CA2511403A1 - Hybrid turbo expander and refrigerated lean oil absorber system - Google Patents

Hybrid turbo expander and refrigerated lean oil absorber system Download PDF

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Publication number
CA2511403A1
CA2511403A1 CA002511403A CA2511403A CA2511403A1 CA 2511403 A1 CA2511403 A1 CA 2511403A1 CA 002511403 A CA002511403 A CA 002511403A CA 2511403 A CA2511403 A CA 2511403A CA 2511403 A1 CA2511403 A1 CA 2511403A1
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Canada
Prior art keywords
lean oil
turbo expander
gas
natural gas
ethane
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Abandoned
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CA002511403A
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French (fr)
Inventor
Ian M.J. Richardson
Glen F. Perry
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ENERGY TRUST MARKETING LTD.
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Priority to CA002511403A priority Critical patent/CA2511403A1/en
Publication of CA2511403A1 publication Critical patent/CA2511403A1/en
Abandoned legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • 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
    • F25J3/0209—Natural gas or substitute natural gas
    • 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
    • F25J3/0233—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 1 carbon atom 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
    • F25J3/0238—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
    • F25J3/0242—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 3 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
    • F25J3/0247—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 4 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/30—Processes or apparatus using separation by rectification using a side column in a single pressure column system
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/94—Details relating to the withdrawal point
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed 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
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Description

Hydrid Turbo Expander and Refrigerated Lean Oil Absorber System Background Information - Current Industry Practice There are essentially three processes that are utilized to recover natural gas liquids ("NGLs") from natural gas, depending primarily on the desired degree of ethane recovery. These include:
1. Lean oil absorption for low ethane recovery percentages - The objective in these applications is to minimize capital costs while capturing most of the propane and heavier components in the natural gas. Any ethane that's recovered tends to be incidental, generally in the 10 to 15% range.
2. Refrigerated lean oil absorption for intermediate ethane recovery percentages - The objective in these applications is to increase NGL
recovery percentages, including those for ethane, if ethane recovery is desirable, while minimizing capital costs. Ethane recovery percentages are typically in the 30°!° range. It utilizes a lean oil system but chills the incoming natural gas and the lean oil using mechanical refrigeration (usually a propane system). This type of system might also be utilized when the natural gas pressure is too low to warrant the installation of a turbo expander as discussed in 3.
3. Turbo expander for high ethane recovery percentages ("deep cut") -The turbo expander drops the pressure of the incoming natural gas and captures the "cold" produced in the expansion process, thus eliminating the need for mechanical refrigeration. Depending on the inlet pressure and C02 content of the gas, ethane recovery percentages can bewery high, exceeding 90%. When high efficiency operations are not required a Joule-Thompson (JT) valve might be utilized instead of a turbo expander; however, inlet gas pressures exceeding 1000 psi are required to provide reasonable ethane recoveries.
40220183.1 ,.

Unigue Combination of Current Technologies to Provide New Processing S-_ sY tem There are several unique aspects incorporated in this new processing system, namely:
1. Removes C02 from all the natural gas fed to the system prior to NGL
recovery.
2. Splits the natural gas flow, utilizing a turbo expander on part of the gas to provide high ethane recovery and refrigeration for a refrigerated lean oil system for absorption of NGLs from the other part of the natural gas.
3. The flow to the turbo expander can be adjusted to control the amount of refrigeration available to the process and the level of ethane recovery. This flexibility is important not only in adjusting to variable ethane compositions in the natural gas feed and demand requirements, but also in minimizing operating costs with seasonal ambient temperature variations.
4. The liquids from the cold separator downstream of the turbo expander, which contain about 50% methane, can be pumped, resulting in a significant operating cost saving versus compression, and utilized for condensing ethane from the de-ethanizer overhead, and as chilled lean oil for feed to the absorber. This eliminates the de-methanizer that must be supplied downstream of the turbo expanders in current turbo expander applications, resulting in significant capital cost savings.
5. Minimizes gas re-compression requirements with only the gas from the cold separator downstream of the turbo expander, less internal fuel gas requirements, requiring significant re-compression. The gas processed through the lean oil absorber only requires about 50 psi of re-compression,, resulting in both significant capital and operating cost savings.
6. Allows for intermediate ethane recovery levels while eliminating mechanical refrigeration and the accompanying relatively high maintenance costs associated with its operation.
7. By integrating the lean oil stripper with the de-ethanizer and taking a propane/butane (C3/C4) side-stream from this tower, the process 40220183.1 eliminates the need and cost for a separate tower to recover the natural gas condensate (C5+) which is utilized as lean oil and recycled to the lean oil absorber.
8. The process utilizes C5+ as lean oil and does not have to purchase and inventory an external supply of lean oil.
Description of The New Processing System 1. Inlet Natural Gas Treating The inlet natural gas is treated for C02 removal and subsequent dehydration. This step eliminates the potential for the formation of hydrates or solid C02 during the subsequent processing steps.
2. Turbo Expander for Refrigeration Reguirements After treating, part of the natural gas is routed to the Turbo Expander where the pressure drop across the expander results in the liquefaction of most of the NGLs. The re-compression side of the Turbo Expander is utilized to recapture some of this pressure drop by re-compressing the lean gas from Cold Separator 1, downstream of the Turbo Expander, after this cold gas has been utilized in the Cold Box to cool the inlet gas and the C5+ lean oil which are routed to the Lean Oil Absorber. The flow to the Turbo Expander is controlled to provide adequate refrigeration to provide the desired ethane recovery percentage from the overall system. The NGLs from Cold Separator 1 are pumped to the De-ethanizer Overhead Condenser to provide cooling to condense the ethane coming overhead from the De-ethanizer. The NGLs then flow to the Lean Oil Absorber as intermediate lean oil. The lean gas from the outlet of the re-compressor flows to a compressor which boosts the pressure back to that of the inlet natural gas.
3. Refrigerated Lean Oil Absorber The remaining natural gas, not routed to the Turbo Expander, flows to the Cold Box where it is cooled utilizing the cold gas from the Lean Oil 40220183.1 Absorber and Cold Separator 1. It then flows to Cold Separator 2 where the condensed NGLs are separated from the gas and pumped to the Lean Oil Absorber as another intermediate lean oil stream. The gas flows to the bottom of the Lean Oil Absorber where it contacts various lean oil streams (C5+ introduced at the top of the absorber, NGLs from Cold Separator 2, introduced to the absorber at a lower section in the tower and NGLs from Cold Separator 2 introduced below that) all on a counter current basis. The C5+ lean oil has been recovered at the bottom of the De-ethanizer and chilled in the Cold Box prior to recycle to the absorber. The lean gas flowing overhead from the Lean Oil Absorber is routed to the Cold Box to cool the inlet gas and C5+ and is then re-compressed to the original inlet natural gas pressure. This re-compression requirement is minimal (about 50 psi) since the pressure has only been reduced by the pressure drop across the Inlet Natural Gas Treating, Cold Box and Lean Oil Absorption components of the process. The rich lean oil, containing the extracted NGLs, from the bottoms of this tower flows to the De-methanizer.
4. De-methanizer The De-methanizer, utilizing a bottoms reboiler, drives the methane contained in the lean oil overhead, where it joins the gas from the outlet of the Turbo Expander Re-compressor and is then compressed to the original inlet natural gas pressure. Any gases that are not condensed in the De-ethanizer Overhead Condenser are routed from the De-ethanizer Reflux Accumulator to the De-methanizer for recovery of methane. A slip stream of chilled C5+ is routed to the top of the De-methanizer as lean oil to minimize the amount of NGLs that go overhead with the methane.
5. De-ethanizer The De-ethanizer, which includes a bottoms reboiler, serves several functions including the production of specification ethane, a C3/C4 mix as a side-stream and production of C5+ as a bottoms product and lean oil for recycle to the Lean Oil Absorber and De-methanizer. The side-40220183.1 ,, stream for production of a C3/C4 mix includes a reboiled Side-Stream Stripper to drive ethane into the overhead product.
Drawin The invention is described further in the attached Figure.
40220183.1

Claims

-6-~

Claim
1.~The new, useful and inventive features, singly and in combination, as set out in the foregoing description and the Figure.
CA002511403A 2005-07-05 2005-07-05 Hybrid turbo expander and refrigerated lean oil absorber system Abandoned CA2511403A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CA002511403A CA2511403A1 (en) 2005-07-05 2005-07-05 Hybrid turbo expander and refrigerated lean oil absorber system

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CA002511403A CA2511403A1 (en) 2005-07-05 2005-07-05 Hybrid turbo expander and refrigerated lean oil absorber system

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CA2511403A1 true CA2511403A1 (en) 2007-01-05

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2016053668A1 (en) 2014-09-30 2016-04-07 Dow Global Technologies Llc Process for increasing ethylene and propylene yield from a propylene plant

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2016053668A1 (en) 2014-09-30 2016-04-07 Dow Global Technologies Llc Process for increasing ethylene and propylene yield from a propylene plant
US10808999B2 (en) 2014-09-30 2020-10-20 Dow Global Technologies Llc Process for increasing ethylene and propylene yield from a propylene plant

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