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US20190145703A1 - Mehod for gradual sealing of a gas - Google Patents

Mehod for gradual sealing of a gas Download PDF

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Publication number
US20190145703A1
US20190145703A1 US15/999,800 US201715999800A US2019145703A1 US 20190145703 A1 US20190145703 A1 US 20190145703A1 US 201715999800 A US201715999800 A US 201715999800A US 2019145703 A1 US2019145703 A1 US 2019145703A1
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Prior art keywords
main line
feedback amount
pressure
compression
pressure level
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Abandoned
Application number
US15/999,800
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English (en)
Inventor
Torben Hofel
Sean McCracken
Martin Kamann
Eva-Maria Katzur
Jorg Matthes
Thomas Bretschneider
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Linde GmbH
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Linde GmbH
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Assigned to LINDE AKTIENGESELLSCHAFT reassignment LINDE AKTIENGESELLSCHAFT ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: BRETSCHNEIDER, THOMAS, MATTHES, JORG, KATZUR, EVA-MARIE, HOFEL, TORBEN, KAMANN, MARTIN, McCracken, Sean
Publication of US20190145703A1 publication Critical patent/US20190145703A1/en
Abandoned legal-status Critical Current

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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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/029—Mechanically coupling of different refrigerant compressors in a cascade refrigeration system to a common driver
    • 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
    • F04D29/00—Details, component parts, or accessories
    • F04D29/58—Cooling; Heating; Diminishing heat transfer
    • F04D29/582—Cooling; Heating; Diminishing heat transfer specially adapted for elastic fluid pumps
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
    • F25J1/0282—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
    • F25J3/0204—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 characterised by the feed stream
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • 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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/0238—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 characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • 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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/0266—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 characterised by the separated product stream separation of carbon dioxide
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/62—Ethane or ethylene
    • 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
    • F25J2230/04—Compressor cooling arrangement, e.g. inter- or after-stage cooling or condensate removal
    • 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
    • F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
    • 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
    • F25J2230/22—Compressor driver arrangement, e.g. power supply by motor, gas or steam turbine
    • 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
    • F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
    • 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
    • F25J2230/80—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being carbon dioxide
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/80—Quasi-closed internal or closed external carbon dioxide refrigeration cycle
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/88—Quasi-closed internal refrigeration or heat pump cycle, if not otherwise provided
    • 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
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • the invention relates to a method for compressing a gas in stages in a compressor arrangement having a plurality of compression stages which are connected together sequentially by a main line, and to a corresponding compressor arrangement according to the preamble of the independent claims.
  • gas mixtures are obtained which, after separating water and oily constituents, if present (so-called pyrolysis oil), still substantially contain hydrogen, methane and hydrocarbons having two and more carbon atoms.
  • Gas mixtures of this type can be separated in separating sequences, as are basically known to a person skilled in the art and are also described in the mentioned article.
  • the conventional target product in steam cracking namely ethylene, is also separated from the other components in appropriate separating sequences. In this respect, ethylene is typically drawn off from the top of a so-called C2 splitter.
  • ethylene can be released to the plant limit under different conditions.
  • ethylene is released under elevated pressure in the form of gas.
  • compression is carried out in single-stage or multi-stage turbocompressors. Since ethylene is also used as a refrigerant in the mentioned separating sequences, it is also compressed for this purpose.
  • Ethylene is typically compressed for the mentioned purposes in a common turbocompressor having a plurality of compression stages and intermediate cooling, which is thus also used as the product compressor and as the refrigerant compressor.
  • the ethylene is removed from this turbocompressor for use as refrigerant and as product at different pressure levels corresponding to different compression stages.
  • a corresponding turbocompressor is shown schematically in the accompanying FIG. 1 and is described in more detail below. However, in principle it is also possible to use a plurality of separate, in particular multi-stage, turbocompressors for refrigerant and product compression.
  • the release of ethylene at a supercritical pressure level is required.
  • the ethylene can either be liquefied and then conveyed at a supercritical pressure level by a pump, or it is brought to the corresponding pressure level in a multi-stage compressor of the described type.
  • the latter case is shown schematically in the accompanying FIG. 2 and is also described in more detail below.
  • the product is compressed in stages IV to VI and the refrigerant is compressed in stages I to III. Compression without liquefaction is the more favourable alternative in terms of energy.
  • the invention proposes a method for compressing a gas in stages in a compressor arrangement having a plurality of compression stages which are connected together sequentially by a main line, and a corresponding compressor arrangement having the features of the independent claims.
  • Embodiments are the subject of the dependent claims and of the following description.
  • pressure level and “temperature level”, which are intended to signify that corresponding pressures and temperatures in a corresponding plant do not have to be used as exact pressure and temperature values in order to realise the inventive concept.
  • pressures and temperatures are typically within particular ranges which lie, for example ⁇ 1%, 5%, 10%, 20% or even 50% around an average.
  • corresponding pressure levels and temperature levels can lie within disjoint ranges or within overlapping ranges.
  • pressure levels include pressure losses which are unavoidable or which are to be expected. The same applies accordingly to temperature levels.
  • Pressure levels which are stated here in bar are absolute pressures.
  • the critical temperature of ethylene is approximately 8° C. This temperature is low enough for liquefaction to be ruled out by an intermediate cooling with cooling water downstream of a compression stage. Cooling water is typically at a temperature of at least 10° C.
  • howevor, typically provided in multi-stage turbocompressors are return lines, or so-called kickbacks, which, under partial load or other intermittently occurring operating states, expand ethylene to a lower pressure level from the pressure side of a compression stage and feed it back on the suction side to the same compression stage or to a compression stage which is arranged upstream thereof. This is also shown in FIG. 2 and is described in more detail below.
  • the present invention proposes a method for compressing a gas in stages in a compressor arrangement having a plurality of compression stages which are connected together sequentially by a main line.
  • the compression stages can be configured in particular as turbocompression stages, as previously described.
  • the compression stages can be partly or entirely driven by common mechanical devices, for example common shafts, and in this way they are coupled together mechanically.
  • the gas used in the present invention can be, for example, an ethylene-rich gas.
  • An ethylene-rich gas of this type can also be pure or substantially pure ethylene, i.e. it can contain at least 90%, 95% or 99% ethylene. Since in the context of the present invention the ethylene-rich gas can be removed in particular from the top of a known C2 splitter (see the specialist literature mentioned at the beginning), it has in particular the usual ethylene content in this connection. For simplification purposes, a corresponding ethylene-rich gas will also be referred to in the following as “ethylene”.
  • the present invention is also suitable, for example, for the compression of ethane or carbon dioxide, which have comparable thermodynamic characteristic quantities, or for corresponding ethane-rich and carbon dioxide-rich gases.
  • the gas which is guided through the main line is respectively compressed from a suction-side pressure level to a pressure-side pressure level and is heated by this compression from a suction-side temperature level to a pressure-side temperature level.
  • suction-side pressure level is understood as meaning the pressure level at which the gas is fed to the compression stage. This suction-side pressure level is also commonly known as “suction pressure”.
  • pressure-side pressure level is the pressure level to which the compression stage compresses the gas.
  • suction-side temperature level is understood as meaning the temperature level at which a corresponding gas is fed to the compression stage. This temperature level is no longer actively influenced before the gas is fed into the compressor, in particular the gas is no longer actively heated or cooled from a suction-side temperature level.
  • a “pressure-side temperature level” denotes the temperature level directly downstream of a corresponding compression stage, thus the pressure-side temperature level is the pressure level at which a corresponding gas leaves the compression stage. Therefore, downstream of the compression stage, the temperature level is no longer actively influenced to reach the pressure-side temperature level, in particular there is no heating or active cooling in a cooler. If an intermediate cooler is used downstream of the compression stage, the “pressure-side temperature level” is present up to the entry of the gas into the intermediate cooler.
  • a feedback amount of the gas guided through the main line is at least temporarily removed from the main line downstream of one of the compression stages, is fed to an expansion process and after expansion is fed back into the main line upstream of the same compression stage.
  • feedback “upstream of the same compression stage” can mean, as also explained below, feedback directly upstream of the compression stage downstream of which the feedback amount was removed; however, feedback can also take place upstream of one or more further compression stages which are arranged upstream of the compression stage downstream of which the feedback amount was removed from the main line.
  • a corresponding liquid phase formation cannot exclusively occur when the pressure-side pressure level of the compression stage downstream of which the feedback amount is removed from the main line is above a supercritical pressure level and this feedback amount is expanded to a subcritical pressure level, but during normal operation of a corresponding plant it is a disadvantage particularly during a “transcritical” expansion of this type. Therefore, the present invention focuses on corresponding cases of transcritical compression and expansion.
  • the invention therefore provides that the pressure-side pressure level of the compression stage downstream of which the feedback amount is removed from the main line is a supercritical pressure level, that the feedback amount is expanded to a subcritical pressure level and that the feedback amount is fed to the expansion process at the pressure-side temperature level of the compression stage downstream of which it is removed from the main line.
  • the feedback amount is cooled only after being expanded and before and/or after being fed back into the main line.
  • corresponding problems can also arise if the feedback amount is expanded during normal operation from a supercritical to a supercritical pressure level (i.e. for example in stage VI of the arrangement shown in FIG. 2 or of a corresponding feedback amount).
  • a supercritical pressure level i.e. for example in stage VI of the arrangement shown in FIG. 2 or of a corresponding feedback amount.
  • the pressure level of the feedback can temporarily lie below the critical pressure level or can fall to a corresponding value.
  • considerable fluctuations in the pressure levels can potentially be recorded until a corresponding plant has (again) reached a steady state.
  • An advantageous embodiment of the method according to the invention therefore provides that a further feedback amount of the gas, guided through the main line, is at least temporarily removed from the main line downstream of a further compression stage, is fed to an expansion process, and is fed back into the main line upstream of the same further compression stage, that the pressure-side pressure level of the further compression stage downstream of which the further feedback amount is removed from the main line is a supercritical pressure level, that this further feedback amount is expanded to a supercritical pressure level, and that the feedback amount is cooled only after being expanded and before and/or after being fed back into the main line. In this way, liquefaction is also avoided in this case.
  • liquefaction can also occur when a pressure-side pressure level is below the supercritical pressure level, namely when the feedback amount before expansion is at a subcritical pressure level and simultaneously at a temperature level at which the two-phase region can be achieved by simple expansion.
  • a pressure level of approximately 48 bar and a temperature level of approximately 10° C.
  • a point defined by a corresponding pressure level and temperature level is located above the two phase line.
  • a further embodiment of the present invention provides that an additional feedback amount of the gas, guided through the main line, is at least temporarily removed from the main line downstream of an additional compression stage, is fed to an expansion process, and is fed back into the main line upstream of the same additional compression stage, that the pressure-side pressure level of the additional compression stage downstream of which the further feedback amount is removed from the main line is a subcritical pressure level, that this additional feedback amount is expanded to a subcritical pressure level, and that the feedback amount is cooled only after being expanded and before and/or after being fed back into the main line.
  • the present invention solves the problem of liquefaction in the mentioned cases in that the feedback amount (the following explanations also relate to a plurality of feedback amounts) is fed to the expansion process at the pressure-side temperature level of the compression stage downstream of which it is removed from the main line.
  • a corresponding feedback amount is not cooled downstream of the relevant compression stage at which the feedback amount is formed, before the expansion thereof.
  • the expansion preferably takes place isenthalpically, i.e. a throttle valve is preferably used for the expansion.
  • cooling does not take place before the expansion of the feedback amount after it has been removed from the main line.
  • the feedback amount is cooled following expansion and before and/or after being fed back into the main line, for which purpose a separate heat exchanger can be provided in a return line used for returning the feedback amount and/or in the main line downstream of the infeed point of the feedback amount.
  • a separate heat exchanger of this type can be advantageous, because in this way the cooling of a corresponding feedback amount can be adapted individually to the respectively required conditions.
  • the feedback amount is fed into the main line without cooling or after (partial) cooling in a separate heat exchanger in the return line and is cooled there by the heat exchanger, which is also used for cooling the remaining gas which has not been fed back and is present in the main line.
  • a corresponding plant can be set up in a relatively simple and cost-effective manner.
  • the feedback amount does not necessarily have to be fed back into the main line directly upstream of the compression stage downstream of which it was removed from the main line.
  • the feedback amount can be advantageously fed back into the main line upstream of one or more compression stages which are arranged upstream of the compression stage downstream of which the feedback amount is removed from the main line.
  • the suction-side pressure levels of a plurality of upstream compression stages can be influenced in a particularly advantageous manner using a feedback amount.
  • the feedback amount is advantageously controlled based on an attainable or attained suction-side or pressure-side pressure level of one of the compression stages.
  • the product pressure can be fixed by a controlled valve which is arranged downstream of the last compression stage. This valve fixes the product pressure, i.e. the pressure-side pressure level of the last compression stage.
  • a pressure level of this type can be for example approximately 125.6 bar.
  • the pressure-side temperature level, downstream of an aftercooling downstream of the last compression stage can be for example approximately 40° C.
  • the suction-side pressure level of an upstream compression stage which is charged with ethylene from a high pressure ethylene refrigerant circuit and which compresses the gas in the main line to a pressure level of, for example, approximately 22.5 bar can be adjusted by the rotational speed of this compression stage.
  • the suction-side pressure level of the compression stages arranged upstream thereof is also fixed thereby in a corresponding multi-stage turbocompressor. If a corresponding suction-side pressure level is not attained, for example during partial load, a control can be carried out by opening appropriate kickbacks, i.e. by providing or increasing an appropriate feedback amount.
  • the entry conditions of the individual compression stages can vary to different extents.
  • the thermodynamic characteristics of the fluid under elevated pressure can have a disproportionate effect. Consequently, downstream compression stages in a corresponding multi-stage turbocompressor increasingly generate too much pressure, possibly during partial load or if the cooling water is too cold.
  • a control can be carried out by adjusting appropriate feedback amounts.
  • the present invention is particularly advantageous in cases of fluctuating cooling water temperatures, because within the context of the present invention the temperature of the feedback amount can no longer fall below the cooling water temperature, because this is firstly expanded and is only then cooled.
  • the temperature level will fall below the cooling water temperature, because further cooling takes place starting from the temperature reached by cooling.
  • the suction-side pressure level of a compression stage is set by the opening the provision or increase of the feedback amount.
  • the pressure-side temperature level of such a compression stage becomes increasingly cold by increasing the correspondingly cold feedback amount. This produces disadvantages in terms of control in this compression stage and in the downstream compression stages.
  • a plurality of the compression stages may be driven by one or more common shafts, to which the respective compression stages are mechanically coupled.
  • Appropriate shafts allow a plurality of compression stages to be driven jointly, so that only one drive unit has to be provided.
  • the use of a plurality of shafts is advantageous if particular compression stages are to be controlled separately, particularly in the previously mentioned cases.
  • a plurality of the compression stages can be respectively driven by a plurality of common shafts, thereby simplifying a corresponding control.
  • a plurality of common shafts can be mechanically coupled together by a transmission, so that for example a particular transmission ratio, which can also be adjustable by an adjustable transmission, can be achieved.
  • the present invention also relates to a plant which is configured for compressing a gas in stages and to a compressor arrangement which comprises a plurality of compression stages which are connected together sequentially by a main line and in which the gas, guided through the main line, can be respectively compressed from a suction-side pressure level to a pressure-side pressure level and can be heated by this compression from a suction-side temperature level to a pressure-side temperature level, means being provided which are configured to at least temporarily remove a feedback amount of the gas, guided through the main line, from the main line downstream of one of the compression stages, to feed it to an expansion process and to feed it back into the main line upstream of the same compression stage.
  • the plant is configured to be operated such that the pressure-side pressure level of the compression stage downstream of which the feedback amount is removed from the main line is a supercritical pressure level and the feedback amount is expanded to a subcritical pressure level.
  • Means are provided which are configured to feed the feedback amount to the expansion process at the pressure-side temperature level of the compression stage downstream of which the feedback amount is removed from the main line.
  • means are provided which are configured to cool the feedback amount only after it has been expanded and before and/or after it is fed back into the main line.
  • a plant of this type benefits from the previously explained features and advantages. It is advantageously configured to implement a method which has been previously described. Therefore, reference is explicitly made to the corresponding features and advantages.
  • FIG. 1 shows a multi-stage compressor arrangement according to an embodiment which is not according to the invention.
  • FIG. 2 shows a multi-stage compressor arrangement according to an embodiment which is not according to the invention.
  • FIG. 3 shows a multi-stage compressor arrangement according to a particularly preferred embodiment of the invention.
  • FIG. 4 shows a multi-stage compressor arrangement according to a particularly preferred embodiment of the invention.
  • FIG. 5 shows a multi-stage compressor arrangement according to a particularly preferred embodiment of the invention.
  • FIG. 1 shows a multi-stage compressor arrangement according to an embodiment which is not according to the invention and is designated overall by reference sign 500 .
  • the compressor arrangement 500 is configured to provide ethylene at a pressure level of approximately 40 bar, i.e. at a subcritical pressure level.
  • the invention is also suitable for compressing other gases such as methane and carbon dioxide.
  • the compressor arrangement 500 comprises a plurality of compression stages which are designated here by Roman numerals I to IV.
  • the compression stages I to IV are connected together by a main line 1 .
  • the compression stages I to IV are arranged on a common shaft 8 in the compressor arrangement 500 .
  • Ethylene is fed to compression stages I, II and III from ethylene refrigerant circuits at different pressure and temperature levels via corresponding lines 2 to 4 .
  • Line 2 conveys ethylene out of a low-pressure refrigerant circuit at approximately 1.05 bar
  • line 3 conveys ethylene out of a medium-pressure refrigerant circuit at approximately 3 bar
  • line 4 conveys ethylene out of a high-pressure refrigerant circuit at approximately 8.1 bar.
  • the ethylene is compressed from the mentioned 1.05 bar, the suction-side pressure level of the first compression stage I, to a pressure-side pressure level of approximately 3 bar, which is at the same time the suction-side pressure level of the second compression stage II.
  • Compression stage II compresses the ethylene in the main line 1 to a pressure-side pressure level of approximately 8.1 bar, which is at the same time the suction-side pressure level of the third compression stage III.
  • the ethylene is compressed to a pressure-side pressure level of approximately 22.5 bar, which is at the same time the suction-side pressure level of the fourth compression stage IV.
  • the ethylene is compressed to a pressure-side pressure level of approximately 40 bar, at which it can be released as product via a line 5 .
  • ethylene is fed in, for example from the top of a C2 splitter.
  • the compressor arrangement 500 is configured as a combined refrigerant and product compressor, an intermediate extraction line 6 is provided for extracting refrigerant and optionally a return flow to the C2 splitter.
  • respective aftercoolers IIa to IVa are provided in which the ethylene is respectively cooled to approximately 40° C. Since on the suction side of the third compression stage III cold ethylene is also fed in from the high-pressure refrigerant circuit, upon entry into the third compression stage III a mixed temperature of approximately 18° C. is produced.
  • the entry temperature of the ethylene out of the low-pressure refrigerant circuit into the first compression stage I is approximately ⁇ 57° C. and the entry temperature of the ethylene out of the medium-pressure refrigerant circuit into the second compression stage II is approximately 14° C.
  • feedback amounts can be respectively removed from the main line 1 downstream of compression stages II to IV and can be fed back into the main line 1 upstream of these compression stages.
  • the feedback amounts are expanded via valves which are not denoted separately.
  • the problem of the initially mentioned liquefying effects typically arises to a lesser extent, because a supercritical pressure level is not reached here.
  • FIG. 2 shows a compressor arrangement 600 according to a further embodiment which is not according to the invention.
  • the compression stages I to IV and the interconnection thereof has already been described.
  • the compression stages I to IV are arranged on a common shaft 8 .
  • two further compression stages V and VI are provided in the compressor arrangement 600 according to FIG. 2 . These are arranged on a common shaft 9 in the compressor arrangement 600 and further compress the ethylene, released via the line 5 as product in the compressor arrangement 500 according to FIG. 1 to a supercritical pressure level.
  • the ethylene compressed to approximately 40.2 bar and cooled to a temperature level of approximately 40° C., is fed to the fifth compression stage V in the compressor arrangement 600 .
  • the suction-side pressure level of this compression stage V is approximately 40.2 bar.
  • the ethylene is compressed to a pressure-side pressure level of approximately 70.4 bar from this suction-side pressure level. In so doing it heats up, and is cooled in an aftercooler Va to approximately 40° C.
  • the ethylene is fed to a compression stage VI in which it is compressed to a pressure-side pressure level of approximately 125.6 bar. After cooling in an aftercooler VIa to approximately 40° C., the ethylene is released as product at a temperature level of approximately 40° C. and at the mentioned pressure level via a line 5 .
  • compression stages V and VI are also provided downstream of compression stages V and VI , by which feedback amounts can be respectively removed from the main line 1 and can be fed back into the main line upstream of the respective compression stages.
  • return lines 7 by which feedback amounts can be respectively removed from the main line 1 and can be fed back into the main line upstream of the respective compression stages.
  • the shafts 8 and 9 can be connected together by a transmission, as also shown in the following FIGS. 3 and 4 .
  • the rotational speed of compression stages I to VI can no longer be controlled independently of the other compression stages. If the suction-side pressure level of compression stage V is now reduced, for example because a smaller amount of ethylene is fed in via line 4 , this can only be counteracted by opening the return line 7 downstream of the aftercooler Va. This is not a problem provided that it is ensured by the cooling water temperature in the aftercooler Va that the feedback amount, guided in the return line 7 downstream of the aftercooler Va, is at a sufficiently high temperature, for example approximately 40° C.
  • the feedback amount, guided in the return line 7 downstream of the aftercooler Va, can fall to a value of for example 20° C.
  • This temperature is further reduced due to the expansion in the expansion valve.
  • the suction-side temperature level of compression stage V thereby also falls, and thus also the suction-side pressure level.
  • this can only be counteracted by returning a greater feedback amount which in turn, however, causes the suction-side temperature level of compression stage V to fall further.
  • a very large amount of ethylene is circulated without any benefit. This also affects the downstream compressor stages.
  • FIG. 3 schematically shows a compressor arrangement according to an embodiment of the invention which is designated overall by reference sign 100 .
  • the compressor arrangement 100 is largely the same as the compressor arrangement 600 according to FIG. 2 .
  • the return line 7 is arranged downstream of the aftercooler Va
  • a corresponding return line, designated here by reference sign 10 for the purposes of clarity, according to the embodiment of the compressor arrangement 100 according to the invention which is shown in FIG. 3 branches off from the main line 1 upstream of this aftercooler and directly downstream of compression stage 5 .
  • This measure can ensure that a feedback amount which is guided through the return line 10 and is branched off from the main line 1 is expanded in an expansion device 11 , for example an expansion valve, from a higher temperature level than in the compressor arrangement 600 according to FIG. 2 . In this way, no liquefying effects can occur during expansion in the expansion device 11 .
  • an expansion device 11 for example an expansion valve
  • a separate cooler 12 which can cool the expanded feedback amount in the return line 10 . After cooling, the feedback amount is fed back into the main line 1 out of the return line 10 .
  • the embodiment of the compressor arrangement 100 according to the invention which is shown in FIG. 3 also differs from the compressor arrangement 600 according to FIG. 2 in that the common shaft 8 interconnects compression stages I to IV and the common shaft 9 interconnects compression stages V and VI.
  • the shafts 8 and 9 are connected together by a transmission 13 .
  • a common drive 14 for example a steam turbine, can thus drive the shaft 8 and the shaft 9 .
  • the speed of the transmission 13 can be configured to be variable or fixed.
  • FIG. 4 shows a compressor arrangement according to a further embodiment of the invention which is designated overall by reference sign 200 .
  • the compressor arrangement 200 according to FIG. 4 is largely the same as the compressor arrangement 100 according to FIG. 3 , although here as well, the return line is configured downstream of compression stage VI, just as the return line downstream of compression stage V.
  • the same reference signs are used and reference is made to the above descriptions.
  • undesirable liquefaction is thus avoided which could occur during abnormal operating states, such as start-up or malfunction.
  • FIG. 5 shows a compressor arrangement according to a further embodiment of the invention which is designated overall by reference sign 300 .
  • the return line 10 branches off directly downstream of compression stage VI and delivers a feedback amount of ethylene to an expansion process in an expansion valve 11 .
  • the ethylene is fed back into the main line 1 directly downstream of the expansion in the expansion device 17 , more specifically not directly upstream of compression stage VI, but upstream of compression stage V.
  • a further aftercooler 15 is provided downstream of the ethylene feed-in point of the return flow from the return line 16 .
  • the shafts 8 and 9 of the compressor arrangement 300 are configured separately from one another, separate drives 14 being respectively provided.

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  • Engineering & Computer Science (AREA)
  • General Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Chemical & Material Sciences (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Applications Or Details Of Rotary Compressors (AREA)
  • Structures Of Non-Positive Displacement Pumps (AREA)
  • Control Of Positive-Displacement Pumps (AREA)
  • Control Of Positive-Displacement Air Blowers (AREA)
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US15/999,800 2016-02-19 2017-02-20 Mehod for gradual sealing of a gas Abandoned US20190145703A1 (en)

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EP16156574.2 2016-02-19
EP16156574.2A EP3208465B1 (de) 2016-02-19 2016-02-19 Verfahren zur stufenweisen verdichtung eines gases
PCT/EP2017/053796 WO2017140910A1 (de) 2016-02-19 2017-02-20 Verfahren zur stufenweisen verdichtung eines gases

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TW201740023A (zh) 2017-11-16
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ZA201806120B (en) 2022-05-25
EA201891652A1 (ru) 2019-02-28
ES2718742T3 (es) 2019-07-04
TWI708013B (zh) 2020-10-21
AU2017220699A1 (en) 2018-08-30
KR20180121909A (ko) 2018-11-09
WO2017140910A1 (de) 2017-08-24
BR112018016711A2 (pt) 2018-12-26
CN108884836B (zh) 2020-08-11
EP3208465B1 (de) 2019-01-09
EA037004B1 (ru) 2021-01-26
EP3208465A1 (de) 2017-08-23
MY192620A (en) 2022-08-29
CA3013993A1 (en) 2017-08-24

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