CN117815948A - Industrial mixed gas proportioning process and device - Google Patents
Industrial mixed gas proportioning process and device Download PDFInfo
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- CN117815948A CN117815948A CN202311848306.8A CN202311848306A CN117815948A CN 117815948 A CN117815948 A CN 117815948A CN 202311848306 A CN202311848306 A CN 202311848306A CN 117815948 A CN117815948 A CN 117815948A
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- 238000000034 method Methods 0.000 title claims abstract description 100
- 239000007789 gas Substances 0.000 claims abstract description 436
- 239000002994 raw material Substances 0.000 claims abstract description 267
- 238000009826 distribution Methods 0.000 claims abstract description 69
- 238000003860 storage Methods 0.000 claims abstract description 24
- 230000001105 regulatory effect Effects 0.000 claims description 54
- 239000000203 mixture Substances 0.000 claims description 40
- 230000005540 biological transmission Effects 0.000 claims description 37
- 239000007788 liquid Substances 0.000 claims description 32
- 238000002309 gasification Methods 0.000 claims description 5
- 238000010521 absorption reaction Methods 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- 230000000630 rising effect Effects 0.000 claims 1
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 174
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 156
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 128
- 229910052786 argon Inorganic materials 0.000 description 95
- 229910052757 nitrogen Inorganic materials 0.000 description 83
- 239000001569 carbon dioxide Substances 0.000 description 64
- 229910002092 carbon dioxide Inorganic materials 0.000 description 64
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 58
- 238000012546 transfer Methods 0.000 description 54
- 229910052734 helium Inorganic materials 0.000 description 46
- 239000001307 helium Substances 0.000 description 42
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 42
- 229910052760 oxygen Inorganic materials 0.000 description 15
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 9
- 229910001882 dioxygen Inorganic materials 0.000 description 9
- 239000001301 oxygen Substances 0.000 description 9
- 238000013461 design Methods 0.000 description 8
- 238000010586 diagram Methods 0.000 description 8
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 8
- 238000004364 calculation method Methods 0.000 description 7
- 238000003466 welding Methods 0.000 description 7
- 238000012360 testing method Methods 0.000 description 6
- 230000001276 controlling effect Effects 0.000 description 5
- 238000002474 experimental method Methods 0.000 description 5
- 238000005192 partition Methods 0.000 description 5
- 229910001873 dinitrogen Inorganic materials 0.000 description 4
- 229910052697 platinum Inorganic materials 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- HSFWRNGVRCDJHI-UHFFFAOYSA-N Acetylene Chemical compound C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000178 monomer Substances 0.000 description 3
- 229910000838 Al alloy Inorganic materials 0.000 description 2
- 239000000956 alloy Substances 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000006200 vaporizer Substances 0.000 description 2
- 238000011161 development Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 238000001802 infusion Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910052754 neon Inorganic materials 0.000 description 1
- GKAOGPIIYCISHV-UHFFFAOYSA-N neon atom Chemical compound [Ne] GKAOGPIIYCISHV-UHFFFAOYSA-N 0.000 description 1
- 230000002688 persistence Effects 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
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Abstract
The invention relates to an industrial mixed gas proportioning process and a device, wherein a heat exchange procedure is additionally arranged in the industrial mixed gas proportioning process in the prior art, namely, after all the industrial pure gases with different temperatures are output from a gas source, the industrial mixed gas is fully exchanged by a heat exchanger, after the heat exchange is finished, all the industrial pure gases are input into a gas distribution device and are sequentially filled into a mixed gas container with constant volume by adopting a partial pressure method, the device sequentially comprises all the raw material pure gas storage devices, the heat exchanger, the gas distribution device and the mixed gas container with constant volume according to the process flow, the heat exchange procedure is integrated into an automatic mixed gas proportioning control system, a thermometer is arranged at an outlet of the heat exchanger, and the temperature difference value of the outlet is used as a control condition for the flow rate of the gas entering the heat exchanger.
Description
Technical Field
The invention belongs to the field of industrial gas preparation, and particularly relates to an industrial mixed gas proportioning process and an industrial mixed gas proportioning device.
Background
The industrial mixed gas consists of two or more industrial pure gases, and is prepared according to a certain proportion according to the use requirement. The industrial mixed gas comprises different components such as binary, ternary, quaternary and the like and industrial mixed gas with different contents, namely, the industrial mixed gas is formed by mixing two, three or four different pure gases.
The industrial mixed gas is prepared through a weight method, a partial pressure method and a flow method. According to the Dalton partial pressure law, all the industrial pure gases of the components forming the mixed gas are sequentially filled into a mixed gas container with constant volume, the proportional concentration of all the industrial pure gases of the components in the industrial mixed gas is expressed by pressure ratio, and the proportional concentration of all the industrial pure gases of the components is equal to the ratio of the pressure variation value of the industrial pure gases filled into the components to the total pressure of the mixed gas.
The industrial mixed gas is prepared by adopting a partial pressure method and is relatively simple, and an industrial mixed gas distribution device of the industrial mixed gas distribution device consists of raw material pure gas storage equipment, distribution equipment and a mixed gas cylinder; in addition, the cost of the gas distribution device for preparing the industrial mixed gas by adopting the partial pressure method is lower, the preparation time of the industrial mixed gas is shorter, and the yield is higher, so that the partial pressure method is widely applied to the industrial mixed gas production industry. It should be noted that the raw material pure gas mentioned above and later includes a gaseous state and a liquid state.
The principle of the partial pressure method is based on Dalton's law of partial pressure, namely the total pressure of the mixed gas is equal to the sum of the partial pressures of the pure gases of all the components; the pure gas partial pressure of each component is the pressure that each component pure gas independently occupies the total volume of the mixed gas under the condition of the temperature of the mixed gas at the time. According to the basic law of ideal gas, when the volume of a mixed gas container is constant, the pressure of the gas is in direct proportion to the temperature, namely, as the temperature of the mixed gas rises or falls, the total pressure of the mixed gas and the partial pressure of pure gas of each component are correspondingly increased or reduced. Therefore, when the calculated values of the pure gas component pressures of the components in the mixed gas deviate, the proportional concentration of the pure gas of the components in the prepared mixed gas is caused to generate errors, and the larger the calculated deviation value of the pure gas component pressures of the components is, the larger the proportional concentration error value of the pure gas of the components in the prepared mixed gas is.
Referring to fig. 1, 2, 3 and 4, when the prior art adopts a partial pressure method to prepare industrial mixed gas, the temperature of each component pure gas is different when the pure gas enters the gas distribution equipment, but the calculated partial pressure of each component pure gas is calculated according to the temperature corresponding to the ideal gas law, and the temperature is different from the temperature actually entering the gas distribution equipment. In actual operation, the pure gases of each component have different temperatures when entering the gas distribution equipment and are different in temperature difference, and enter the gas mixture container sequentially through the gas distribution equipment, and in the gas mixture container, the pure gases of each component with different temperatures enter the gas mixture container and exchange heat, so that the temperature of the mixed gas is changed, the actual partial pressure of the pure gases of each component in the gas mixture is correspondingly changed, and deviation is generated from the partial pressure calculated according to the ideal gas state, so that the concentration error value of the pure gases of each component is correspondingly increased.
The prior art proportioning process has the following problems to be improved.
Firstly, in the proportioning process of the industrial mixed gas, the temperature difference value between the pure gases of each component is not more than 5 ℃, the industrial mixed gas is prepared by a partial pressure method, and the calculated partial pressure deviation value of the pure gas proportioning of each component can be reduced by a plurality of mixed gas proportioning tests until the concentration deviation value of the pure gas proportion of each component is not more than 2%. And (3) carrying out a plurality of mixed gas proportioning tests to reduce the calculated partial pressure deviation value of each component pure gas proportioning, and having higher requirements on the professional ability of industrial mixed gas proportioning personnel.
In the process of proportioning the mixed gas in the prior art, the temperature difference value between the pure gases of all components is larger than 5 ℃ and smaller than 12 ℃, the industrial mixed gas is prepared by a partial pressure method, a large amount of mixed gas proportioning tests are needed to reduce the calculated partial pressure deviation value of the pure gas of all components so that the concentration error value of the pure gas of all components is not larger than 5%, the professional capability of industrial mixed gas proportioning personnel is required, and the mixed gas proportioning test time is long.
Thirdly, in the gas mixture proportioning process in the prior art, the temperature difference value between the pure gases of all components is larger than 12 ℃, the industrial gas mixture is prepared by a partial pressure method, the calculated partial pressure deviation value of the pure gas mixture ratio of all components is reduced by a great amount of gas mixture proportioning tests, and the calculated partial pressure deviation value of the pure gas mixture ratio of all components can be not larger than 8 percent, so that the great amount of gas mixture ratio tests are carried out, and the calculated partial pressure deviation value of the pure gas mixture ratio of all components is reduced.
The larger the temperature difference value among the pure gases of each component of the raw materials is, the larger the concentration error value of the proportion of the gas mixture is, the higher the proportion cost of the gas mixture is, and the longer the time consumption is.
Disclosure of Invention
(one) solving the technical problems
The invention provides an industrial mixed gas proportioning process and device for reducing the temperature change value of each component pure gas in the mixed gas proportioning process to the maximum extent, and improving the calculated partial pressure accuracy of each component pure gas, so that the application range of a partial pressure method for preparing industrial mixed gas is enlarged, and the preparation variety of industrial mixed gas is increased.
(II) technical scheme
In order to solve the technical problems in the prior art, the invention is realized by the following technical scheme that: an industrial mixed gas proportioning process and a device.
The invention relates to an industrial mixed gas proportioning process and a device thereof, wherein the process adopts a partial pressure method to sequentially fill all the industrial pure gases of components forming the mixed gas into a mixed gas container with constant volume, and the proportion concentration of all the industrial pure gases of the components in the industrial mixed gas is expressed by pressure ratio. The process adopts a partial pressure method to sequentially fill all the components of industrial pure gas forming the mixed gas into a mixed gas container with constant volume, the proportion concentration of all the components of industrial pure gas in the industrial mixed gas is expressed by pressure ratio, the device sequentially comprises all the components of raw material pure gas storage equipment, heat exchange equipment, gas distribution equipment and a mixed gas container with constant volume according to the process flow, and the gas distribution equipment comprises a pressure proportioning valve, a gas feeding valve, a gas transmission pipeline between the pressure proportioning valve and the gas feeding valve and a pressure transmitter arranged on the gas transmission pipeline; the invention adds heat exchange equipment in the existing industrial mixed gas proportioning process and device, namely adds heat exchange equipment after the outlets of the pure gas storage equipment and before the inlets of the gas distribution equipment, wherein the heat exchange equipment comprises raw gas inlet pipelines between the pure gas storage equipment and the inlets of the heat exchangers, inlet regulating valves on the pipelines, heat exchangers, gas transmission pipelines between the outlets of the heat exchangers and the pressure proportioning valves in the gas distribution equipment, and thermometers arranged on the gas transmission pipelines. Pure gases of all component raw materials with different temperatures are output from storage equipment, enter a heat exchanger through an air inlet pipeline to exchange heat, the temperature difference value of the pure gases of all component raw materials is reduced through heat transfer, the pure gases are respectively input into mixed gas proportioning equipment from an outlet of the heat exchanger through an air transmission pipeline, the pressure is respectively regulated to the calculated partial pressure of proportioning setting through a pressure proportioning valve in the mixed gas proportioning equipment, and then the mixed gas is sequentially input into a mixed gas container through control of an air supply valve according to the sequence from low pressure to high pressure, so that industrial mixed gas is obtained through proportioning.
According to the invention, the heat transfer theory is utilized in the proportioning process of industrial mixed gas, so that all component raw material pure gases with different temperatures exchange heat with each other before entering the gas distribution equipment, the raw material pure gases with relatively high temperatures release heat and cool, and meanwhile, the raw material pure gases with relatively low temperatures absorb heat and heat, so that the temperature difference value among all component raw material pure gases in different temperature states is reduced to the greatest extent in the heat exchange process; when the temperature change value of the pure gas of each component raw material in the mixed gas container is reduced, the error value of the actual partial pressure and the calculated partial pressure of the mixture ratio of each component gas is correspondingly reduced, so that the proportional concentration deviation value of each component pure gas is reduced.
The invention further adopts the technical scheme that: according to the physical property characteristics of pure gas of each component raw material in the mixed gas, the heat exchanger is designed to be a plate-fin heat exchanger. In the plate-fin heat exchanger, all component raw material pure gases are separated by the solid heat transfer surface, so that material exchange cannot be performed, heat is transferred through the solid heat transfer surface while the purity of all component raw material pure gases is not influenced, the plate-fin heat exchanger is large in conduction area and high in heat transfer efficiency, and the full and effective heat exchange of all component raw material pure gases with different temperatures is facilitated.
The plate-fin heat exchanger is preferably an aluminum dividing wall type heat exchanger, is composed of a partition plate, fins and sealing strips, has the characteristics of small volume, large unit heat exchange area, high heat transfer efficiency, multi-strand fluid heat exchange and the like, and can be used for simultaneous heat exchange of 2-element, 3-element or 4-element raw material pure gases of components such as gaseous or liquid oxygen, nitrogen, argon, hydrogen, carbon dioxide, neon, helium and the like.
The invention further adopts the technical scheme that: in the mixed gas proportioning heat exchange process, the plate-fin heat exchanger adopts a countercurrent heat exchange process, namely, raw material pure gas inlet pipelines needing heat absorption, temperature rise or gasification are arranged in the same direction with inlets connected with the heat exchanger, the inlets of the heat exchanger are reversely arranged, and the raw material pure gas is reversely led into the heat exchanger; the raw material pure gas inlet pipeline needing heat release and cooling is arranged in the same direction with each inlet connected with the heat exchanger, the inlets of the heat exchangers are all arranged in the forward direction, the raw material pure gas is all guided into the heat exchangers in the forward direction, and the countercurrent process arrangement can enable the raw material gas to exchange heat fully, so that the temperature difference value between the raw material pure gases of each component is reduced to the maximum extent.
The technical scheme of the invention is preferably as follows:
the first preferred scheme is as follows: when the pure gas of each component raw material is in a gaseous state, the temperature difference is small, the pure gas of the raw material has no phase change in the mixed gas proportioning process, and the temperature difference of the pure gas of each component raw material at the forward flow outlet and the reverse flow outlet of the plate-fin heat exchanger is not more than 1 ℃, the heat exchanger in the mixed gas proportioning process is configured as a monomer plate-fin heat exchanger.
And a second preferred scheme is as follows: when the temperature difference between the pure gases of the raw materials of all components is large, or the phase state of the raw materials of all components changes from liquid gasification to gas state in the mixed gas proportioning process, the heat transfer quantity between the pure gases of all the raw materials of all the components is large, the temperature difference between the pure gases of all the raw materials of all the components of the forward flow outlet and the reverse flow outlet of the heat exchanger is more than 1 ℃ and less than or equal to 3 ℃, and the heat exchanger in the mixed gas proportioning process is configured as a combined plate-fin heat exchanger.
According to a heat transfer calculation formula F=Q/aDeltat (F: heat transfer area, Q: heat transfer quantity, a: heat transfer coefficient, deltat: heat transfer temperature difference), calculating the heat transfer area of the plate-fin heat exchanger, and designing the structure of the plate-fin heat exchanger according to the calculated heat transfer area. According to the calculated heat transfer area, 1 group of single plate-fin heat exchangers or combined plate-fin heat exchangers are designed, and when the calculated heat transfer area is large, 2 groups or multiple groups of single plate-fin heat exchangers are configured in parallel to be combined plate-fin heat exchangers by adopting a modularized design.
The device of the invention has the further technical proposal that: a pneumatic air inlet regulating valve is respectively arranged in each component raw material pure gas inlet pipeline between each component raw material pure gas storage device and the inlet of the plate-fin heat exchanger and is used for controlling and regulating the flow rate of each component raw material pure gas entering the heat exchanger, in particular for regulating the flow rate of forward flow and reverse flow of each component raw material pure gas in the heat exchanger; meanwhile, a thermal resistance thermometer is respectively arranged on gas pipelines between each component raw material pure gas outlet of the plate-fin heat exchanger and a pressure proportioning valve in the gas distribution equipment, and the raw material pure gas temperature in each gas pipeline at the outlet of the heat exchanger is continuously measured on line.
The device of the invention has the further technical proposal that: the automatic control program of the heat exchange procedure is integrated into an automatic control system of the mixture ratio, an air inlet regulating valve arranged on a raw material air inlet pipeline between the pure gas storage equipment of each component raw material and an inlet of a heat exchanger, and a thermometer arranged on an air transmission pipeline between an outlet of the heat exchanger and a pressure proportioning valve of air distribution equipment are connected into the automatic control system of the mixture ratio, the temperature difference value between the raw material gases of each component at the outlet of the heat exchanger is set as an interlocking control condition of the air inlet regulating valve, and the flow rate of the pure gas of each component entering the heat exchanger is regulated by timely regulating the opening of the air inlet regulating valve, so that the temperature difference of the pure gas of each component raw material entering the air distribution equipment after heat exchange reaches a set temperature difference value, and the set temperature difference value is usually the relative optimal temperature difference value which can be reached after the pure gas of each component raw material obtained through a large number of experiments is fully exchanged.
(III) beneficial effects
The invention provides an industrial mixed gas proportioning process and device, which have the following beneficial effects:
1. the proportioning process and the proportioning device for the industrial mixed gas realize the remarkable effects of greatly reducing the proportion concentration deviation value of pure gas of each component in the industrial mixed gas and improving the production efficiency of the industrial mixed gas by a partial pressure method.
2. The device adopts the PLC technology as the control technology of the system, and the air inlet regulating valve is set to be a pneumatic valve, so that the aim of full-automatic control is fulfilled by the industrial mixed gas proportioning process and the device.
3. The device fully utilizes the technical development result of the heat exchanger, and improves the running safety and stability of equipment.
4. The application of the technology expands the application range of the partial pressure method for preparing the industrial mixed gas, increases the types of the industrial mixed gas preparation, is convenient for application and implementation and has obvious implementation effect.
Drawings
FIG. 1 is a schematic diagram of a 2-element welding mixture (25% He+75% Ar) proportioning process and device in the prior art
FIG. 2 prior art 2-element electric light source gas mixture (40% N) 2 +60% Ar) proportioning process and device schematic diagram
FIG. 3 prior art 2-element fresh-keeping gas mixture (20% CO) 2 +80％O 2 ) Proportioning process and device schematic diagram
FIG. 4 prior art 3-membered fresh-keeping gas mixture (20% O) 2 +30％N 2 +50％CO 2 ) Proportioning process and device schematic diagram
FIG. 5 is a schematic diagram of a 2-element welding gas mixture (25% He+75% Ar) proportioning process and device according to an embodiment of the invention
FIG. 6A 2-element electric light source gas mixture (40% N) according to an embodiment of the invention 2 +60% Ar) proportioning process and device schematic diagram
FIG. 7 embodiment of the invention2-element fresh-keeping mixed gas (20% CO) 2 +80％O 2 ) Proportioning process and device schematic diagram
FIG. 8A 3-membered fresh-keeping gas mixture (20% O) according to an embodiment of the invention 2 +30％N 2 +50％CO 2 ) Proportioning process and device schematic diagram
Detailed Description
Embodiments of the present invention will now be described more fully with reference to fig. 5, 6, 7 and 8. The industrial mixtures are of a wide variety, and it is apparent that the examples described below are only some, but not all, examples of the invention.
Embodiment one: referring to fig. 5, a 2-element welding gas mixture (25% he+75% ar) proportioning process and device.
The proportion concentration of the 2-element welding mixed gas is designed to be 25% of pure helium and 75% of pure argon. Raw material pure helium and pure argon are respectively stored in gas cylinders A1 and A2 in a gaseous form, and the raw material pure helium and pure argon have no phase change in the proportioning process of the 2-element welding mixed gas. The pressure of pure helium and pure argon in the raw material gas cylinder is 15MPa of the set pressure in the gas cylinder filling national standard, and the raw material pure helium and pure argon are filled at the same atmospheric environment temperature, wherein the temperature difference of the pure helium and pure argon in the raw material gas cylinder is 5 ℃.
The embodiment of the invention discloses A2-element welding mixed gas proportioning process and A2-element welding mixed gas proportioning device, which comprise a raw material pure helium bottle A1, a matched bottle valve V1, a raw material pure argon bottle A2 and a matched bottle valve V2, wherein two paths of air inlet pipelines are connected behind the raw material pure helium bottle valve V1 and the raw material pure argon bottle valve V2 and are connected with a heat exchanger E1, a raw material pure helium regulating valve V3 and a raw material pure argon regulating valve V4 are respectively arranged on the two paths of air inlet pipelines, two paths of air transmission pipelines of raw material pure helium and pure argon are respectively arranged at the outlet of the heat exchanger E1, meanwhile, a thermal resistance thermometer TI and a thermal resistance T2 are respectively arranged on the two paths of air transmission pipelines, the two paths of air transmission pipelines are respectively connected into an air transmission valve V7 in an air distribution device D1 after the thermal resistance thermometer TI and the thermal resistance T2, a pressure proportioning valve V6 and a pressure proportioning valve V5 are respectively arranged on the two paths of air transmission pipelines in the air distribution device D1, a pressure transmitter P1 and P2 are respectively arranged behind the two paths of air transmission pipelines, and the raw material pure helium and pure argon are sequentially filled into the mixed gas bottle A8 through the air transmission valves.
And opening a raw material pure helium bottle valve V1 and a raw material pure argon bottle valve V2, respectively inputting raw material pure helium and pure argon into two paths of air inlet pipelines from the raw material helium bottle A1 and the raw material argon bottle A2, regulating flow through a raw material helium regulating valve V3 and a raw material argon regulating valve V4, entering a heat exchanger E1 for countercurrent heat exchange, heating the raw material pure helium while cooling the raw material pure argon, and inputting the temperature difference of the raw material pure helium and the raw material pure argon into a mixed gas distribution device D1 when the temperature difference of the raw material pure helium and the raw material pure argon is reduced to a design value.
The heat exchanger E1 is a plate-fin heat exchanger, and the partition plates, fins and seals of the heat exchanger E1 are all made of aluminum materials, and the heat transfer medium is gas, so that straight fins are selected. In the heat exchanger E1, raw material pure helium and pure argon are subjected to heat exchange by adopting a countercurrent process, the raw material pure argon is cooled, the heat is designed to be released by forward flow, and the raw material pure helium is heated, and the heat is designed to be absorbed by countercurrent.
The temperature difference of pure helium and pure argon in a raw material gas cylinder is 5 ℃, according to experiments, the optimal temperature difference delta t obtained after heat exchange is 0.8 ℃, according to a heat transfer calculation formula Q=WpCp delta t, the heat transfer quantity required to be achieved is 800064J/h, according to the straight fin heat exchanger, the heat transfer coefficient a of a heat exchanger E1 is selected to be 60-69K/W (m 2. K) -1, the minimum heat transfer coefficient is selected, the required heat transfer quantity Q= 800064J/h is converted into the heat transfer quantity per second to be Q=800064/3600, and then the heat transfer calculation formula F=Q/adelta t=800064/3600/(60×0.8) =4.63 m2 is obtained, so that the heat transfer area F of the required plate-fin heat exchanger E1 is 4.63m 2 . In order to keep the temperature difference Deltat of the raw material at the outlet of the heat exchanger E1 not more than 0.8 ℃, the heat transfer area redundancy of the plate-fin heat exchanger E1 is increased to be 0.37m2, so the actual heat transfer area F of the plate-fin heat exchanger E1 is designed to be 5m 2 。
The heat transfer area F of the heat exchanger E1 of this embodiment is small. Meanwhile, the gas supply process of the raw material pure helium and pure argon is gas cylinder gas supply, and can intermittently supply gas, and the flow of the raw material pure helium and pure argon in the heat exchanger E1 is low. For this purpose, the heat exchanger E1 is designed as a 1-group, monolithic plate-fin heat exchanger. The thickness of the partition plate is 0.8mm, the width of the seal is 15mm and the thickness of the fin is 0.15mm according to the design that the heat transfer area F is 5m 2.
Because the gas source gas is gas cylinder gas supply, the flow of raw material pure helium and pure argon entering the heat exchanger E1 is low, and the raw material pure helium and pure argon are intermittently supplied, the pneumatic gas inlet regulating valves V3 and V4 are pneumatic small-flow single-seat regulating valves, and the designed valve diameter is 20mm. And the thermal resistance thermometers T1 and T2 are platinum thermal resistance thermometers.
In the embodiment, the length of a gas transmission pipeline from a pure helium gas and a pure argon gas outlet of the heat exchanger E1 to pure helium gas and pure argon gas pressure proportioning valves V6 and V5 of the raw materials is 25m. The volume of the mixed gas bottle A1 of the embodiment is 10 liters, and the maximum value of the volume of the gas filled into the mixed gas bottle according to the national standard of 10 liters is 1.5m 3 According to the design, the diameter of the gas transmission pipeline is 280mm, and the matching of the internal volume of the gas transmission pipeline and the volume of the mixed gas cylinder A8 after heat exchange can be satisfied.
The proportioning process and the automatic operation steps of the device for the 2-element welding mixed gas (25 percent of He+75 percent of Ar) are as follows:
in a PLC control system of a gas mixture distribution device, the temperature difference value between two thermometers T1 and T2 on a two-way gas transmission pipeline of pure helium and pure argon serving as the outlet of a heat exchanger E1 is set to be 0.8 ℃, and the temperature difference value is used as an interlocking condition for opening pneumatic pressure proportioning valves V5 and V6 of gas mixture distribution equipment D1, wherein the set values of the pressure transmitters P1 and P2 of the pure helium and the pure argon serving as the raw materials are respectively proportioning partial pressure values of 2.5MPa and 10MPa, and the gas mixture is sequentially injected into a gas mixture bottle A8 according to the sequence of the partial pressure values from small to large.
1. Before the mixed gas distribution device is started, the cylinder valve V1 of the raw material helium cylinder A1, the cylinder valve V2 of the raw material argon cylinder A2 and the cylinder valve V8 of the mixed gas cylinder A8 are respectively fully opened. According to the proportion concentration of the mixed gas to be prepared, namely 25% pure helium and 75% pure argon, in the PLC interlocking control program of the mixed gas distribution equipment D1, the temperature difference between the pure helium and the pure argon serving as raw materials is set to be 0.8 ℃, and the proportion partial pressure values are respectively 2.5MPa and 10MPa.
2. And starting 2-element welding gas mixture distribution equipment D1, starting a gas distribution equipment switch in a PLC system operation platform of the gas mixture distribution equipment D1, automatically opening raw material pure helium and pure argon gas inlet regulating valves V3 and V4, and automatically regulating the flow of raw material pure helium and pure argon gas entering the heat exchanger E1 according to the temperature difference set value of 0.8 ℃ of the raw material pure helium and pure argon gas at the outlet of the heat exchanger E1.
3. When the set condition is met, namely the temperature difference value of raw material pure helium and pure argon at the outlet of the heat exchanger E1 reaches 0.8 ℃, a raw material pure helium pressure proportioning valve V6 and an air supply valve V7 in the air distribution device D1 are opened, raw material pure helium is filled into a mixed air bottle A8, when a raw material pure helium pressure transmitter P1 displays that the set proportioning partial pressure value reaches 2.5MPa, the raw material pure helium pressure proportioning valve V6 is closed, then the raw material pure argon pressure proportioning valve V5 is opened, raw material pure argon is filled into the mixed air bottle A8, and when the raw material pure argon pressure transmitter P2 displays that the set proportioning partial pressure value reaches 10MPa, the raw material pure argon pressure proportioning valve V5 is closed.
4. The PLC control system of the mixed gas distribution equipment D1 starts a shutdown program, raw material pure helium gas, pure argon gas inlet regulating valves V3 and V4 and an air supply valve V7 are automatically closed, and 2-element welding mixed gas (25 percent of He+75 percent of Ar) is proportioned.
Embodiment two: referring to fig. 6, a 2-element electric light source mixed gas proportioning process and a device thereof.
The proportion concentration of the 2-element electric light source mixed gas is designed to be 40% pure nitrogen and 60% pure argon. Raw material pure nitrogen and pure argon are stored in liquid form in a liquid nitrogen storage tank A3 and a liquid argon storage tank A4, the temperature of raw material pure liquid nitrogen is-196 ℃, the temperature of pure liquid argon is-186 ℃, and the temperature difference of the raw material pure liquid nitrogen and the pure liquid argon is 10 ℃. Raw material pure liquid nitrogen and pure liquid argon in a liquid nitrogen storage tank A3 and a liquid argon storage tank A4 are pressurized by a storage tank pressurizer, are gasified to gaseous raw material pure nitrogen and pure argon respectively through gasifiers E2 and E3, the pressure of the raw material pure nitrogen and the pure argon is regulated and controlled to be 15MPa in the set pressure of a gas bottle filling national standard, and the temperature difference of the raw material pure nitrogen and the pure argon is 10 ℃ under the same atmospheric environment temperature after gasification.
The heat transfer capacity required by larger temperature difference is correspondingly larger, so the fins of the plate-fin heat exchanger are designed to be zigzag fins, the thickness of the designed baffle is 1mm, the width of the seal is 25mm, and the thickness of the fins is 0.2mm.
The temperature difference of the pure nitrogen and the pure argon of the raw materials is 10 ℃, the optimal temperature difference delta t obtained after heat exchange is 1 ℃ according to experiments, and the required temperature is calculated according to a heat transfer calculation formula Q=WpCp delta t The heat transfer quantity is 2000000J/h, the heat transfer coefficient a of the heat exchanger E1 is selected to be 80-89K/W (m 2. K) -1 according to the zigzag fin heat exchanger, the minimum heat transfer coefficient is selected, the required heat transfer quantity Q=2000000J/h is converted into the heat transfer quantity Q=2000000/3600 per second, and the heat transfer area F of the required plate-fin heat exchanger is obtained to be 6.94m according to the heat transfer calculation formula F=Q/aΔt=2000000/3600/(80×1) =6.94 m2 2 . In order to keep the temperature difference Deltat of the raw material at the outlet of the heat exchanger not more than 1 ℃, the redundancy of the heat transfer area of the plate-fin heat exchanger is increased to be 0.56m < 2 >, so that the actual heat transfer area F of the plate-fin heat exchanger is designed to be 7.5m 2 。
The heat exchanger in the 2-element electric light source mixed gas proportioning process is designed to be composed of three groups of monomer plate-fin heat exchangers E4, E5 and E6 with the same model, and the heat transfer area of each group of heat exchanger is 2.5m 2 Three groups of plate-fin heat exchangers E4, E5 and E6 are arranged in parallel. In the heat exchangers E4, E5 and E6, countercurrent process is adopted for heat exchange, raw material pure argon is cooled, forward flow heat release is designed, raw material pure nitrogen is heated, countercurrent heat absorption is designed, raw material pure argon and pure nitrogen are respectively divided into three branch pipes from a two-way air inlet main pipe and enter three heat exchangers which are connected in parallel, the air quantity is evenly distributed, and after heat exchange is completed, the three branch pipes are respectively converged into one pure argon pipeline and one pure nitrogen pipeline, and the three branch pipes enter air distribution equipment D2.
The embodiment 2 element electric light source mixed gas proportioning process and device are as follows: the raw material liquid nitrogen and liquid argon are output from a liquid nitrogen storage tank A3 and a liquid argon storage tank A4, gasified to gaseous raw material pure nitrogen and pure argon by a liquid nitrogen gasifier E2 and a liquid argon gasifier E3, flow is regulated by a raw material pure nitrogen pneumatic air inlet regulating valve V9 and a raw material pure argon pneumatic air inlet regulating valve V10 after entering an air inlet pipeline, and the raw material pure nitrogen and pure argon air inlet main pipeline is divided into three branch pipelines after the pneumatic air inlet regulating valves V9 and V10 and simultaneously enters heat exchangers E4, E5 and E6 for heat exchange, raw material pure argon is cooled and raw material pure nitrogen is heated, and when the temperature difference of the raw material pure nitrogen and pure argon is reduced to a design value, the raw material pure nitrogen and pure argon enters a mixed gas distribution device D2. In the mixed gas distribution equipment D2, the proportioning partial pressure of a raw material pure nitrogen pressure transmitter P3 and a raw material pure argon pressure transmitter P4 is set according to the mixed gas proportion concentration requirement, the raw material pure nitrogen and the pure argon are respectively regulated to the required proportioning partial pressure set values through pressure proportioning valves V21 and V20, and are controlled by an air supply valve V7 and sequentially input into a mixed gas cylinder A8.
Because the raw material pure nitrogen and pure argon gas supply process is that the raw material liquid nitrogen storage tank A3 and the raw material liquid argon storage tank A4 supply gas, the air flow in the heat exchangers E4, E5 and E6 is higher and the persistence is longer, the pneumatic air inlet regulating valves V9 and V10 are all top guide type single-seat regulating valves, and the diameter of the valves is designed to be 25mm. 1 raw material pure nitrogen thermal resistance thermometer T3 and raw material pure argon thermal resistance thermometer T4 are respectively designed in a raw material gas input pipeline after heat exchange between outlets of the heat exchangers E4, E5 and E6, the raw material pure nitrogen pressure proportioning valve V21 and the raw material pure argon pressure proportioning valve V20, and the thermal resistance thermometers T3 and T4 are platinum thermal resistance thermometers.
In a PLC control system of the gas mixture distribution device, pure nitrogen and pure argon with temperature difference of 1 ℃ are designed as opening interlocking conditions of the pneumatic pressure proportioning valves V21 and V20 for outlet raw materials of the heat exchangers E4, E5 and E6.
The embodiment designs the heat exchangers E4, E5 and E6 from the pure nitrogen and pure argon outlets to the pure nitrogen pressure proportioning valve V21 and the pure argon pressure proportioning valve V20, and the length of the gas pipeline is 25m. The volume of the mixed gas bottle A8 of the embodiment is 10 liters, and the maximum value of the volume of the gas filled into the mixed gas bottle according to the national standard of 10 liters is 1.5m 3 According to the design, the diameter of the gas transmission pipeline is 280mm, and the matching of the internal volume of the gas transmission pipeline and the volume of the mixed gas cylinder A8 after heat exchange can be satisfied.
Example 2-element electric light source gas mixture (40% N) 2 +60% Ar) proportioning process and automatic operation method of the device are as follows:
1. before the mixed gas distribution device is started, a liquid nitrogen storage tank A3 and a liquid argon storage tank A4 infusion valves V12 and V11 are respectively opened, and a liquid nitrogen vaporizer E2 and a liquid argon vaporizer E3 are respectively put into operation. In the PLC interlocking control system of the mixed gas distribution equipment D2, the temperature difference value of the pure nitrogen and pure argon thermal resistance thermometer at the outlet of the heat exchanger is set to be 1 ℃, the partial pressure value of the pure nitrogen pressure transmitter of the raw material is set to be 4MPa, and the partial pressure value of the pure argon pressure transmitter is set to be 10MPa.
2. Starting a mixed gas distribution device, automatically opening raw material pure nitrogen and pure argon gas inlet regulating valves V9 and V10, regulating the flow of the raw material pure nitrogen and pure argon gas entering heat exchangers E4, E5 and E6, and controlling the temperature difference value of the raw material pure nitrogen and pure argon gas at outlets of the heat exchangers E4, E5 and E6 to be not more than 1 ℃.
3. When the temperature difference value of the pure nitrogen and the pure argon of the raw materials at the outlets of the heat exchangers E4, E5 and E6 reaches 1 ℃ or less than 1 ℃, the pure nitrogen pressure proportioning valve V21 of the raw materials is opened, the air supply valve V7 of the raw materials is opened, the pure nitrogen of the raw materials is filled into the mixed gas cylinder A8, when the pure nitrogen pressure transmitter P3 of the raw materials shows that the set partial pressure value reaches 4MPa, the pure nitrogen pressure proportioning valve V21 of the raw materials is closed, then the pure argon pressure proportioning valve V20 of the raw materials is opened, the pure argon of the raw materials is filled into the mixed gas cylinder A8, and when the pure argon pressure transmitter P4 of the raw materials shows that the set partial pressure value reaches 10MPa, the pure argon pressure proportioning valve V20 of the raw materials is closed.
4. The PLC control system of the mixed gas distribution equipment D2 starts a shutdown program, raw material pure nitrogen gas and pure argon gas inlet regulating valves V9 and V10 are automatically and fully closed with a gas supply valve V7, and 2-element electric light source mixed gas (40% N) 2 +60% Ar) proportioning is completed.
Embodiment III: referring to fig. 7, a 2-element fresh-keeping mixed gas proportioning process and a device thereof.
The fresh-keeping mixed gas of the embodiment 2 consists of carbon dioxide with the proportion concentration of 20% and oxygen with the proportion concentration of 80%, wherein raw material pure carbon dioxide is stored in a gas cylinder A5 in a liquid state, and raw material pure oxygen is stored in a gas cylinder A6 in a gaseous state. In the 2-element fresh-keeping mixed gas proportioning process, pure oxygen as a raw material has no phase change, and pure carbon dioxide as a raw material can be gasified from a liquid state to a gas state. The pressure of the pure carbon dioxide and the pure oxygen in the raw material gas cylinder is 15MPa of the set pressure in the national standard of gas cylinder filling, and the temperature difference between the pure carbon dioxide and the pure oxygen is 15 ℃ through on-site actual measurement.
The embodiment provides a 2-element fresh-keeping mixed gas proportioning process and device, which comprises a raw material carbon dioxide (liquid) gas cylinder A5, a matched cylinder valve V14, a raw material oxygen cylinder A6 and a matched cylinder valve V15, wherein the raw material carbon dioxide cylinder valve V14 and the raw material oxygen cylinder valve V15 are connected with a heat exchanger through a two-way gas inlet pipeline, one raw material carbon dioxide gas inlet pipeline is divided into two gas inlet branch pipelines which are respectively reversely connected with the heat exchangers E7 and E8, the other raw material oxygen gas inlet pipeline is divided into two gas inlet branch pipelines which are respectively and positively connected with the heat exchangers E7 and E8, a raw material carbon dioxide regulating valve V17 and a raw material oxygen regulating valve V18 are respectively arranged on the two gas inlet main pipelines, raw material carbon dioxide after heat exchange is output from the two branch pipelines connected with outlets of the heat exchangers E7 and E8 and is summarized into one gas transmission pipeline which enters into a gas distribution device D3 and is connected with a carbon dioxide pressure proportioning valve V22, a thermal resistance thermometer T5 is arranged on the raw material carbon dioxide gas inlet pipeline in front of the carbon dioxide pressure proportioning valve V22, and a gas transmission pipeline is provided with a gas transmission pipeline P7 through a gas transmission valve P7 in the gas transmission pipeline after the carbon dioxide pressure proportioning valve V22; the raw material oxygen is output from two branch pipelines connected with the outlets of the heat exchangers E7 and E8 and is summarized into a gas transmission pipeline, the gas transmission pipeline enters the mixed gas distribution equipment D3 and is connected with the oxygen pressure proportioning valve V23, a thermal resistance thermometer T6 is arranged on the raw material oxygen gas transmission pipeline in front of the oxygen pressure proportioning valve V23, a pressure transmitter P6 is arranged on the gas transmission pipeline behind the oxygen pressure proportioning valve V23, and the raw material oxygen gas transmission pipeline is filled into the mixed gas bottle A8 through the gas transmission valve V7.
The raw materials of pure carbon dioxide, and the partition plates, fins and seals of the pure oxygen heat exchangers E7 and E8 are all made of aluminum alloy materials. As the raw material pure carbon dioxide is vaporized and heated, the fins of the plate-fin heat exchangers E7 and E8 are designed to be porous fins, the thickness of the designed baffle is 1.1mm, the width of the seal is 25mm, and the thickness of the fins is 0.23mm.
The temperature difference between the pure carbon dioxide as raw material and the pure oxygen as raw material is 15 ℃, the optimal temperature difference Deltat obtained after heat exchange is 1.2 ℃ according to experiments, the heat transfer quantity required to be achieved is 1600000J/h according to a heat transfer calculation formula Q=WPC Deltat, the heat transfer coefficients a of the heat exchangers E7 and E8 are selected to be 70-85K/W (m2.K) -1 according to the porous fin heat exchanger, the minimum heat transfer coefficient is selected, the required heat transfer quantity Q=1600000J/h is converted into the heat transfer quantity per second to be Q=1600000/3600, and the heat transfer calculation formula is used againF＝Q/aΔt＝1600000/3600/(70×1.2)＝5.29m 2 The heat transfer area F of the required plate-fin heat exchangers E7 and E8 is 5.29m 2 . In order to keep the temperature difference Deltat of the raw materials at the outlets of the heat exchangers E7 and E8 not to be more than 1.2 ℃, the redundancy of the heat transfer area of the plate-fin heat exchanger E1 is increased to be 0.21m 2 Therefore, the total heat transfer area of the plate-fin heat exchanger is designed to be 5.5m 2 Because the heat exchangers E7 and E8 are the same in model, the heat transfer areas of the heat exchangers E7 and E8 are designed to be 2.25m 2 。
The raw material pure carbon dioxide pneumatic air inlet regulating valve V17 is a low-temperature single-seat regulating valve, the raw material pure oxygen pneumatic air inlet regulating valve V18 is a pneumatic small-flow single-seat regulating valve, and the diameters of the valves are all designed to be 20mm. And the thermal resistance thermometers T5 and T6 are platinum thermal resistance thermometers.
And after the outlet thermometers T5 and T6 of the heat exchangers E7 and E8 are designed, the lengths of gas pipelines from the outlet thermometers T5 and T6 to the raw material pure carbon dioxide pressure proportioning valve V22 and the raw material pure oxygen pressure proportioning valve V23 are 25m. The volume of the mixed gas bottle A8 of the embodiment is 10 liters, and the maximum value of the volume of the gas filled into the mixed gas bottle according to the national standard of 10 liters is 1.5m 3 According to the design, the diameter of the gas transmission pipeline is 280mm, and the matching of the internal volume of the gas transmission pipeline and the volume of the mixed gas cylinder A8 after heat exchange can be satisfied.
The 2-element fresh-keeping mixed gas (20% CO) 2 +80％O 2 ) The proportioning process and the device have the following automatic operation steps:
1. before the mixed gas distribution device is started, cylinder valves V14 and V15 of a raw material pure carbon dioxide cylinder A5 and a raw material pure oxygen cylinder A6 are respectively opened, a temperature difference value between a raw material pure carbon dioxide thermometer T5 and a pure oxygen thermometer T6 on a gas transmission pipeline between outlets of heat exchangers E7 and E8 and the mixed gas distribution device D3 is set to be 1.2 ℃ in a PLC interlocking control system of the mixed gas distribution device D3, the temperature difference value is used as an interlocking condition for controlling pneumatic pressure proportioning valves V22 and V23 of the mixed gas distribution device D3 to be opened, and partial pressure values of raw material pure carbon dioxide and pure oxygen pressure transmitters P5 and P6 in the mixed gas distribution device D3 are set to be 2.0MPa and 10MPa.
2. Starting 2-element fresh-keeping mixed gas distribution equipment, starting a gas distribution switch in a control system, simultaneously and automatically starting a raw material pure carbon dioxide gas inlet regulating valve V17 and a pure oxygen gas inlet regulating valve V18, regulating the flow of raw material pure carbon dioxide and pure oxygen gas entering heat exchangers E7 and E8, and controlling the temperature difference value of raw material pure carbon dioxide and pure oxygen gas at the outlets of the heat exchangers E7 and E8 to be not more than 1.2 ℃.
3. When the linkage condition that the temperature difference of pure carbon dioxide and pure oxygen at the outlets of the heat exchangers E7 and E8 is 1.2 ℃ is met, a raw material pure carbon dioxide pressure proportioning valve V22 of the air distribution device D3 is opened, an air supply valve V7 is opened, raw material pure carbon dioxide is filled into a mixed gas cylinder A8, when a partial pressure value of a raw material pure carbon dioxide pressure transmitter P5 reaches 2.0MPa, the raw material pure carbon dioxide pressure proportioning valve V22 is closed, then a raw material pure oxygen pressure proportioning valve V23 is opened, raw material pure oxygen is filled into the mixed gas cylinder A8, and when the partial pressure value of the raw material pure oxygen pressure transmitter P6 reaches 10MPa, the raw material pure oxygen pressure proportioning valve V23 is closed.
4. The PLC control system of the mixed gas distribution equipment D3 is started in an automatic stop program, and raw material pure carbon dioxide, pure oxygen inlet regulating valves V17 and V18 and an air supply valve V7 are automatically closed, so that the 2-element fresh-keeping mixed gas proportioning is completed.
Embodiment four: referring to fig. 8, a 3-element fresh-keeping mixed gas proportioning process and a device thereof.
The 3-element fresh-keeping mixed gas in the embodiment consists of oxygen with the proportion concentration of 20%, nitrogen with the proportion concentration of 30% and pure carbon dioxide with the proportion concentration of 50%. Raw material pure carbon dioxide is stored in a liquid form in a gas cylinder A5, raw material pure oxygen is stored in a gaseous form in a gas cylinder A6, and raw material pure nitrogen is stored in a gaseous form in a gas cylinder a 30.
The pressure of pure oxygen, pure nitrogen and pure carbon dioxide in the raw material gas cylinder is 15MPa of the set pressure in the national standard of gas cylinder filling, and the temperature difference between the pure oxygen and the pure nitrogen of the raw material is 5 ℃ and the temperature difference between the pure carbon dioxide of the raw material and the pure oxygen of the raw material is 15 ℃ and 20 ℃ respectively under the same condition of the atmospheric environment temperature. In the 3-element fresh-keeping mixed gas proportioning process, pure oxygen and nitrogen serving as raw materials have no phase change, are in a gaseous state, and are gasified by pure carbon dioxide serving as raw materials, and have the phase change.
The embodiment relates to a 3-element fresh-keeping mixed gas proportioning process and a device, wherein the device comprises: raw material pure carbon dioxide gas bottle A5 and supporting bottle valve A14, raw material pure oxygen gas bottle A6 and supporting bottle valve A15, raw material pure nitrogen gas bottle A30 and supporting bottle valve A30, install raw material pure carbon dioxide, raw material pure oxygen and raw material pure nitrogen three routes air inlet main pipeline respectively behind bottle valves A14, A15 and A30, three routes air inlet main pipeline divide into two routes air inlet branch pipeline respectively and connect and get into heat exchanger E30 and E31, heat exchanger E30 and E31 parallelly connected the setting. The two-way raw material pure oxygen inlet branch pipelines and the two-way raw material pure nitrogen inlet branch pipelines respectively enter the heat exchangers E30 and E31 in the forward direction, the two-way pure carbon dioxide inlet branch pipelines reversely enter the heat exchangers E30 and E31, three raw material pure gases are respectively output from three gas branch pipelines respectively distributed at the outlets of the two heat exchangers E30 and E31 after heat exchange, two output branch pipelines of the same raw material gases are summarized into a gas distribution device D30, three gas distribution pipelines of raw material pure carbon dioxide, raw material pure oxygen and raw material pure nitrogen are respectively connected with pressure proportioning valves V22, V23 and V32 of the gas distribution device D30, simultaneously three gas distribution pipelines between the outlets of the heat exchangers E30 and E31 and the pressure proportioning valves V22, V23 and V32 are respectively provided with a raw material pure carbon dioxide pressure thermal resistance thermometer T5, a raw material pure oxygen thermal resistance thermometer T6 and a raw material pure nitrogen thermal resistance thermometer T9, three gas pipelines between the pressure proportioning valves and the gas distribution valve V7 are respectively provided with a pressure proportioning valve P5, a pressure transducer P7 and a pressure transducer V7, and a pressure transducer V8 are respectively connected with the three gas distribution valve P7, and the pressure transducer V7 is connected with the pressure transducer V8.
Because the temperature difference between the pure oxygen and the pure nitrogen of the raw material is 5 ℃, the temperature difference between the pure carbon dioxide (liquid state) of the raw material, the pure oxygen and the pure nitrogen of the raw material are 15 ℃ and 20 ℃, respectively, the pure carbon dioxide of the raw material is gasified, the heat transfer quantity is larger, and the required heat transfer area is correspondingly larger, therefore, the 3-element fresh-keeping mixed gas proportioning process heat exchanger is designed to be a combination type, and consists of 2 groups of monomer heat exchangers E30 and E31. In the heat exchangers E30 and E31, pure oxygen, pure nitrogen and pure carbon dioxide are designed to exchange heat by adopting a countercurrent process, pure oxygen and pure nitrogen are designed to cool, forward flow heat release is designed, pure carbon dioxide is gasified and heated, reverse flow heat absorption is designed, namely on the heat exchangers E30 and E31, pure oxygen and pure nitrogen inlet branch pipes are arranged in the same direction and in the forward flow, and pure carbon dioxide inlet branch pipes are arranged in the reverse direction and in the reverse flow. The heat exchangers E30 and E31 are designed to be identical in model number, are arranged in parallel, and raw material pure oxygen, pure nitrogen and pure carbon dioxide are respectively led into the heat exchangers E30 and E31 through two paths of air inlet branch pipes, and the air quantity is uniformly distributed in the heat exchangers E30 and E31.
According to the optimal value obtained by experiments, the temperature difference between pure oxygen and pure nitrogen of raw materials at the forward flow same-direction outlets of the heat exchangers E30 and E31 is set to be 0.5 ℃, and the temperature difference between pure carbon dioxide of raw materials at the reverse flow outlets of the heat exchangers E30 and E31 and pure oxygen and pure nitrogen of raw materials at the forward flow outlets is set to be 1 ℃ and 1.5 ℃ respectively.
The heat exchangers E30 and E31 are plate-fin heat exchangers, and the partition plates, the fins and the sealing strips are made of aluminum alloy materials, and the heat exchange quantity is large because the raw material pure carbon dioxide is gasified and heated, so the fins of the plate-fin heat exchangers E30 and E31 are designed to be porous fins.
The raw material pure carbon dioxide pneumatic air inlet regulating valve V17 is a low-temperature single-seat regulating valve, the raw material pure oxygen and pure nitrogen pneumatic air inlet regulating valves V18 and V31 are pneumatic small-flow single-seat regulating valves, and the diameters of the valves are 20mm. The raw materials of pure oxygen, pure nitrogen and pure carbon dioxide thermal resistance thermometers T6, T9 and T5 are platinum thermal resistance thermometers.
In a PLC control system of a gas mixture distribution device, the temperature difference between the forward flow and the same-direction outlet of raw material pure oxygen and pure nitrogen in heat exchangers E30 and E31 is set to be 0.5 ℃, the temperature difference between the reverse flow outlet temperature of raw material pure carbon dioxide in the heat exchangers E30 and E31 and the forward flow outlet temperature of the raw material pure oxygen and pure nitrogen is set to be 1 ℃ and 1.5 ℃, and the temperature difference is set to be the interlocking condition that pneumatic pressure proportioning valves V23, V32 and V22 of gas distribution equipment D30 are opened.
This example shows a 3-membered fresh-keeping gas mixture (20% O) 2 +30％N 2 +50％CO 2 ) The proportioning process and the automatic operation method of the device are as follows:
1. before the mixed gas distribution device is started, a cylinder valve V14 of a raw material pure carbon dioxide (liquid) cylinder A5, a cylinder valve V15 of a raw material pure oxygen cylinder A6 and a cylinder valve V30 of a raw material pure nitrogen cylinder A30 are respectively opened. In a PLC control system of a gas mixture distribution device, a temperature difference interlocking value among a raw material pure oxygen thermal resistance thermometer T6, a raw material pure nitrogen thermal resistance thermometer T9 and a raw material pure carbon dioxide thermal resistance thermometer T5 at an outlet of a heat exchanger is set to be 0.5 ℃ and 1 ℃ respectively, 1.5 ℃, and meanwhile, a raw material pure oxygen pressure proportioning valve V23, a raw material pure nitrogen pressure proportioning valve V32 and a raw material pure carbon dioxide pressure proportioning valve V22 are set to be 2.0MPa, 5.0MPa and 10MPa respectively.
2. Starting 3-element fresh-keeping mixed gas distribution equipment D30, starting a gas distribution switch in a control system, simultaneously and automatically starting a raw material pure carbon dioxide gas inlet regulating valve V17, a pure oxygen gas inlet regulating valve V18 and a pure nitrogen gas inlet regulating valve V31, automatically regulating the flow of raw material pure carbon dioxide, pure oxygen gas and pure nitrogen gas entering heat exchangers E30 and E31 according to temperature difference set values, and controlling the temperature difference values between three raw material gases at the outlets of the heat exchangers E30 and E31 to be not more than 0.5 ℃ and 1 ℃ and 1.5 ℃ respectively.
3. When the temperature difference value of the forward flow outlet of pure oxygen and pure nitrogen of raw materials of the heat exchangers E30 and E31 is not more than 0.5 ℃, and the temperature difference value of the reverse flow outlet of pure carbon dioxide, the pure oxygen and pure nitrogen of raw materials of the forward flow outlet are not more than 1 ℃ and 1.5 ℃ respectively, the raw material pure oxygen pressure proportioning valve V23, the raw material pure nitrogen pressure proportioning valve V32 and the raw material pure carbon dioxide pressure proportioning valve V22 are sequentially opened, the air supply valve V7 is opened, and the raw material pure oxygen, pure nitrogen and pure carbon dioxide are sequentially input into the mixed gas bottle A8; when the pressure values of the raw material pure oxygen pressure transmitter P6, the pure nitrogen pressure transmitter P9 and the pure carbon dioxide pressure transmitter P5 reach the set partial pressure values of 2.0MPa, 5.0MPa and 10MPa respectively, the raw material pure oxygen pressure proportioning valve V23, the raw material pure nitrogen pressure proportioning valve V32 and the raw material pure carbon dioxide pressure proportioning valve V22 are closed successively.
4. The PLC system gas distribution stop switch of the gas mixture distribution equipment D30 is automatically put into operation, the raw material pure oxygen, pure nitrogen and pure carbon dioxide gas inlet regulating valves V18, V17 and V31 are automatically fully closed with the gas supply valve V7, and the 3-element fresh-keeping gas mixture is proportioned.
For the convenience of description and understanding of the technical scheme of the invention, the data related to the above embodiments are experimental data, the device adopts equipment, a connection mode and the like as reference for examples only, the device is not used for limiting the claims of the invention, the industrial mixed gas is various, and suitable equipment and a combination mode can be adopted on the basis of the technical principle of the technical scheme of the invention.
Claims (8)
1. The industrial mixed gas proportioning process comprises the steps of sequentially filling all the industrial pure gases forming the mixed gas into a mixed gas container with constant volume by adopting a partial pressure method, wherein the proportion concentration of all the industrial pure gases in the industrial mixed gas is represented by pressure ratio, the device sequentially comprises all the raw material pure gas storage equipment, heat exchange equipment, gas distribution equipment and a mixed gas container with constant volume according to the process flow, and the gas distribution equipment comprises a pressure proportioning valve, a gas feeding valve, a gas transmission pipeline between the pressure proportioning valve and the gas feeding valve and a pressure transmitter arranged on the gas transmission pipeline, and is characterized in that: the heat exchange equipment is additionally arranged in the existing industrial mixed gas proportioning process and device, namely, the heat exchange equipment is additionally arranged after the outlets of the pure gas storage equipment of each component raw material and before the inlets of the gas distribution equipment, and comprises a raw gas inlet pipeline between the pure gas storage equipment of each component raw material and the inlets of the heat exchangers, a heat exchanger outlet and a gas transmission pipeline between the pressure proportioning valves in the gas distribution equipment.
2. The industrial mixed gas proportioning process and device as claimed in claim 1, wherein the industrial mixed gas proportioning process and device are characterized in that: the heat exchanger is a plate-fin heat exchanger, and pure gas of each component raw material of the industrial mixed gas is not in direct contact in the heat exchanger.
3. The industrial mixed gas proportioning process and device as claimed in claim 2, wherein the industrial mixed gas proportioning process and device are characterized in that: the plate-fin heat exchanger adopts a countercurrent heat exchange process, namely raw material pure gas inlet pipelines needing heat absorption, temperature rising or gasification are arranged in the same direction as inlets connected with the heat exchanger, the inlets of the heat exchanger are reversely arranged, and raw material pure gas is reversely led into the heat exchanger; the raw material pure gas inlet pipeline needing heat release and cooling is arranged in the same direction as each inlet connected with the heat exchanger, the inlets of the heat exchanger are all arranged in the forward direction, and the raw material pure gas is all guided into the heat exchanger in the forward direction.
4. The industrial mixed gas proportioning process and device as claimed in claim 3, wherein: when the temperature difference between the pure gas sources of all the component raw materials is smaller and the pure gas sources are all in a gaseous state, and the temperature difference between the pure gas sources of all the component raw materials at the forward flow outlet and the reverse flow outlet of the plate-fin heat exchanger is not more than 1 ℃, the heat exchanger in the industrial mixed gas proportioning device is configured as a single plate-fin heat exchanger.
5. The industrial mixed gas proportioning process and device as claimed in claim 3, wherein: when the temperature difference between the pure gas sources of all the component raw materials is larger, or the phase state of the raw materials is changed from a liquid gas source gasification to a gaseous state in the mixed gas proportioning process, the temperature difference between the pure gas sources of all the component raw materials at the forward flow outlet and the reverse flow outlet of the heat exchanger is more than 1 ℃ and less than or equal to 3 ℃, and the heat exchanger in the industrial mixed gas proportioning device is configured as a combined plate-fin heat exchanger.
6. The industrial mixed gas proportioning process and device as claimed in claim 2, wherein the industrial mixed gas proportioning process and device are characterized in that: and a pneumatic air inlet regulating valve is respectively arranged in each component raw material pure gas inlet pipeline between each component raw material pure gas storage device and the inlet of the plate-fin heat exchanger.
7. The industrial mixed gas proportioning process and device as claimed in claim 6, wherein the industrial mixed gas proportioning process and device are characterized in that: and a thermal resistance thermometer is respectively arranged on a gas pipeline between a pure gas outlet of each component raw material of the plate-fin heat exchanger and a pressure proportioning valve in the gas distribution equipment.
8. The industrial mixed gas proportioning process and device as claimed in claim 7, wherein: and the automatic control program of the heat exchange procedure is integrated into an automatic control system of the mixture ratio, an air inlet regulating valve arranged on a raw material air inlet pipeline between the pure gas storage equipment of each component raw material and the inlet of the heat exchanger, and a thermometer arranged on an air transmission pipeline between the outlet of the heat exchanger and the pressure proportioning valve of the distribution equipment are connected into the automatic control system of the mixture ratio, and the temperature difference value between the raw material gases of each component at the outlet of the heat exchanger is set as the interlocking control condition of the air inlet regulating valve.
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| CN202311848306.8A CN117815948A (en) | 2023-12-29 | 2023-12-29 | Industrial mixed gas proportioning process and device |
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| CN202311848306.8A CN117815948A (en) | 2023-12-29 | 2023-12-29 | Industrial mixed gas proportioning process and device |
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