CN103946654A - Compression method and air separation - Google Patents

Compression method and air separation Download PDF

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Publication number
CN103946654A
CN103946654A CN201280018560.9A CN201280018560A CN103946654A CN 103946654 A CN103946654 A CN 103946654A CN 201280018560 A CN201280018560 A CN 201280018560A CN 103946654 A CN103946654 A CN 103946654A
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CN
China
Prior art keywords
compressor
compression stage
flow rate
compression
pressure
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN201280018560.9A
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Chinese (zh)
Inventor
D.D.德摩尔
R.L.贝克
J.H.罗亚尔
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Praxair Technology Inc
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Praxair Technology Inc
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Filing date
Publication date
Priority claimed from US13/087,734 external-priority patent/US20120260693A1/en
Application filed by Praxair Technology Inc filed Critical Praxair Technology Inc
Publication of CN103946654A publication Critical patent/CN103946654A/en
Pending legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D25/00—Pumping installations or systems
    • F04D25/02—Units comprising pumps and their driving means
    • F04D25/06—Units comprising pumps and their driving means the pump being electrically driven
    • F04D25/0606—Units comprising pumps and their driving means the pump being electrically driven the electric motor being specially adapted for integration in the pump
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D17/00—Radial-flow pumps, e.g. centrifugal pumps; Helico-centrifugal pumps
    • F04D17/08—Centrifugal pumps
    • F04D17/10—Centrifugal pumps for compressing or evacuating
    • F04D17/12—Multi-stage pumps
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D27/00—Control, e.g. regulation, of pumps, pumping installations or pumping systems specially adapted for elastic fluids
    • F04D27/02—Surge control
    • F04D27/0261—Surge control by varying driving speed
    • 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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
    • F25J3/04121—Steam turbine as the prime mechanical driver
    • 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
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
    • F25J3/04133—Electrical motor as the prime mechanical driver
    • 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
    • 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
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • 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
    • F25J3/044—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 single pressure main column system only
    • 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
    • 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
    • F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
    • 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
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being air
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/70—Efficient control or regulation technologies, e.g. for control of refrigerant flow, motor or heating

Abstract

A compression method, a multistage compression system and an air separation method and plant in which a gas is compressed in a series of compression stages to produce a compressed gas and each of the compression stages incorporate a variable speed compressor. In such compression method and system, the compressed air is produced at a pressure that remains stable during both normal operational conditions and during turn down conditions during which the flow rate of the gas is reduced. This reduction is accomplished by reducing the speed of the compressor in an initial compression stage such that the compressor operates at a point along its peak efficiency operating line at which the pressure ratio is directly proportional to the flow rate and such that the lower turn down flow rate is obtained at a reduced pressure which is made up in successive compression stages.

Description

Compression method and air separation
related application
The application is in the continuation part of the previous U.S. Patent Application Serial Number 13/087,734 of submission on April 15th, 2011, is incorporated to by reference herein.
Technical field
The present invention relates to a kind of method and system for Compressed Gas and a kind of air separating method and factory that combines this type of method and system, therein, gas or air are compressed into higher pressure in a series of compression stages, this higher pressure under normal operating condition and in the time of the gas of the lower flow rate of needs (flow rate) or air turn down (turndown) running status during be all maintained.More specifically, the present invention relates to the method and system and air separating method and factory, therein, compression stage has the variable speed motor of drive compression machine and the speed of each compressor is adjusted during turning down, and makes the initial portion (initial) of compression stage in the some place operation along peak efficiencies travel line.
Background technology
Many industrial process need the compression of gas.For example, in air separation, air is compressed, be cooled to the temperature that reaches or approach dew point, and is then introduced in that in distillation column system, to come by low temperature distillation be its part by air separation, for example, and nitrogen, oxygen and argon.Many application relate to the liquefaction of gas, and gas is compressed and then sufficiently cooled to produce liquid therein.
Although in any compression applications, likely Compressed Gas in single level, more commonly Compressed Gas in continuous compression stage.The reason of doing is like this in the time that gas is compressed, its temperature rise, and the gas temperature raising need to the increase on energy compress this gas.At gas, in level in compressed situation, gas can be cooling to reduce overall energy requirement between level, because cooling than not carrying out inter-stage, this process more approaches isotherm compression.In the typical compressor set that has utilized independent grade, use centrifugal compressors at different levels, the gas that enters to the import of compressor in this centrifugal compressor is disseminated to the compressor wheels with blade, and this compressor wheels rotates to accelerate gas and thus rotating energy is passed to gas.Increase and pressure that increase on this energy is accompanied by speed raise.Pressure recovers in static band blade or on-bladed diffuser, and this surrounds compressor wheels and play the function that reduces gas velocity with blade or on-bladed diffuser, and makes thus the gas pressure of Compressed Gas increase.
The independent compressor of compression stage can be driven by transmission device by the generic drive such as electro-motor, and this transmission device comprises the single gear wheel that drives driven gear, and this driven gear is connected to the axle of compressor.The problem of this collating unit is, air separation plant not always has identical demand being settled aspect conveying products.For example, produce in the air separation plant of oxygen in design, demand can change with in time and one week different in one day different days.Because the prime cost that makes air separation plant operation is electric power, what can expect is can turn down (turn down) factory and make its operation output ratio factory in next life common fertile oxygen still less during normal operating condition.This can complete by the air mass flow being lowered in the multi-stage compression system of using for the air of factory in compression.By reducing the speed of compressor, can make air mass flow reduce.Therefore,, in gear collating unit, if the speed of the motor of drive compression machine reduces, the rotary speed of all compressors reduces the amount with identical.The problem of doing is like this, the output pressure of multi-stage compression system also will reduce.Nowadays,, the in the situation that of producing oxygen or other gas taking specified pressure as client at needs, the reduction on this type of pressure also will make the pressure decreased of product.So, sometimes, can not make air separation plant move turning down under running status.The problem of these same types will occur in any type in service that relates to gas compression in level.
Another problem of common gear collating unit is, all compressors all must be positioned at around geared system.In addition, in the gear collating unit of this type of compressor, exist the efficiency deficiency being caused by the heat loss of geared system or gear-box.For fear of compressor being arranged on to gear-box around or the problem of thermodynamic efficiency deficiency, geared system or gear-box can be eliminated, and compressor can drive separately and control with speed control.For example, Application No. 2007/0189905 discloses a kind of multi-stage compression system, and this multi-stage compression system comprises the compressor that the inter-stage cooling device between compressor is connected in series.Each compressor is controlled separately by speed control.But the speed of compressor is controlled in this patent, make in the time that speed improves or reduce, the ratio of the speed of any two motors remains unchanged.Therefore, in this system, exist with the gear train using in air separation plant in the same difficulties that exists.Although this system can be turned down and move during turning down running status, discharge pressure will reduce.
As discussed, the invention provides the special method and apparatus that can be applicable to air separation, multi-stage compression system can move turning down under running status therein, continues transporting compressed gas body simultaneously under the pressure obtaining during normal operating condition.
Summary of the invention
The invention provides a kind of method of Compressed Gas.According to the method, gas is compressed to higher pressure from lower pressure in a series of compression stages.Described compression stage moves under normal operating condition, and during this period, gas is supplied with higher pressure and with higher flow rate, and described compression stage moves turning down under state, and during this period, gas is supplied with higher pressure and with lower flow rate.In this respect, when in this article with claim in while using, term " flow rate " refers to mass flowrate.Compression stage has the compressor being driven by variable speed motor, this variable speed motor can be with multiple speed drive compressor, these speed can be adjusted independently for each compressor, adjust thus by the flow rate of compressor with across the pressure ratio of (across) compressor.In this respect, when in this article with claim in while using, term " variable speed motor " refers to the device of any type, this device can give rotatablely moving compressor and therein speed can change.The example of variable speed motor comprises variable-ratio electro-motor, variable-ratio hydraulic motor, variable-ratio explosive motor and variable-ratio stream turbine.During turning down running status, the speed of variable speed motor is adjusted, and therefore, the speed of compressor and adjusted across the pressure ratio of compressor, make the initial portion of the compressor being associated with the initial portion of compression stage in the some place operation along its peak efficiencies travel line, herein across the initial pressure of the initial portion of compressor than directly proportional with flow rate, and lower than the initial pressure ratio of normal operating condition, obtain thus lower flow rate.Be arranged in continuous compression stage and at the continuous compressor in the downstream of the initial portion of compression stage with lower flow rate and with higher pressure ratio operation, this will can carry with higher pressure gas.
In the time that multi-stage compression system moves according to the present invention, as explained above, flow rate reduces during turning down running status, allows gas to carry with the pressure obtaining during normal operating condition simultaneously.Therefore, method of the present invention allows multi-stage compression system to be used in application, and in these application, stable pressure all needs under all operation architectures.Except aforementioned, while operation during multi-stage compression system is being turned down state, method of the present invention is to have especially energy efficiency.Such reason is, is maximum by the power of the multi-stage compression system consumption with multiple grades at initial compression level place, because the volume flow rate maximum in this grade, this is because gas in the time compressing in initial level has the fact of least density.In the time that gas is compressed continuously, density increase and therefore consumption power still less in compression stage subsequently.But, due to initial compression level operation and turn down the point along its peak efficiencies travel line, while being less than the some operation along its peak efficiencies travel line by the power consuming at this grade at the place of turning down by the power having consumed.Continuously level will be recovered in the first order of compression owing to turning down the pressure drop producing, and therefore, will be probably not along their peak efficiencies travel line operation.But because continuous level is by consumption rate initial compression level power still less, the loss in efficiency is by more than move the efficiency compensating at its peak efficiencies place by initial ministerial level.Therefore, can both obtain according to the power consumption of reduction and the higher stress level of normal operating condition of making in service of compressibility of the present invention, if compression stage is turned down with constant velocity ratio, this state can not obtain.
Although exist the application of multistage multi-stage compression system, in these application, move to compressor thermal insulation, in majority application, gas will be cooled between compression stage, and be cooled after compressing in a series of compression stages.
In the application of the present invention that relates to air separation, cooling and rear cooling will the use unchangeably of inter-stage.In this respect, the invention provides a kind of method that separates air, therein, air is compressed in a series of compression stages, carries out cooling and the rear cooling so that air of inter-stage between compression stage and in a series of compressive states, after compression, is cooled.Air is compressed to higher pressure from lower pressure within compression stage.Compression stage moves with turning down under running status at normal operating condition.During normal operating condition, air is supplied to main heat exchanger with higher pressure and with higher flow rate.During turning down state, air is supplied to main heat exchanger with higher pressure and with lower flow rate.After compressed, air is cooling in main heat exchanger, and be then introduced into distillation column system with produce return stream and product stream.Return to stream and product stream is heated so that air is cooling within main heat exchanger.Compression stage has the compressor being driven by variable speed motor, and these variable speed motor can be with multiple speed drive compressor, and these speed can be adjusted independently for each compressor, adjusts thus by the flow rate of compressor with across the pressure ratio of compressor.During turning down running status, the speed of the speed of variable speed motor and therefore compressor and adjusted across the pressure ratio of compressor, make the initial portion of the compressor being associated with the initial portion of compression stage in the some place operation along its peak efficiencies travel line, herein across the initial pressure of the initial portion of compressor than directly proportional with flow rate, and this initial pressure compares lower than the initial pressure ratio under normal operating condition, lower flow rate described in obtaining thus.Be arranged in continuous compression stage and at the continuous compressor in the downstream of the initial portion of compression stage with described lower flow rate and with described pressure ratio operation, this will can carry with higher pressure gas.
In the method for the invention, at normal operating condition with during turning down running status, the final compressor supply that gas can be from the final compression stage of compression stage.In an alternative of the present invention, during normal operating condition, gas can described pressure and with described higher flow rate from final compressor supply, and auxiliary compressor is by bypass.During turning down running status, when middle and final compressor stage must be when exceeding their efficiency pressure ratio state or to exceed their mechanically acceptable speed operation, auxiliary compressor can be set as become with final compressor fluid be communicated with, and gas subsequently with described pressure and with described lower flow rate from auxiliary compressor supply.In the situation that method of the present invention is applied to air separation plant, gas will be air certainly.In addition,, in any method of the present invention, variable speed motor can be direct drive motor.Speed control is connected on direct drive motor to control the speed of each direct drive motor.
On the other hand, the invention provides a kind of multi-stage compression system for Compressed Gas.According in this respect, a series of compression stages provide gas are compressed to the higher pressure the final level of compression stage from lower pressure.This multi-stage compression system is constructed to move at normal operating condition with in turning down running status.During normal operating condition, gas is supplied with described higher pressure and with described higher flow rate from described compression stage.During turning down running status, and gas is supplied with described higher pressure and with described lower flow rate from described compression stage.Compression stage has the compressor being driven by variable speed motor, these variable speed motor can be with multiple speed drive compressor, these speed can be adjusted independently for each compressor, adjust thus and pass through the flow rate of compressor and the pressure ratio across compressor, and compression stage has the variable speed control that is connected on compressor and is constructed to the speed of adjusting independently compressor.Master controller is connected on variable speed control, and be constructed such that the speed of variable speed motor during turning down running status and the therefore speed of compressor and adjusted across the pressure ratio of compressor, make the initial portion of the compressor being associated with the initial portion of compression stage in the some place operation along its peak efficiencies travel line, herein across the initial pressure of the initial portion of compressor than directly proportional with flow rate, and this initial pressure, than lower than the initial pressure ratio under normal operating condition, obtains lower flow rate thus.The continuous compressor in downstream that is arranged in continuous compression stage and be positioned at the initial portion of compression stage is with described lower flow rate and with the operation of described pressure ratio, and this will make compression stage carry gas with described higher pressure.
As already pointed out, intercooler can be positioned between compression stage.Aftercooler can be connected on a series of compression stages, gas is cooled after compressing in these a series of compression stages.
The present invention also provides a kind of air separation plant, and this factory adopts a series of compression stages that air is compressed to the higher pressure the final level of compression stage from lower pressure.Intercooler is positioned between a series of compression stages, and aftercooler is connected in the final level of compression stage.Multi-stage compression system is constructed at normal operating condition and turns down under running status and move.During normal operating condition, air is supplied with described higher pressure and with described higher flow rate from described compression stage.During turning down running status, air is supplied with described higher pressure and with described lower flow rate from described compression stage.Compression stage has the compressor being driven by variable speed motor, these variable speed motor can be with multiple speed drive compressor, these speed can be adjusted independently for each compressor, adjust thus and pass through the flow rate of compressor and the pressure ratio across compressor, and compression stage has the variable speed control that is connected on compressor and is constructed to the speed of adjusting independently compressor.Main heat exchanger is connected on multi-stage compression system, and is constructed to make this air cooling after air is compressed.Be configured to produce and return to stream and the distillation column system of product stream is connected on main heat exchanger, make air be introduced into distillation column system after cooling in main heat exchanger, and return stream and product stream within main heat exchanger, heated so that air is cooling.Master controller is connected on variable speed control, and be constructed such that the speed of variable speed driver during turning down running status and therefore the speed of compressor is adjusted, make the initial portion of the compressor being associated with the initial portion of compression stage in the some place operation along its peak efficiencies travel line, the initial pressure of the initial portion of compressor is than directly proportional with flow rate herein, and initially this pressure ratio, lower than the initial pressure ratio under normal operating condition, obtains lower flow rate thus.The continuous compressor in downstream that is positioned in continuous compression stage and be positioned at the initial portion of compression stage is with described lower flow rate and with the operation of described pressure ratio, and this will make compression stage carry gas with described higher pressure.
At multi-stage compression system according to the present invention or adopt in the air separation plant of this type of multi-stage compression system, compression stage can be constructed to make at normal operating condition with during turning down running status, and gas is the final compressor supply from the final compression stage of compression stage all.Alternatively, compression stage can be provided with the final compressor in the final compression stage of compression stage and the auxiliary compressor in the auxiliary compression stage of compression stage.Flow-control network is made as to be had bypass line, be positioned at this bypass line and be connected to the first valve between the aftercooler on final compressor.Second valve is positioned between aftercooler and auxiliary compressor.Each in the first valve and second valve is exercisable, to be set in closed position and open position, make during normal operating condition, the first valve is set in open position, and second valve is set in closed position, and gas by bypass line with described pressure and with described higher flow rate from final compressor supply, and auxiliary compressor is by bypass.During turning down running status, the first valve is set in closed position, and second valve is set in open position, auxiliary compressor is connected on aftercooler, and gas with described pressure and with described lower flow rate from auxiliary compressor supply.In the situation that multi-stage compression system of the present invention is applied to air separation plant, gas will be air certainly.In any embodiment of the present invention, variable speed motor can be direct drive motor.
Brief description of the drawings
Although the present invention includes the claim of clearly pointing to according to theme of the present invention, believe in the time being associated with accompanying drawing and will understand better the present invention, in the accompanying drawings:
Fig. 1 is the schematic diagram of the multi-stage compression system for implementing a method according to the present present invention;
Fig. 2 is the diagrammatic representation of the multi-stage compression system that shows in Fig. 1 compressor performance figure during normal operating condition.
Fig. 3 is the diagrammatic representation of turning down the compressor performance figure of the multi-stage compression system showing during turning down running status in Fig. 1.
Fig. 4 is the alternative of Fig. 1; And
Fig. 5 is the schematic diagram of air separation plant, and this air separation plant combines the multi-stage compression system showing at Fig. 1 or Fig. 4 for implementing the method according to this invention.
Detailed description of the invention
With reference to figure 1, illustrate according to multi-stage compression system 1 of the present invention.Multi-stage compression system 1 is the multi-stage compression unit with four compression stages 10,12,14 and 16, these compression stages are designed to be compressed to higher pressure by being included in the gas of carrying in stream 18 from lower pressure, and produce the flow of the compressed gas 20 that contains higher pressures of gases thus.Understand, can comprise the level of more or less quantity according to multi-stage compression system of the present invention.
Compression stage 10 is provided with the compressor 22 being driven by variable speed motor 24.Understand, compressor 22 can be the centrifugal compressor by the type described above of variable-ratio electric permanent magnetic motor driving.In compression stage 10, variable speed motor 24 is controlled by the speed control 26 that can be variable frequency controller, and driver 24 is variable-ratio electric permanent magnetic motors herein.To be pointed out that, any other motor of variable speed motor 24 or use related to the present invention can be the device of another type, for example, and the steam turbine of throttle valve control.Continuously compression stage 12,14 and 16 is respectively equipped with compressor 28,30 and 32, variable speed motor 34,36 and 38 and speed control 40,42 and 44 similarly.
It is cooling and rear cooling that multi-stage compression system 1 also combines inter-stage.As known in the art, in the time that gas is compressed in compressions at different levels, the temperature of gas raises.As a result, the density of gas reduces, and in level, must consume more energy and carry out Compressed Gas.By make gas cooled between level, the density of gas is greater than and does not experience this type of cooling gas, and result has been saved energy.That is to say, likely obtain cooling without centre or rear cooling multistage compressor installation, desired is to produce the heated gas that can use in lower procedure herein.But, in illustrated embodiment, cooling being illustrated out in the middle of this type of, and for this purpose, after gas is compressed in compressor 22, gas is cooling in interstage cooler 46 before the import that is transported to downstream compressor 28.Similarly, after gas is further compressed in compressor 28, this gas is cooling in interstage cooler 48 before the import that is conveyed into compressor 30, and after gas is compressed in compressor 30, this gas is cooling in interstage cooler 50.After gas is compressed in compressor 32, this gas is cooling to remove the heat of compression in aftercooler 52.Interstage cooler 46,48 and 50 is well known in the art, and can be made up of wing formula and the tubing heat exchanger of liquid cooling.Aftercooler 52 preferably also combines the wing formula of liquid cooling and the direct contact heat exchange of tubing heat exchanger structure or liquid cooling.
Compound compressor system 1 is designed to produce flow of the compressed gas 20 with specific pressure and flow rate.In the time that compound compressor system 1 is moved in this way, it moves under normal operating condition.When desired be while reducing the flow of flow of the compressed gas 20, compound compressor system 1 is by still with the identical specified pressure needing under normal operating condition but carry out transporting compressed gas body stream with the flow reducing.In such cases, compound compressor system 1 is called as and moves turning down under running status.Control is undertaken by programmable logic controller (PLC) 54, this programmable logic controller (PLC) 54 sends suitable control signal by controlling network 56, this control network 56 can be one group of data line to variable speed control 26,40,42 and 44, these data lines play the effect of the speed of controlling motor 24,34,36 and 38, and therefore play the effect of the speed of controlling compressor 22,28,30 and 32.
With reference to figure 2, illustrate the standardization figure of compressor performance, therein, under design and operation state, all compressors 22,28,30 and 32 all move along their peak efficiencies travel line, pressure ratio is proportional with the flow by compressor herein, and therefore, and these compressors are with peak efficiency and with their 100% speed operation under normal operating condition.According to the present invention, desired be to turn down flow is reduced under running status in the situation that, the speed of compressor 22 is adjusted to a point down along peak efficiencies travel line.The adjustment of speed can be little by little along this travel line or simply controlled so that speed be directly reduced to corresponding to the point of turning down state from normal operating condition.In this respect, likely must in the design of any array of compressed, make compromise, and therefore, under normal operating condition, compressor 22 or continuous downstream compressor may be moved at their level wide pneumatic peak efficiencies place just.Therefore, during normal operating condition, possible, the compressor in array of compressed possibly cannot move just on peak efficiencies travel line.In addition, if compressor has different designs, not polymerization like that as shown in Figure 2 of their travel line.In any case the speed that reduces compressor 22 will make flow reduce, it is transferred the decline causing across the pressure ratio of compressor 22.This lower general who has surrendered must compensate in the continuous compressor 28,30 and 32 of continuous compression stage.One of method of accomplishing this point is the compression ratio calculating between the initial compression level 10 of having turned down, and the pressure ratio calculating is on average divided between continuous compression stage 12,14 and 16 and (may be existed than the ratio calculating being evenly divided into the more excellent method of remaining level).As understood, exist potentially the additive method that recovers pressure.In illustrated embodiment, calculating is carried out in programmable logic controller (PLC) 54, and this programmable logic controller (PLC) 54 also produces required control signal, and these control signals are applied to variable speed control by controlling network 56.Although one or more may no longer the operation along peak efficiencies travel line in compressor 28,30 and 32 subsequently, the compressor 22 of initial compression level 10 will keep along the operation of peak efficiencies travel line, and therefore operation efficiently.The importance of doing is like this, compressor 22 has a maximum electricity needs by immutable.Therefore,, during turning down running status, compound compressor system declines to step together more efficient by the speed such as fruit compressor unchangeably as providing in the prior art.
With reference to figure 3 and following form, show the example of the operation of multi-stage compression system 1 in addition, it can be applicable to following especially by the cryogenic air separation plant of illustrated type in the Fig. 4 discussing.
Form
Inlet pressure, pica 15
Row blowdown presssure, psia 90
Progression 4.0
Row pressure ratio 6.00
The wide pressure ratio of design level 1.565
Turn down rate 80%
First order peak efficiencies pressure ratio under turning down 70%
As shown in form, carrying the inlet pressure of stream 18 is about 15 psia (pound/square inch (absolute pressures), and for 6.00 the overall pressure ratio across compound compressor system 1, the required blowdown presssure of flow of the compressed gas 20 is 90 psia.Each in compressor 22,28,30 and 32 operation under 1.57 design pressure ratio.As illustrated, in the time that the compression of gas reduces gas density, volume flow reduces, and therefore reduces by the flow of continuous compressor.80% flow turn down running status during, will be adjusted to 0.7 along peak efficiencies travel line across the standardization pressure ratio of compressor 22.If required pressure ratio is adjusting fifty-fifty between level 12,14 and 16 continuously, according to power law, each compressor 28,30 and 32 is by the standardization pressure ratio operation with 1.126.In other words, 0.700 × 1.126 × 1.126 × 1.126 equal 1.00, or adopt actual pressure ratio, and 1.10 × 1.76 × 1.76 × 1.76 equal 6.00.Therefore, although multi-stage compression system 1 is turned down the flow to 80%, it will flow 20 with 90 psia transporting compressed gas bodies, or in other words, the design pressure of carrying is carried out to transporting compressed gas body stream 20 during normal operating condition.In order to obtain these states, the speed of compressor 22,28,30 and 32 will be adjusted to the speed of being indicated by Fig. 3 by their variable speed controls 26,40,42 and 44 separately: compressor 22 is by about 83% operation with its design speed; Compressor 28 is by about 107% operation with its design speed; Compressor 30 is by about 104% operation with its design speed; And compressor 32 is by about 103% operation with its design speed.At this again, suitably be pointed out that, although continuous compressor is that this can be only the situation in final compression stage with higher rotating speed operation in the above specified pressure restoration methods of discussing, upstream stage can move to save electric power with lower speed.Programmable logic controller (PLC) 54 can be programmed to have simply one group of default state of turning down or calculate can be as explained above multi-stage compression system 1 is turned down to one group and is turned down flow rate, this group is turned down flow rate using as the input to logic controller 54.
In addition, as illustrated, exist pressure transducer 59,60,62 and 64 and measure the pressure ratio across compressor 28,30 and 32.Pressure transducer 58 is provided to measure the blowdown presssure of compressor 22, and adjusts well the speed of this compressor 22, to guarantee the specific location of this compressor 22 on service chart shown in Fig. 2, for example, when turning down while moving under running status.The signal that can reflect pressure serves as further input, transfers to programmable logic controller (PLC) 54 respectively by data line 65,66,68,70 and 72.Equally, flowmeter 74 can be sent to programmable logic controller (PLC) 54 by signal via data line 76, pressure transducer 78 and the data line 80 that is associated with this pressure transducer 78 also can together with occur.
This device and programmable logic controller (PLC) 54 can be used to carry out the controlling run of multi-stage compression system 1 described above.In order to reach this result, programmable logic controller (PLC) 54 can be programmed to receive the input data that can reflect desired flow rate, and then according to the Algebraic Expression of Fig. 3 or according to comprising that within Fig. 3, the database of data calculates the speed for the reduction of variable speed motor 24, and generation can reflect the control signal of the speed of this reduction calculating.Control signal is inputted variable speed control 26 by data line 56 subsequently, and the speed that this variable speed control 26 transfers to control variable speed motor 24 is to obtain the speed reducing.Flowmeter 74 produces the signal of the mass flowrate that can reflect flow of the compressed gas 20, and this signal transmits by data line 80 as the input to programmable logic controller (PLC) 54.Programmable logic controller (PLC) is programmed for: if flow rate not the flow rate of the expectation of input programmable logic controller (PLC) 54 2% within, this programmable logic controller (PLC) respond this signal and by amendment afterwards signal be sent to variable-speed controller 26.In the time that flow rate is set, further calculate and undertaken by programmable logic controller (PLC) 54, to adopt the mode calculating pressure ratio of setting forth and produce control signal in above example, this control signal transfers to variable speed control 40,42 and 44 by data line 56, to transfer to adjust the speed of variable speed motor 34,36 and 38, and therefore adjust compressor 28,30 and 32, to obtain the desired pressure ratio being calculated by programmable logic controller (PLC) 54.The pressure signal that can reflect import and outlet pressure is produced by pressure transducer 59,60,62 and 64, and enter programmable 54 as another input, this programmable 54 is calculated actual pressure ratio, and then produce according to necessity and individually upgrade and be sent to the control signal of variable speed control 40,42 and 44, until the pressure recording the pressure ratio calculating 2% within.Increase thereafter, the data that produce on the basis of signal that can reflect mass flow, the signal being produced by flowmeter 74, for confirming to have obtained desired row flow.If do not obtain desired flow rate, repeat above general introduction process until flow rate desired flow rate about 2% within.
For the object of simplifying, Fig. 2 with 3 and above example hypothesis be air force identical compressor stage; That is, although physically different and with different pressure and volume flow operation, at different levelsly meet identical design rule, and operation to make their hydrodynamic flow be the modification of convergent-divergent effectively each other.
But the operation of multi-stage compression system 1 is not limited to use the identical compressor stage in air force ground.Also can use the not identical level in air force ground.This needs programmable logic controller (PLC) 54 to use the Algebraic Expression of unique flow for example at different levels, pressure and speed behavior.
With reference to figure 4, illustrate multi-stage compression system 1'.For the simplification illustrating, if illustrated element is described in Fig. 1 in Fig. 4, will identify with identical reference number.In multi-stage compression system 1', final compression stage 14' is illustrated as the auxiliary compressor 32'' having in final compressor 30' and auxiliary compression stage 16'.Also comprise flow-control network 90.This flow-control network 90 is provided with bypass line 92, is positioned at the first valve 94 within this bypass line 92 and is positioned at aftercooler 50 second valve 96 between auxiliary compressor 32'.Each in the first valve 94 and second valve 96 can be set as moving in closed position and open position, and be activated by being electrically connected 98 and 100 respectively by programmable logic controller (PLC) 54'.Programmable logic controller (PLC) is programmed, make during normal operating condition, the first valve 94 is set in open position, and second valve 96 is set in closed position, and flow of the compressed gas 20' thus from final compressor 30' with design pressure and supply by bypass line 92 with higher flow rate.In the case, auxiliary compressor 32' is by bypass.During turning down running status, the first valve 94 is set in closed position, and second valve 96 is set in open position, makes auxiliary compressor 30' compressed gas supplying by aftercooler 50, and this Compressed Gas is supplied to auxiliary compressor 32'.Auxiliary compressor 32' thus from its associated aftercooler 52 with identical design pressure but the lower flow rate obtaining is carried out to compressed gas supplying stream 20' during turning down running status.In this respect, multi-stage compression system 1' turns down in the mode that is similar to multi-stage compression system 1, the speed that is the initial compression machine 22 of compression stage 10 is adjusted to a place down along peak efficiencies travel line, and the required pressure of compressor 28,30' and 32' is subsequently divided, to adopt the above mode of setting forth to carry out transporting compressed gas body stream 20' with needed design discharge pressure.Each during along its peak efficiencies travel line when turning down compressor 30' and turning down level before it, compressor assembly 1' allows the conveying of the flow reducing with design pressure.May be necessary to replace single compressor 32' with a series of compression stages, to obtain design pressure under the state of the flow reducing.
With reference to figure 5, illustrate air separation plant 2, this air separation plant 2 combines multi-stage compression system 110, and this multi-stage compression system 110 can be with illustrated form associated with Fig. 1 or Fig. 4, and to control in method described above.Compressibility 110 has compressed air supply stream 112, flows to produce by the compressed air of reference number 114 marks, and therefore this compressed air stream can be compressive flow 20 or the 20' being produced by multi-stage compression system 1 and 1' respectively.Also will be pointed out that, air separation plant 2 does not comprise the preliminary clearning unit for remove high-boiling-point impurity from air supply stream 112, because air separation plant 2 is designed in the encirclement district of air separation plant (enclave), therefore air supply can be focused on.For the same reason, use if air separation plant 2 will be served as independently factory, preliminary clearning unit can be positioned at the downstream of multi-stage compression system 110.Compressed air stream 114 is divided into main air stream 116 and two attached compressed air streams 118 and 120.Main air stream 116 is cooled to and is suitable for the temperature that it distills in air gas separation unit 124 in main heat exchanger 122.
Attached compressed air stream 118 is compressed with production charge air flow 128 in booster compressor 126, this charge air flow 128 is cooled in aftercooler 130, and then within main heat exchanger 122, is partly cooled to the medium temperature between the warm end of the cold-peace temperature of main heat exchanger 122.After cooling by part, charge air flow 128 is introduced into the turbo-expander 138 being connected on booster compressor 126 with production discharge stream 140, and this discharge stream 140 is introduced main heat exchanger 122 and then completely cooling and be introduced into air gas separation unit 124 again.Aforesaid object is that by for air separation plant 2 provides refrigeration, this is for following purpose: overcome the loss of warm end heat exchanger, overcome the heat that enters the ice chest that holds air gas separation unit 124 and rush down leakage, and produce liquid.But, understand, exist the air separation plant of freezing therein and externally being applied, and similarly have the concentrated air separation plant applying in encirclement district of freezing therein.Equally, as being widely known by the people in the art, also exist with the next additive method to air separation plant supply refrigeration of turbo-expander.Therefore, be only to show for illustrated object for the aforementioned means that refrigeration is provided in air separation plant 2, and be not intended to limit scope of the present invention.
Attached compressed air stream 120 then be introduced into booster compressor 142 to produce charge air flow 144, after this charge air flow 144 is cooling in aftercooler 144, completely cooling to produce liquid air stream 146 in main heat exchanger 122, this liquid air stream 146 is also introduced into air gas separation unit 124.The generation of charge air flow 144 is necessary, heated with the stream 152 that returns that makes pumping, and this returns to stream can be liquid oxygen or liquid nitrogen and only show for illustrated object.
As known in the art, air gas separation unit 124 can be double tower unit, and this double tower unit has by condensation reboiler with heat transfer relation operation ground interior associated high-pressure tower and lower pressure column each other.This type of tower all has quality and transmits contact element, such as the combination of dish, structuring filling, random filler or this class component.These elements are the liquid and gas of ingress of air in a manner known in the art, make in the time that liquid phase declines in high or low pressure column, and this liquid phase becomes and is more rich in oxygen, and in the time that gas phase rises in high or low pressure column, this gas phase becomes and is more rich in nitrogen.As known in the art, high-pressure tower is produced rough liquid oxygen bottoms, this rough liquid oxygen bottoms further refines in lower pressure column, and high-pressure tower production nitrogen-rich steam overhead materials, and this nitrogen-rich steam overhead materials is condensation backflow for high and low-pressure tower with generation in condensation reboiler.Lower pressure column is produced oxygen enriched liquid, this oxygen enriched liquid can be used as and returns to stream and 148 be removed, this oxygen enriched liquid is pumped to produce returning of pumping and flows 150 in pump 152, and this returns to stream 150 and is completely heated and produce product with certain pressure in main heat exchanger 122.Lower pressure column is also produced nitrogen-rich steam overhead materials, and this nitrogen-rich steam overhead materials can be used as to be returned to stream and 154 be removed, and then in main heat exchanger 122, is heated to produce nitrogen product completely.
Although not shown, air gas separation unit 124 is in connection with other known heat exchanger, such as sub-cooling unit, to make to the backflow of lower pressure column with by excessively cold the rough liquid oxygen further refining in lower pressure column, and air gas separation unit 124 is in connection with expansion valve, to make this type of stream be expanded to the convenient pressure for introducing lower pressure column.In illustrated embodiment, liquid air stream 146 can expand by expansion valve, and is introduced into lower pressure column and is also introduced into high-pressure tower.Discharge stream 140 can be introduced into lower pressure column maybe may be introduced into high-pressure tower.The unit that main heat exchanger typically is brazed aluminum unit or is arranged in parallel.In addition, main heat exchanger also can be in conjunction with high voltage unit, and this high voltage unit is designed so that charge air flow 142 is cooling and the stream 152 that returns of pumping is heated.Another kind of known possibility is that air gas separation unit 124 can be produced argon product in conjunction with one or more argon columns.Equally, air gas separation unit 124 can be the single tower that is designed to produce nitrogen product.
As indicated above, multi-stage compression unit 110 is designed to play the effect of producing compressed air stream 114 during the normal operating condition of air separation plant 2 with constant pressure, now air separation plant 2 manufactures a product with the speed of production of design, flow 152 such as returning of pumping, and multi-stage compression unit 110 is designed to play the effect of producing compressed air stream 114 with constant pressure during running status of turning down in air separation plant 2, and now product is produced with lower flow rate.Turning down run duration, multi-stage compression system 110 is turned down to reduce the flow rate of compressed air stream 114.Compressed air stream 114 is divided into main air stream 116 and two attached compressed air streams 118 and 120.The flow reducing in compressed air stream 114 can distribute between following stream: attached compressed air stream 120, reduces the production of liquid air stream 146 thus; Attached compressed air stream 118, thus the refrigeration that can be used for air separation plant 2 reduced; And/or the flow rate of reduction compressed air stream 116, make yield reducation.Distribution from the flow of the minimizing of compressed air stream 114 can distribute by any way in compressed air stream 116,118,120, makes the summation of the flow in compressed air stream 116,118 and 120 reach the flow in compressive flow 114.As having the example being designed in the high pressure of production pressurised oxygen product and the factory of lower pressure column, the stream 152 that returns of pumping will be made up of the oxygen enriched liquid removing from lower pressure column.If desired is the production that reduces pressurised oxygen product during turning down running status, flows so 116 and with 120 flow, the flow rate of minimizing and stream 118 can be remained consistent with design and operation process.The speed of booster compressor 142 must increase, to allow blowdown presssure to remain on design level.
Although described the present invention with reference to preferred embodiment, as those of skill in the art will expect, can carry out a large amount of changes, interpolation and omission and not depart from the spirit and scope of the present invention of being set forth as in appended claims.

Claims (20)

1. a method for Compressed Gas, it comprises:
In a series of compression stages, described gas is compressed to higher pressure from lower pressure;
Described compression stage is moved under normal operating condition, and during this period, described gas is with described higher pressure and supply with higher flow rate; And described compression stage is moved turning down under running status, and during this period, described gas is with described higher pressure and supply with lower flow rate;
Described compression stage has the compressor being driven by variable speed motor, these variable speed motor can be with compressor described in multiple speed drive, described speed can be adjusted independently for each described compressor, adjusts thus by the flow rate of described compressor with across the pressure ratio of described compressor; And
Described turn down running status during, adjust the speed of described variable speed motor, and therefore adjust the speed of described compressor and the pressure ratio across described compressor, make the initial portion of the described compressor being associated with the initial portion of described compression stage in the some place operation along its peak efficiencies travel line, herein across the initial pressure of the described initial portion of described compressor than directly proportional with flow rate, and described initial pressure is than the pressure ratio lower than described normal operating condition, lower flow rate described in obtaining thus, and be arranged in continuous compression stage and at the continuous compressor in the downstream of the described initial portion of described compression stage with described lower flow rate and with described pressure ratio operation, this will can carry with described higher pressure described gas.
2. method according to claim 1, wherein, described normal operating condition and described in turn down running status during, described gas is the final compressor supply from the final compression stage of described compression stage all.
3. method according to claim 1, wherein:
During described normal operating condition, described gas with described pressure and with described higher flow rate from final compressor supply, and auxiliary compressor is by bypass;
Described turn down running status during, described auxiliary compressor become with described final compressor fluid be communicated with, and described gas with described pressure and with described lower flow rate from described auxiliary compressor supply.
4. method according to claim 1, wherein, described gas is cooled between described compression stage, and is cooled after compressing in described a series of compression stages.
5. method according to claim 1, wherein, described variable speed motor is direct drive motor, and speed control is connected on described direct drive motor to control the speed of each described direct drive motor.
6. method according to claim 4, wherein, described variable speed motor is direct drive motor, and speed control is connected on described direct drive motor to control the speed of each described direct drive motor.
7. a method that separates air, it comprises:
In a series of compression stages, compress described air, cooling and rear coolingly after compressing in described a series of compressive states, make described air cooling with the inter-stage between described compression stage, described air is compressed to higher pressure from lower pressure within described compression stage;
Described compression stage is moved under normal operating condition, and during this period, described air is with described higher pressure and be provided to main heat exchanger with higher flow rate; And described compression stage is moved turning down under running status, and during this period, described air is with described higher pressure and be provided to described main heat exchanger with lower flow rate;
Make described air cooling in described main heat exchanger after compressed, and described air introducing distillation column system is produced and returned to stream and product stream;
Described in making, return stream and product stream is heated in described main heat exchanger so that described air is cooling;
Described compression stage has the compressor being driven by variable speed motor, these variable speed motor can be with compressor described in multiple speed drive, described speed can be adjusted independently for each described compressor, adjusts thus by the flow rate of described compressor with across the pressure ratio of described compressor; And
Described turn down running status during, adjust the speed of described variable speed motor, and therefore adjust the speed of described compressor and the pressure ratio across described compressor, the initial portion of the described compressor being associated with the initial portion of described compression stage is being moved along its peak efficiencies travel line point place, herein across the initial pressure of the described initial portion of described compressor than directly proportional with flow rate, and described pressure ratio is lower than the pressure ratio under normal operating condition, lower flow rate described in obtaining thus, and be arranged in continuous compression stage and at the continuous compressor in the downstream of the described initial portion of described compression stage with described lower flow rate and with described pressure ratio operation, this will can carry with described higher pressure described gas.
8. method according to claim 7, wherein, during described normal operating condition and described in turn down running status during, described air is the final compressor supply from the final compression stage of described compression stage all.
9. method according to claim 7, wherein:
During described normal operating condition, described air with described higher pressure and with described higher flow rate from final compressor supply, and auxiliary compressor is by bypass; And
Described turn down running status during, described auxiliary compressor become with described final compressor fluid be communicated with, and described gas with described higher pressure and with described lower flow rate from described auxiliary compressor supply.
10. method according to claim 7, wherein, described variable speed motor is direct drive motor, and speed control is connected on described direct drive motor to control the speed of each described direct drive motor.
11. 1 kinds of multi-stage compression systems for Compressed Gas, it comprises:
A series of compression stages, to be compressed to the higher pressure the final level of described compression stage by described gas from lower pressure;
Described multi-stage compression system is constructed to: under normal operating condition, move, during this period, described gas is from described compression stage with described higher pressure and supply with higher flow rate; And move turning down under running status, during this period, described gas is from described compression stage with described higher pressure and supply with lower flow rate;
Described compression stage has the compressor being driven by variable speed motor, these variable speed motor can be with compressor described in multiple speed drive, described speed can be adjusted independently for each described compressor, adjust thus by the flow rate of described compressor with across the pressure ratio of described compressor, and described compression stage has variable speed control, described variable speed control is connected on described compressor and is constructed to adjust independently the speed of described compressor; And
Be connected to the master controller on described variable speed control, and described master controller be constructed to make described turn down running status during, the speed of the speed of described variable speed motor and therefore described compressor and adjusted across the pressure ratio of described compressor, thereby make the initial portion of the described compressor being associated with the described initial portion of described compression stage in the some place operation along its peak efficiencies travel line, herein across the initial pressure of the described initial portion of described compressor than directly proportional with flow rate, and described initial pressure ratio is lower than the initial pressure ratio under normal operating condition, lower flow rate described in obtaining thus, and be arranged in continuous compression stage and at the continuous compressor in the downstream of the described initial portion of described compression stage with described lower flow rate and with described pressure ratio operation, this will make described compression stage to provide described gas with described higher pressure.
12. multi-stage compression systems according to claim 11, wherein, described compression stage be constructed to make described normal operating condition and described in turn down running status during, described gas is the final compressor supply from the final compression stage of described compression stage all.
13. multi-stage compression systems according to claim 11, wherein:
Described compression stage has the final compressor in the final compression stage of described compression stage and the auxiliary compressor in the auxiliary compression stage of described compression stage;
Flow-control network, its there is bypass line, be positioned at described bypass line and be connected to the first valve between the aftercooler on described final compressor and be positioned at described aftercooler and described auxiliary compressor between second valve;
Each in described the first valve and described second valve is set to and can in closed position and open position, moves, make during described normal operating condition, described the first valve is set in described open position and described second valve is set in described closed position, and described gas is supplied by described bypass line with described higher pressure and with described higher flow rate from final compressor, and described auxiliary compressor is by bypass; And
Described turn down running status during, described the first valve is set in described closed position, and described second valve is set in described open position, described auxiliary compressor is connected on described aftercooler, and described gas with described higher pressure and with described lower flow rate from described auxiliary compressor supply.
14. multi-stage compression systems according to claim 11, wherein, described intercooler is positioned between described compression stage, and aftercooler is connected to described a series of compression stage, makes described gas being cooled after compression in described a series of compression stages.
15. multi-stage compression systems according to claim 11, wherein, described variable speed motor is direct drive motor.
16. multi-stage compression systems according to claim 14, wherein, described variable speed motor is direct drive motor.
17. 1 kinds of air separation plant, it comprises:
A series of compression stages, to be compressed to the higher pressure the final level of described compression stage by described air from lower pressure;
At the intercooler between described a series of compression stages and be connected to the aftercooler in the described final level of described compression stage;
Described multi-stage compression system, it is constructed to: under normal operating condition, move, during this period, described air is from described compression stage with described higher pressure and supply with higher flow rate; And move turning down under running status, during this period, described air is from described compression stage with described higher pressure and supply with lower flow rate;
Described compression stage has the compressor being driven by variable speed motor, these variable speed motor can be with compressor described in multiple speed drive, described speed can be adjusted independently for each described compressor, adjust thus by the flow rate of described compressor with across the pressure ratio of described compressor, and described compression stage has variable speed control, described variable speed control is connected on described compressor and is constructed to adjust independently the speed of described compressor;
Main heat exchanger, it is connected on described multi-stage compression system and is constructed to make described air cooling after described air is compressed;
Distillation column system, it is constructed to produce return and flows and product stream, described distillation column system is connected on described main heat exchanger, make described air be introduced into described distillation column system after cooling in described main heat exchanger, and described in return stream and product stream is heated in described main heat exchanger so that described air is cooling; And
Master controller, it is connected on described variable speed control, and be constructed to make described turn down running status during, the speed of the speed of described variable speed motor and therefore described compressor is adjusted, make the initial portion of the described compressor being associated with the initial portion of described compression stage in the some place operation along its peak efficiencies travel line, herein across the initial pressure of the described initial portion of described compressor than directly proportional with flow rate, and described initial pressure ratio is lower than the initial pressure ratio under described normal operating condition, lower flow rate described in obtaining thus, be arranged in continuous compression stage and at the continuous compressor in the downstream of the described initial portion of described compression stage with described lower flow rate and with described pressure ratio operation, this will make described compression stage to supply described gas with described higher pressure.
18. air separation plant according to claim 17, wherein, described compression stage be constructed to make described normal operating condition and described in turn down running status during, the final compressor supply of described air from the final compression stage of described compression stage.
19. air separation plant according to claim 17, wherein:
Described compression stage has the final compressor in the final compression stage of described compression stage and the auxiliary compressor in the auxiliary compression stage of described compression stage;
Flow-control network is connected on described final compressor and described auxiliary compressor, described capaciated flow network there is bypass line, be positioned at described bypass line and be connected to the first valve between the aftercooler on described final compressor and be positioned at described aftercooler and described auxiliary compressor between second valve;
Each in described the first valve and described second valve is set to and can in closed position and open position, moves, make during described normal operating condition, described the first valve is set in described open position, and described second valve is set in described closed position, and described air is supplied by described bypass line with described higher pressure and with described higher flow rate from final compressor, and described auxiliary compressor is by bypass; And
During turning down running status, described the first valve is set in closed position and described second valve is set in open position, described auxiliary compressor is connected on described aftercooler, and described air with described higher pressure and with described lower flow rate from described auxiliary compressor supply.
20. air separation plant according to claim 17, wherein, described variable speed motor is direct drive motor.
CN201280018560.9A 2011-04-15 2012-03-29 Compression method and air separation Pending CN103946654A (en)

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Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106762756A (en) * 2016-12-15 2017-05-31 福建景丰科技有限公司 A kind of weaving air compression system and air compression method
CN107202011A (en) * 2016-03-16 2017-09-26 株式会社日立产机系统 Compound compressor
CN108139144A (en) * 2015-10-15 2018-06-08 普莱克斯技术有限公司 For compressing the method for the feed air stream in low temp air fractionation system
CN108139147A (en) * 2015-10-15 2018-06-08 普莱克斯技术有限公司 For compressing and cooling down the system of the feed air stream in low temp air fractionation system and device
CN108139148A (en) * 2015-10-30 2018-06-08 普莱克斯技术有限公司 For controlling the method for the compression into the feed air stream of low temp air fractionation system
CN108139145A (en) * 2015-10-15 2018-06-08 普莱克斯技术有限公司 For compressing the method for the feed air stream in low temp air fractionation system
CN108139146A (en) * 2015-10-15 2018-06-08 普莱克斯技术有限公司 For compressing the method for the feed air stream in low temp air fractionation system

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20150114037A1 (en) * 2013-10-25 2015-04-30 Neil M. Prosser Air separation method and apparatus
US10378536B2 (en) * 2014-06-13 2019-08-13 Clark Equipment Company Air compressor discharge system
DE102016112453A1 (en) * 2016-07-07 2018-01-11 Man Diesel & Turbo Se Geared turbine machine
CN108691851A (en) * 2018-06-04 2018-10-23 肇庆市高新区晓靖科技有限公司 A kind of Pneumatic fixture of intermetallic composite coating polishing

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6178775B1 (en) * 1998-10-30 2001-01-30 The Boc Group, Inc. Method and apparatus for separating air to produce an oxygen product
CN1296162A (en) * 1999-11-12 2001-05-23 普拉塞尔技术有限公司 Low-temp. system for producing cencentraded air
US20020119050A1 (en) * 2001-02-23 2002-08-29 Kabushiki Kaisha Kobe Seiko Sho (Kobe Steel, Ltd) Multi-stage variable speed compressor
CN1402814A (en) * 1999-10-26 2003-03-12 艾拉斯科普库空气动力股份有限公司 Multistage compressor unit and method for regulating such multistage compressor unit
CN101501431A (en) * 2006-06-09 2009-08-05 普莱克斯技术有限公司 Air separation method

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4853567A (en) * 1987-03-02 1989-08-01 Yokogawa Electric Corporation Direct drive motor
WO2007095537A1 (en) * 2006-02-13 2007-08-23 Ingersoll-Rand Company Multi-stage compression system and method of operating the same
WO2009056987A2 (en) * 2007-11-01 2009-05-07 Danfoss Turbocor Compressors Bv. Multi-stage compressor

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6178775B1 (en) * 1998-10-30 2001-01-30 The Boc Group, Inc. Method and apparatus for separating air to produce an oxygen product
CN1402814A (en) * 1999-10-26 2003-03-12 艾拉斯科普库空气动力股份有限公司 Multistage compressor unit and method for regulating such multistage compressor unit
CN1296162A (en) * 1999-11-12 2001-05-23 普拉塞尔技术有限公司 Low-temp. system for producing cencentraded air
US20020119050A1 (en) * 2001-02-23 2002-08-29 Kabushiki Kaisha Kobe Seiko Sho (Kobe Steel, Ltd) Multi-stage variable speed compressor
CN101501431A (en) * 2006-06-09 2009-08-05 普莱克斯技术有限公司 Air separation method

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108139144A (en) * 2015-10-15 2018-06-08 普莱克斯技术有限公司 For compressing the method for the feed air stream in low temp air fractionation system
CN108139147A (en) * 2015-10-15 2018-06-08 普莱克斯技术有限公司 For compressing and cooling down the system of the feed air stream in low temp air fractionation system and device
CN108139145A (en) * 2015-10-15 2018-06-08 普莱克斯技术有限公司 For compressing the method for the feed air stream in low temp air fractionation system
CN108139146A (en) * 2015-10-15 2018-06-08 普莱克斯技术有限公司 For compressing the method for the feed air stream in low temp air fractionation system
CN108139144B (en) * 2015-10-15 2020-10-20 普莱克斯技术有限公司 Method for compressing a feed air stream in a cryogenic air separation plant
CN108139148A (en) * 2015-10-30 2018-06-08 普莱克斯技术有限公司 For controlling the method for the compression into the feed air stream of low temp air fractionation system
CN107202011A (en) * 2016-03-16 2017-09-26 株式会社日立产机系统 Compound compressor
CN106762756A (en) * 2016-12-15 2017-05-31 福建景丰科技有限公司 A kind of weaving air compression system and air compression method
CN106762756B (en) * 2016-12-15 2019-05-31 福建景丰科技有限公司 A kind of weaving air compression system and air compression method

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