CN112938903A - Oxygen generation and supply device and method for operating room and ICU - Google Patents
Oxygen generation and supply device and method for operating room and ICU Download PDFInfo
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- CN112938903A CN112938903A CN202110248333.6A CN202110248333A CN112938903A CN 112938903 A CN112938903 A CN 112938903A CN 202110248333 A CN202110248333 A CN 202110248333A CN 112938903 A CN112938903 A CN 112938903A
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 192
- 239000001301 oxygen Substances 0.000 title claims abstract description 192
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 192
- 238000000034 method Methods 0.000 title claims abstract description 28
- 239000012528 membrane Substances 0.000 claims abstract description 107
- 239000010457 zeolite Substances 0.000 claims abstract description 91
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 85
- 238000001179 sorption measurement Methods 0.000 claims abstract description 85
- 239000007789 gas Substances 0.000 claims abstract description 84
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 83
- 238000001035 drying Methods 0.000 claims abstract description 21
- 238000000746 purification Methods 0.000 claims abstract description 16
- 230000001105 regulatory effect Effects 0.000 claims abstract description 16
- 230000001276 controlling effect Effects 0.000 claims abstract description 4
- 238000000926 separation method Methods 0.000 claims description 47
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 26
- 239000000463 material Substances 0.000 claims description 18
- 239000012535 impurity Substances 0.000 claims description 16
- 239000002912 waste gas Substances 0.000 claims description 15
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 13
- 239000001569 carbon dioxide Substances 0.000 claims description 13
- 239000000047 product Substances 0.000 claims description 13
- 239000002808 molecular sieve Substances 0.000 claims description 12
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 12
- 239000002994 raw material Substances 0.000 claims description 11
- 239000003463 adsorbent Substances 0.000 claims description 10
- -1 aluminosilicates Chemical compound 0.000 claims description 9
- 206010002091 Anaesthesia Diseases 0.000 claims description 8
- 230000037005 anaesthesia Effects 0.000 claims description 8
- 229930195733 hydrocarbon Natural products 0.000 claims description 8
- 150000002430 hydrocarbons Chemical class 0.000 claims description 8
- 239000012466 permeate Substances 0.000 claims description 8
- 230000003584 silencer Effects 0.000 claims description 7
- 238000004140 cleaning Methods 0.000 claims description 6
- 230000029058 respiratory gaseous exchange Effects 0.000 claims description 6
- 239000011148 porous material Substances 0.000 claims description 5
- 239000012465 retentate Substances 0.000 claims description 5
- 229920006395 saturated elastomer Polymers 0.000 claims description 5
- 229910000323 aluminium silicate Inorganic materials 0.000 claims description 4
- 238000004132 cross linking Methods 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 229910052751 metal Inorganic materials 0.000 claims description 4
- 239000002184 metal Substances 0.000 claims description 4
- 230000008929 regeneration Effects 0.000 claims description 4
- 238000011069 regeneration method Methods 0.000 claims description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 3
- 229910019142 PO4 Inorganic materials 0.000 claims description 2
- 238000004458 analytical method Methods 0.000 claims description 2
- 230000005540 biological transmission Effects 0.000 claims description 2
- 239000000919 ceramic Substances 0.000 claims description 2
- 229910052733 gallium Inorganic materials 0.000 claims description 2
- 150000002739 metals Chemical group 0.000 claims description 2
- 235000021317 phosphate Nutrition 0.000 claims description 2
- 239000000758 substrate Substances 0.000 claims description 2
- 230000000712 assembly Effects 0.000 claims 1
- 238000000429 assembly Methods 0.000 claims 1
- 238000012423 maintenance Methods 0.000 abstract description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 28
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 22
- 229910052757 nitrogen Inorganic materials 0.000 description 14
- 230000008569 process Effects 0.000 description 13
- 229910052786 argon Inorganic materials 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 10
- 238000010586 diagram Methods 0.000 description 7
- 239000004215 Carbon black (E152) Substances 0.000 description 6
- 238000010168 coupling process Methods 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 230000008878 coupling Effects 0.000 description 5
- 238000005859 coupling reaction Methods 0.000 description 5
- 238000001514 detection method Methods 0.000 description 5
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 238000007906 compression Methods 0.000 description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 230000000737 periodic effect Effects 0.000 description 2
- 230000010287 polarization Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 206010017740 Gas poisoning Diseases 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- UNYSKUBLZGJSLV-UHFFFAOYSA-L calcium;1,3,5,2,4,6$l^{2}-trioxadisilaluminane 2,4-dioxide;dihydroxide;hexahydrate Chemical compound O.O.O.O.O.O.[OH-].[OH-].[Ca+2].O=[Si]1O[Al]O[Si](=O)O1.O=[Si]1O[Al]O[Si](=O)O1 UNYSKUBLZGJSLV-UHFFFAOYSA-L 0.000 description 1
- 229910052676 chabazite Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000003749 cleanliness Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 208000037265 diseases, disorders, signs and symptoms Diseases 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
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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
-
- 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
- C01B2210/0043—Impurity removed
- C01B2210/0046—Nitrogen
-
- 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
- C01B2210/0043—Impurity removed
- C01B2210/0051—Carbon dioxide
-
- 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
- C01B2210/0043—Impurity removed
- C01B2210/0062—Water
-
- 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
- C01B2210/0043—Impurity removed
- C01B2210/0078—Noble gases
- C01B2210/0082—Argon
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Separation Of Gases By Adsorption (AREA)
- Oxygen, Ozone, And Oxides In General (AREA)
Abstract
The invention belongs to the technical field of medical gas engineering, and particularly relates to an oxygen generation and supply device and method for an operating room and an ICU. The oxygen-generating and gas-supplying device comprises: at least two sets of separators connected in series; the former stage is a pressure swing adsorption drying purification separator, and the latter stage is a zeolite membrane separator; at least one oxygen buffer tank for receiving the oxygen output from the zeolite membrane separator, the outlet end of the oxygen buffer tank is provided with a flow control valve and an automatic regulating valve for controlling the output rich oxygen; the control assembly and related control valves and connecting pipelines; and a port for receiving compressed air provided by the hospital, a medical oxygen source port, and a port for outputting oxygen to an external respirator. The invention can prepare medical oxygen with the purity being equal to or larger than 99.5 percent; the device has no power equipment, and the oxygen source at the front end is directly introduced to serve as emergency oxygen supply, so that the fault safety strategy is complete in guidance and extremely high in reliability; the device is simple to operate and can be used when being opened; and the maintenance is convenient.
Description
Technical Field
The invention belongs to the technical field of medical gas engineering, and particularly relates to an oxygen generation and supply device and method for an operating room and an ICU.
Background
The clinical medical treatment needs medical oxygen, and the purity of the medical oxygen is not less than 99.5 percent according to the mandatory provision of the national standard GB8982-2009 oxygen for medical and aviation breathing. In addition, "oxygen" (medical oxygen) is also specified in the chinese pharmacopoeia (2015 edition), and the oxygen purity should be ≧ 99.5%; meanwhile, the impurity requirements are specified in detail, and in clinical application, oxygen is managed according to medicines, and not all oxygen can be used for clinical treatment in ICU, operating rooms and the like.
Industrial oxygen, which can reach 99.5% purity, cannot be used for clinical treatment because "purity is satisfied, but what is 0.5% except 99.5%", obviously, if 0.5% is harmful, the cure rate will be reduced.
In addition, the national manufacturing chain is drawn in a standard way, the national standard and pharmacopoeia both standardize the purity of oxygen, the standard of the air mixing and distribution of the breathing machine and the anesthesia machine is 99.5%, and if the purity does not reach the standard, the misoperation and the alarm of medical instruments for clinical treatment of the breathing machine, the anesthesia machine and the like are obviously caused, so that disorder and serious treatment of patients are caused, and the treatment of the patients is possibly delayed.
In addition, some patients must be treated with medical oxygen with the purity reaching the standard, typically, the patients are subjected to gas poisoning and the like, and the patients also contain oxygen for critical operations, anesthesia and the like, and the patients are treated with legal medical oxygen for standard operation in the hospital.
At present, most hospitals in China still adopt legal medical oxygen to be purchased to meet the clinical treatment requirements, typically, medical liquid oxygen and bottle oxygen are purchased and transported to the hospitals for use, but the transportation is inconvenient and the supply is interrupted. Liquid oxygen and high-pressure bottle oxygen have great potential safety hazards in the links of transportation, storage, operation and use and the like due to the characteristics and pressure of media.
In addition, some hospitals with smaller scale adopt medical molecular sieve oxygen generation to generate oxygen on site because of inconvenient supply of liquid oxygen and bottle oxygen, the oxygen is generated on site, the oxygen is used immediately after being opened, the safety is good, the cost is low, but the oxygen purity of about 93 percent can be only prepared, which is also called as oxygen-enriched air or 93 oxygen, the oxygen requirement of general recovery treatment can be met, the problems of safety and the like are solved to a certain extent, the contradiction of oxygen supply is relieved, but the purity does not meet the requirements of national standard and pharmacopoeia, and the qualified medical oxygen can not be provided for operating rooms and ICUs, so that the hospitals are limited to a certain extent.
Therefore, an effective solution is urgently needed in the aspect of providing medical oxygen with qualified purity for operating rooms and ICUs for clinical treatment in a plurality of hospitals.
Disclosure of Invention
In view of the above circumstances, an object of the present invention is to provide an oxygen generating and supplying apparatus and method for operating rooms and ICUs, which is simple in structure, small in size, low in noise, and high in reliability.
The device and the method for producing and supplying oxygen for operating rooms and ICUs provided by the invention are combined with a compressed air source of a hospital (such as an air source for surgical instruments, a compressed air source matched with medical molecular sieve oxygen producing equipment and the like), couple a pressure swing adsorption purification technology with a zeolite membrane separation technology, and directly extract medical oxygen with the purity of not less than 99.5% from compressed air, thereby effectively solving the current oxygen supply problem of the hospital.
The oxygen generation and supply device for operating rooms and ICUs, provided by the invention, has the structure shown in figures 1, 2 and 3, and comprises:
(1) at least one compressed air inlet B for receiving compressed air provided by the hospital at a certain pressure from point B; the device also comprises an air pretreatment device (not shown in the drawing) for pretreating the raw air, wherein impurities, moisture and the like in the air are removed, and a necessary compressed air conveying soft pipeline is also included;
(2) at least one original medical oxygen source access port A of the hospital for receiving the oxygen provided by the hospital from the point A and a necessary delivery hose for delivering the original medical oxygen of the hospital to an oxygen output port C through a pipeline to form a pipeline A-C;
(3) at least one oxygen output port C for cross-linking the oxygen generated by the device with the pipeline A-C through a pipeline and then sending the oxygen to the oxygen output port C, wherein the cross-linking point is Y; the oxygen output port C is connected to terminal gas equipment, such as a breathing machine and an anesthesia machine, and further comprises a gas supply hose required for oxygen transmission from the device to the terminal gas equipment;
(4) at least one set of medical membrane separation oxygen generating equipment and air supply loop B-Y, after receiving the compressed air with certain pressure provided by the hospital from the point B, the generated oxygen is converged into the point Y, as shown in figure 1, it includes:
1) at least two or more series of separators (e.g., 101A, M01A connected in series and 101B, M01B connected in series) connected in series, wherein the front stage (e.g., 101A, 101B) is a pressure swing adsorption dry purification separator as known in the art, and contains one or more combinations of molecular sieves capable of adsorbing moisture, carbon dioxide, total hydrocarbons, etc., such as activated alumina, 13X, etc.; the later stage (such as M01A, M01B) is a zeolite membrane separator, the interior of which is provided with a zeolite membrane separation material, and the zeolite membrane separator is provided with three interfaces: a raw material gas side inlet, a retentate gas side interface and a permeate gas side interface; removing nitrogen and argon from the detention side and generating oxygen from the permeation side; in addition, the serial connection means that the product end of the pressure swing adsorption drying purification separator is communicated with the raw material gas end of the zeolite membrane separator; the air is treated by a pressure swing adsorption drying purification separator to remove moisture, carbon dioxide, total hydrocarbon and the like, so that a subsequent zeolite membrane separator can be protected from being polluted by the moisture and the carbon dioxide contained in the compressed air;
2) the gas inlet end (raw material gas end) of at least two groups of pressure swing adsorption drying purification separators (such as 101A and 101B) which are sequentially connected in series is provided with an automatic switching valve and a necessary pipeline which can respectively introduce compressed air, and a switching valve and a necessary pipeline which can respectively discharge gas reserved in the separators to the atmosphere; preferably, a silencer and a necessary connecting pipeline are arranged after the switching valve and before the switching valve is discharged to the atmosphere, so that noise is reduced;
3) the gas retention side of at least two groups and more than two groups of zeolite membrane separators (such as M01A and M01B) which are sequentially connected in series is also provided with necessary pipelines and regulating valves (such as JV 01) which can communicate the two groups and are used for limiting the flow;
4) at least two groups and more than two groups of zeolite membrane separators (such as M01A and M01B) which are connected in series in sequence are provided with necessary pipelines which can respectively send oxygen generated by the zeolite membrane separators to an oxygen buffer tank (such as PV 101), and a check valve (a one-way valve) is arranged at a permeate gas outlet of each zeolite membrane separator (such as M01A and M01B) to prevent the sent oxygen from flowing backwards;
5) at least one oxygen buffer tank (such as PV 101), the inlet end of the buffer tank is used for receiving the oxygen discharged from the permeation side of the zeolite membrane separator, and the outlet end of the buffer tank is provided with a flow control valve (such as JV 02) and an automatic regulating valve, the automatic regulating valve can automatically control the output rich oxygen, and the flow output range of the automatic regulating valve can be from 0 to 100 percent;
(5) at least one air supply loop formed by connecting B-Y and A-Y in parallel, necessary valves and pipelines, and used for receiving oxygen sources provided by a hospital from the point A and converging the oxygen sources into the point Y, and an automatic switching valve is arranged between the A and the Y to serve as emergency air supply, so that when the air supply loop from the B-Y fails, the original oxygen source used by the hospital can be directly switched to be used as an emergency backup air source, and the emergency backup air source preferably selects medical oxygen meeting the requirements, but does not exclude the use of oxygen-enriched air by the hospital according to the advice;
(6) a set of control components for performing necessary operation control on the valve member on the loop to realize safe gas supply, and also includes, but is not limited to, components including detection and analysis instruments, alarms and the like.
Different from the prior art:
the method directly obtains oxygen with the purity of more than 99.5 percent from the air by coupling the pressure adsorption, drying, purification and separation technology with the zeolite membrane separation process, and can comprehensively meet the requirements of oxygen purity and impurity gas content of medical oxygen technical indexes.
In addition, the coupling separation process can not only protect the later-stage zeolite membrane separator under the condition of low cleanliness of a compressed air source in a hospital and meet the long-term durable use of the zeolite membrane separator, but also ensure the impurity gas content of medical oxygen technical indexes, and because of the coupling separation process, the regenerated gas comes from the waste gas of the zeolite membrane separator, and the overall recovery rate of the system is improved.
Moreover, the zeolite membrane separator adopted by the invention is used for removing nitrogen and argon from compressed air which is obtained by removing moisture, carbon dioxide, total hydrocarbon and the like from a bed layer of the adsorption drying purification separator, and oxygen/nitrogen and oxygen/argon separation is carried out, so that medical oxygen with the purity of more than 99.5 percent can be directly obtained, instead of adopting multi-stage pressure swing adsorption, well-known organic membrane separator or multi-stage organic membrane separation process, high-purity oxygen can be obtained.
The important characteristic of the coupling separation system adopted by the invention is that at least a part of the waste gas generated in the zeolite membrane separation process flows back to the bed layer of the front-stage adsorption drying purification separator to be used as the cleaning gas in the regeneration stage.
In addition, the zeolite membrane separator adopted by the invention is provided with the one-way valve after extracting and producing the oxygen, and the subsequent processes of regenerating, cleaning or repressurizing the product oxygen are not needed.
In addition, the invention adopts the air supply loop which is mutually backed up with the oxygen source such as hospital emergency backup, and the like, and directly switches to the emergency backup air source under the failure conditions of core separation (oxygen generation) process failure, insufficient flow and the like, thereby having extremely high reliability.
The invention has the advantages that:
1. high oxygen purity, compliance with standards: can prepare medical oxygen with the purity being equal to or larger than 99.5 percent;
2. one machine has multiple functions: not only can prepare medical oxygen with the purity of not less than 99.5 percent, but also can prepare oxygen-enriched air with higher yield and the purity of not less than 90 percent;
3. high reliability: the membrane separation technology is adopted to produce oxygen, which is similar to filtration and has no power equipment; in addition, because the oxygen-enriched air at the front end of the hospital is introduced, when equipment fails or the prepared oxygen does not meet the oxygen demand of a terminal, the oxygen source at the front end is directly introduced to serve as emergency oxygen supply, the guidance of a failure safety strategy is complete, and the reliability is extremely high;
4. the operation is simple: one-key starting, namely starting to use;
5. the maintenance is basically free: because the product does not need matching power equipment, and the separator has over 10 years of service life, the system is basically free of maintenance.
Drawings
FIG. 1 is a schematic diagram of the structure and flow of an oxygen and gas generating and supplying device for operating rooms and ICUs.
Fig. 2 is a schematic diagram of the external connection of the medical membrane separation oxygen generator for operating rooms and ICUs.
Fig. 3 is a schematic appearance diagram of a medical membrane separation oxygen generator for operating rooms and ICUs, which adopts the medical membrane separation oxygen generator.
Detailed Description
The invention is further described below with reference to the figures and examples.
Fig. 1 is a flow chart of an oxygen generation and supply device for an operating room and an ICU, and fig. 2 is an external connection schematic diagram of a medical membrane separation oxygen generator for the operating room and the ICU, which adopts the invention.
Some names referred to in this disclosure are explained as follows:
the adsorbent of the adsorption separation process, also called molecular sieve, is used for removing impurity gases such as moisture, carbon dioxide, total hydrocarbon and the like based on a balance adsorption theory by using a pressure swing adsorption, drying and purification molecular sieve such as 13X, activated alumina and the like;
an adsorption column, which may also be referred to as an adsorber, an adsorption bed, a separator, refers to a vessel filled with at least one adsorbent, such as those described above, having a relatively strong adsorption capacity for the more readily adsorbed components of the gas mixture;
the product gas of the adsorption process refers to gas which is difficult to be adsorbed by the adsorbent, for example, for a nitrogen adsorbent, nitrogen is easy to be adsorbed, and oxygen and argon are difficult to be adsorbed;
the waste gas of the adsorption process refers to gas which is easier to be adsorbed by the adsorbent relative to the product gas, such as nitrogen, moisture and the like which are easier to be adsorbed by the nitrogen adsorbent relative to oxygen;
the terms Pressure Swing Adsorption, adsorptive separation, PSA, and the like, as those skilled in the art will understand, refer not only to PSA processes, but also to processes similar thereto, such as Vacuum Swing Adsorption (VSA) or Mixed Pressure Swing Adsorption (MPSA) processes, and the like, in a broader sense, that is, for Adsorption pressures of periodic cycles, a higher Pressure relative to a higher Pressure of the desorption step, may include greater than or equal to atmospheric Pressure, and desorption pressures of periodic cycles, a lower Pressure relative to a lower Pressure of the Adsorption step, may include less than or equal to atmospheric Pressure.
The zeolite membrane separator M01A and the separator B shown in fig. 1 are 3-port zeolite membrane separators, each zeolite membrane separator is composed of 1 raw material gas inlet, 1 retentate gas outlet and 1 permeate gas outlet, the zeolite membrane separator has the function of separating oxygen from nitrogen and argon, the oxygen is easier to permeate, and the nitrogen and argon are harder to pass through.
As is well known, zeolitic materials are generally referred to as aluminosilicate molecular sieves, but zeolites are sometimes also referred to as crystalline molecular sieves, and zeolites are generally referred to herein as molecular sieves, including, for example, aluminosilicates, aluminophosphates, gallium phosphates and variants of these materials substituted with metals, and are generally considered to be molecular sieve materials, but in practice, by controlling their composition and manufacture, the structure may be made to contain a plurality of pore sites or cavities of a particular size such that atoms or molecules having a desired maximum size are effectively filtered and/or adsorbed, and the zeolitic materials may be made to have desired electrical polarization characteristics, polar molecules or atoms or molecules susceptible to polarization being selectively attracted to the zeolitic material, thereby combining size selectivity (which is possessed by the pores and channels of the zeolitic material being of similar size to the molecules) with control of the electrical characteristics of the zeolitic material, the control of the type of gas adsorbed and adsorbed on the zeolite membrane and, therefore, the zeolite material can be used as a membrane separation material having selectivity for a specific component, such that the crystal structure of the material allows the atoms or molecules of the gas desired to be separated to be adsorbed therein and to diffuse through the material, typically, such as a membrane made of a readily polarizable zeolite material, such as chabazite, since one of the components to be separated in the gas mixture is adsorbed to the polarized zeolite material, thus increasing the rate at which the opposite component is initially adsorbed on the zeolite membrane material, and once the component to be separated is adsorbed in the membrane, the pore channel size of the zeolite material is such that only oxygen molecules, for example, pass therethrough but nitrogen and argon, for example, do not diffuse therethrough, so that the rate at which oxygen is adsorbed on the membrane is greater than the rate at which the other gases in the gas mixture, such as nitrogen and argon, for example, pass therethrough, Argon) can significantly improve the separation efficiency.
For zeolite membrane separators, the zeolite membrane may comprise a porous substrate such as sintered metal or ceramic and a layer of zeolite membrane formed thereon, the important feature being that the zeolite membrane is substantially defect free, having no "pinholes" or small cavities throughout the entire thickness of the membrane similar or larger in size to the pores of the zeolite material itself, as described in international patent WO 94/01209.
For a feed gas of a mixture of oxygen, nitrogen and argon, the retentate gas of the zeolite membrane separator is rich in nitrogen and argon, also known as waste gas, while the permeate gas of the zeolite membrane separator is rich in oxygen, also known as product gas.
In the present invention, reference to pressure is to gauge pressure unless explicitly noted.
In the attached drawings of the invention, automatic control valves such as 01A and 02A, emergency air supply valves, automatic regulating valves and the like are all automatic control valves which can be opened or closed according to preset logic, and of course, the automatic control valves can also have flow control regulating performance, and the valves can be pneumatically controlled or electric and hydraulic controlled automatic valves;
DXV01A, DXV01B, etc. represent check valves, which may be any valve capable of restricting the unidirectional flow of fluid;
JV01, JV02, etc. represent manual regulating valves, which can be all valves that can limit the fluid flow;
101A, 101B are adsorption towers, filled with adsorbent;
the silencer is a device for reducing the fluid discharge noise, and can be any silencer capable of reducing the fluid discharge noise; PV101, etc. represents a surge tank;
M01A, M01B represent zeolite membrane separators;
point B, which is a hospital compressed air access point, for receiving compressed air provided by a hospital under a certain pressure, preferably including a device (not shown in the drawing) required for air pre-treatment, typically providing compressed air of ≧ 0.6MPa, and necessary compressed air delivery hoses, which can be accessed from hospital equipment belt and tower crane interfaces;
the point A is an original medical oxygen source access point of a hospital and is used for receiving oxygen provided by the hospital from the point A, typically, an oxygen source with the pressure of not less than 0.4MPa is provided, so that the use requirements of a subsequent breathing machine and an anesthesia machine can be met, and necessary conveying hoses can be connected with interfaces of equipment belts and a hanging tower of the hospital;
point C is an oxygen output port C of the apparatus of the present invention, and is configured to connect oxygen generated by the apparatus of the present invention to a terminal gas appliance, such as a ventilator or an anesthesia machine, typically, a pressure of ≧ 0.4MPa needs to be satisfied, and further includes an air supply hose required for oxygen delivery from the apparatus of the present invention to the terminal gas appliance;
y point, the parallel air supply gathering point of the original oxygen source of the hospital and the oxygen prepared by the oxygen preparation system constructed by the invention is conveyed to an oxygen output port C by a pipeline after gathering is finished, the oxygen is sent to an outlet C by a pipeline and is accessed to terminal air equipment, such as a respirator and an anesthesia machine, an air supply loop formed by connecting B-Y and A-Y in parallel, necessary valves and pipelines are used for receiving the oxygen source provided by the hospital from the point A and are gathered to the point Y, an automatic switching valve is arranged between the points A and Y and is used as emergency air supply (the automatic switching valve can also be selected as a manual valve), the requirement that when the air supply loop from the point B-Y fails, the original oxygen source used by the hospital can be directly switched to be used as an emergency backup air source, the emergency backup air source preferably meets the requirement of medical oxygen, but does not exclude the use of air by the hospital according to medical advice, and the air supply hose and reduced pressure air supply equipment ( Out).
The invention provides an oxygen-making and air-supplying device for operating rooms and ICUs, which has a typical core structure, namely a B-Y loop, and comprises the following components:
the method comprises the following steps: two adsorption towers, namely 101A and 101B, two zeolite membrane separators, namely M01A and M01B, and a buffer tank, namely PV101, wherein the adsorption tower 101A is connected with the zeolite membrane separator M01A in series, and the adsorption tower 101B is connected with the zeolite membrane separator M01B in series; automatic control valves 01A and 01B are respectively arranged between the node B of the medical compressed air pipeline of the hospital and the air inlets of the adsorption tower 101A and the adsorption tower 101B; bypasses are arranged on the air inlet pipelines of the adsorption tower 101A and the adsorption tower 101B behind the automatic control valves 01A and 01B and connected to the silencer, and automatic control valves 02A and 02B are correspondingly arranged on the two bypasses; the product gas outlets of the adsorption tower 101A and the adsorption tower 101B are respectively connected with the raw material gas side interfaces of the zeolite membrane separators M01A and M01B to form two parallel drying and separating systems; the permeation gas side interfaces of the two zeolite membrane separators M01A and M01B are connected through a pipeline, and a regulating valve JV01 is arranged on the connecting pipeline; check valves DXV01A and DXV01B are correspondingly arranged on the stagnant gas side interfaces of the two zeolite membrane separators M01A and M01B, and outlet pipelines of the two check valves DXV01A and DXV01B are connected and then connected with a buffer tank PV 101; surge tank PV101 is connected to junction point Y via a pipe, on which a regulator valve JV02 and an automatic regulator valve are provided in this order.
Inputting compressed air with the pressure of 0.45-1.0 MPa from a point B, wherein the compressed air is a relatively clean raw material gas subjected to pretreatment; the air is compressed by a compressor to the separation pressure required by the subsequent separation (the pressure difference of the subsequent separation system is designed according to 0.05-0.1 MPa, and the pressure of the terminal air supply is designed according to ≧ 0.4MPa meeting the standard requirement), at least 0.45-0.5 MPa needs to be met, but compression to higher pressure is not excluded, such as: 0.45-2.0 MPa; the water, solid particle impurities and oil content in the compressed air are removed by a pretreatment system consisting of an active carbon oil remover or a filter, a freeze dryer or an adsorption dryer and the like which are singly or in various combinations through a filter, and then the compressed air enters an air buffer tank, as known technology, the water, solid particle impurities and oil content are very necessary for a gas separation system, wherein the filter can be in a multi-stage and combined type, the adsorption dryer and the freeze dryer can be combined or independently adopted, preferably, a method for recovering compressed air compression heat energy to regenerate the water of a selected adsorption dryer is adopted, preferably, the adsorption dryer selects an adsorbent capable of selectively removing the carbon dioxide in the air to remove the carbon dioxide, wherein the precision of filtration and the air handling capacity of the filter, the outlet dew point of the freeze dryer or the dew point in the air after being treated by the adsorption dryer and the treatment requirement of trace carbon dioxide in order to meet the use requirement of a subsequent separation system and the use requirement of the gas The carbon dioxide or oil content required by the component outlets is taken as a reference, and a buffer tank is not necessary and can be realized by adopting a variable-frequency compression process of the known technology or by bypass emptying, so that the aim is to avoid frequent starting of the compressor and possible process overpressure, and according to the common design requirements, the components and the design requirements contained in the pretreatment system can be flexibly mastered by the technical personnel in the field.
As mentioned above, the raw air after being processed is different from hospitals in matching conditions, in order to avoid uncertainty of gas source impurities processed by a pre-stage pretreatment system, and to ensure medical oxygen gas indexes, especially impurity gases such as moisture, carbon dioxide, total hydrocarbon content and the like, the invention is provided with a drying and purifying system based on adsorption separation as the known technology, after the raw air enters a pressure swing adsorption separation system as the known technology described in the attached figure 1, components such as moisture, carbon dioxide, total hydrocarbon and the like are removed from a silencer, and medical oxygen with purity not less than 99.5% and meeting medical oxygen national standard and requirements of Chinese pharmacopoeia is output from a gas production loop composed of DXV01A, V3B, D03 and pipelines thereof; the two groups of separation systems which are switched to operate and composed of 101A/101B are typical double-tower adsorption systems, when an air inlet valve 01A is opened, 101A adsorbs and removes impurity content, 02B is opened, namely regeneration is carried out, regeneration gas comes from waste gas of another group of zeolite membrane separators M01B which are connected in series in sequence, when the 101A is saturated in adsorption, the other group 101B is started to be switched to carry out adsorption, then, 101A starts to exhaust the atmosphere, moisture, carbon dioxide, total hydrocarbon and waste gas such as nitrogen, a small amount of oxygen and the like contained in the waste gas from the zeolite membrane separators are removed from silencers, and simultaneously, 101B opens the air inlet valve 01B to enter air, and the adsorption and separation process based on the equilibrium adsorption mechanism is carried out by adopting the two-tower device in a sequence with different phases of 101A and 101B.
Therefore, a coupled separation process is formed by following a preceding-stage pressure swing adsorption drying purification cycle of the prior art, the system is simple, the number of valves is small, and particularly, adsorption drying is integrated, so that the uncertainty of the purification quality of front-end compressed air is greatly reduced, a zeolite membrane separator is protected, the content and the purity of medical oxygen impurity gas are ensured, and the reliability is improved, wherein typically, the operation steps of the coupled separation system shown in the attached figure 1 are as follows:
(1) opening the automatic control valve 01A, operating the adsorption tower 101A and the zeolite membrane separator M01A, adsorbing and purifying impurity gas by the adsorption tower 101A, generating oxygen by the zeolite membrane separator M01A, and discharging waste gas to the adsorption tower 101B by the regulating valve JV 01; meanwhile, an automatic control valve 02B is opened, an adsorption tower (a drying and purifying adsorption bed layer) 101B is emptied, and regenerated gas comes from waste gas of a zeolite membrane separator M01A; at the same time, check valve DXV01A (mechanical valve) is opened; when the adsorption of the dried and purified 101A is saturated, the next step is carried out;
(2) opening an automatic control valve 02A, emptying an adsorption tower (a drying and purifying adsorption bed layer) 101A, and discharging regenerated gas from waste gas of a zeolite membrane separator M01B; meanwhile, the automatic control valve 01B is opened, the adsorption tower 101B and the zeolite membrane separator M01B work, the adsorption tower 101B adsorbs and purifies impurity gas, oxygen is generated through the zeolite membrane separator M01B, and waste gas is discharged to the adsorption tower 101A through the regulating valve JV 01; at the same time, check valve DXV01B (mechanical valve) is opened; when the adsorption of the adsorption tower (dry purge) 101B is saturated, the cycle proceeds to the previous step.
In the above steps, all the valves except the appointed opening valve are in a closing state;
the flow of quantitative cleaning can be controlled by adjusting the adjusting valve JV01 to set the flow opening, and the flow of oxygen can be controlled by adjusting the adjusting valve JV 02;
the flow rate of quantitative cleaning is controlled by adjusting the shutoff valve; adjusting the flow opening by the adjusting valve JV01, and adjusting the oxygen yield by controlling the JV02 and the automatic adjusting valve;
the circulation can generate more than 99.5% of oxygen, and of course, the oxygen yield can be improved, but the oxygen concentration is reduced, and typically, 93% of oxygen-enriched air can be output.
In addition, the product gas buffer tank PV101, which may be used as described in the prior art, may have the necessary packing added to the tank to achieve a more economical buffer volume.
The purpose of coupling the zeolite membrane separator in the adsorption drying system can also be to ensure that the systems in which a plurality of zeolite membrane separators operate are not communicated with each other, and can be in parallel and in multiple groups, namely, the gas transfer between the zeolite membrane separators is not generated when the zeolite membrane separators operate according to the steps.
The system can be designed to operate completely according to the required pressure and purity by arranging the necessary gas detection equipment at the outlet end of the zeolite membrane separator and installing the necessary pressure detection, dew point detection and purity detection on the zeolite membrane separator and the buffer tank, the required intelligent control program supports that although the system looks complicated, the realization is not difficult, and an experienced technician may find that the debugging process of the equipment is almost the process of self-adapting to the stability of the system, and in the judgment of faults, the control program gives more sufficient information to maintenance personnel and even directly specifies the fault point.
Various changes may be made in the methods and apparatus described above and illustrated in the drawings without departing from the scope of the invention. Thus, while it is preferred to use 1 or more zeolite membrane separators of any desired configuration, i.e., either fixed volume or fixed pressure, coupled to a preceding adsorption drying system and subsequent 1 or more stages and forming a complete coupled separation process system with product gas surge tanks and necessary power plants, the process may also utilize more than two zeolite membrane separators and multiple storage tanks, multiple power plants. Further, the gas flow pattern through the zeolite membrane separator of the present invention may be in the form of axial flow, radial flow, lateral flow, or other patterns. With respect to the individual zeolite membrane separators, each may include a plurality of primary membrane separation layers, or may be devoid of or provided with one or more pretreatment layers for removing other components such as water vapor. In addition, each membrane separation layer may comprise a single species of membrane separation material or a mixture of two or more membrane separation materials.
Example 1
Fig. 2 is an external connection schematic diagram of a medical membrane separation oxygen generator for operating rooms and ICUs according to the present invention, wherein the oxygen generator comprises an oxygen generation device of fig. 1, which is used for an oxygen generation and supply method for operating rooms and ICUs and the device flow schematic diagram of the adsorption separation, drying, purification and zeolite membrane separator coupling process, the system is connected with 0.6MPa compressed air from a compressed air inlet B (a compressed air interface of a hospital operating room tower) of fig. 1, and connected with an emergency standby oxygen source from a medical oxygen source inlet a (an oxygen supply interface of the hospital operating room tower) of fig. 1, and medical oxygen with purity not less than 0.5MPa and purity not less than 99.5% which meet the requirements of national standard and chinese pharmacopoeia can be output from an oxygen output port C of fig. 2.
The device constructed by the invention is an appearance schematic diagram of a medical membrane separation oxygen generator for operating rooms and ICUs, which is based on a membrane separation technology, and the medical membrane separation oxygen generator is used for generating oxygen based on the membrane separation technology, wherein the oxygen generation process is a pure physical process, does not have phase change, only consumes electric power and compressed air, and can directly extract medical oxygen meeting medical requirements from the compressed air (the oxygen purity is not less than 99.5 percent).
As shown in fig. 2 and 3, a standard interface is configured to receive compressed air and an oxygen source of a hospital, wherein the compressed air is used as a raw material gas to be purified into medical oxygen with purity of 99.5% or more, and the received oxygen source can be used as emergency backup oxygen when the system fails, the product shown in fig. 3 can provide legal medical oxygen for clinical operating rooms and ICU treatment, extract medical oxygen (3L/min) with purity of 99.5% or more from the compressed air, and can also reduce purity output of oxygen-enriched air (10L/min), and when the oxygen generation system of the product fails or the generated medical oxygen flow is not enough to meet the requirement of an oxygen terminal, the oxygen source from the receiving end can be directly sent to the terminal for output, and the main technical performance parameters are listed as follows:
Claims (7)
1. an oxygen and gas supply device for operating room and ICU, which is characterized in that the device comprises:
(1) at least one compressed air inlet B for receiving compressed air provided by the hospital at a certain pressure from point B; the system also comprises an air pretreatment device, a compressed air conveying soft pipeline and a control device, wherein the air pretreatment device is used for pretreating raw material air, and comprises a step of removing impurities, moisture and the like in the air;
(2) at least one original medical oxygen source access port A of the hospital for receiving the oxygen provided by the hospital from the point A and a necessary delivery hose for delivering the original medical oxygen of the hospital to an oxygen output port C through a pipeline to form a pipeline A-C;
(3) at least one oxygen output port C for cross-linking the generated oxygen with the pipeline A-C through a pipeline and then sending the oxygen to the oxygen output port C, and recording the cross-linking point as Y; the oxygen output port C is connected to terminal gas equipment, comprises a breathing machine and an anesthesia machine, and further comprises a gas supply hose required for oxygen transmission from the device to the terminal gas equipment;
(4) at least one set of medical membrane separation oxygenerator and air feed return circuit B-Y, receive the compressed air of certain pressure that the hospital provided from point B after, produce oxygen and converge Y point, this return circuit includes:
1) at least two sets of separators connected in series in sequence, wherein the front stage is a pressure swing adsorption drying purification separator, and a molecular sieve adsorbent is filled in the front stage; the latter stage is a zeolite membrane separator, in which the zeolite membrane separation material is mounted, and the zeolite membrane separator has three interfaces: a raw material gas side inlet, a retentate gas side interface and a permeate gas side interface; the sequential series connection means that the product end of the pressure swing adsorption drying purification separator is communicated with a raw material gas side interface of the zeolite membrane separator;
2) the air inlet ends of at least two groups of pressure swing adsorption drying purification separators which are sequentially connected in series are provided with an automatic switching valve and a necessary pipeline which can respectively introduce compressed air, and a switching valve and a necessary pipeline which can respectively discharge gas reserved in the separators to the atmosphere; a silencer and necessary connecting pipelines are arranged after the switching valve and before the switching valve is discharged to the atmosphere, so that noise is reduced;
3) the retentate sides of at least two groups and more than two groups of zeolite membrane separators which are sequentially connected in series are also provided with necessary pipelines and regulating valves which can communicate the two groups and are used for limiting the flow;
4) the permeate gas side of at least two groups and more than two groups of zeolite membrane separators which are connected in series in sequence is provided with a necessary pipeline which can respectively send oxygen generated by the zeolite membrane separators to an oxygen buffer tank, and the permeate gas outlet of each zeolite membrane separator is provided with a check valve to prevent the sent oxygen from flowing backwards;
5) the inlet end of the buffer tank is used for receiving oxygen discharged from the permeation side of the zeolite membrane separator, and the outlet end of the buffer tank is provided with a flow control valve and an automatic regulating valve which can automatically control the output rich oxygen;
(5) at least one air supply loop formed by connecting B-Y and A-Y in parallel, necessary valves and pipelines, and used for receiving oxygen sources provided by a hospital from the point A and converging the oxygen sources into the point Y, and an automatic switching valve is arranged between the A and the Y to serve as emergency air supply, so that when the air supply loop from the B-Y fails, the original oxygen source used by the hospital can be directly switched to be used as an emergency backup air source, and the emergency backup air source preferably selects medical oxygen meeting the requirements, but does not exclude the use of oxygen-enriched air by the hospital according to the advice;
(6) the control assembly is used for carrying out necessary operation control on the valve on the loop so as to realize safe gas supply, and also comprises an analysis detecting instrument, an alarm and other assemblies.
2. Oxygen supply apparatus for operating theatres, ICUs, of claim 1 wherein the typical structure of the B-Y loop comprises:
two adsorption towers, namely 101A and 101B, two zeolite membrane separators, namely M01A and M01B, a buffer tank, namely PV101, and related control valves and connecting pipelines; wherein:
the adsorption tower 101A is connected with a zeolite membrane separator M01A in series, and the adsorption tower 101B is connected with a zeolite membrane separator M01B in series; automatic control valves 01A and 01B are respectively arranged between the node B of the medical compressed air pipeline of the hospital and the air inlets of the adsorption tower 101A and the adsorption tower 101B;
bypasses are arranged on the air inlet pipelines of the adsorption tower 101A and the adsorption tower 101B behind the automatic control valves 01A and 01B and connected to the silencer, and automatic control valves 02A and 02B are correspondingly arranged on the two bypasses;
the product gas outlets of the adsorption tower 101A and the adsorption tower 101B are respectively connected with the raw material gas side interfaces of the zeolite membrane separators M01A and M01B to form two parallel drying and separating systems;
the permeation gas side interfaces of the two zeolite membrane separators M01A and M01B are connected through a pipeline, and a regulating valve JV01 is arranged on the connecting pipeline;
check valves DXV01A and DXV01B are correspondingly arranged on the stagnant gas side interfaces of the two zeolite membrane separators M01A and M01B, and outlet pipelines of the two check valves DXV01A and DXV01B are connected and then connected with a buffer tank PV 101;
surge tank PV101 is connected to junction point Y via a pipe, on which a regulator valve JV02 and an automatic regulator valve are provided in this order.
3. The oxygen generation and supply method for the operating room and the ICU based on the device of claim 2 is characterized by comprising the following steps:
(1) opening the automatic control valve 01A, operating the adsorption tower 101A and the zeolite membrane separator M01A, adsorbing and purifying impurity gas by the adsorption tower 101A, generating oxygen by the zeolite membrane separator M01A, and discharging waste gas to the adsorption tower 101B by the regulating valve JV 01; meanwhile, the automatic control valve 02B is opened, the adsorption tower 101B is emptied, and the regeneration gas comes from the waste gas of the zeolite membrane separator M01A; at the same time, check valve DXV01A is open; when the adsorption of the dried and purified 101A is saturated, the next step is carried out;
(2) opening an automatic control valve 02A, emptying the adsorption tower 101A, and discharging regenerated gas from waste gas of the zeolite membrane separator M01B; meanwhile, the automatic control valve 01B is opened, the adsorption tower 101B and the zeolite membrane separator M01B work, the adsorption tower 101B adsorbs and purifies impurity gas, oxygen is generated through the zeolite membrane separator M01B, and waste gas is discharged to the adsorption tower 101A through the regulating valve JV 01; at the same time, check valve DXV01B is open; when the adsorption tower 101B is saturated, the cycle is shifted to the previous step;
in the above steps, all the valves except the appointed opening valve are in a closing state;
the flow of quantitative cleaning can be controlled by adjusting the adjusting valve JV01 to set the flow opening, and the flow of oxygen can be controlled by adjusting the adjusting valve JV 02;
the flow of quantitative cleaning is controlled by adjusting the shutoff valve; adjusting the flow opening by the adjusting valve JV01, and adjusting the oxygen yield by controlling the JV02 and the automatic adjusting valve;
the circulation is repeated, and more than 99.5 percent of oxygen can be generated.
4. The oxygen generation and air supply method for operating rooms and ICUs according to claim 3, wherein the pressure of the compressed air input from the point B is 0.45-2.0 MPa.
5. The method of oxygen generation and supply for operating theatres, ICUs, of claim 3 wherein the adsorbent is one or more combinations of activated alumina, 13X molecular sieve that adsorbs moisture, carbon dioxide, total hydrocarbons, etc.
6. The method of oxygen generation and gas supply for operating theatres, ICUs, of claim 3 wherein the zeolite membrane separation material is an aluminosilicate molecular sieve including aluminosilicates, aluminophosphates, gallium phosphates and variations of these materials substituted with metals.
7. The oxygen generation and gas supply method for operating rooms and ICUs according to claim 6, characterized in that the zeolite membrane separation material is a porous substrate of sintered metal or ceramic and a layer of zeolite membrane formed thereon, which has no "pinholes" or small cavities throughout the whole thickness of the membrane, similar or larger to the size of the pores of the zeolite material itself.
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| WO2022263965A1 (en) * | 2021-06-16 | 2022-12-22 | Northman Ip Holdco Limited | Respiratory device |
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