CN108072234B - Control method of air separation device - Google Patents
Control method of air separation device Download PDFInfo
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- CN108072234B CN108072234B CN201611021408.2A CN201611021408A CN108072234B CN 108072234 B CN108072234 B CN 108072234B CN 201611021408 A CN201611021408 A CN 201611021408A CN 108072234 B CN108072234 B CN 108072234B
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- air separation
- fractionating tower
- tower system
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- molecular sieve
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- 238000000926 separation method Methods 0.000 title claims abstract description 108
- 238000000034 method Methods 0.000 title claims abstract description 48
- 239000002808 molecular sieve Substances 0.000 claims abstract description 54
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 54
- 239000011810 insulating material Substances 0.000 claims abstract description 26
- 239000012774 insulation material Substances 0.000 claims abstract description 23
- 238000009833 condensation Methods 0.000 claims abstract description 4
- 230000005494 condensation Effects 0.000 claims abstract description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 112
- 239000007788 liquid Substances 0.000 claims description 82
- 229910052757 nitrogen Inorganic materials 0.000 claims description 56
- 239000002699 waste material Substances 0.000 claims description 32
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 21
- 239000001301 oxygen Substances 0.000 claims description 21
- 229910052760 oxygen Inorganic materials 0.000 claims description 21
- 230000009467 reduction Effects 0.000 abstract description 4
- 238000010438 heat treatment Methods 0.000 description 29
- 239000007789 gas Substances 0.000 description 19
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 14
- 238000005265 energy consumption Methods 0.000 description 14
- 238000005194 fractionation Methods 0.000 description 14
- 229910001562 pearlite Inorganic materials 0.000 description 8
- 239000004576 sand Substances 0.000 description 8
- 229910052786 argon Inorganic materials 0.000 description 7
- 238000001704 evaporation Methods 0.000 description 7
- 230000008020 evaporation Effects 0.000 description 6
- 230000000630 rising effect Effects 0.000 description 6
- 238000001179 sorption measurement Methods 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 238000000605 extraction Methods 0.000 description 4
- 238000010926 purge Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 229920006395 saturated elastomer Polymers 0.000 description 4
- GWVKDXOHXJEUCP-UHFFFAOYSA-N [N].[O].[Ar] Chemical compound [N].[O].[Ar] GWVKDXOHXJEUCP-UHFFFAOYSA-N 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- OLBVUFHMDRJKTK-UHFFFAOYSA-N [N].[O] Chemical compound [N].[O] OLBVUFHMDRJKTK-UHFFFAOYSA-N 0.000 description 2
- 238000007664 blowing Methods 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910052743 krypton Inorganic materials 0.000 description 1
- DNNSSWSSYDEUBZ-UHFFFAOYSA-N krypton atom Chemical compound [Kr] DNNSSWSSYDEUBZ-UHFFFAOYSA-N 0.000 description 1
- 238000011068 loading method 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
- 239000000126 substance Substances 0.000 description 1
- 210000004243 sweat Anatomy 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 229910052724 xenon Inorganic materials 0.000 description 1
- FHNFHKCVQCLJFQ-UHFFFAOYSA-N xenon atom Chemical compound [Xe] FHNFHKCVQCLJFQ-UHFFFAOYSA-N 0.000 description 1
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04812—Different modes, i.e. "runs" of operation
- F25J3/04824—Stopping of the process, e.g. defrosting or deriming; Back-up procedures
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2280/00—Control of the process or apparatus
- F25J2280/30—Control of a discontinuous or intermittent ("batch") process
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention provides a control method of an air separation device, the air separation device comprises a cold box, a fractionating tower system positioned in the cold box, a heat insulation material filled in the cold box, a compressor and a molecular sieve adsorber connected between the compressor and the fractionating tower system, the fractionating tower system comprises an upper tower, a lower tower and a main condensation evaporator connected between the upper tower and the lower tower and communicated with the upper tower, the control method of the air separation device comprises the following steps: when the air separation device is shut down, the compressor and the molecular sieve adsorber are controlled to be closed, and the fractionating tower system is not heated, so that the temperature of the fractionating tower system is not higher than that of the heat-insulating material. According to the control method of the air separation device, when the air separation device is shut down, the fractionating tower system is not heated, so that the temperature of the fractionating tower system is increased due to heat exchange between the fractionating tower system and the heat insulation material, and the negative suction phenomenon caused by pressure reduction in the fractionating tower system is avoided.
Description
Technical Field
The invention relates to the technical field of air separation, in particular to a control method of an air separation device.
Background
The air separation device (air separation plant) is a high energy consumption plant, the energy consumption of the air separation plant is very large, the energy consumption of the air separation plant used in the chemical industry and the metallurgical industry at present accounts for more than 10% of the total energy consumption, the energy consumption of the air separation plant in operation accounts for more than 80% of the total cost, and the raw material air compressor (compressor) is also an energy consumption major household of the air separation plant.
The existing low-temperature deep-cooling air separation equipment adopts the adsorption of the front end of a molecular sieve to remove moisture, carbon dioxide and hydrocarbon in raw material air, and the process does not provide a separate heating flow path (a drier, a Roots blower and a heater are heating pipelines), but directly uses the positive flow raw material air dried by a molecular sieve adsorber to heat a fractionating tower system (a main heat exchanger, an upper tower, a lower tower, a subcooler, a crude argon I tower, a crude argon II tower, a fine argon tower, a pipeline, a krypton, xenon, neon and helium rare gas separation tower and the like) in a cold box, so that many air separation equipment are heated by starting a raw material air compressor, and the heating time-space compressor also has great diffusion and energy consumption.
The conventional operation regulations stipulate that the low-temperature cryogenic air separation equipment needs to be drained when the air separation equipment is shut down for more than 48 hours, and the air separation equipment needs to be heated systematically before the air separation equipment is shut down or (and) started. The system heating is to stop the machine after heating the equipment in the cold box to 5-10 ℃, the time of the process is different, and the general oxygen nitrogen argon three-high process needs about 24 hours.
The traditional heating method consumes more energy, and easily causes the negative suction of outside air into a fractionating tower system, when the air separation device is started again, the air separation device must be thoroughly heated to be dried, thereby further increasing the energy consumption.
Disclosure of Invention
The present invention is directed to solving at least one of the problems of the prior art.
To this end, the invention aims to provide a control method of an air separation unit.
In order to achieve the above object, an embodiment of the present invention provides a method for controlling an air separation apparatus, the air separation apparatus including a cold box, a fractionating tower system located in the cold box, a thermal insulation material filled in the cold box, a compressor, and a molecular sieve adsorber connected between the compressor and the fractionating tower system, the fractionating tower system including an upper tower, a lower tower, and a main condensing evaporator connected between the upper tower and the lower tower and communicated with the upper tower, the method comprising: and when the air separation device stops working, the compressor and the molecular sieve adsorber are controlled to be closed, and the fractionating tower system is not heated, so that the temperature of the fractionating tower system is not higher than that of the heat-insulating material.
In the control method of the air separation apparatus provided in the above embodiment of the present invention, when the apparatus is shut down, the compressor and the molecular sieve adsorber are turned off, and the fractionating tower system is not heated, so that the temperature of the fractionating tower system is not higher than the temperature of the heat insulating material, where the temperature of the fractionating tower system 1 refers to the average temperature of the fractionating tower system 1, and the temperature of the heat insulating material refers to the average temperature of the heat insulating material, so that when the temperature of the fractionating tower system is lower than the temperature of the heat insulating material, the temperature of the fractionating tower system can be increased by exchanging heat with the heat insulating material, so that the pressure in the fractionating tower system is not lower than the atmospheric pressure, and when the temperature of the fractionating tower system is equal to the temperature of the heat insulating material, the fractionating tower system and the heat insulating material exchange heat with the outside, so that the temperature of the fractionating tower system, the negative suction cannot be caused, and then external wet air cannot enter the fractionating tower system, so that when the air separation device is started up again and heated, the air separation device does not need to be thoroughly heated and blown for a long time, the energy consumption is reduced, and compared with the prior art, the air separation device is heated once when stopped and started up, the heating operation is not required to be heated when stopped, the heating operation frequency is reduced, and the energy consumption is further reduced.
Specifically, in the related art, when the air separation device is shut down, the heat insulation material in the cold box is still in a low-temperature state, so if the air separation device is heated, the temperature change trend in the fractionating tower system before and after heating is in a low-high-low-high condition, namely, the temperature of the fractionating tower system in the cold box is increased from the heating time when the system is heated, the temperature is decreased after the equipment absorbs the cold energy in the heat insulation material after the heating is stopped, and if the air separation device is shut down continuously for a long time, the temperatures of the fractionating tower system and the heat insulation material exchange heat with the outside again after the temperatures of the heat insulation material and the fractionating tower system reach a balance, so that the temperature is increased. 6500m3For example, the air separation device is heated to 5 ℃, after the heating is stopped, the temperature of the main tower is reduced to-40 ℃ and the temperature of the crude argon tower and the like reaches below-60 ℃ after the cold quantity of the heat insulation material in the cold box is absorbed by the fractionating tower system, and when the temperature of the fractionating tower system is reduced, the volume of the gas in the original fractionating tower is reduced, so that the outside air is sucked in a negative way. The calculation is as follows: the total volume of the fractionating tower system is R, the gas in the fractionating tower system is regarded as ideal gas, the temperature is T1-5-278K and the pressure is P1 after the heating is finished, and the heat-insulating material transmits cold energy after the heating is stoppedThe temperature is delivered to a fractionating tower system, the average temperature of the fractionating tower system in a cold box is reduced to T2 which is equal to minus 40 ℃ and equal to 233K, and P2 which is equal to P1 multiplied by T2/T1 which is equal to 233/278 which is equal to 0.84, the volume is reduced to 84 percent of the original volume, the pressure in the tower is reduced, negative pressure is formed instead to cause negative absorption of wet air, the volume of the original gas is reduced in the shutdown stage in a pressure-time curve, and the pressure is lower than the atmospheric pressure P0 (a dotted line in figure 2); when restarting, because of the wet air entering, the drying must be done by heating thoroughly, and the two heating increases the energy consumption.
Do not heat after shutting down in this application, no matter fractionating tower system and insulation material heat transfer or fractionating tower system and insulation material be together with external heat transfer, the temperature of whole fractionating tower system is in the in-process that rises all the time, and temperature T > T0 before the start anytime, then pressure P (T/T0) P0>1, wherein, P0 is atmospheric pressure, is the malleation all the time in the so fractionating tower system, can not lead to the burden and inhale.
In addition, the control method of the air separation device provided by the above embodiment of the present invention further has the following additional technical features:
in the above technical solution, preferably, before the air separation unit is shut down, the air separation unit is controlled to discharge a part of the liquid in the upper column and discharge the liquid in the lower column.
In the above embodiment, the liquid is discharged under pressure before the air separation apparatus is stopped, the lower tower is drained of the liquid, the upper tower is not drained of the liquid, and the upper tower is communicated with the main condensing evaporator, so that the liquid remaining in the upper tower flows into the main condensing evaporator. Liquid evaporates naturally along with the heat transfer of cold box and external world, when beginning to evaporate, forms the malleation in the tower, even the liquid evaporates completely the back, does not have the malleation in the tower, though fractionating tower system and insulation material are the low temperature state, nevertheless along with external heat transfer, the temperature of fractionating tower system and insulation material rises back naturally, can not appear the temperature reduction, can not cause the gaseous volume in the tower to reduce and form the negative pressure to external humid air can't get into in the fractionating tower system.
In the above technical solution, preferably, the liquid level of the liquid left in the upper tower is less than or equal to twenty-five percent of the normal liquid level of the main condensation evaporator, so as to avoid that the amount of the liquid left is too much, which results in too long time for evaporating the liquid.
In the above technical solution, preferably, the liquid level of the liquid left in the upper tower accounts for fifteen percent of the normal liquid level of the main condensing evaporator.
In the above technical solution, preferably, the upper tower is connected to a product output line, the product output line is provided with a control valve, and the control method of the air separation apparatus further includes: and before the liquid left in the upper tower is completely evaporated, controlling and adjusting the opening of the control valve so as to ensure that the pressure in the fractionating tower system is not less than the atmospheric pressure.
In the above embodiment, before the liquid left in the upper tower is evaporated, the fractionating tower system exhausts the gas to the outside, and the opening of the control valve is adjusted, so that the pressure in the fractionating tower system is not over-pressure or lower than the atmospheric pressure P0 due to the evaporation of the liquid, thereby ensuring that the external wet air cannot enter the fractionating tower system. In one embodiment, the pressure in the fractionation column system can be made neither overpressure nor less than atmospheric pressure by reducing the opening of the control valve. Of course, the opening of the control valve may not be adjusted to be small, and in this case, the pressure in the fractionation column system may be equal to the atmospheric pressure.
In the above technical solution, preferably, the product output pipeline includes an oxygen output pipeline, a nitrogen output pipeline and a waste nitrogen output pipeline; the control valve comprises an oxygen control valve arranged on the oxygen output pipeline, a nitrogen control valve arranged on the nitrogen output pipeline and a waste nitrogen control valve arranged on the waste nitrogen output pipeline.
Before the liquid left in the upper tower is evaporated, the opening of the oxygen control valve, the nitrogen control valve and the waste nitrogen control valve are all reduced, so that the pressure in the fractionating tower system is greater than the atmospheric pressure. Of course, only one or two of the oxygen control valve, the nitrogen control valve, and the dirty nitrogen control valve may be adjusted small, or one or two thereof may be closed.
In the above technical solution, preferably, the molecular sieve adsorber is connected to the waste nitrogen output pipeline, and valves are disposed on a connection pipeline between the molecular sieve adsorber and the waste nitrogen output pipeline, a connection pipeline between the molecular sieve adsorber and the compressor, and a connection pipeline between the molecular sieve adsorber and the fractionating tower system, and the control method of the air separation apparatus further includes: and controlling the valve to be closed before the liquid left in the upper tower is completely evaporated.
In the above embodiment, the molecular sieve adsorber is connected to the compressor through the first connection line, connected to the fractionating tower system through the second connection line, and connected to the waste nitrogen output line through the third connection line, wherein valves (switching valves) are respectively disposed on the first connection line, the second connection line, and the third connection line, wherein on/off of the switching valves is controlled to adjust and adjust the operating modes of the two molecular sieve adsorbers (air enters one molecular sieve adsorber, after the molecular sieve adsorber is saturated, the air is controlled to enter the other molecular sieve adsorber to continue to adsorb, the molecular sieve adsorber with saturated adsorption is heated by inputting high-temperature waste nitrogen, and then the molecular sieve adsorber is cooled by inputting cold waste nitrogen, so that the molecular sieve adsorber recovers the adsorption capacity). Preferably, the air separation unit comprises two molecular sieve adsorbers.
Before the liquid in the upper tower is completely evaporated, the valve is closed to prevent the wet air from entering the fractionating tower system through the molecular sieve adsorber.
In the above technical solution, preferably, the control method of the air separation apparatus further includes: and after the liquid remained in the upper tower is completely evaporated, controlling the control valve to be closed.
After the liquid left in the upper tower is evaporated, when the temperature of the upper tower is slightly raised, the control valve is closed to prevent the wet air from entering the fractionating tower system through the oxygen output pipeline, the nitrogen output pipeline and the waste nitrogen output pipeline. Because no liquid is evaporated in the upper column at this time, no overpressure condition occurs in the fractionation column system by closing the control valve.
In the above embodiment, after the liquid left in the upper tower is evaporated, the oxygen control valve, the nitrogen control valve and the waste nitrogen control valve are closed, so as to prevent external wet air from entering the fractionating tower system through the oxygen output pipeline, the nitrogen output pipeline and the waste nitrogen output pipeline.
After the liquid is completely evaporated, the fractionating tower system and the heat insulating material exchange heat with the outside, the temperature is raised, the gas in the fractionating tower system expands, and the pressure in the fractionating tower system may be slightly higher than the atmospheric pressure or equal to the atmospheric pressure.
In the above technical solution, preferably, the control method of the air separation apparatus further includes: and before the air separation device is started again, the compressor and the molecular sieve adsorber are controlled to be started so as to heat the fractionating tower system.
In the above technical solution, preferably, the heat insulating material is pearlite sand.
The air separation device comprises high-purity nitrogen equipment, oxygen-nitrogen double-high equipment, oxygen-nitrogen-argon triple-high equipment and rare gas partial extraction or total extraction equipment. The control method of the air separation device is characterized in that when the air separation device is stopped intermittently for a long time (generally more than 48 hours), liquid in the fractionating tower is not discharged completely during the stop, the liquid is naturally evaporated to keep the micro-positive pressure, and the system is not required to be heated and thawed before the air separation device is stopped or started, so that the air separation device is suitable for occasions that the low-temperature air separation device with the molecular sieve adsorber at the front end is stopped for a long time but does not overhaul the pearlite sand.
Even if the residual liquid in the tower is evaporated to cause cold quantity to move outwards, certain low temperature is formed at the outlet of the product pipe, at most, only a small amount of wet air is condensed on the inner wall at the outlet of the product pipe and cannot enter the equipment, and the moisture is blown off when the gas flowing back during driving passes through.
Additional aspects and advantages of the invention will be set forth in part in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention.
Drawings
The above and/or additional aspects and advantages of the present invention will become apparent and readily appreciated from the following description of the embodiments, taken in conjunction with the accompanying drawings of which:
FIG. 1 is a schematic view showing the relationship between the temperature in a fractionating tower system according to the related art and the change with time;
FIG. 2 is a schematic diagram showing the pressure in the fractionation column system as a function of time in the related art;
FIG. 3 is a schematic structural view of an air separation unit according to an embodiment of the present invention;
FIG. 4 is a schematic flow diagram of a method of controlling an air separation plant according to an embodiment of the present invention;
FIG. 5 is a schematic diagram of temperature in a fractionation column system over time according to an embodiment of the present invention;
fig. 6 is a schematic of the pressure inside the fractionation column system as a function of time according to an embodiment of the present invention.
Wherein, the corresponding relationship between the reference numbers and the names of the components in fig. 3 is:
1 fractionating tower system, 2 heat-insulating material, 3 compressor, 4 molecular sieve adsorber and 5 cold box.
Detailed Description
In order that the above objects, features and advantages of the present invention can be more clearly understood, a more particular description of the invention will be rendered by reference to the appended drawings. It should be noted that the embodiments and features of the embodiments of the present application may be combined with each other without conflict.
In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention, however, the present invention may be practiced otherwise than as specifically described herein, and thus the scope of the present invention is not limited by the specific embodiments disclosed below.
A method of controlling an air separation plant according to some embodiments of the invention is described below with reference to the accompanying drawings.
As shown in fig. 3 and 4, according to some embodiments of the present invention, there is provided a method for controlling an air separation apparatus, the air separation apparatus includes a cold box 5, a fractionating tower system 1 located in the cold box 5, a thermal insulation material 2 filled in the cold box 5, a compressor 3, and a molecular sieve adsorber 4 connected between the compressor 3 and the fractionating tower system 1, the fractionating tower system 1 includes an upper tower, a lower tower, and a main condensing evaporator connected between and communicating with the upper tower, the method for controlling the air separation apparatus includes: when the air separation device is shut down, the compressor 3 and the molecular sieve adsorber 4 are controlled to be closed, and the fractionating tower system 1 is not heated, so that the temperature of the fractionating tower system 1 is not higher than that of the heat insulation material 2.
In the control method of the air separation device provided in the above embodiment of the present invention, when the air separation device is shut down, the compressor 3 and the molecular sieve adsorber 4 are closed, and the fractionating tower system 1 is not heated, so that the temperature of the fractionating tower system 1 is not higher than the temperature of the heat insulating material 2, where the temperature of the fractionating tower system 1 refers to the average temperature of the fractionating tower system 1, and the temperature of the heat insulating material 2 refers to the average temperature of the heat insulating material 2, so that when the temperature of the fractionating tower system 1 is lower than the temperature of the heat insulating material 2, the temperature of the fractionating tower system 1 can be raised by exchanging heat with the heat insulating material 2, so that the temperature of the fractionating tower system 1 is not lower than the internal pressure and the atmospheric pressure, and when the temperature of the fractionating tower system 1 is equal to the temperature of the heat insulating material 2, the fractionating tower system 1 and the heat insulating material, similarly, the pressure in the fractionating tower system 1 is not lower than the atmospheric pressure, negative suction cannot be caused, and then external wet air cannot enter the fractionating tower system 1, so that when the air separation device is started up again and heated, long-time thorough heating and purging are not needed, the energy consumption is reduced, and compared with the prior art that heating is carried out once when the air separation device is stopped and started up, heating is not needed when the air separation device is stopped, the heating operation frequency is reduced, and the energy consumption is further reduced.
Specifically, in the related art, the fractionation tower system 1 is heated during shutdown, and since the thermal insulation material 2 in the cold box 5 is still in a low temperature state after the air separation apparatus has been operated for a long time, if the system is heated, as shown in fig. 1, the temperature change trend in the fractionation tower system before and after heating is in a "low-high-low-high" condition, that is, the temperature of the fractionation tower system 1 in the cold box 5 is first raised to T1 when the system is heated, and then the temperature is lowered to T2 after the equipment absorbs the cold in the thermal insulation material 2 after the heating is stopped, and if the system is continuously stopped for a long time, after the temperatures of the thermal insulation material 2 and the fractionation tower system 1 reach equilibrium, the fractionation tower system 1 and the thermal insulation material 2 are again lowered to T2 again after theThe heat exchange with the outside is carried out, the temperature is increased, and the temperature is increased when the starting is carried out again at the position A1 in figure 1. At 6500m3For example, the air separation device is heated to 5 ℃, after the heating is stopped, the fractionating tower system 1 absorbs the cold energy of the heat insulating material 2 in the cold box 5, the temperature of the main tower is reduced to-40 ℃, the temperature of the crude argon tower and the like reaches below-60 ℃, and when the temperature of the fractionating tower system 1 is reduced, the volume of the gas in the original fractionating tower is reduced, so that the outside air is sucked in a negative way. The calculation is as follows: the total volume of the fractionating tower system 1 is R, the gas in the fractionating tower system 1 is regarded as an ideal gas, the temperature at the end of heating is T1 ℃ ═ 5 ℃ ═ 278K, as shown in fig. 2, the pressure is P1, the section a2 in fig. 2 represents the heating process, after the heating is stopped, the heat insulating material 2 transmits cold energy to the fractionating tower system 1, the average temperature of the fractionating tower system 1 in the cold box 5 is reduced to T2 ℃ ═ 40 ℃ ═ 233K, and the section P2 ═ P1 × T2/T1 ═ 233/278 ═ 0.84, then the volume is reduced to 84% of the original volume, the pressure in the tower is reduced, and negative pressure is formed, and accordingly, the original volume of the wet air is reduced, and the pressure is lower than the atmospheric pressure P4 (dotted line in fig. 2) in the shutdown phase A3 in the pressure curve of fig. 2; when restarting (section a4 in fig. 2), because of the wet air entering, it is necessary to warm more thoroughly for drying, and this two warming times increases the energy consumption.
The back does not heat up stopping in this application, no matter fractionating tower system 1 and insulation material 2 heat transfer or fractionating tower system 1 and insulation material 2 together with external heat transfer, whole fractionating tower system 1's temperature is in the in-process that rises all the time, as shown in fig. 5 and fig. 6, temperature T > T0 at any time before the start-up, then pressure P ═ is (T/T0) P0>1, wherein, P0 is atmospheric pressure, so be the malleation in the fractionating tower system all the time, can not lead to the negative suction.
Preferably, the air separation unit is controlled to remove a portion of the liquid from the upper column and to remove liquid from the lower column before the air separation unit is shut down.
In the above embodiment, the liquid is discharged under pressure before the air separation apparatus is stopped, the lower tower is drained of the liquid, the upper tower is not drained of the liquid, and the upper tower is communicated with the main condensing evaporator, so that the liquid remaining in the upper tower flows into the main condensing evaporator. Liquid evaporates naturally along with cold box 5 and external heat transfer, when beginning to evaporate, forms the malleation in the tower, even liquid evaporates the back completely, does not have the malleation in the tower, though fractionating tower system 1 and insulation material 2 are the low temperature state, nevertheless along with external heat transfer, the temperature of fractionating tower system 1 and insulation material 2 rises back naturally, can not appear the temperature reduction, can not cause the gaseous volume in the tower to reduce and form the negative pressure to external humid air can't get into in the fractionating tower system 1.
Preferably, the liquid level of the liquid left in the upper tower accounts for less than or equal to twenty-five percent of the normal liquid level of the main condensing evaporator, so that the phenomenon that the amount of the liquid left is too much, which causes too long liquid evaporation time, is avoided.
Preferably, the level of liquid remaining in the upper column is equal to fifteen percent of the normal level of the main condenser evaporator.
Preferably, the upper tower is connected with a product output pipeline, the product output pipeline is provided with a control valve, and the control method of the air separation device further comprises the following steps: before the liquid in the upper tower is completely evaporated, the opening of the control valve is controlled and adjusted so that the pressure in the fractionating tower system 1 is not less than the atmospheric pressure.
In the above embodiment, as shown in fig. 6, before the liquid left in the upper column is evaporated, the fractionating column system 1 exhausts the gas to the outside, and the opening of the control valve is controlled, so that the pressure in the fractionating column system 1 is not lower than the atmospheric pressure P0 due to the evaporation of the liquid, thereby ensuring that the external humid air cannot enter the fractionating column system 1. Of course, the opening degree of the control valve may not be set small, and in this case, the pressure in the fractionation column system 1 may be equal to the atmospheric pressure.
Preferably, the product output lines include an oxygen output line, a nitrogen output line, and a waste nitrogen output line; the control valve comprises an oxygen control valve arranged on the oxygen output pipeline, a nitrogen control valve arranged on the nitrogen output pipeline and a waste nitrogen control valve arranged on the waste nitrogen output pipeline.
Before the liquid left in the upper tower is evaporated, the opening degree of the oxygen control valve, the opening degree of the nitrogen control valve and the opening degree of the waste nitrogen control valve are all adjusted to be small, so that the pressure in the fractionating tower system 1 is larger than the atmospheric pressure. Of course, only one or two of the oxygen control valve, the nitrogen control valve, and the dirty nitrogen control valve may be adjusted small, or one or two thereof may be closed.
Preferably, as shown in fig. 3, the molecular sieve adsorber 4 is connected to the waste nitrogen output pipeline, wherein valves are disposed on a connection pipeline between the molecular sieve adsorber 4 and the compressor 3, a connection pipeline between the molecular sieve adsorber 4 and the fractionating tower system 1, and a connection pipeline between the molecular sieve adsorber 4 and the waste nitrogen output pipeline, and the control method of the air separation apparatus further includes: the control valve is closed before the liquid remaining in the upper column is completely evaporated. Preferably, two molecular sieve adsorbers 4 are provided between the compressor 3 and the fractionating column system 1.
In the above embodiment, the molecular sieve adsorber 4 is connected to the compressor 3 through a first connecting line, connected to the fractionating tower system 1 through a second connecting line, and connected to the waste nitrogen output line through a third connecting line, wherein valves (switching valves) are respectively disposed on the first connecting line, the second connecting line, and the third connecting line, wherein on/off of the switching valves is controlled, so as to adjust the operating modes of the two molecular sieve adsorbers 4 (air enters one molecular sieve adsorber 4, after the molecular sieve adsorber 4 is saturated, the air is controlled to enter the other molecular sieve adsorber 4 to continue adsorption, and for the molecular sieve adsorber 4 with saturated adsorption, high-temperature waste nitrogen is input to heat the molecular sieve adsorber 4, and then cold waste nitrogen is input to cool the molecular sieve adsorber 4, so that the molecular sieve adsorber 4 recovers the adsorption capacity).
Before the liquid in the upper tower is completely evaporated, the valve is closed to prevent the wet air from entering the fractionating tower system 1 through the molecular sieve adsorber 4.
Preferably, the control method of the air separation plant further comprises: after the liquid remained in the upper tower is completely evaporated, the control valve is closed.
After the liquid left in the upper tower is evaporated, the control valve is closed when the temperature of the upper tower is slightly raised, and the wet air is prevented from entering the fractionating tower system 1 through the oxygen output pipeline, the nitrogen output pipeline and the waste nitrogen output pipeline. Because no liquid is evaporated in the upper column at this time, no overpressure will occur in the fractionation column system 1 by closing the control valve.
In the above embodiment, after the liquid remaining in the upper tower is evaporated, the oxygen control valve, the nitrogen control valve and the waste nitrogen control valve are closed, so as to prevent the external humid air from entering the fractionating tower system 1 through the oxygen output pipeline, the nitrogen output pipeline and the waste nitrogen output pipeline.
After the liquid is completely evaporated, the fractionating tower system 1 and the heat insulating material 2 exchange heat with the outside, the temperature is increased, the gas in the fractionating tower system 1 is expanded, and the pressure in the fractionating tower system 1 may be slightly higher than the atmospheric pressure or equal to the atmospheric pressure.
Preferably, the control method of the air separation plant further comprises: before the air separation device is started again, the compressor 3 and the molecular sieve adsorber 4 are controlled to be started so as to heat the fractionating tower system 1.
In the above technical solution, preferably, the heat insulating material 2 is pearlite sand.
When the machine is stopped, only the liquid is discharged and not heated, even a certain amount of liquid is left, the residual liquid in the upper tower is evaporated to form positive pressure at the beginning, even if the liquid is evaporated, the positive pressure does not exist in the fractionating tower system 1, as shown in fig. 5, although the fractionating tower system 1 and the pearlite sand are in a low-temperature state, the temperature naturally rises, the temperature rising curve is also in a single side and upwards, the temperature rising curve is always in the rising process, the process of descending from high to low cannot be caused, the volume is reduced to form negative pressure, the liquid is completely evaporated at the position B in fig. 5, the heating is started again at the position C, the pressure curve in the fractionating tower system 1 is divided into two sections in fig. 6, the first section has liquid vaporization pressure rising, but actually exhausts the gas, the second section has no liquid, the gas in the tower rises along with the pearlite sand, the volume slowly expands, the pressure is also rising, but the slope is small, where D indicates that the liquid has evaporated, and possibly the actual pressure in the fractionation tower system 1 is slightly above atmospheric pressure (atmospheric pressure is shown by the dotted line a in fig. 3), the oxygen control valve, the nitrogen control valve, and the waste nitrogen control valve may be closed at this stage to avoid the entry of humid air as much as possible. As shown in FIG. 6, in both stages I and II, the pressure is always greater than the atmospheric pressure P0, and no negative pressure is generated.
The air separation device comprises high-purity nitrogen equipment, oxygen-nitrogen double-high equipment, oxygen-nitrogen-argon triple-high equipment and rare gas partial extraction or total extraction equipment. The control method of the air separation device is characterized in that when the air separation device is stopped intermittently for a long time (generally more than 48 hours), liquid in the fractionating tower is not discharged completely during the stop, the liquid is naturally evaporated to keep the micro-positive pressure, and the system is not required to be heated and thawed before the air separation device is stopped or started, so that the air separation device is suitable for occasions that the low-temperature air separation device with the molecular sieve adsorber 4 at the front end is stopped for a long time but the pearlite sand is not overhauled.
In one embodiment of the invention, for a 6500m stand3In the air separation equipment, when the air separation device is shut down, only liquid discharged by the air separation device is not heated, a small amount of liquid is left in the upper tower to be naturally evaporated, the liquid basically evaporates light after about 8 days (the temperature of the fractionating tower system 1 does not basically rise after evaporation is finished, and the temperature of the fractionating tower system 1 starts rising after evaporation is finished, as shown in figure 5), the temperature of the middle part of the main heat exchanger is reduced due to liquid evaporation, and a small amount of sweat and frost are generated at the hot end. When the system is restarted after 26 days, purging is carried out on the system for more than 0.5 hour, all equipment is not heated to the normal temperature completely, the temperature of an argon tower is still about-30 ℃ when the turbo expander is started after purging is finished (the argon tower is generally difficult to heat), the cooling speed of the air separation device is higher when the air separation device is started, the temperature of the middle part of a main heat exchanger is also normal after liquid loading is finished and one expander is stopped, and then the air separation device runs all normally.
Purging for 0.5h only, firstly, because the molecular sieve adsorber 4 of the molecular sieve flow device is completely normal in the previous operation, the content of carbon dioxide and the like discharged from the adsorber is very low, and in addition, the resistance of the main heat exchanger is not increased, and as long as the system does not generate negative absorption, the humid air cannot go deep into the system; and secondly, even if a small amount of moisture is frozen at the pipe openings of the return product pipes (the oxygen output pipeline, the nitrogen output pipeline and the waste nitrogen output pipeline), when the blowing is restarted or even after the normal start-up is carried out, the return gas from the product pipes is not only dried under low pressure but also reheated at normal temperature, and can remove and take away the moisture. On the contrary, if the liquid is heated after being discharged, negative absorption is caused, wet air enters, and the relatively thorough heating and blowing for a long time is needed when restarting is carried out, so that the experience needs to thoroughly re-heat the liquid, generally 10 to 12 hours, but the experience is not goodBecome energy waste (set 6500 m)3Heating the air separation plant for 34h before and after the air separation plant for total power consumption of about 15 ten thousand KWh).
Even if the residual liquid in the tower is evaporated to cause cold quantity to move outwards, certain low temperature is formed at the outlet of the product pipe, at most, only a small amount of wet air is condensed on the inner wall at the outlet of the product pipe and cannot enter the equipment, and the moisture is blown off when the gas flowing back during driving passes through.
In summary, in the control method of the air separation device provided in the embodiment of the present invention, when the air separation device is shut down, the compressor 3 and the molecular sieve adsorber 4 are closed, so that the fractionating tower system 1 is not heated, the temperature of the fractionating tower system 1 is raised by heat exchange with the pearlite sand, and further the pressure in the fractionating tower system 1 is not lower than atmospheric pressure, negative absorption cannot be caused, and then external wet air cannot enter the fractionating tower system 1, thereby avoiding temperature reduction of the fractionating tower system 1 caused by heat exchange between the heated fractionating tower system 1 and the pearlite sand, and further negative absorption of the fractionating tower system 1.
In the description of the present invention, the term "plurality" means two or more unless explicitly specified or limited otherwise; the terms "connected," "secured," and the like are to be construed broadly and unless otherwise stated or indicated, and for example, "connected" may be a fixed connection, a removable connection, an integral connection, or an electrical connection; may be directly connected or indirectly connected through an intermediate. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
In the description of the present specification, it is to be understood that the terms "upper", "lower", "front", "rear", "left", "right", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of describing the present invention and simplifying the description, but do not indicate or imply that the referred device or unit must have a specific direction, be configured and operated in a specific orientation, and thus, should not be construed as limiting the present invention.
In the description herein, the description of the terms "one embodiment," "some embodiments," "specific embodiments," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A method for controlling an air separation apparatus, the air separation apparatus comprising a cold box, a fractionating tower system located in the cold box, a thermal insulation material filled in the cold box, a compressor, and a molecular sieve adsorber connected between the compressor and the fractionating tower system, the fractionating tower system comprising an upper tower, a lower tower, and a main condensing evaporator connected between the upper tower and the lower tower and in communication with the upper tower, the method comprising:
and when the air separation device stops working, the compressor and the molecular sieve adsorber are controlled to be closed, and the fractionating tower system is not heated, so that the temperature of the fractionating tower system is not higher than that of the heat-insulating material.
2. The method of controlling an air separation plant of claim 1, further comprising:
and before the air separation device is stopped, controlling the air separation device to discharge part of liquid in the upper tower and discharge liquid in the lower tower.
3. The control method of an air separation plant according to claim 2,
and the liquid left in the upper tower accounts for less than or equal to twenty-five percent of the normal liquid level of the main condensation evaporator.
4. The control method of an air separation plant according to claim 3,
the liquid left in the upper tower accounts for fifteen percent of the normal liquid level of the main condensation evaporator.
5. The control method of an air separation plant according to any one of claims 2 to 4,
the upper tower is connected with a product output pipeline, the product output pipeline is provided with a control valve, and the control method of the air separation device further comprises the following steps: and before the liquid left in the upper tower is completely evaporated, controlling and adjusting the opening of the control valve so as to ensure that the pressure in the fractionating tower system is not less than the atmospheric pressure.
6. The control method of an air separation plant according to claim 5,
the product output pipeline comprises an oxygen output pipeline, a nitrogen output pipeline and a waste nitrogen output pipeline;
the control valve comprises an oxygen control valve arranged on the oxygen output pipeline, a nitrogen control valve arranged on the nitrogen output pipeline and a waste nitrogen control valve arranged on the waste nitrogen output pipeline.
7. The control method of an air separation plant according to claim 6,
the molecular sieve adsorber is connected with the waste nitrogen output pipeline, valves are arranged on a connecting pipeline of the molecular sieve adsorber and the waste nitrogen output pipeline, a connecting pipeline of the molecular sieve adsorber and the compressor, and a connecting pipeline of the molecular sieve adsorber and the fractionating tower system, and the control method of the air separation device further comprises the following steps: controlling the valve to close before the liquid remaining in the upper column is completely vaporized.
8. The method of controlling an air separation plant of claim 5, further comprising:
and after the liquid remained in the upper tower is completely evaporated, controlling the control valve to be closed.
9. The method of controlling an air separation plant according to any one of claims 1 to 4, further comprising:
and before the air separation device is started again, the compressor and the molecular sieve adsorber are controlled to be started so as to heat the fractionating tower system.
10. The control method of an air separation plant according to any one of claims 1 to 4,
the heat-insulating material is pearlife.
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| JPS51133695A (en) * | 1975-05-15 | 1976-11-19 | Nippon Atom Ind Group Co Ltd | Process for treating the off-gas discharged from the nuclear power fac ility |
| DE4415747C2 (en) * | 1994-05-04 | 1996-04-25 | Linde Ag | Method and device for the low-temperature separation of air |
| PE20060989A1 (en) * | 2004-12-08 | 2006-11-06 | Shell Int Research | METHOD AND DEVICE FOR PRODUCING A LIQUID NATURAL GAS CURRENT |
| CN203048597U (en) * | 2012-12-14 | 2013-07-10 | 广东富睿实业集团有限公司 | Heating, unfreezing and blowing-out system for nitrogen generating equipment |
| CN104034124B (en) * | 2014-06-27 | 2016-05-18 | 莱芜钢铁集团有限公司 | A kind of air-separating plant and fluid-discharge method with pressure |
| CN104677052B (en) * | 2015-03-12 | 2017-01-11 | 开封东京空分集团有限公司 | Air separation fractionating tower system and technology utilizing air separation fractioning tower system to prepare low-purity oxygen |
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Effective date of registration: 20220617 Address after: 3007, Hengqin international financial center building, No. 58, Huajin street, Hengqin new area, Zhuhai, Guangdong 519031 Patentee after: New founder holdings development Co.,Ltd. Patentee after: SUZHOU SUXIN SPECIAL STEEL Co.,Ltd. Patentee after: JIANGSU SUZHOU STEEL GROUP Co.,Ltd. Address before: 100871, Beijing, Haidian District Cheng Fu Road 298, founder building, 9 floor Patentee before: PEKING UNIVERSITY FOUNDER GROUP Co.,Ltd. Patentee before: SUZHOU SUXIN SPECIAL STEEL Co.,Ltd. Patentee before: JIANGSU SUZHOU STEEL GROUP Co.,Ltd. |
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