AU2005202364A1 - Method for starting up a liquefaction process - Google Patents
Method for starting up a liquefaction process Download PDFInfo
- Publication number
- AU2005202364A1 AU2005202364A1 AU2005202364A AU2005202364A AU2005202364A1 AU 2005202364 A1 AU2005202364 A1 AU 2005202364A1 AU 2005202364 A AU2005202364 A AU 2005202364A AU 2005202364 A AU2005202364 A AU 2005202364A AU 2005202364 A1 AU2005202364 A1 AU 2005202364A1
- Authority
- AU
- Australia
- Prior art keywords
- hydrocarbon
- process step
- rich
- liquefaction
- fraction
- 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.)
- Abandoned
Links
- 238000000034 method Methods 0.000 title claims description 100
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 46
- 229930195733 hydrocarbon Natural products 0.000 claims description 38
- 150000002430 hydrocarbons Chemical class 0.000 claims description 38
- 239000004215 Carbon black (E152) Substances 0.000 claims description 36
- 239000003345 natural gas Substances 0.000 claims description 23
- 239000002826 coolant Substances 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 8
- 150000001875 compounds Chemical class 0.000 claims 1
- 239000003949 liquefied natural gas Substances 0.000 description 23
- 238000001816 cooling Methods 0.000 description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 238000004781 supercooling Methods 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 238000001035 drying Methods 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- GNFTZDOKVXKIBK-UHFFFAOYSA-N 3-(2-methoxyethoxy)benzohydrazide Chemical compound COCCOC1=CC=CC(C(=O)NN)=C1 GNFTZDOKVXKIBK-UHFFFAOYSA-N 0.000 description 1
- FGUUSXIOTUKUDN-IBGZPJMESA-N C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 Chemical compound C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 FGUUSXIOTUKUDN-IBGZPJMESA-N 0.000 description 1
- 101001098066 Naja melanoleuca Basic phospholipase A2 1 Proteins 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
Classifications
-
- 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
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. 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
- 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
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
- F25J1/0247—Different modes, i.e. 'runs', of operation; Process control start-up of the process
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/50—Processes or apparatus using other separation and/or other processing means using absorption, i.e. with selective solvents or lean oil, heavier CnHm and including generally a regeneration step for the solvent or lean oil
-
- 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
- F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
-
- 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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/62—Separating low boiling components, e.g. He, H2, N2, 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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
AUSTRALIA
PATENTS ACT 1990 COMPLETE SPECIFICATION NAME OF APPLICANT(S):: Linde Aktiengesellschaft ADDRESS FOR SERVICE: DAVIES COLLISON CAVE Patent Attorneys 1 Nicholson Street, Melbourne, 3000, Australia INVENTION TITLE: Method for starting up a liquefaction process The following statement is a full description of this invention, including the best method of performing it known to me/us:- 5102 1 a P 04081- DE I AVA Description The invention relates to a method for liquefying a hydrocarbon-rich flow, in particular a natural gas flow, the hydrocarbon-rich flow being liquefied in heat exchange with at least one coolant circuit and/or at least one coolant mixture circuit, and the liquefaction method comprising at least one further process step in additionto the "liquefaction" process step.
The terms "coolant" and "coolant circuit" will be used from now on; in this context, the term "coolant" stands for mono-component as well as multicomponent coolant (mixtures), while the term "coolant circuit" is intended to mean all types of coolant circuits in which mono-component as well as multicomponent coolant (mixtures) circulate.
A large number of widely varied methods for liquefying a hydrocarbon-rich flow are known in the prior art, although these will not be dealt with in detail below.
Natural gas liquefaction plants are designed either as so-called LNG baseload plants i.e. plants for liquefying natural gas to supply natural gas as primary energy or as so-called peak shaving plants i.e. plants for liquefying natural gas to cope with peak demand.
LNG baseload plants are generally operated with cooling circuits, in which case the coolants circulating in the cooling circuit consist of hydrocarbon mixtures.
These mixture circuits are energetically more efficient than expander circuits, and correspondingly permit relatively low energy consumptions for the large liquefaction capacities of LNG baseload plants.
When the aforementioned liquefaction methods are put into operation in what follows, the term "starting up" will be used to mean both starting up for the first time and starting up again the hydrocarbon-rich flow to be liquefied has been used in the past so that those plant parts or process steps of the liquefaction method which need to be dried and/or cooled can be dried and/or cooled by means of the hydrocarbon-rich flow. In this case, the plant parts or process steps up to and including the "precooling" process step are dried and/or cooled first, before the hydrocarbon-rich flow used for this is flared off. As soon as the process steps which precede the "liquefaction" and "supercooling" process steps can be put into operation, the two aforementioned "liquefaction" and "supercooling" process steps are also cooled by means of the hydrocarbon-rich flow, and this flow is flared off.
A common feature of the known start-up procedures, which differ from one another merely in detail, is that they involve a not inconsiderable, and undesirable, loss of the hydrocarbon-rich flow actually to be liquefied.
Furthermore, the flare-off of the hydrocarbon-rich flow used for the drying and/or cooling leads to an environmentally harmful and therefore undesirable carbon dioxide output.
It is an object of the present invention to provide a method for liquefying a hydrocarbon-rich flow according to the generic type, in which it is possible to avoid disposal of the hydrocarbon-rich flow, in particular flare-off, and therefore the aforementioned disadvantages associated with the flare-off.
In order to achieve this object, a method for liquefying a hydrocarbon-rich flow is provided, which is characterised in that a) when starting up the liquefaction method, a hydrocarbon-rich foreign fraction is at least temporarily added before the first process step, b) the plant parts of the individual process steps to be dried and/or cooled are dried and/or cooled by means of the hydrocarbon-rich foreign fraction, and the individual process steps are subsequently put into operation, and c) the hydrocarbon-rich foreign fraction sent through the individual process steps is fed back before the first process step.
The method according to the invention for liquefying a hydrocarbon-rich flow, and further embodiments thereof, will be explained in more detail below with reference to the procedures represented in the figure.
The figure represents a method for liquefying a hydrocarbon-rich flow belonging to the prior art in a highly schematised form. Such a liquefaction method has the following plant components and process steps: A: "pretreatment" process step, for example removal of CO2, drying, absorptive removal of higher hydrocarbons, etc.
B: "precooling" process step b: cooling circuit of the precooling B C: "heavy hydrocarbon removal" process step D: heater unit E: compressor unit F: "liquefaction" process step f: cooling circuit of the liquefaction F G: "supercooling" process step g: cooling circuit of the supercooling G H: "nitrogen removal" process step The methodology for liquefying a hydrocarbon-rich flow, for example a natural gas flow, after the liquefaction method has been started up will firstly be explained below.
The natural gas flow is fed via a line 1 to the "pretreatment" process step A, where it is subjected according to its composition for example to CO2 removal, drying and/or absorptive removal of heavy metals. The natural gas flow treated in this way is then fed via a line 2 to the "precooling" process step B where it is precooled, or cooled, by means of the cooling circuit b so that the C3+ hydrocarbons can be separated from the precooled natural gas flow in the subsequent "heavy hydrocarbon removal" process step C, to which the precooled natural gas flow is fed via a line 3. Via a line 8, C 3
H
8 or a C3 -rich fraction is fed or added as a scrubbing liquid to the "heavy hydrocarbon removal" process step C.
The natural gas flow is then fed via a line 4 to the "liquefaction" process step F and via a line 5 to the "supercooling" process step G. The aforementioned two process steps F and G are respectively assigned cooling circuits f and g, against which the precooled natural gas flow is liquefied and supercooled.
The liquefied and supercooled natural gas is then fed via a line 6 to an optionally provided "nitrogen removal" process step H, where the undesired nitrogen is separated and the natural gas product is subsequently fed via a line 7 for its further use and/or temporary storage.
In normal operation, the heater unit D is used for evaporation of the liquefied and supercooled natural gas, which is fed to the heater unit D via the line 13, and for gaseous export of this natural gas fraction. The component of the evaporated natural gas which is fed back as a drier-regenerator gas via a line 11 into the liquefaction process is compressed in the compressor unit E to the desired or required pressure.
When starting up the liquefaction method according to the invention, a hydrocarbon-rich foreign fraction is fed via a line 12 before the first process step A. In what follows, the term "hydrocarbon-rich foreign fraction" (referred to below by the term "LNG") is intended to mean a hydrocarbon-rich fraction which is available and/or needs to be bought in, for example Liquefied Natural Gas.
Especially in larger natural gas liquefaction plants, the aforementioned LNG is available at least for the restarting procedures since the liquefied natural gas product is generally stored temporarily in the immediate vicinity of the liquefaction plant in large storage containers. In order to be able to carry out the method according to the invention, therefore, it is necessary to buy LNG in only when starting up a liquefaction plant or a liquefaction process for the first time.
The LNG used for starting up must firstly be warmed and evaporated, before it can be fed via the lines 12 and 1 to the "pretreatment" process step A.
Evaporators present in the scope of the liquefaction processes, for example the hot gas evaporator, may be employed for this warming and evaporation of the LNG being used. The LNG fed to the "pretreatment" process step A is preferably at a temperature of between 15 and 300C and a pressure of between and 60 bar. As soon as the plant parts of the process step A to be dried have been dried, the process step A or its individual process steps can be put into operation.
Via the lines 2, 3 and 9 the line 4 is still closed at this time the LNG is fed through the process steps B and C to the heater unit D. The heater exit temperature is kept at a temperature of between 15 and 30 0 C, as in the further operation. Following this, the LNG is fed via a line 10 to the compressor unit E, where it is compressed to the pressure required for feeding again into the process step A, and is subsequently fed back via the lines 11 and 1 to the process step A.
According to the invention, the LNG flow used for drying and/or cooling the individual process steps is now recycled so that flare-off can be avoided.
In a second step, the "precooling" process step B, or its cooling circuit b, is put into operation and at the same time, by adding a C 3 fraction via a line 8 to the "heavy hydrocarbon removal" process step C, this process is also put into operation.
The C 3 fraction to be fed via a line 8 to the process step C as well should also preferably come from a temporary store, provided in the environment of the liquefaction process or the liquefaction plant.
LNG continues to be cycled via the lines 1, 2, 3, 9, 10 and 11 until the process steps B and C have stabilised to such an extent that they can be operated according to the intended specifications. Additional LNG is optionally fed via the line 12 during the aforementioned phase, since some of the cycled LNG is removed after starting up the "heavy hydrocarbon removal" process step C, and therefore taken out of the circuit.
In a third step, the "liquefaction" and "supercooling" process steps F and G, or the cooling circuits f and g assigned to them, are put into operation. To this end, at least a partial flow of the LNG is fed to the two process steps F and G via a line 4 and, after having passed through them, is likewise fed via the line 13 to the aforementioned heater unit D and to the compressor unit E.
By means of suitable measures, it is possible to distribute the circulating LNG flow between the lines 4 and 9 so that firstly as mentioned only a partial flow of the circulating natural gas flow is fed to the process steps F and G. During the aforementioned phase, additional LNG is likewise fed via the line 12.
When starting up the "liquefaction" and "supercooling" process steps F and G, a small partial flow of the circulating LNG is fed via a line 6 to the "nitrogen removal" process step H, so that the process step H is cooled. The LNG discharged via a line 7 from the process step H, having been freed of nitrogen, can then be fed directly for further use and/or temporary storage.
Once all the aforementioned process steps A to H have been put into operation, then it is possible to commence normal operation i.e. liquefaction of natural gas delivered via a line 1. Further feeding of (evaporated) LNG via the line 12 is no longer necessary.
Whereas the start-up procedures previously carried out require a time outlay of at least 30 days, the method according to the invention makes it possible to start up a liquefaction process in a timeframe of from 10 to 15 days.
Throughout the start-up procedure, furthermore, no natural gas is flared off so that on the one hand natural gas losses are reduced and, on the other hand, the undesirable output of carbon dioxide is avoided.
The reference numerals in the following claims do not in any way limit the scope of the respective claims.
Throughout this specification and the claims which follow, unless the context requires otherwise, the word "comprise", and variations such as "comprises" and "comprising", will be understood to imply the inclusion of a stated integer or step or group of integers or steps but not the exclusion of any other integer or step or group of integers or steps.
The reference to any prior art in this specification is not, and should not be taken as, an acknowledgement or any form of suggestion that that prior art forms part of the common general knowledge in Australia.
Claims (4)
1. Method for liquefying a hydrocarbon-rich flow, in particular a natural gas flow, the hydrocarbon-rich flow being liquefied in heat exchange with at least one coolant circuit and/or at least one coolant mixture circuit, and the liquefaction method comprising at least one further process step in addition to the "liquefaction" process step, characterised in that a) when starting up the liquefaction method, a hydrocarbon-rich foreign fraction (12) is at least temporarily added before the first process step b) the plant parts of the individual process steps (A H) to be dried and/or cooled are dried and/or cooled by means of the hydrocarbon-rich foreign fraction, and the individual process steps (A H) are subsequently put into Operation, and c) the hydrocarbon-rich foreign fraction sent through the individual process steps (A H) is fed back before the first process step
2. Method according to Claim 1, characterised in that a hydrocarbon-rich fraction which is available and/or needs to be bought in is used as the hydrocarbon-rich foreign fraction (12).
3. Method according to Claim 1 or 2, the liquefaction method containing a "heavy hydrocarbon removal" process step, characterised in that a C3 fraction is at least temporarily fed to the "heavy hydrocarbon removal" process step when starting up the liquefaction method. S, i 8
4. A method of liquefying, substantially as hereinbefore described with reference to the drawings and/or Examples. The steps, features, compositions and compounds disclosed herein or referred to or indicated in the specification and/or claims of this application, individually or collectively, and any and all combinations of any two or more of said steps or features. DATED this THIRTIETH day of MAY 2005 Linde Aktiengesellschaft by DAVIES COLLISON CAVE Patent Attorneys for the applicant(s) 5108
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102004028052.5 | 2004-06-09 | ||
| DE200410028052 DE102004028052A1 (en) | 2004-06-09 | 2004-06-09 | Process to liquefy natural gas by first-stage introduction of hydrocarbon-enriched fraction |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| AU2005202364A1 true AU2005202364A1 (en) | 2006-01-05 |
Family
ID=35295257
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2005202364A Abandoned AU2005202364A1 (en) | 2004-06-09 | 2005-05-30 | Method for starting up a liquefaction process |
Country Status (4)
| Country | Link |
|---|---|
| AU (1) | AU2005202364A1 (en) |
| DE (1) | DE102004028052A1 (en) |
| NO (1) | NO20052658L (en) |
| RU (1) | RU2005117707A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NO20121093A1 (en) * | 2010-02-26 | 2012-09-26 | Statoil Petroleum As | Procedure for starting a liquefied natural gas (LNG) plant |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1895254A1 (en) * | 2006-08-29 | 2008-03-05 | Shell Internationale Researchmaatschappij B.V. | Method for starting up a plant for the liquefaction of a hydrocarbon stream |
| FR2920529B1 (en) * | 2007-09-04 | 2009-12-11 | Total Sa | METHOD FOR STARTING A HYDROCARBON MIXED REFRIGERATION CYCLE. |
| CN102405389B (en) * | 2008-02-08 | 2014-12-03 | 国际壳牌研究有限公司 | Method and apparatus for cooling down a cryogenic heat exchanger and method of liquefying a hydrocarbon stream |
-
2004
- 2004-06-09 DE DE200410028052 patent/DE102004028052A1/en not_active Withdrawn
-
2005
- 2005-05-30 AU AU2005202364A patent/AU2005202364A1/en not_active Abandoned
- 2005-06-02 NO NO20052658A patent/NO20052658L/en not_active Application Discontinuation
- 2005-06-08 RU RU2005117707/06A patent/RU2005117707A/en not_active Application Discontinuation
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NO20121093A1 (en) * | 2010-02-26 | 2012-09-26 | Statoil Petroleum As | Procedure for starting a liquefied natural gas (LNG) plant |
| NO20121095A1 (en) * | 2010-02-26 | 2012-09-26 | Statoil Petroleum As | Procedure for Shutdown of a Liquefied Natural Gas (LNG) Plant |
Also Published As
| Publication number | Publication date |
|---|---|
| NO20052658L (en) | 2005-12-12 |
| DE102004028052A1 (en) | 2005-12-29 |
| RU2005117707A (en) | 2006-12-20 |
| NO20052658D0 (en) | 2005-06-02 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MK1 | Application lapsed section 142(2)(a) - no request for examination in relevant period |