CN109564060A - The method for producing air gas by the cryogenic separation of air - Google Patents
The method for producing air gas by the cryogenic separation of air Download PDFInfo
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- CN109564060A CN109564060A CN201780048225.6A CN201780048225A CN109564060A CN 109564060 A CN109564060 A CN 109564060A CN 201780048225 A CN201780048225 A CN 201780048225A CN 109564060 A CN109564060 A CN 109564060A
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- ice chest
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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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
-
- 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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
-
- 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
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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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
- F25J3/04406—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 using a dual pressure main column system
- F25J3/04412—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 using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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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
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
-
- 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
- F25J3/04836—Variable air feed, i.e. "load" or product demand during specified periods, e.g. during periods with high respectively low power costs
-
- 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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/60—Details about pipelines, i.e. network, for feed or product distribution
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Acyclic And Carbocyclic Compounds In Medicinal Compositions (AREA)
Abstract
A kind of method and apparatus that the cryogenic separation for by air produces air gas, this method may comprise steps of: will purify under conditions of effectively using column system by air stream cryogenic separation at oxygen product and nitrogen and the air of compression is streamed to ice chest, wherein the air stream of the purification and compression is when entering the column system in feed pressure；The oxygen product is extracted under product pressure；The oxygen product is delivered to oxygen channel under delivery pressure, wherein the oxygen channel has pipeline pressure；Wherein during second operator scheme, this method may include monitoring pipeline pressure；And the difference between reduction pipeline pressure and delivery pressure.By operating in a dynamic fashion, energy conservation may be implemented in the case where wherein pipeline pressure deviates its peak.
Description
PCT Patent Application
Related application
This application claims the priority for the U.S.Provisional Serial 62/356,962 submitted on June 30th, 2016,
The U.S. Provisional Application is hereby incorporated by its entirety by reference.
Technical field
Present invention relates in general to a kind of method and apparatus for effectively operating air separation equipment, which is produced
At least one of object is fed in pipeline.
Background technique
Air separation equipment separates atmospheric air into its main component: nitrogen and oxygen, and once in a while argon gas, xenon and
Krypton.These gases are sometimes referred to as air gas.
Typical cryogenic air separation process may comprise steps of: (1) air filtering is crossed, it may damage master to remove
The big particle of air compressor；(2) pre-filtered air is compressed and using cascade EDFA in main air compressor with from pressure
Contracting air setting goes out；(3) make compressed air stream by front end purification unit to remove remaining water and carbon dioxide；
(4) in a heat exchanger by the indirect heat exchange with the technique stream from deep cooling distillation column come the air of cooling and purifying；(5) make
At least part cold air expansion, to provide refrigeration for system；(6) cold air introducing distillation column is used for rectifying therein；(7)
It is in the oxygen of liquid from the collected overhead nitrogen of column (being usually in gas) and from the bottom collection of column.
In some cases, air gas separation unit (" ASU ") can be used for for one of its air gas being supplied to neighbouring pipe
Road (for example, oxygen or nitrogen pipeline), to supply one or more be not at close to the client near ASU.Supplying this
In the typical ASU of ground pipeline, it can be common that using the Process configuration using internal compression (pumping) circulation, in the feelings of oxygen channel
Under condition, this means that the supreme pressure in the pipeline pressure will be pumped from the liquid oxygen that lower pressure column generates from low pressure and in heat exchange
Evaporation in device, it is most commonly empty for the high pressure from booster air compressor (" BAC ") or main air compressor (" MAC ")
Air-flow.As used herein, booster air compressor is the double stage compressor positioned at clean unit downstream, for effectively
The purpose of evaporation product liquid oxygen stream be used to make a part of primary air Feed Pressurization.
Under normal operation, it is designed to generate oxygen under a constant to the ASU of oxygen channel charging oxygen.This
It is because ASU is operated to full blast under steady state conditions, a reactor.But pipeline cannot operate under a constant.For example, oxygen hose
(that is, pressure change of about 200psig) operation is not uncommon between 400 and 600psig in one day in road.This can be due to variable
Customer demand and/or the variable supply of pipeline is occurred.
It is hitherto known in the prior art, be commonly designed ASU with provide be higher than for highest expected from pipeline
Oxygen under the constant pressure of pressure.It is related to pipeline pressure variation in order to solve the problems, such as, usually just introducing oxygen into pipe
The pressure of gaseous oxygen is reduced with substantially matching with the pressure of pipeline across control valve before road.However, being lower than ASU in pipeline pressure
Design pressure whenever, the method is by poor efficiency.Thus, it would be advantageous to provide operate in a more effective manner
Method and apparatus.
Summary of the invention
The present invention be directed to meet the method and apparatus of at least one in these demands.
In one embodiment, the present invention may include a kind of for adjusting air gas (for example, nitrogen and oxygen)
One or more produces pressure to meet pipeline pressure, to the method for the reduction power consumption when pipeline pressure reduces.
In one embodiment, such poor efficiency can be minimized in the following manner: equipment used in design ASU
(for example, main heat exchanger, liquid oxygen (" LOX ") pump, BAC, MAC etc.), with enough flexibilities with can be based on pipeline
Gaseous oxygen (" GOX ") is delivered under the different pressures level of pressure.In another embodiment, this method and equipment may include work
Skill control strategy, to adjust the GOX product pressure come out from main heat exchanger automatically and continuously to meet pipeline pressure.
In another embodiment, adjustable since adjustable GOX product pressure is to match oxygen channel
The discharge pressure of BAC is to match the heating curves of the LOX of pressurization.It will also be appreciated by the skilled artisan that if the unit not
Using BAC, then the discharge pressure of MAC can be adjusted in a similar way.
In a specific embodiment, which may include being set as the automatic pipeline GOX charging of 100% opening
Valve, wherein GOX stream is controlled by flow indicator controller (" FIC "), which can operate to realize with LOX
The change of pump speed.The discharge pressure of BAC can be based on the practical ASU GOX by control loop, preferably feed forward control loop
Pressure.As pipeline pressure reduces, the discharge pressure of BAC and LOX pump will reduce, to provide significant energy conservation.
In addition, the stability of entire ASU technique not will receive the influence due to these dynamic process conditions.This mainly by
There is dynamics more faster than pipeline in ASU, because pipeline often contains such a large amount of gas；In contrast, pressure change
Slowly.
In other embodiments, pipeline can be nitrogen pipeline, and the nitrogen pipeline is by being generated by internal compression process
High-pressure gaseous nitrogen (" GAN ") charging.Control strategy also can be used any GOX and/or GAN pressure that can permit and be automated to correspond with pipe
The substitution control program in road is implemented.For example, the pressure difference by control across product control valve to pipeline, adjustable ASU is produced
Object pressure is to meet pipeline.In one embodiment, it is less than 5psi across the pressure difference of product control valve.In another embodiment
In, ASU product pressure, so that the holding of product control valve be allowed to fully open, causes across product in the 5psi of pipeline pressure
The pressure loss of control valve is minimum.
In one embodiment, the method for producing air gas for the cryogenic separation by air may include following step
It is rapid:
A) air is compressed to the pressure suitable for air deep-cooling rectifying, to generate the moist airflow of compression, the compression
Humid air stream have first pressure Po；
B) the moist airflow purification of the compression is removed into water and carbon dioxide in front end purification system, to generate and be somebody's turn to do
The moist airflow of compression compares the dry air stream with reduced water and amount of carbon dioxide；
C) first part of the dry air stream is compressed in booster compressor to form pressurizing air air-flow, the pressurized air
Stream has the first boost pressure PB1；
D) under conditions of efficiently separating air to form air gas product by the second part of the dry air stream and
The pressurizing air air-flow is introduced into ice chest, and wherein the air gas product is selected from the group being made of oxygen, nitrogen and combinations thereof；
E) the air gas product is extracted from the ice chest, which has the first product pressure PP1；
F) the air gas product is introduced into pipeline, wherein the pipeline is configured to for the air gas product being transported to
Positioned at the position of the pipe downstream, wherein the pipeline is in pipeline pressure PPLLower operation, wherein by the air gas product first
Delivery pressure PD1It is lower to be introduced into the pipeline；
G) the pipeline pressure P in the pipeline is monitoredPL；And
H) it is based on pipeline pressure PPLAdjust one or more pressure set-points in the ice chest.
In the optional embodiment for the method that the cryogenic separation by air produces air gas:
The one or more pressure set-point of step h) is the first product pressure PP1；
Adjust the first boost pressure PB1, so that the first delivery pressure PD1With pipeline pressure PPLBetween difference lower than giving
Determine threshold value；
The threshold value is less than 5psi, preferably smaller than 3psi；
Ice chest include main heat exchanger, the column system with the twin columns being made of lower pressure column and elevated pressures column,
It is arranged in the condenser and liquid oxygen pump of the bottom of lower pressure column；
The air gas product is oxygen and the pipeline is oxygen channel；
Liquid oxygen from lower pressure column is forced into the first product pressure P by liquid oxygen pumpP1；
Pipeline pressure P based on monitoringPLAdjust the first product pressure PP1；
Based on the first product pressure PP1Adjust the first boost pressure PB1；And/or
The air gas product is nitrogen and the pipeline is nitrogen pipeline.
In another aspect of the invention, a kind of method that the cryogenic separation by air produces air gas may include
First operator scheme and second operator scheme, wherein during first operator scheme and second operator scheme, this method include with
Lower step: will purification and compression under conditions of effectively using the column system cryogenic separation air stream to form air gas product
Air stream to ice chest, wherein the air stream of the purification and compression is in feed pressure P when entering the ice chestFUnder, wherein
The air gas product is selected from the group being made of oxygen, nitrogen and combinations thereof；In product pressure PPOUnder extract the air gas
Product；In delivery pressure PDOLower that the air gas product is delivered to air gas pipeline, wherein the air gas pipeline has
Pipeline pressure PPL；Wherein during the second operator scheme, this method further includes steps of monitoring pipeline pressure PPL；
And reduce pipeline pressure PPLWith delivery pressure PDOBetween difference.
In the optional embodiment for the method that the cryogenic separation by air produces air gas:
Reduce pipeline pressure PPLWith delivery pressure PDOBetween difference the step of further comprise adjust product pressure
PPO；
Reduce pipeline pressure PPLWith delivery pressure PDOBetween difference the step of further comprise adjust feed pressure PF
The step of；
Product pressure PPOWith delivery pressure PDOIt is essentially identical；
Air gas product is oxygen, and wherein ice chest includes main heat exchanger, has by lower pressure column and higher pressure
Power column constitute twin columns column system, be arranged in lower pressure column bottom condenser and liquid oxygen pump；
Ice chest further comprises gaseous oxygen (GOX) inlet valve, wherein the outlet of GOX inlet valve and liquid oxygen pump and air gas
The entrance of body pipeline, which is in, to be in fluid communication；
Reduce pipeline pressure PPLWith delivery pressure PDOBetween difference the step of include do not adjust GOX inlet valve；
Reduce pipeline pressure PPLWith delivery pressure PDOBetween difference the step of include keep GOX inlet valve beat completely
It opens；
This method can also be included in the step of ice chest upstream provides main air compressor, wherein reducing pipeline pressure PPL
With delivery pressure PDOBetween difference the step of further comprise adjust liquid oxygen pump operation and main air compressor operation
Step, so that adjusting product pressure PPOWith feed pressure PF；And/or
This method can also be included in the step of main air compressor downstream and ice chest upstream offer booster compressor,
Middle reduction pipeline pressure PPLWith delivery pressure PDOBetween difference the step of further comprise adjust liquid oxygen pump operation and pressurization
The step of operation of compressor, so that adjusting product pressure PPOWith feed pressure PF。
In another aspect of the invention, a kind of equipment is provided.In this embodiment, which may include:
A) main air compressor, the main air compressor are configured to for air being compressed to suitable for air deep-cooling rectifying
Pressure, to generate the moist airflow of compression, the moist airflow of the compression has first pressure Po；
B) front end purification system, the moist airflow purification which is configured to compress remove water and two
Carbonoxide, to generate the dry air stream compared with the moist airflow of the compression with reduced water and amount of carbon dioxide；
C) it is in the booster compressor being in fluid communication with front end purification system, wherein the booster compressor is configured to compress
To form pressurizing air air-flow, which has the first boost pressure P for the first part of dry air streamB1；
D) ice chest, the ice chest include main heat exchanger, with the twin columns being made of lower pressure column and elevated pressures column
Column system, be arranged in lower pressure column bottom condenser and liquid oxygen pump, wherein the ice chest is configured to efficiently separating
Air receives the second part of pressurizing air air-flow and dry air stream to be formed under conditions of air gas product, wherein the air
Gaseous product is selected from the group being made of oxygen, nitrogen and combinations thereof；
E) for monitoring the device of pipeline pressure, wherein the pipeline and ice chest, which are in, is in fluid communication, so that pipeline is configured
At the air gas product from ice chest is received, which has the first product pressure PP1；And
F) device that one or more pressure set-points of the equipment are adjusted for pipeline pressure based on monitoring, wherein should
One or more pressure set-points of equipment are selected from discharge pressure, the discharge pressure of booster air compressor, master by liquid oxygen pump
The discharge pressure of air compressor, and combinations thereof composition group.
In the optional embodiment for the equipment that the cryogenic separation by air produces air gas:
Adjust the first product pressure PP1, so that the first product pressure PP1With the first delivery pressure PD1Between difference it is low
In given threshold value；
The threshold value is less than 5psi, preferably smaller than 3psi；
The air gas product is oxygen and the pipeline is oxygen channel；
Liquid oxygen from lower pressure column is forced into the first product pressure P by liquid oxygen pumpP1；
Based on the first product pressure PP1Adjust the first boost pressure PB1；And/or
The air gas product is nitrogen and the pipeline is nitrogen pipeline.
In another aspect of the invention, the equipment for the cryogenic separation production air gas by air may include
Ice chest, the ice chest are configured to connect under conditions of effectively using column system cryogenic air separation stream to form air gas product
The air stream of purification and compression is received, wherein the air stream of purification and compression is in feed pressure P when entering ice chestFUnder, wherein
Air gas product is selected from the group being made of oxygen, nitrogen and combinations thereof, and wherein ice chest is configured in product pressure PPOLower production
Raw air gas product；For air gas product to be transferred to the device of air gas pipeline from ice chest；Pressure monitoring device,
The pressure monitoring device is configured to monitor pipeline pressure PPL；And controller, the controller are configured to based on pipeline pressure
PPLAdjust the product pressure P of the air gas product come out from ice chestPO。
In the optional embodiment for the equipment that the cryogenic separation by air produces air gas:
Air gas product is oxygen, and wherein ice chest includes main heat exchanger, has by lower pressure column and higher pressure
Power column constitute twin columns column system, be arranged in lower pressure column bottom condenser and liquid oxygen pump；
Controller is further configured to reduce pipeline pressure PPLWith delivery pressure PDOBetween difference；
Controller is further configured to that the discharge pressure of liquid oxygen pump is connected to and adjusted with liquid oxygen pump；
Product pressure PPOWith delivery pressure PDOIt is essentially identical；
Controller is connected to pressure monitoring device；
The equipment can there is no be configured to reduce pipeline pressure PPLWith delivery pressure PDOBetween difference GOX
Inlet valve；
The equipment can have gaseous oxygen (GOX) inlet valve, wherein the outlet and air of the GOX inlet valve and liquid oxygen pump
The entrance of gas pipeline, which is in, to be in fluid communication, and wherein the GOX inlet valve is maintained at fully open position；
The equipment can have the main air compressor for being arranged in ice chest upstream, and wherein controller is further configured to
Adjust the discharge pressure of main air compressor；And/or
The equipment may include the booster compressor in main air compressor downstream and ice chest upstream, wherein controller quilt
It is further configured to adjust the discharge pressure of booster compressor.
Detailed description of the invention
With reference to be described below, claims and drawing, these and other features, aspects and advantages of the invention will become more
It is good to understand.It should be noted, however, that attached drawing shows only several embodiments of the invention and is therefore not considered as to this
The limitation of invention scope, because the present invention can permit other equivalent embodiments.
Fig. 1 provides the embodiment of the present invention.
Fig. 2 provides another embodiment of the invention.
Fig. 3 provides the data diagram for one embodiment of the present of invention.
Specific embodiment
Although the present invention will be described in conjunction with several embodiments, it should be understood that, it is not intended to the present invention is limited
It is formed on those embodiments.On the contrary, it is intended to cover the spirit and model of the invention being defined by the appended claims can be included in
Enclose interior all alternative solutions, modification and equivalent.
Now return to Fig. 1.Air 2 is introduced into main air compressor 10 and is compressed, preferably up at least 55psig is extremely
The pressure of 75psig (or pressure about 5psig higher than elevated pressures column).Then by resulting pressure in front end purification system 20
The purification of moist airflow 12 of contracting removes and CO2, to generate dry air stream 22.In one embodiment, all dryings
Air stream 22 enters ice chest 40 via pipeline 26.The pressure of dry air stream 22 is measured by first pressure indicator PI1a.?
In ice chest 40, by air cooling and subzero treatment is carried out, to divide air into air gas product 42.Then by air
Gaseous product 42 passes through product control valve 50 from removal in ice chest 40 and before entering air gas pipeline 60.Preferred real
It applies in example, the pressure and flow rate of air gas product 42 can pass through second pressure indicator PI2 and flow indicator respectively
FI1 measurement.The pressure of air gas pipeline 60 can be measured by pressure indicator PI3.
In one embodiment, various pressure and flow indicator/sensor are configured to communicate with process controller 55
(for example, wirelessly or non-wirelessly communicating), monitors various flow rates and pressure by process controller 55, the technique control
Device processed is configured to the flow based on measurement and pressure adjusts the various settings in entire technique.
In addition, the embodiment of the present invention can also include booster air compressor 30.The embodiment is represented by the dotted line, because
It is optional embodiment.In this embodiment, a part of dry air stream 22 is sent via pipeline 24 to pressurizing air air pressure
Contracting machine 30, and in the compression that takes a step forward being introduced into ice chest 40 to form pressurizing air air-flow 32.Booster air compressor 30 adds
Adding allows finely tuning the additional degree in the technique, as will be explained in more detail below.In this embodiment, the first pressure
Power indicator PI1b is located on pipeline 32 rather than on pipeline 26.Similarly, with the pressure controller 14a of main air compressor 10
It compares, pressure controller 14b is connected to booster air compressor 30.Although the implementation of Fig. 1 is illustrated as single compressor
Booster air compressor 30, but it will be appreciated by those of ordinary skill in the art that booster air compressor 30 can be more than one
A physical compressor.In addition, booster air compressor 30 can also be compound compressor.
Although the figures illustrate from each pressure and flow indicator to the tie line of process controller 55,
It is that the embodiment of the present invention should not be so limited.On the contrary, it will be appreciated by those of ordinary skill in the art that the embodiment of the present invention
It may include the case where certain indicators are directly communicated with related pressure controller.
Fig. 2 provides the more detailed view of the ice chest 40 of the optional embodiment for including booster air compressor 30.?
In this embodiment, ice chest 40 further includes heat exchanger 80, turbine 90, valve 100, twin columns 110, elevated pressures column 120, auxiliary heat
Exchanger 130, lower pressure column 140, condenser/reboiler 150 and liquid oxygen pump 160.Turbine 90 can be via common axis
It is attached on booster 70.Just as in Fig. 1, air 2 is introduced into main air compressor 10 and is compressed, preferably up at least
The pressure of 55psig to 75psig (or pressure about 5psig higher than elevated pressures column).It then will in front end purification system 20
The purification of moist airflow 12 of resulting compression removes water and CO2, to generate dry air stream 22.By the of dry air stream
A part 24 is sent to booster air compressor 30, and the rest part 26 of dry air stream enters ice chest 40, and wherein it is being introduced into
Elevated pressures column 120 before wherein being separated in heat exchanger 80 to be thoroughly cooled.In booster air compressor 30
After middle pressurization, pressurizing air air-flow 32 in the bottom for being introduced into elevated pressures column 120 before it is preferably complete in heat exchanger 80
It is complete cooling, and then expanded across valve 100.
It is preferred that from booster air compressor 30 before partial boost air stream 37 is further compressed in booster 70
It removes in interior grade, and then cools down in aftercooler 75 to form the second pressurization stream 72.Second pressurization stream 72 is in heat exchange
Experience part is cooling in device 80, wherein it is extracted from the middle section of heat exchanger 80, and then in turbine 90
Expansion, to form expanded air stream 92, then the expanded air stream can before being introduced into elevated pressures column 120 with drying
The second part 26 of air stream combines.
Elevated pressures column 120 is configured to permit progress air rectifying in it, to generate oxygen enriched liquid simultaneously in bottom
And rich nitrogen gaseous flow is generated at top.Oxygen enriched liquid 122 is extracted from the bottom of elevated pressures column 120, it is useless with low pressure later
Nitrogen 114 and low pressure nitrogen product 112 carry out heat exchange in secondary unit 130, and then across expanding in valve and introduce
In lower pressure column 140.As known in the art, elevated pressures column 120 and lower pressure column 140 are a part of twin columns 110,
And the two columns are thermally coupled via condenser/reboiler 150, which will be from the upper of elevated pressures column 120
The nitrogen-rich gas risen is condensed and will be evaporated in the liquid oxygen of the bottom collection of lower pressure column 140.In the illustrated embodiment, by two
A nitrogen-rich liquid stream 126,128 is extracted from elevated pressures column 120, exchanges heat with low pressure nitrogen product 112 and low pressure waste nitrogen 114
Amount is then expanded across their own valve, and is then introduced into lower pressure column 140.Higher pressure nitrogen product 129 may be used also
To be extracted from elevated pressures column 120, and then heated in heat exchanger 80.
In the bottom collection liquid oxygen of lower pressure column 140, and it is extracted by liquid oxygen pump 160 and is forced into suitably
Pressure, to form liquid oxygen product 162.Then liquid oxygen product 162 is evaporated in heat exchanger 80, to form air gas production
Object 42.The pressure and flow rate of air gas product 42 can be measured via second pressure sensor PI2 and FI1 respectively.Such as
Shown in Fig. 1, air gas product 42 flows across product control valve 50 and enters in air gas pipeline 60.
As previously noted, the pressure of air gas pipeline 60 is tended to drift about at any time.In hitherto known method
In, the aperture by adjusting product control valve 50 solves this to lead to the problem of pressure drop appropriate.However, doing so low efficiency.
On the contrary, the pressure set-point in the adjustable ice chest of the embodiment of the present invention, for example, the discharge pressure of liquid oxygen pump 160.Passing through will
This pressure reduces amount appropriate, and product control valve 50 can keep fully opening, so as to cause across the swollen of product control valve 50
Swollen loss reduction.In one embodiment, amount appropriate generates less than the difference between the PI2 and PI3 of 5psi, preferably smaller than 3psi
Value.
In another embodiment, by changing the pressure of liquid oxygen product 162, evaporating temperature will also change.In addition, excellent
Choosing, liquid oxygen product 162 are evaporated against condensation air stream (for example, pressurizing air air-flow 32).Similarly, preferably implementing
In example, the discharge pressure of booster air compressor 30 also changes amount appropriate.In one embodiment, amount appropriate is preferably
The amount for causing the heating curves between liquid oxygen product 162 and pressurizing air air-flow 32 to improve.
In the embodiment that wherein air gas product is nitrogen, which may include from elevated pressures column 120
The higher pressure nitrogen product 129 in liquid is extracted, and uses liquid nitrogen pump (not shown) will before heating in heat exchanger 80
It is forced into pressure appropriate.Then by the nitrogen product of resulting heating with about similar fashion described in gaseous oxygen product
It is introduced into nitrogen pipeline.Alternatively, liquid nitrogen stream can be removed from lower pressure column rather than in elevated pressures column.
Fig. 3 provides diagram of the pressure for the embodiment of the present invention as the function of time.It can be seen such as in Fig. 3
Out, ASU GOX pressure is kept to be slightly above (for example, between 3-4psi) GOX pipeline pressure.This is pumped by change from LOX
LOX discharge pressure and change both booster air compressor (BAC) discharge pressures to complete.By being operated with speed change pattern
LOX pump and BAC, the embodiment of the present invention can save power consumption in the case where no any flow rate production loss,
And therefore show the fabulous advantage better than hitherto known method.
Lower Table I and Table II show the correlation data at 610psig and 400psig for each stream of oxygen production.
Table II: 400psig GOX
Shown in table as above, when pipeline pressure changes, the pressure of adjustable stream 32,37,42 and 162 is protected simultaneously
It is essentially identical to hold every other condition.As will be readily understood, can reduce can to the compression requirements of LOX pump 160 and BAC 30
To lead to significant energy conservation.In addition, this does not have without any production loss in terms of flow rate and to the operating condition of twin columns
It is completed in the case where having any interfere significantly with.
Term " rich nitrogen " and " oxygen-enriched " will be appreciated by those skilled in the art as with reference to the composition of air.Similarly, rich
Nitrogen covers the fluid that the nitrogen content having is greater than the nitrogen content of air.Similarly, the oxygen-enriched oxygen content having that covers is greater than sky
The fluid of the oxygen content of gas.
Although having been combined it, specific examples describe the present invention, it is evident that in view of many alternatives of preceding description
Case, modification and variation will be apparent those skilled in the art.Therefore, it is intended to comprising such as falling into appended claims
All such alternative solutions, modification and variation in spirit and broad scope in book.The present invention can be suitably comprising disclosed
Element, be made of disclosed element or be substantially made of disclosed element, and can be there is no undisclosed
It is practiced under element.In addition, if in the presence of the language for referring to sequence, such as first and second, it should on illustrative sense and
Do not understood in restrictive sense.For example, it will be appreciated by the appropriately skilled person that certain steps can be combined into list
In one step.
Singular "/kind (a/an) " and " being somebody's turn to do (the) " include plural referents, unless context is expressly otherwise
It points out.
" include (comprising) " in claim is open transitional term, refer to it is later determined that right want
Seeking element is without exclusive inventory (that is, other anythings can additionally be included and be maintained at the range of "comprising"
It is interior).Unless otherwise indicated herein, otherwise "comprising" as used herein can by be more restricted transitional term " mainly by ...
Composition " and " consist of " replace.
" provide (providing) " in claim be defined as confession under directions to, supply, make can get or prepare certain
Object.Step can be carried out under there is no the representation language in the opposite claim by any actor.
It is optional or optionally mean that the event then described or situation may occur or may not occur.This explanation includes
The wherein event or the example happened and the example that wherein event or situation do not occur.
It can be expressed as in this range from about occurrence, and/or arrive about another occurrence.When such range of statement
When, it should be understood that another embodiment is from an occurrence and/or to another occurrence, together in the range
Interior all combinations.
Herein determine all bibliography respectively hereby by reference is integrated in the application in its entirety, and be for
Specific information, each bibliography is cited is exactly for the specifying information.
Claims (14)
1. a kind of method that the cryogenic separation for by air produces air gas, method includes the following steps:
A) pressure suitable for air deep-cooling rectifying is arrived into air (2) compression (10), to generate the moist airflow (12) of compression,
The humid air stream of the compression has first pressure Po；
B) the moist airflow purification of the compression is removed into water and carbon dioxide in front end purification system (20), to generate and be somebody's turn to do
The moist airflow (12) of compression compares the dry air stream (22) with reduced water and amount of carbon dioxide；
C) first part (24) of the dry air stream is compressed in booster compressor (30) to form pressurizing air air-flow (32), be somebody's turn to do
Pressurizing air air-flow has the first boost pressure PB1；
D) by the second part of the dry air stream under conditions of efficiently separating air to form air gas product (42)
(26) it is introduced into ice chest (40) with the pressurizing air air-flow, which has the first product pressure PP1, the wherein air
Gaseous product is selected from the group being made of oxygen, nitrogen and combinations thereof；
E) the air gas product is extracted from the ice chest；
F) the air gas product is introduced into pipeline (60), wherein the pipeline is configured to for the air gas product being transported to
Positioned at the position of the pipe downstream, wherein the pipeline is in pipeline pressure PPLLower operation, wherein by the air gas product first
Delivery pressure PD1It is lower to be introduced into the pipeline；
G) the pipeline pressure P in the pipeline is monitoredPL(PI3)；And
H) it is based on pipeline pressure PPLAdjust one or more pressure set-points in the ice chest.
2. the method for claim 1, wherein the one or more pressure set-point of step h) is the first product pressure
Power PP1。
3. method as described in any one of the preceding claims, wherein adjust first boost pressure PB1, so that this first is passed
Pressurization pressure PD1With pipeline pressure PPLBetween difference be lower than given threshold value, wherein the given threshold value is preferably smaller than 5psi, more excellent
Choosing is less than 3psi.
4. method as described in any one of the preceding claims, wherein the ice chest include main heat exchanger (80), have by compared with
The column system (110) for the twin columns that low-pressure column (140) and elevated pressures column (120) are constituted, the bottom for being arranged in the lower pressure column
The condenser (150) and liquid oxygen pump (160) in portion.
5. method as claimed in claim 4, wherein the air gas product is oxygen and the pipeline is oxygen channel, and
And wherein, which is pressurized to first product pressure P for the liquid oxygen from the lower pressure columnP1。
6. method as described in any one of the preceding claims, wherein the pipeline pressure P based on the monitoringPLAdjust this first
Product pressure PP1。
7. method as claimed in claim 6, wherein be based on first product pressure PP1Adjust first boost pressure PB1。
8. method as claimed in claim 4, wherein the air gas product is nitrogen and the pipeline is nitrogen pipeline.
9. a kind of method for producing air gas by the cryogenic separation of air, this method includes first operator scheme and the
Two operation modes, wherein during the first operator scheme and the second operator scheme, method includes the following steps:
It will purification under conditions of effectively using column system (110) the cryogenic separation air stream to form air gas product (42)
And the air stream (26,32) of compression is sent to ice chest (40), wherein the air stream of the purification and compression is in when entering the ice chest
Feed pressure PFUnder, wherein the air gas product is selected from the group being made of oxygen, nitrogen and combinations thereof；
In product pressure PPOUnder the air gas product is extracted from the ice chest；
In delivery pressure PDOLower that the air gas product is delivered to air gas pipeline (60), wherein the air gas pipeline has
There is pipeline pressure PPL；
Wherein during the second operator scheme, this method is further included steps of
Monitor pipeline pressure PPL(PI3)；And
Reduce pipeline pressure PPLWith delivery pressure PDOBetween difference.
10. method as claimed in claim 9, wherein reduce pipeline pressure PPLWith delivery pressure PDOBetween difference
Step adjusts the product pressure P while further comprising in the ice chestPO。
11. the method as described in claim 9 or 10, wherein reduce pipeline pressure PPLWith delivery pressure PDOBetween difference
The step of value further comprises adjusting feed pressure PFThe step of (14a, 14b).
12. the method as described in any one of claim 9-11, wherein product pressure PPOWith delivery pressure PDOBasic phase
Together.
13. a kind of equipment that the cryogenic separation for by air produces air gas, the equipment include:
A) main air compressor (10), the main air compressor are configured to for air (2) being compressed to suitable for air deep-cooling essence
The pressure evaporated, to generate the moist airflow (12) of compression, the moist airflow of the compression has first pressure Po；
B) front end purification system (20), the front end purification system be configured to remove the purification of the moist airflow of the compression water and
Carbon dioxide, to generate the dry air stream compared with the moist airflow of the compression with reduced water and amount of carbon dioxide
(22)；
C) it is in the booster compressor (30) being in fluid communication with the front end purification system, wherein the booster compressor is configured to press
Contract the dry air stream first part (24) to form pressurizing air air-flow, the pressurizing air air-flow have the first boost pressure PB1；
D) ice chest (40), the ice chest include main heat exchanger (80), have by lower pressure column (140) and elevated pressures column
(120) constitute twin columns column system (110), be arranged in the lower pressure column bottom condenser (150) and liquid oxygen pump
(160), wherein the ice chest is configured to receive the pressurizing air under conditions of efficiently separating air to form air gas product
The second part (26) of air-flow (32) and the dry air stream, wherein the air gas product is selected from by oxygen, nitrogen and its group
The group being combined into；
E) for monitoring the device of the pressure (PI3) of pipeline (60), wherein the pipeline and the ice chest, which are in, is in fluid communication, so that should
Pipeline is configured to receive the air gas product from the ice chest, which has the first product pressure PP1；With
And
F) device of one or more pressure set-points of the equipment (55) is adjusted for the pipeline pressure based on the monitoring, wherein
The one or more pressure set-point of the equipment is selected from the discharge pressure by the liquid oxygen pump (160), the booster air compressor
(30) discharge pressure of discharge pressure, the main air compressor (10), and combinations thereof composition group.
14. equipment as claimed in claim 13, wherein adjust first product pressure PP1, so that first product pressure PP1
With first delivery pressure PD1Between difference be lower than given threshold value, wherein the given threshold value be preferably smaller than 5psi, more preferably it is small
In 3psi.
Applications Claiming Priority (7)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US201662356962P | 2016-06-30 | 2016-06-30 | |
| US62/356,962 | 2016-06-30 | ||
| US15/382,902 US10267561B2 (en) | 2016-06-30 | 2016-12-19 | Apparatus for the production of air gases by the cryogenic separation of air |
| US15/382,896 | 2016-12-19 | ||
| US15/382,896 US10302356B2 (en) | 2016-06-30 | 2016-12-19 | Method for the production of air gases by the cryogenic separation of air |
| US15/382,902 | 2016-12-19 | ||
| PCT/US2017/039950 WO2018005768A1 (en) | 2016-06-30 | 2017-06-29 | Method for the production of air gases by the cryogenic separation of air |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109564060A true CN109564060A (en) | 2019-04-02 |
| CN109564060B CN109564060B (en) | 2021-08-13 |
Family
ID=65019174
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201780048225.6A Active CN109564060B (en) | 2016-06-30 | 2017-06-29 | Method for producing air gas by cryogenic separation of air |
Country Status (6)
| Country | Link |
|---|---|
| EP (1) | EP3479040A1 (en) |
| CN (1) | CN109564060B (en) |
| BR (1) | BR112018077490A2 (en) |
| CA (1) | CA3029667A1 (en) |
| RU (1) | RU2741174C2 (en) |
| SG (1) | SG11201811684PA (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5471843A (en) * | 1993-06-18 | 1995-12-05 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and installation for the production of oxygen and/or nitrogen under pressure at variable flow rate |
| CN101063592A (en) * | 2006-04-13 | 2007-10-31 | 林德股份公司 | Process and device for generating a pressurized product by low-temperature air fractionation |
| CN101981399A (en) * | 2008-03-27 | 2011-02-23 | 普莱克斯技术有限公司 | Distillation method and apparatus |
| CN102472575A (en) * | 2009-07-24 | 2012-05-23 | 大阳日酸株式会社 | Air liquefaction and separation method and device |
| CN104061757A (en) * | 2014-07-07 | 2014-09-24 | 开封空分集团有限公司 | Liquid oxygen and liquid nitrogen preparation device and method |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU637600A1 (en) * | 1977-03-14 | 1978-12-15 | Предприятие П/Я А-3605 | Method of regulating air separation plant operation |
| US6568207B1 (en) * | 2002-01-18 | 2003-05-27 | L'air Liquide-Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude | Integrated process and installation for the separation of air fed by compressed air from several compressors |
| FR2895068B1 (en) * | 2005-12-15 | 2014-01-31 | Air Liquide | AIR SEPARATION METHOD BY CRYOGENIC DISTILLATION |
-
2017
- 2017-06-29 RU RU2019101433A patent/RU2741174C2/en active
- 2017-06-29 SG SG11201811684PA patent/SG11201811684PA/en unknown
- 2017-06-29 CN CN201780048225.6A patent/CN109564060B/en active Active
- 2017-06-29 BR BR112018077490A patent/BR112018077490A2/en unknown
- 2017-06-29 CA CA3029667A patent/CA3029667A1/en active Pending
- 2017-06-29 EP EP17737992.2A patent/EP3479040A1/en not_active Withdrawn
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5471843A (en) * | 1993-06-18 | 1995-12-05 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and installation for the production of oxygen and/or nitrogen under pressure at variable flow rate |
| CN101063592A (en) * | 2006-04-13 | 2007-10-31 | 林德股份公司 | Process and device for generating a pressurized product by low-temperature air fractionation |
| CN101981399A (en) * | 2008-03-27 | 2011-02-23 | 普莱克斯技术有限公司 | Distillation method and apparatus |
| CN102472575A (en) * | 2009-07-24 | 2012-05-23 | 大阳日酸株式会社 | Air liquefaction and separation method and device |
| CN104061757A (en) * | 2014-07-07 | 2014-09-24 | 开封空分集团有限公司 | Liquid oxygen and liquid nitrogen preparation device and method |
Also Published As
| Publication number | Publication date |
|---|---|
| RU2019101433A (en) | 2020-07-20 |
| RU2741174C2 (en) | 2021-01-22 |
| CA3029667A1 (en) | 2018-01-04 |
| BR112018077490A2 (en) | 2019-04-09 |
| SG11201811684PA (en) | 2019-01-30 |
| RU2019101433A3 (en) | 2020-10-09 |
| CN109564060B (en) | 2021-08-13 |
| EP3479040A1 (en) | 2019-05-08 |
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