CN112938903B - Oxygen generation and gas supply device and method for operating room and ICU - Google Patents
Oxygen generation and gas supply device and method for operating room and ICU Download PDFInfo
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- CN112938903B CN112938903B CN202110248333.6A CN202110248333A CN112938903B CN 112938903 B CN112938903 B CN 112938903B CN 202110248333 A CN202110248333 A CN 202110248333A CN 112938903 B CN112938903 B CN 112938903B
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 184
- 239000001301 oxygen Substances 0.000 title claims abstract description 184
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 184
- 239000007789 gas Substances 0.000 title claims abstract description 74
- 238000000034 method Methods 0.000 title claims abstract description 31
- 239000012528 membrane Substances 0.000 claims abstract description 113
- 239000010457 zeolite Substances 0.000 claims abstract description 102
- 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 95
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 92
- 238000001179 sorption measurement Methods 0.000 claims abstract description 84
- 230000001105 regulatory effect Effects 0.000 claims abstract description 30
- 238000001035 drying Methods 0.000 claims abstract description 23
- 230000001276 controlling effect Effects 0.000 claims abstract description 6
- 238000000926 separation method Methods 0.000 claims description 44
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 28
- 239000003463 adsorbent Substances 0.000 claims description 15
- 239000000047 product Substances 0.000 claims description 15
- 238000000746 purification Methods 0.000 claims description 15
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 14
- 239000001569 carbon dioxide Substances 0.000 claims description 14
- 239000012535 impurity Substances 0.000 claims description 14
- 239000002912 waste gas Substances 0.000 claims description 13
- 239000000463 material Substances 0.000 claims description 12
- 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
- 238000004519 manufacturing process Methods 0.000 claims description 11
- 239000012466 permeate Substances 0.000 claims description 11
- 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
- 239000002994 raw material Substances 0.000 claims description 8
- -1 aluminophosphate Chemical compound 0.000 claims description 7
- 230000029058 respiratory gaseous exchange Effects 0.000 claims description 7
- 238000001514 detection method Methods 0.000 claims description 6
- 229920006395 saturated elastomer Polymers 0.000 claims description 5
- 230000003584 silencer Effects 0.000 claims description 5
- 229910000323 aluminium silicate Inorganic materials 0.000 claims description 4
- 238000004140 cleaning Methods 0.000 claims description 4
- 238000007599 discharging 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
- 230000005540 biological transmission Effects 0.000 claims description 3
- 238000004132 cross linking Methods 0.000 claims description 3
- 230000014759 maintenance of location Effects 0.000 claims description 3
- 239000002184 metal Substances 0.000 claims description 3
- 229910052751 metal Inorganic materials 0.000 claims description 3
- 239000012465 retentate Substances 0.000 claims description 3
- 238000004458 analytical method Methods 0.000 claims description 2
- 229910000154 gallium phosphate Inorganic materials 0.000 claims 1
- LWFNJDOYCSNXDO-UHFFFAOYSA-K gallium;phosphate Chemical compound [Ga+3].[O-]P([O-])([O-])=O LWFNJDOYCSNXDO-UHFFFAOYSA-K 0.000 claims 1
- 238000012423 maintenance Methods 0.000 abstract description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 26
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 18
- 229910052757 nitrogen Inorganic materials 0.000 description 13
- 230000008569 process Effects 0.000 description 10
- 229910052786 argon Inorganic materials 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 6
- 239000004215 Carbon black (E152) Substances 0.000 description 5
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 5
- 238000007906 compression Methods 0.000 description 4
- 238000010168 coupling process Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 238000002203 pretreatment Methods 0.000 description 4
- 230000006835 compression Effects 0.000 description 3
- 230000008878 coupling Effects 0.000 description 3
- 238000005859 coupling reaction Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical class C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 229910001882 dioxygen Inorganic materials 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 206010017740 Gas poisoning Diseases 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000001949 anaesthesia Methods 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000003749 cleanliness Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000013461 design Methods 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
- 239000000945 filler Substances 0.000 description 1
- 229910052733 gallium Inorganic materials 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 150000002739 metals Chemical group 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 235000021317 phosphate Nutrition 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000000241 respiratory effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
Classifications
-
- 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
Landscapes
- 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-making and gas-supplying device and method for operating rooms and ICU. The oxygen-generating and gas-supplying device of the invention comprises: at least two sets of separators connected in series in sequence; the front stage is a pressure swing adsorption drying purifying separator, and the rear stage is a zeolite membrane separator; at least one oxygen buffer tank for receiving oxygen from the zeolite membrane separator, and a flow control valve and an automatic regulating valve for controlling the oxygen enriched in the output; a control assembly and associated control valves and connecting lines; and an interface for receiving compressed air provided by a hospital, a medical oxygen source interface, and an interface for outputting oxygen to an external respirator and the like. The invention can prepare medical oxygen with purity not less than 99.5%; the device is unpowered, a front-end oxygen source is directly introduced to serve as emergency oxygen supply, the fault safety strategy is complete, and the reliability is extremely high; the device is simple to operate and can be used immediately after being opened; 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 operating rooms and ICU.
Background
Medical oxygen is required for clinical medical treatment, and the purity of the medical oxygen is not less than 99.5 percent according to the mandatory provision of national standard GB8982-2009 medical and aviation respiratory oxygen. In addition, "oxygen" (medical oxygen) is also specified in the chinese pharmacopoeia (2015 edition) and should have an oxygen purity of ≡ 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 of ICU, operating room and the like.
Industrial oxygen can reach 99.5% purity, but cannot be used for clinical treatment because: although the purity is satisfied, the remaining 0.5% is harmful substances except 99.5%, and the treatment rate is lowered.
In addition, the national manufacturing chains are all drawn by standards, the national standards and pharmacopoeias standardize the purity of oxygen, the standard of air mixing and air distribution of a breathing machine and an anesthesia machine is 99.5 percent, and if the purity does not reach the standard, the mishandling and alarming of medical instruments for clinical treatment such as the breathing machine, the anesthesia machine and the like are obviously caused, so that the confusion and the serious delay of the treatment of patients are caused.
In addition, some patients must be treated with medical oxygen with the purity reaching the standard, typically, gas poisoning and the like, and oxygen used in critical operations, anesthesia and the like are also included, and the normal operation of a trimethyl hospital is legal medical oxygen.
At present, most hospitals in China still adopt 'medical oxygen' which is legal and compliant to purchase to meet the clinical treatment requirements, typically, medical liquid oxygen and bottle oxygen are purchased and transported to the hospitals for use, but because transportation is not likely to be intermittent. The liquid oxygen and the high-pressure bottle oxygen have great potential safety hazards in the links of transportation, storage, operation and use and the like because of the medium characteristics and the pressure.
In addition, some hospitals with smaller scale can only prepare about 93% of oxygen purity, also called "oxygen-enriched air" or "93 oxygen", because the liquid oxygen and the bottle oxygen are inconvenient to supplement, and the medical molecular sieve is adopted to prepare oxygen on site, and the oxygen is prepared on site, so that the safety is good, the cost is low, the oxygen demand of general restorative treatment can be met, the safety and other problems are solved to a certain extent, the oxygen supply contradiction is relieved, and the purity is not up to national standard and pharmacopoeia requirements, and the medical oxygen can not be provided for operating rooms and ICU and is limited to a certain extent.
Therefore, there is a need for an effective solution in providing "medical oxygen" of standard purity to the operating theatres, ICUs, of clinical care in numerous hospitals.
Disclosure of Invention
In view of the above, the present invention aims to provide an oxygen supply device and method for operating rooms and ICUs, which have a simple structure, a small volume, low noise and high reliability.
The oxygen preparing and supplying device and method for operating rooms and ICU combines a hospital compressed air source (such as providing an air source for surgical instruments, adopting medical molecular sieve oxygen preparing equipment to be matched with the compressed air source, and the like), couples a pressure swing adsorption purification technology with a zeolite membrane separation technology, and directly extracts medical oxygen with purity of 99.5% or more from the compressed air, thereby effectively solving the current oxygen supplying problem of hospitals.
The invention provides an oxygen generating and supplying device for operating rooms and ICU, the structure of which is shown in figures 1,2 and 3, comprising:
(1) At least one compressed air inlet B for receiving a pressure of compressed air supplied from a hospital at point B; the device also comprises an air pretreatment device (not shown in the drawing) for pretreating raw air, wherein the pretreatment device comprises the steps of removing impurities, moisture and the like in the air, and further comprises a necessary compressed air conveying soft pipeline;
(2) At least one original medical oxygen source access port A of the hospital is used for receiving oxygen provided by the hospital from the point A and a necessary conveying hose, and the original medical oxygen of the hospital is conveyed to an oxygen output port C through a pipeline to form a pipeline A-C;
(3) At least one oxygen outlet C for crosslinking the oxygen generated by the device with the pipeline A-C and then sending the oxygen into the oxygen outlet C, and marking the crosslinking point as Y; the oxygen outlet C is connected with 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 an air supply loop B-Y, after receiving compressed air with certain pressure provided by a hospital from the point B, generating oxygen to be converged into the point Y, as shown in figure 1, comprises:
1) At least two or more series-connected separators (for example, 101A, M A series-connected, 101B, M B series-connected), wherein the front stage (for example, 101A, 101B) is a pressure swing adsorption dry purification separator as known in the art, and one or more combinations of molecular sieves capable of adsorbing moisture, carbon dioxide, total hydrocarbons, etc. such as activated alumina, 13X, etc. are contained therein; the later stage (such as M01A, M B) is a zeolite membrane separator, the zeolite membrane separator is internally provided with a zeolite membrane separation material, and the zeolite membrane separator is provided with three interfaces: a feed 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 sequential series connection means that the product end of the pressure swing adsorption drying and purifying 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 the subsequent zeolite membrane separator can be protected from being polluted by the moisture and the carbon dioxide contained in the compressed air;
2) At least two or more pressure swing adsorption dry purification separators (e.g., 101A, 101B) connected in series in sequence are provided with an automatic switching valve and a necessary pipeline for introducing compressed air respectively, and a switching valve and a necessary pipeline for discharging the gas remaining in the separators to the atmosphere respectively; preferably, the device further comprises a muffler and necessary connecting lines after the switching valve and before the switching valve is discharged to the atmosphere, so as to reduce noise;
3) The detention gas side of at least two groups of zeolite membrane separators (such as M01A, M B) which are sequentially connected in series is also provided with a necessary pipeline and a regulating valve (such as JV 01) which can be communicated with each other, and the regulating valve is used for limiting the flow;
4) At least two groups of zeolite membrane separators (such as M01A, M B) connected in series in sequence are provided with necessary pipelines for respectively sending oxygen generated by the zeolite membrane separators to an oxygen buffer tank (such as PV 101) on the permeate gas side, and a check valve (one-way valve) is arranged at the permeate gas outlet of each zeolite membrane separator (such as M01A, M B) so as to prevent the backflow of the sent oxygen;
5) At least one oxygen buffer tank (such as PV 101), the inlet end of the buffer tank is used for receiving oxygen discharged from the permeation side of the zeolite membrane separator, the outlet end 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 oxygen enrichment, and the flow output range can be from 0 to 100%;
(5) At least one air supply loop connected with the A-Y in parallel and necessary valves and pipelines for receiving oxygen source supplied by a hospital from the A point to the Y point, and an automatic switching valve is arranged between the A-Y to serve as emergency air supply, so that when the air supply loop from the B-Y fails, the air supply loop can be directly switched to the original oxygen source used by the hospital as an emergency backup air source, and the emergency backup air source preferably meets the required medical oxygen, but does not exclude the oxygen-enriched air from being used by the hospital according to medical orders;
(6) A set of control components for performing necessary operation control on the valve element in the loop to realize safe air supply, and also comprises but is not limited to components including detection and analysis instruments, alarms and the like.
Unlike the prior art:
the method uses the pressure adsorption drying purification separation technology to couple with the zeolite membrane separation process to directly obtain the oxygen with the purity of more than 99.5 percent from the air, 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 protect the later-stage zeolite membrane separator under the condition of low cleanliness of the compressed air source of a hospital, meet long-term durable use of the later-stage zeolite membrane separator, and ensure the impurity gas content of medical oxygen technical indexes.
The zeolite membrane separator is used for removing nitrogen and argon in compressed air from which moisture, carbon dioxide, total hydrocarbon and the like are removed from the adsorption, drying and purification separator bed, and oxygen/nitrogen and oxygen/argon separation is carried out, so that medical oxygen with the purity of more than 99.5% can be directly obtained, and the high-purity oxygen can be obtained by adopting a multi-stage pressure swing adsorption process, a well-known organic membrane separator or a multi-stage organic membrane separation process.
And, the coupling separation system adopted by the invention is characterized in that at least a part of waste gas in the zeolite membrane separation process is refluxed to the bed layer of the preceding-stage adsorption drying purification separator to be used as the purge gas in the regeneration stage.
In addition, the zeolite membrane separator adopted by the invention is provided with the one-way valve after oxygen is extracted and produced, and the subsequent product oxygen is not required to be regenerated, cleaned or repressurized.
In addition, the invention adopts the air supply loop which is mutually backed up with oxygen sources such as emergency backup of a hospital, and the like, and is directly switched to the emergency backup air source under the failure conditions of faults, insufficient flow and the like in the process of separating (oxygen production) of a core, so that the invention has extremely high reliability, and obviously, the consumption of the emergency backup air source is reduced because the oxygen production is adopted in the field for most of the time, and in general, the emergency backup air source is required to be transported to the hospital for use remotely, and the requirement of logistic guarantee of the hospital is reduced.
The invention has the advantages that:
1. high oxygen purity and compliance standard: medical oxygen with the purity of not less than 99.5 percent can be prepared;
2. One machine is multipurpose: not only can prepare medical oxygen with the purity of not less than 99.5 percent, but also can prepare oxygen-enriched air with the higher yield and the purity of not less than 90 percent;
3. High reliability: oxygen is produced by adopting a membrane separation technology, the shape of the oxygen is the same as that of 'filtration', and no power equipment is used; in addition, because oxygen-enriched air at the front end of a hospital is introduced, when equipment faults or the prepared oxygen is insufficient to meet the oxygen demand of a terminal, 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 direction and extremely high in reliability;
4. The operation is simple: one key is started, and the product is used immediately after being opened;
5. Basically maintenance-free: because the product does not need matched power equipment, and the separator has an extremely long service life of more than 10 years, the system is basically maintenance-free.
Drawings
FIG. 1 is a schematic view of the structure and flow of an oxygen generating and supplying device for operating rooms and ICUs according to the present invention.
Fig. 2 is a schematic view of external connection of a medical membrane separation oxygenerator for operating rooms, ICUs, employing the present invention.
Fig. 3 is a schematic view showing the appearance of a medical membrane separation oxygenerator for an operating room or ICU according to the present invention.
Detailed Description
The invention is further described below with reference to the drawings and examples.
Fig. 1 is a schematic flow diagram of an oxygen generating and supplying device for an operating room and an ICU according to the present invention, and fig. 2 is a schematic external connection diagram of a medical membrane separation oxygen generator for an operating room and an ICU according to the present invention.
Some of the names referred to in this disclosure are defined as follows:
the adsorbent of the adsorption separation process, also called molecular sieve, is used for pressure swing adsorption, drying and purifying molecular sieves such as 13X, activated alumina and the like, and removing impurity gases such as moisture, carbon dioxide, total hydrocarbon and the like based on equilibrium adsorption theory;
An adsorption column, which may also be referred to as an adsorber, an adsorbent bed, a separator, refers to a vessel filled with at least one adsorbent such as the one described above, the adsorbent having a strong adsorption capacity for components of the mixed gas that are more easily adsorbed;
The product gas of the adsorption process refers to gas which is difficult to be adsorbed by the adsorbent, for example, nitrogen is easy to be adsorbed by the nitrogen adsorbent, 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 compared with the product gas, such as nitrogen, moisture and other relative oxygen, and is easier to be adsorbed by the nitrogen adsorbent;
the terms pressure swing adsorption, adsorption separation, PSA, and the like, will be understood by those skilled in the art to refer to methods other than PSA, but also to methods similar thereto, such as vacuum pressure swing adsorption (Vacuum Swing Adsorption-VSA) or mixed pressure swing adsorption (Mixed Pressure Swing Adsorption-MPSA) methods, and the like, and are to be understood in a broader sense, that is, for the adsorption pressure of the periodic cycle, a higher pressure relative to the desorption step may include greater than or equal to atmospheric pressure, while a lower pressure relative to the desorption step includes less than or equal to atmospheric pressure.
The zeolite membrane separator M01A and the zeolite membrane separator B shown in the attached figure 1 are 3-port zeolite membrane separators, each zeolite membrane separator consists of 1 feed gas inlet, 1 retention gas outlet and 1 permeate gas outlet, and the zeolite membrane separator has the separation function of oxygen, nitrogen and argon, and the oxygen is easier to permeate and the nitrogen and the argon are harder to pass through.
Zeolite materials are known to be generally referred to as aluminosilicate molecular sieves, but zeolite is sometimes referred to generally as crystalline molecular sieves, and the present specification zeolite is generally referred to generally as zeolite molecular sieves, including, for example, aluminosilicates, aluminophosphates, gallium phosphates and variations of these materials substituted with metals, and zeolite materials are generally considered to be molecular sieve materials, but in practice, by controlling their composition and manufacture, zeolite materials may be made to have a plurality of pores or cavities of a specific size so that atoms or molecules of a desired largest dimension are effectively filtered and/or adsorbed therein, and in addition, zeolite materials may be made to have desired electrically polarized characteristics so that polar molecules or easily polarized atoms or molecules may be selectively attracted to zeolite materials, and thus, in combination with control of the electrical characteristics of zeolite materials, the zeolite materials may be controlled for gas species attracted to and adsorbed onto zeolite membranes, and also, as a membrane separation material having selectivity for a specific component so that the crystalline structure may enable the atoms or molecules of a desired largest dimension to be attracted to zeolite materials, such as to be made to have a relatively small rate of oxygen-selective membrane separation by absorption into a membrane, such as is typically made to be a zeolite membrane, and by a small rate of oxygen-selective membrane separation material such as may be made to be attracted to a zeolite material by a small-size-selective membrane material, such as zeolite membrane-permeable to be easily one of the zeolite-permeable to the zeolite membrane, the separation efficiency can be significantly improved by such a control method that the rate of oxygen adsorption onto the membrane is made greater than the adsorption rate of other gases (e.g., nitrogen, argon) in the gas mixture.
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 so that there are no "pinholes" or small cavities throughout the thickness of the membrane that are similar or larger to the size of the zeolite material itself, such as the membrane described in International patent WO 94/01209.
The retentate gas of the zeolite membrane separator is enriched in nitrogen, argon, also known as off-gas, and the permeate gas of the zeolite membrane separator is enriched in oxygen, also known as product gas, in terms of the feed gas being a mixed component of oxygen, nitrogen and argon.
In the present invention, unless explicitly noted otherwise, the pressure referred to in the present invention is gauge pressure.
In the drawings, 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 with flow control and regulation performance can also be pneumatic control or electric and hydraulic control automatic valves;
DXV01A, DXV B, etc. represent check valves, which can be any valve that can restrict the unidirectional flow of fluid;
JV01, JV02, etc. represent manual regulating valves, which can be any valve that can limit fluid flow;
101A, 101B are adsorption towers filled with adsorbent;
the silencer is a device for reducing the noise of fluid discharge, and can be any silencer capable of reducing the noise of fluid discharge;
PV101 and the like represent buffer tanks;
M01A, M B represents a zeolite membrane separator;
Point B, which is a hospital compressed air access point for receiving compressed air of a certain pressure provided by a hospital, preferably comprising a device (not shown in the figure) required for air pretreatment, typically providing compressed air of 0.6MPa or more, and necessary compressed air delivery hoses, accessible from a hospital equipment belt, tower crane interface;
The point A is an original medical oxygen source access point of a hospital, is used for receiving oxygen provided by the hospital from the point A, typically provides an oxygen source of not less than 0.4MPa, can meet the use requirements of a subsequent breathing machine and an anesthesia machine, and can be accessed from a hospital equipment belt and a crane interface through a necessary conveying hose;
The point C is an oxygen outlet C of the device, and is used for connecting oxygen generated by the device to gas equipment for a terminal, such as a breathing machine and an anesthesia machine, and typically, the pressure of not less than 0.4MPa is required to be met;
Y point, the parallel connection air supply collection point of original oxygen source of hospital and oxygen gas produced by adopting oxygen-producing system of the invention, after collection is completed, the oxygen gas is delivered to oxygen outlet C by pipeline, and fed into outlet C and connected into terminal air-using equipment, such as breathing machine and anaesthesia machine, and the air-supplying loop formed from B-Y and A-Y in parallel connection and necessary valve and pipeline are used for receiving oxygen source supplied by hospital from A point and collecting into Y point, and between A-Y an automatic switching valve is set as emergency air supply (said automatic switching valve can also be selected as manual valve), when the air supply loop from B-Y fails, the air supply loop can be directly switched to an original oxygen source used by a hospital as an emergency backup air source, and the emergency backup air source preferably meets the medical oxygen requirement, but does not exclude the oxygen-enriched air used by the hospital according to the medical order, and the air supply loop comprises an air supply hose and a pressure reduction air supply device (not shown) which are required by oxygen transmission from the device to the terminal air utilization device.
The invention provides an oxygen-making and air-supplying device for operating rooms and ICU, which has a typical core structure, namely a B-Y loop and comprises:
Comprising the following steps: two adsorption towers, namely 101A and 101B, two zeolite membrane separators, namely M01A, M B, 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 hospital medical compressed air pipeline node B and the air inlets of the adsorption tower 101A and the adsorption tower 101B; bypass is arranged on the air inlet pipeline of the adsorption tower 101A and the adsorption tower 101B and positioned behind the automatic control valves 01A and 01B, and is connected to the silencer, and the automatic control valves 02A and 02B are correspondingly arranged on the two bypass; the product gas outlets of the adsorption tower 101A and the adsorption tower 101B are respectively connected with the raw material gas side interface of the zeolite membrane separator M01A, M B to form two parallel drying and separating systems; the permeate air side interfaces of the two zeolite membrane separators M01A, M B are connected through a pipeline, and a regulating valve JV01 is arranged on the connecting pipeline; the air retention side interface of the two zeolite membrane separators M01A, M B is correspondingly provided with a check valve DXV01A, DXV B, and the outlet pipelines of the two check valves DXV01A, DXV B are connected with the buffer tank PV101 after being connected; the buffer tank PV101 is connected to the junction Y through a pipe, and a regulating valve JV02 and an automatic regulating valve are sequentially provided on the connecting pipe.
Inputting compressed air with the pressure of 0.45-1.0 MPa from the point B, wherein the compressed air is usually pretreated cleaner raw material gas; air is compressed to the separation pressure required by the subsequent separation by a compressor (the pressure difference of the subsequent separation system is designed according to 0.05-0.1 MPa, the terminal air supply pressure is designed according to the specification that is not less than 0.4 MPa), and at least 0.45-0.5 MPa is required, but compression to higher pressure is not excluded, such as: 0.45-2.0 MPa; the pre-treatment system comprising an activated carbon oil remover or a filter, a freeze dryer or an adsorption dryer and the like singly or in various combinations is used for removing water, solid particle impurities and oil in the compressed air and then enters an air buffer tank, as is necessary for the prior art, wherein the filter can be multistage and combined, the adsorption dryer and the freeze dryer can be combined or can be independently used, a method for recycling compressed air compression heat energy to regenerate the selected adsorption dryer water can be preferably used, the adsorption dryer is preferably used for selecting an adsorbent capable of selectively removing carbon dioxide in the air to remove the carbon dioxide, the accuracy of the filtration and the air treatment amount of the filter, the outlet dew point of the cold dryer or the dew point of the air after the treatment of the adsorption dryer and the treatment requirement on trace carbon dioxide are based on the carbon dioxide or oil required by the gas component outlet of the following separation system, the buffer tank is not necessary, a variable-frequency compression process can be used or can be realized by a bypass evacuation method, the method is used for recycling compressed air compression heat energy to regenerate the selected air, the adsorbent is preferably used for the adsorption dryer, the adsorbent capable of selectively removing carbon dioxide in the air is selected, the adsorbent can be used for the overpressure, the pre-treatment system is usually designed according to the prior art, the pre-treatment system is flexible and the pre-pressurization system can be flexibly designed according to the requirements of the prior art, and the pre-pressurization system can be flexibly and can be flexibly designed according to the requirements and can be well-mastered by the needs.
As described above, in order to avoid uncertainty of gas source impurities after the treatment of the pre-treatment system, and to ensure medical oxygen indexes, especially impurity gases such as moisture, carbon dioxide, total hydrocarbon content, and the like, the invention provides a drying and purifying system based on adsorption separation, which is known in the prior art, wherein after the raw material air enters the pressure swing adsorption separation system of the known art described in the attached figure 1, components such as moisture, carbon dioxide, total hydrocarbon are removed from a silencer, and the purity of a gas production loop formed by DXV01A, V3B and D03 and pipelines thereof is not less than 99.5%, and the medical oxygen meeting the requirements of medical oxygen national standard and Chinese pharmacopoeia is output; the separation system with two groups of switching operations is a typical double-tower adsorption system, when an air inlet valve 01A is opened, 101A is opened to adsorb and remove impurity content, at the same time, 02B is opened to regenerate 101B, its regenerated gas comes from waste gas of another group of zeolite membrane separators M01B which are sequentially connected in series, when 101A is adsorbed and saturated, the separation system is switched to another group of zeolite membrane separators M01B to adsorb, then 101A is used for exhausting the atmosphere, and the muffler is used for removing moisture, carbon dioxide, total hydrocarbons and waste gases such as nitrogen and small amount of oxygen contained in waste gas from zeolite membrane separators, at the same time, 101B is opened to air inlet the air inlet valve 01B.
Thus, following the previous stage variable pressure adsorption drying purification cycle as known technology, a coupled separation process is formed, the system is simple, the valve number is small, especially adsorption drying is integrated, the uncertainty of the purification quality of the front compressed air is greatly reduced, the zeolite membrane separator is protected, the medical oxygen impurity gas content and the oxygen purity are ensured, the reliability is improved, and the operation steps of a typical coupled separation system as shown in figure 1 are as follows:
(1) Opening an automatic control valve 01A, operating an adsorption tower 101A and a 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 an adsorption tower 101B by a regulating valve JV 01; simultaneously, the automatic control valve 02B is opened, the adsorption tower (drying and purifying adsorption bed) 101B is emptied, and the regenerated gas comes from the waste gas of the zeolite membrane separator M01A; at the same time, the check valve DXV01A (mechanical valve) is opened; when the adsorption of the drying and purifying 101A is saturated, the next step is carried out;
(2) Opening an automatic control valve 02A, evacuating an adsorption tower (a drying and purifying adsorption bed) 101A, and enabling regenerated gas to come from waste gas of a zeolite membrane separator M01B; simultaneously, 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 produced by the zeolite membrane separator M01B, and waste gas is discharged to the adsorption tower 101A by the regulating valve JV 01; at the same time, the check valve DXV01B (mechanical valve) is opened; when the adsorption tower (dry purification) 101B is saturated in adsorption, the cycle shifts to the previous step.
In the above steps, all valves except the appointed open valve are in the closed state;
The flow of quantitative cleaning can be controlled by adjusting the opening of the regulating valve JV01 to set the flow, and the oxygen flow can be controlled by adjusting the regulating valve JV 02;
Controlling the flow of quantitative cleaning by adjusting a shutoff valve; the flow opening of the regulating valve JV01 is regulated, and the oxygen yield is regulated by controlling the JV02 and the automatic regulating valve;
In this way, more than 99.5% of oxygen can be produced by cyclic reciprocation, 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 may employ a filler material such as described in the prior art, which may be added to the container as necessary to achieve a more economical buffer volume.
The purpose of coupling the zeolite membrane separators in the adsorption drying system can also ensure that the systems operated by the zeolite membrane separators are not communicated with each other, and can be parallel and multiple groups, namely, the zeolite membrane separators do not generate mutual gas transfer when operated according to the steps, the characteristic can ensure that the zeolite membrane separators are completely separated according to the process requirements, and the skilled person can understand that the design can lead the system to be simpler to expand, as described in the patent, because no more process intermediate gas buffer tanks are matched, the zeolite membrane separator systems can obtain higher recovery rate without adopting interaction among the membrane separators, and obviously, the equipment size is reduced, and the equipment occupation is reduced.
By providing 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, a system can be designed which runs completely according to the required pressure and purity, the required intelligent control program support is not difficult to realize although being complicated, experienced technicians can find that the debugging process of the equipment is almost the system self-adapting to stable process, and the control program gives more sufficient information to maintenance personnel on judging faults, and even directly designates fault points.
Various modifications may be made in the methods and apparatus described above or illustrated in the accompanying drawings without departing from the scope of the invention. Thus, although it is preferred to use any desired configuration, i.e., either fixed volume, or fixed pressure, of 1 or more zeolite membrane separators coupled to the pre-stage adsorption drying system and subsequent stages 1 or more and forming a complete coupled separation process with the product gas buffer tank and the necessary power plant, the present process may utilize more than two zeolite membrane separators and multiple storage tanks, multiple power plants. Furthermore, 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 individual zeolite membrane separators, each may include multiple primary membrane separation layers, or may be devoid of or provided with one or more pretreatment layers for removal of other components such as water vapor. In addition, each membrane separation layer may comprise a single variety of membrane separation materials 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 an operating room and an ICU, which is provided by the invention, wherein the oxygen generator comprises an adsorption separation drying purification and zeolite membrane separator coupling process as shown in fig. 1, the system is free from a compressed air inlet B (a compressed air interface of a hospital operating room tower) of fig. 1 to be connected with 0.6MPa, and free from a medical oxygen source inlet A (an oxygen supply interface of the hospital operating room tower) of fig. 1 to be connected with an emergency standby oxygen source, and free from fig. 2, medical oxygen which is not less than 0.5MPa and not less than 99.5% in purity and meets the requirements of national standard and Chinese pharmacopoeia can be output from an oxygen output port C.
The device constructed by the invention, as shown in figure 3, is an appearance schematic diagram of a medical membrane separation oxygen generator for an operating room and an ICU, and the medical membrane separation oxygen generator is used for preparing oxygen based on a membrane separation technology, the oxygen preparation process is a pure physical process, no phase change exists, only electric power and compressed air are consumed, and medical oxygen meeting medical requirements can be directly extracted from the compressed air (the oxygen purity is not less than 99.5%).
As shown in fig. 2 and 3, a standard interface is matched to receive compressed air and oxygen source of a hospital, wherein the compressed air is used as raw material gas to purify the medical oxygen with purity of 99.5% or more by adopting the product, the received oxygen source can be used as emergency backup oxygen when a system fails, the product shown in fig. 3 can provide legal medical oxygen for clinical operating rooms and ICU relief, extract 99.5% of medical oxygen (3L/min) from the compressed air, reduce purity and output oxygen-enriched air (10L/min), and also can directly send the oxygen source from the receiving end to the terminal to output when the oxygen-making system of the product fails or the generated medical oxygen flow is insufficient to meet the oxygen-using terminal requirement, and the main technical performance parameters are as follows:
Claims (4)
1. An oxygen production and supply method for an operating room or an ICU, wherein the oxygen production and supply method is based on an oxygen production and supply device for the operating room or the ICU, and the oxygen production and supply method comprises the following steps:
(1) At least one compressed air inlet B for receiving compressed air under pressure supplied from a hospital at point B; the device also comprises an air pretreatment device for pretreating raw material air and a compressed air conveying soft pipeline;
(2) At least one original medical oxygen source access port A of the hospital is used for receiving oxygen provided by the hospital from the point A and a conveying hose, and the original medical oxygen of the hospital is conveyed to an oxygen output port C through a pipeline to form a pipeline A-C;
(3) At least one oxygen outlet C for producing oxygen which is crosslinked with the pipeline A-C and then is sent into the oxygen outlet C, and the crosslinking point is marked as Y; the oxygen outlet C is connected with terminal gas equipment, comprises a breathing machine and an anesthesia machine, and also comprises a gas supply hose required by oxygen transmission from the device to the terminal gas equipment;
(4) At least one set of medical membrane separation oxygen generating equipment and an air supply loop B-Y, wherein after receiving compressed air with certain pressure provided by a hospital from the point B, oxygen is generated and is converged into the point Y, and the loop comprises:
1) At least two groups of separators which are sequentially connected in series, wherein the front stage is a pressure swing adsorption drying purification separator, and molecular sieve adsorbent is filled in the front stage; the later stage is a zeolite membrane separator, a zeolite membrane separation material is arranged in the zeolite membrane separator, and the zeolite membrane separator is provided with three interfaces: a feed 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 the 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 and more than two groups of pressure swing adsorption drying purification separators are sequentially connected in series, and are provided with automatic switching valves and pipelines capable of respectively introducing compressed air and switching valves and pipelines capable of respectively discharging the gas reserved in the separators to the atmosphere; the device also comprises a muffler and a connecting pipeline which are arranged after the switching valve and before the switching valve is discharged to the atmosphere, so that noise is reduced;
3) The detention gas side of at least two groups of zeolite membrane separators and more than two groups of zeolite membrane separators which are connected in series in sequence is also provided with a pipeline and an adjusting valve which can be used for communicating the two groups of zeolite membrane separators and the adjusting valve is used for limiting the flow;
4) The permeate gas side of at least two groups of zeolite membrane separators connected in series in sequence is provided with pipelines which can respectively send oxygen generated by the zeolite membrane separators to an oxygen buffer tank, and a permeate gas outlet of each zeolite membrane separator is provided with a check valve to prevent the backflow of the sent oxygen;
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 oxygen enrichment;
(5) At least one air supply loop, a valve and a pipeline which are connected in parallel with the B-Y are used for receiving oxygen source provided by a hospital from the point A and converging to the point Y, and an automatic switching valve is arranged between the A-Y to serve as emergency air supply, so that when the air supply loop from the B-Y fails, the air supply loop is directly switched to the original oxygen source used by the hospital to serve as an emergency backup air source, and the emergency backup air source meets the required medical oxygen but does not exclude the oxygen-enriched air used by the hospital according to medical orders;
(6) The control assembly is used for performing operation control on a valve element on the loop so as to realize safe air supply, and further comprises a detection analysis instrument and an alarm;
The typical structure of the B-Y loop comprises:
Two adsorption towers, denoted as 101A and 101B, two zeolite membrane separators, denoted as M01A, M B, a buffer tank, denoted as PV101, and related control valves and connecting pipelines; wherein:
The adsorption tower 101A is connected in series with the zeolite membrane separator M01A, and the adsorption tower 101B is connected in series with the zeolite membrane separator M01B; automatic control valves 01A and 01B are respectively arranged between the hospital medical compressed air pipeline node B and the air inlets of the adsorption tower 101A and the adsorption tower 101B;
Bypass is arranged on the air inlet pipeline of the adsorption tower 101A and the adsorption tower 101B and positioned behind the automatic control valves 01A and 01B, and is connected to the silencer, and the automatic control valves 02A and 02B are correspondingly arranged on the two bypass;
the product gas outlets of the adsorption tower 101A and the adsorption tower 101B are respectively connected with the raw material gas side interface of the zeolite membrane separator M01A, M B to form two parallel drying and separating systems;
the permeate air side interfaces of the two zeolite membrane separators M01A, M B are connected through a pipeline, and a regulating valve JV01 is arranged on the connecting pipeline;
the air retention side interface of the two zeolite membrane separators M01A, M B is correspondingly provided with a check valve DXV01A, DXV B, and the outlet pipelines of the two check valves DXV01A, DXV B are connected with the buffer tank PV101 after being connected;
the buffer tank PV101 is connected to the junction Y through a pipeline, and a regulating valve JV02 and an automatic regulating valve are sequentially arranged on the connecting pipeline;
The oxygen production and gas supply method comprises the following specific steps:
(1) Opening an automatic control valve 01A, operating an adsorption tower 101A and a 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 an adsorption tower 101B by a regulating valve JV 01; simultaneously, the automatic control valve 02B is opened, the adsorption tower 101B is emptied, and the regenerated gas comes from the waste gas of the zeolite membrane separator M01A; simultaneously, the check valve DXV01A is opened; when the adsorption of the drying and purifying 101A is saturated, the next step is carried out;
(2) Opening an automatic control valve 02A, evacuating the adsorption tower 101A, and enabling regenerated gas to come from waste gas of the zeolite membrane separator M01B; simultaneously, 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 produced by the zeolite membrane separator M01B, and waste gas is discharged to the adsorption tower 101A by the regulating valve JV 01; simultaneously, the check valve DXV01B is opened; when the adsorption tower 101B is saturated, the cycle is shifted to the previous step;
in the above steps, all valves except the appointed open valve are in the closed state;
the flow of quantitative cleaning is controlled by adjusting the opening of the regulating valve JV01 to set the flow, and the oxygen flow is controlled by adjusting the regulating valve JV 02;
controlling the flow of quantitative cleaning by adjusting a shutoff valve; the flow opening of the regulating valve JV01 is regulated, and the oxygen yield is regulated by controlling the JV02 and the automatic regulating valve;
the cycle is repeated in this way, so that more than or equal to 99.5% of oxygen is generated.
2. The method for producing oxygen and supplying air for operating rooms, ICU according to claim 1, wherein the pressure of the compressed air supplied from the point B is 0.45 to 2.0MPa.
3. The oxygen supply method for operating rooms, ICU's of claim 1, wherein the adsorbent is one or more combinations of activated alumina, 13X molecular sieves that adsorb moisture, carbon dioxide, total hydrocarbons.
4. The oxygen supply method for operating rooms, ICU's of claim 1, wherein the zeolite membrane separation material is an aluminosilicate molecular sieve including aluminosilicate, aluminophosphate, gallium phosphate and metal substituted varieties of these materials.
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| TWI859474B (en) * | 2021-10-27 | 2024-10-21 | 台灣奈米碳素股份有限公司 | Device for obtaining newly generated oxygen from atmospheric environment and apparatus for preventing passage of liquid |
| CN114699613B (en) * | 2022-04-02 | 2025-02-11 | 中国人民解放军西部战区总医院 | A new structure of artificial respirator for treating cardiovascular diseases |
| CN117666490A (en) * | 2023-10-24 | 2024-03-08 | 鹰潭市远大气体有限公司 | Oxygen control system for metallurgical industry |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5985003A (en) * | 1994-06-02 | 1999-11-16 | Nippon Sanso Corporation | Oxygen production process by pressure swing adsorption separation |
| KR20020007068A (en) * | 2000-07-15 | 2002-01-26 | 박호군 | Multi Purpose Oxygen Generator using Pressure Swing Adsorption and Method |
| CN102091500A (en) * | 2011-01-19 | 2011-06-15 | 上海穗杉实业有限公司 | Variable pressure absorption oxygen and nitrogen combined separation method and device |
| CN103768891A (en) * | 2014-02-17 | 2014-05-07 | 上海穗杉实业有限公司 | Two-stage series-connection pressure-swing-adsorption oxygen generation system capable of improving oxygen recovery rate and operation method of system |
| CN103801171A (en) * | 2014-02-14 | 2014-05-21 | 上海穗杉实业有限公司 | Two-stage-tandem PSA (pressure swing adsorption) oxygen production system capable of increasing recovery rate of oxygen and operating method of two-stage PSA oxygen production system |
| CN104487152A (en) * | 2012-07-25 | 2015-04-01 | 皇家飞利浦有限公司 | Oxygen separation device for a pressure swing adsorption system |
| CN214693322U (en) * | 2021-03-07 | 2021-11-12 | 中国人民解放军空军军医大学 | An oxygen making and supplying device for operating room and ICU |
-
2021
- 2021-03-07 CN CN202110248333.6A patent/CN112938903B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5985003A (en) * | 1994-06-02 | 1999-11-16 | Nippon Sanso Corporation | Oxygen production process by pressure swing adsorption separation |
| KR20020007068A (en) * | 2000-07-15 | 2002-01-26 | 박호군 | Multi Purpose Oxygen Generator using Pressure Swing Adsorption and Method |
| CN102091500A (en) * | 2011-01-19 | 2011-06-15 | 上海穗杉实业有限公司 | Variable pressure absorption oxygen and nitrogen combined separation method and device |
| CN104487152A (en) * | 2012-07-25 | 2015-04-01 | 皇家飞利浦有限公司 | Oxygen separation device for a pressure swing adsorption system |
| CN103801171A (en) * | 2014-02-14 | 2014-05-21 | 上海穗杉实业有限公司 | Two-stage-tandem PSA (pressure swing adsorption) oxygen production system capable of increasing recovery rate of oxygen and operating method of two-stage PSA oxygen production system |
| CN103768891A (en) * | 2014-02-17 | 2014-05-07 | 上海穗杉实业有限公司 | Two-stage series-connection pressure-swing-adsorption oxygen generation system capable of improving oxygen recovery rate and operation method of system |
| CN214693322U (en) * | 2021-03-07 | 2021-11-12 | 中国人民解放军空军军医大学 | An oxygen making and supplying device for operating room and ICU |
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