if the raw material air is diffused to the top of the adsorption tower A, and pollutes the adsorbent in the adsorption bed layer, so that invalid gas resides in the adsorption tower. At the moment, the equalizing switching valve V6A and the equalizing switching valve V10 are closed, 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 vent switching valve V3A is closed, the vacuum switching valve V4A is opened, the vacuum pump VP vacuumizes the adsorption tower a, and the pressure of the adsorption tower a gradually reaches the vacuum regeneration pressure of the adsorbent, so that the water (H 2 O), carbon dioxide (CO) 2 ) Nitrogen (N) 2 ) Desorbing, and regenerating the adsorbent;
s5, recycling the adsorption tower A: when 2-4S before the end of the step S4, opening a uniform outlet switching valve V11 and a uniform pressure switching valve V6A, and allowing the uniform pressure gas temporarily stored in an air flow channel D13, an air flow channel E14 and an air flow channel F15 in a cluster tube uniform pressure tank VS3 (the uniform pressure gas in the part comes from the previous oxygen generation system oxygen generation cycle, namely, the uniform pressure gas temporarily stored in the air flow channel D13, the air flow channel E14 and the air flow channel F15 in the cluster tube uniform pressure tank VS3 in the S2 process of the adsorption tower B) to flow back into the adsorption tower A through an inlet and outlet air flow distributor C11, the uniform outlet switching valve V11 and the uniform pressure switching valve V6A in sequence under the pressure effect, wherein the uniform pressure gas backflow sequence is as follows: continuously refluxing the low-oxygen concentration equalizing gas to the high-oxygen concentration equalizing gas according to the oxygen concentration gradient. Because of the functions of the inlet and outlet air flow distributor C11, the air flow channel D13, the air flow channel E14 and the air flow channel F15 which are arranged in the bundling pipe pressure equalizing tank VS3, the pressure equalizing air flowing out of the air flow channel D13, the air flow channel E14 and the air flow channel F15 in the bundling pipe pressure equalizing tank VS3 flows in one dimension in the air flow channel, and the phenomenon that the front-stage air resides and the rear-stage air is not generated, so that the pressure equalizing air flowing out of the air flow channel D13, the air flow channel E14 and the air flow channel F15 can keep the oxygen concentration gradient continuously entering the adsorption tower A, the low-oxygen concentration part pressure equalizing air which is firstly obtained by the bundling pipe pressure equalizing tank VS3 enters the adsorption tower A as flushing air, is pumped by a vacuum pump, the high-oxygen concentration part which is uniformly obtained by the bundling pipe pressure equalizing tank VS3 enters the adsorption tower A as displacement air, and is recycled in the adsorption tower A, and the oxygen concentration of the part recycled pressure equalizing air is continuously distributed from bottom to top of the tower in the adsorption tower A from low to high;
In the step S5, the opening of the uniform outlet switching valve V11 is controlled and regulated, so that the uniform pressure air flow and pressure parameters of the reverse uniform recovery process of the adsorption tower A can be regulated, and the uniform pressure air flow and pressure parameters of the uniform pressure process of the adsorption tower A and the bundling tube uniform pressure tank VS3 in the step S2 are regulated;
s6, boosting product gas in the first stage of the adsorption tower A: after the step S5 is finished, the vacuum switching valve V4A and the pressure equalizing switching valve V6A 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 gas flow channel A7, the gas flow channel B8 and the gas flow channel C9 in the product gas transition tank VS2A is used as rising gas of the adsorption tower A and flows 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. 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: 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 of the adsorption tower A in the first stage;
S7, 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, the air is self-priming and enters the bottom of the adsorption tower A through the self-priming switching valve V1A, the product gas and the self-priming air are boosted together for the adsorption tower A, and the pressure of the adsorption tower A is gradually increased to the ambient atmospheric pressure;
s8, 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 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 and the air flow distributor B2, 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 after the adsorption oxygen production process flows back to the adsorption tower A sequentially through the air flow distributor A5, the product gas transition tank inlet 6 and the product gas switching valve V5A under the pushing of the product gas flowing back from 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 the oxygen concentration gradient, and boosting the product gas of the adsorption tower A in the third stage until the adsorption pressure is reached, so that the product gas boosting is completed, the low oxygen concentration product gas of the later stage of the adsorption oxygen production process is used as the product gas boosting gas of the adsorption tower A, the continuously refluxing the adsorption tower A from low oxygen concentration to high oxygen concentration according to the 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 from low to high. 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 by using a blower AC to adsorb and produce air, 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 lifting compressed air in the product air lifting and pressing process of the corresponding adsorption tower, the cluster tube equalizing tank VS2 is used for forward uniform pressure reduction and reverse uniform pressure recovery uniform pressure air, a vacuum pump VP is used for vacuumizing, residual pressure at the bottom of the adsorption tower is automatically discharged after the uniform pressure reduction, and the product air at the first stage of the adsorption tower is used for boosting and then the bottom of the adsorption tower is used for absorbing the atmosphere in a vacuum state.
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.

Claims (5)

1. A three-tower vacuum pressure swing adsorption oxygen generation system is characterized in that: the device 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, 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 VS3 are used for keeping uniform pressure gas to flow in and out one dimension; 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, and the other end of the air inlet main pipe P2 is connected with an air inlet switching valve V2A and an air inlet switching valve in parallelThe other ends of the valve V2B and the air inlet switching valve V2C, 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 the bundling pipe equalizing tank VS3 is connected with an equalizing switching valve V10, the other end of the equalizing switching valve V10 is connected with an equalizing gas main pipe P6, the other end of the equalizing gas main pipe P6 is connected with an equalizing switching valve V6A, an equalizing switching valve V6B and an equalizing switching valve V6C in parallel, and the other ends of the equalizing switching valve V6A, the equalizing switching valve V6B and the equalizing switching valve V6C are respectively connected with the tops of the adsorption tower A, the adsorption tower B and the adsorption tower C; the top of the bundling pipe equalizing tank VS3 is also connected with an equalizing switching valve V11, the other end of the equalizing switching valve V11 is connected with an equalizing gas main pipe P6, and the bottoms of the adsorption tower A, the adsorption tower B and the adsorption tower C are respectively connected with a residual pressure state bottom for the adsorption tower The bottom 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, V1C for self-priming air at the bottom of the adsorption tower in a negative pressure state, and nitrogen (N) is 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.
2. The three-tower vacuum pressure swing adsorption oxygen generating system of claim 1, wherein: the product gas transition tank comprises a tank body A, an air flow distributor B and a vertically distributed bundling pipe A, wherein the air flow distributor A is arranged between an inlet of the product gas transition tank and the bundling pipe A, the air flow distributor B is arranged between an outlet of the product gas transition tank and the bundling pipe A, and an air flow channel A is formed in the inner space of the bundling pipe A; an air flow channel B is formed between the outer wall of the bundling pipe A and the inner wall of the tank body A; an air flow channel C is formed between the outer walls of adjacent pipelines in the bundling pipe A.
3. The three-tower vacuum pressure swing adsorption oxygen generating system of claim 1, wherein: the bundling tube equalizing tank VS3 comprises a tank body B, an air inlet and outlet distributor C and a vertically distributed bundling tube B, wherein the air inlet and outlet distributor C is arranged in the tank body B, the air inlet and outlet distributor C is arranged at the top of the tank body B and is positioned at the inlet and outlet ends of the bundling tube B, and an air flow channel D is formed in the inner space of the bundling tube B; an air flow channel E is formed between the outer wall of the bundling pipe B and the inner wall of the tank body B; an air flow channel F is formed between the outer walls of adjacent pipelines in the bundling pipe B.
4. The three-tower vacuum pressure swing adsorption oxygen generating system of claim 1, wherein: the all-out switching valve V11 is a regulating valve.
5. The oxygen production method of the three-tower vacuum pressure swing adsorption oxygen production system according to any one of claims 1 to 4, characterized by: 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, respectively inputting a switching valve V10 and a pressure equalizing switching valve V11, 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, and sequentially adsorbing water, carbon dioxide and nitrogen in the raw material air by activated alumina, zeolite and a lithium-based molecular sieve filled in the adsorption tower A respectively, wherein oxygen-enriched gas flows out from the top of the adsorption tower A as product gas and flows 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 in sequence;
s2, equalizing pressure between the adsorption tower A and a bundling tube equalizing tank VS 3: 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 an equalizing switching valve V10 are opened, high-pressure air at the adsorption tail end in the adsorption tower A is used as pressure equalizing air and sequentially passes through the pressure equalizing switching valve V6A and the equalizing switching valve V10 and is uniformly introduced into a bundling pipe pressure equalizing tank VS3, 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 temporarily stored in the bundling pipe pressure equalizing tank VS 3;
S3, emptying the bottom of the adsorption tower A: after the step S2 is finished, the pressure of the adsorption tower A is still higher than the ambient atmospheric pressure, the equalizing switching valve V6A is closed, the equalizing switching valve V10 is opened, 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 is 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, carbon dioxide and nitrogen adsorbed by the adsorbent are desorbed, and the adsorbent is regenerated;
s5, recycling the adsorption tower A: starting a uniform outlet switching valve V11 and a uniform pressure switching valve V6A 2-4S before the step S4 is finished, enabling uniform pressure gas temporarily stored in a bundling pipe uniform pressure tank VS3 to flow back into an adsorption tower A through the uniform outlet switching valve V11 and the uniform pressure switching valve V6A in sequence under the pressure effect of the uniform pressure gas, recovering high-pressure gas at the adsorption tail end temporarily stored in the bundling pipe uniform pressure tank VS3 in the step S2 of the adsorption tower B, and replacing low-oxygen concentrated waste gas at the lower part of the adsorption tower A by using the partial gas, wherein the adsorption tower A still performs vacuumizing when uniform pressure gas is recovered;
s6, boosting product gas in the first stage of the adsorption tower A: after the step S5 is finished, closing a vacuum switching valve V4A, a pressure equalizing switching valve V6A and a pressure equalizing switching valve V11, 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;
S7, 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;
s8, 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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