CN104011489B - For removing the method and apparatus of nitrogen from low temperature hydrocarbon composition - Google Patents
For removing the method and apparatus of nitrogen from low temperature hydrocarbon composition Download PDFInfo
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- CN104011489B CN104011489B CN201280061162.5A CN201280061162A CN104011489B CN 104011489 B CN104011489 B CN 104011489B CN 201280061162 A CN201280061162 A CN 201280061162A CN 104011489 B CN104011489 B CN 104011489B
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- stripping
- nitrogen
- liquid
- vapor
- low temperature
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 428
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 215
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 151
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 150
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 126
- 239000000203 mixture Substances 0.000 title claims abstract description 74
- 238000000034 method Methods 0.000 title claims description 125
- 239000007788 liquid Substances 0.000 claims abstract description 134
- 239000003507 refrigerant Substances 0.000 claims abstract description 93
- 238000001816 cooling Methods 0.000 claims abstract description 32
- 238000009833 condensation Methods 0.000 claims abstract description 25
- 230000005494 condensation Effects 0.000 claims abstract description 25
- 239000002912 waste gas Substances 0.000 claims abstract description 13
- 238000007599 discharging Methods 0.000 claims abstract description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 100
- 230000008569 process Effects 0.000 claims description 93
- 239000007789 gas Substances 0.000 claims description 47
- 239000012530 fluid Substances 0.000 claims description 33
- 238000003860 storage Methods 0.000 claims description 24
- 238000010992 reflux Methods 0.000 claims description 23
- 230000005484 gravity Effects 0.000 claims description 18
- 239000000446 fuel Substances 0.000 claims description 13
- 239000007791 liquid phase Substances 0.000 claims description 13
- 238000000926 separation method Methods 0.000 claims description 13
- 239000002737 fuel gas Substances 0.000 claims description 11
- 235000013372 meat Nutrition 0.000 claims description 5
- 238000000605 extraction Methods 0.000 claims description 4
- 239000012071 phase Substances 0.000 claims description 4
- 241000628997 Flos Species 0.000 claims description 2
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 238000007906 compression Methods 0.000 abstract description 9
- 239000000047 product Substances 0.000 description 53
- 238000011068 loading method Methods 0.000 description 18
- 239000003949 liquefied natural gas Substances 0.000 description 12
- 238000007710 freezing Methods 0.000 description 11
- 230000008014 freezing Effects 0.000 description 11
- 230000008901 benefit Effects 0.000 description 9
- 238000010438 heat treatment Methods 0.000 description 8
- 239000003345 natural gas Substances 0.000 description 8
- 238000011144 upstream manufacturing Methods 0.000 description 8
- 238000011084 recovery Methods 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 6
- 230000006835 compression Effects 0.000 description 6
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 5
- 230000001105 regulatory effect Effects 0.000 description 5
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 4
- 230000006837 decompression Effects 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 238000011026 diafiltration Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 239000000945 filler Substances 0.000 description 3
- 239000001294 propane Substances 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 230000005587 bubbling Effects 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 230000007704 transition Effects 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000001066 destructive effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 238000002513 implantation Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000001282 iso-butane Substances 0.000 description 1
- 235000013847 iso-butane Nutrition 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- -1 sulphur compounds Chemical class 0.000 description 1
- 238000002207 thermal evaporation Methods 0.000 description 1
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
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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
- 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
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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
- 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
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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
- 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
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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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/30—Dynamic liquid or hydraulic expansion with extraction of work, e.g. single phase or two-phase turbine
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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
- 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
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
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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
- F25J2280/00—Control of the process or apparatus
- F25J2280/02—Control in general, load changes, different modes ("runs"), measurements
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- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Separation By Low-Temperature Treatments (AREA)
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Abstract
Nitrogen is removed from low temperature hydrocarbon composition.At least Part I of low temperature hydrocarbon composition is fed to nitrogen stripping tower.Nitrogen stripping tower operates under stripping pressure.Stripping steam is passed in nitrogen stripping tower, described stripping steam comprises at least Stripping section of the compression process steam produced by the liquid through nitrogen stripping, from nitrogen stripping tower extract described after the liquid of nitrogen stripping by the described liquid pressure-reducing through nitrogen stripping.By heat being passed to auxiliary refrigerant stream from overhead vapor with certain cooling power, thus produce backflow, described backflow relates to the overhead vapor of partial condensation nitrogen stripping tower.Discharge by the waste gas of the non-condensable vapor fractional composition from overhead vapor.Regulate cooling power to regulate the calorific value of the vapor fraction of discharging.
Description
Technical field
The present invention relates to a kind of method and apparatus for separation of nitrogen from low temperature hydrocarbon composition.
Background technology
Liquefied natural gas (LNG) forms the example important economically of this low temperature hydrocarbon composition.Natural gas is available fuel source, and the source of various hydrocarbon compound.Due to many reasons, usually wish in the source place of natural gas flow or the source close to natural gas flow, liquefied natural gas in LNG plant.Such as, compared to gas form, natural gas is easier to as fluid storage and long apart from interior conveying, because it occupies less volume, and without the need under high pressure storing.
WO2011/009832 describes a kind of method of the heterogeneous hydrocarbon stream for the treatment of being produced by natural gas, wherein by more lower boiling component (as nitrogen) from as described in be separated, to produce the liquefied natural gas stream of this more lower boiling component with more low content heterogeneous hydrocarbon stream.It utilizes two the continuous print gas/liquid separation devices operated at various pressures.Heterogeneous hydro carbons is flow to material to the first gas/liquid separation device under the first pressure.Spread the bottom of described first gas/liquid separation device and be handed to the second gas/liquid separation device, described second gas/liquid separation device is provided in lower than the steam under the second pressure under described first pressure.Steam compresses in overhead stream compressor, and is back to described first gas/liquid separation device as stripping steam stream.
Fig. 2 of aforementioned open WO2011/009832 describes an embodiment, wherein the first gas/liquid separation device provides with the form of the post with Liang Ge district and reflux condenser, and described Liang Ge district has the contact intensifier such as formed by tower tray and/or filler.Reflux condenser is cooled by the slip-stream of the stream phase homogeneous turbulence with the heterogeneous hydrocarbon stream of preparation.Low-pressure fuel air-flow is obtained by the overhead vapor stream of discharging from post, and described overhead vapor stream is passed to burner.
A shortcoming of the method and apparatus as described in WO2011/009832 is, in fuel gas, available calorific value does not mate the needs to calorific value.
Summary of the invention
The invention provides a kind of method removing nitrogen from low temperature hydrocarbon composition, described low temperature hydrocarbon composition comprises the liquid phase containing nitrogen and methane, and described method comprises:
-providing package is containing the low temperature hydrocarbon composition of the liquid phase containing nitrogen and methane;
-the first nitrogen stripping device incoming flow under stripping pressure is fed to nitrogen stripping tower, described nitrogen stripping tower comprises at least one inner rectifying portion section and is arranged at least one the inner stripping portion section in the nitrogen stripping tower below described rectifying portion section gravity, and described first nitrogen stripping device incoming flow comprises the Part I of described low temperature hydrocarbon composition;
-from liquid through nitrogen stripping of the liquid storage spatial extraction of the nitrogen stripping tower below described stripping portion section;
-prepare at least liquid hydrocarbon product stream and process steam by the described liquid through nitrogen stripping, at least comprise the low temperature hydrocarbon composition of providing package containing the liquid phase containing nitrogen and methane;
-the first nitrogen stripping device incoming flow under stripping pressure is fed to nitrogen stripping tower, described nitrogen stripping tower comprises at least one inner rectifying portion section and is arranged at least one the inner stripping portion section in the nitrogen stripping tower below described rectifying portion section gravity, and described first nitrogen stripping device incoming flow comprises the Part I of described low temperature hydrocarbon composition;
-from liquid through nitrogen stripping of the liquid storage spatial extraction of the nitrogen stripping tower below described stripping portion section;
-prepare at least liquid hydrocarbon product stream and process steam by the described liquid through nitrogen stripping, at least comprise the described liquid pressure-reducing through nitrogen stripping to the step of flashing pressure;
-described process steam is compressed at least stripping pressure, obtain compressed vapour thus;
-stripping steam is spread in the nitrogen stripping tower of the At The Height be handed to below described stripping portion section gravity, described stripping steam flow to the Stripping section comprising described compressed vapour less;
-by the intermediate flow of the overhead vapor forming section condensation of the top section available from the nitrogen stripping tower above described rectifying portion section, the intermediate flow of described partial condensation comprises condensate fraction and vapor fraction, described formation comprises by making described overhead vapor and the heat exchange of auxiliary refrigerant stream, thus heat is passed to auxiliary refrigerant stream with certain cooling power from described overhead vapor, thus overhead vapor described in partial condensation;
-under separating pressure, described condensate fraction is separated with described vapor fraction;
-discharge vapor fraction as waste gas, described vapor fraction has calorific value;
-at least refluxing portion of described condensate fraction is entered originate in the nitrogen stripping tower of the height above described rectifying portion section;
-regulate described cooling power to regulate the calorific value of the vapor fraction of discharging.
On the other hand, the invention provides a kind of device for removing nitrogen from low temperature hydrocarbon composition, described low temperature hydrocarbon composition comprises the liquid phase containing nitrogen and methane, and described device comprises:
-for being provided in the low temperature feeding line of the low temperature hydrocarbon composition under initial pressure, described low temperature hydrocarbon composition comprises the liquid phase containing nitrogen and methane;
-nitrogen stripping the tower that is communicated with described low temperature feeding line fluid, described nitrogen stripping tower comprises at least one inner rectifying portion section and is arranged at least one the inner stripping portion section in the nitrogen stripping tower below described rectifying portion section gravity;
-intermediate relief device, described intermediate relief device fluid is connected to described nitrogen stripping tower, and the liquid through nitrogen stripping in the liquid storage space in order to receive the nitrogen stripping tower below comfortable described stripping portion section gravity is set, and by the described liquid pressure-reducing through nitrogen stripping, on the interface of described intermediate relief device between the stripping pressure side comprising described nitrogen stripping tower and flashing pressure side;
-be arranged at liquid hydrocarbon product pipeline on described flashing pressure side, to discharge the liquid hydrocarbon product stream produced by the described liquid through nitrogen stripping;
-be arranged at process steam pipeline on described flashing pressure side, to receive the process steam produced by the described liquid through nitrogen stripping;
-be arranged at process compresses machine in described process steam pipeline, it is arranged in order to receive described process steam and to compress described process steam, compressed vapour is provided, on the described interface of described process compresses machine between stripping pressure side and flashing pressure side with the process compresses machine floss hole place at described process compresses machine;
-stripping steam pipeline, the At The Height of described stripping steam pipeline below the gravity of described stripping portion section is communicated with described nitrogen stripping tower fluid, and arranges at least Stripping section in order to receive from the described compressed vapour of described process compresses machine;
-evaporator overhead condenser, described evaporator overhead condenser arranges overhead vapor and the auxiliary refrigerant stream indirect heat exchange contact of the top section in order to make the nitrogen stripping tower above available from described rectifying portion section, obtain the intermediate flow comprising the partial condensation of condensate fraction and vapor fraction thus, wherein in operation, heat is passed to described auxiliary refrigerant stream with certain cooling power from described overhead vapor;
-discharge pipe line, described discharge pipe line arranges the vapor fraction in order to discharge with calorific value;
-return-flow system, described return-flow system is arranged in order to allow the At The Height of at least refluxing portion of described condensate fraction above described rectifying portion section to enter described nitrogen stripping tower;
-cooling power controller, described cooling power controller is arranged in order to regulate cooling power, to regulate and control the calorific value of the vapor fraction of discharge.
Accompanying drawing explanation
Use embodiment and with reference to accompanying drawing, hereafter further illustrating the present invention, in the accompanying drawings:
Fig. 1 schematically shows process chart, and it represents the method and apparatus introducing one embodiment of the invention; With
Fig. 2 schematically shows process chart, and it represents the method and apparatus introducing another embodiment of the present invention.
In these figures, identical Reference numeral will be used in reference to same or similar parts.In addition, single Reference numeral is by the stream being used for determining pipeline or pipeline and transmitted by this pipeline.
Detailed description of the invention
This description relates to removes nitrogen from the low temperature hydrocarbon composition comprised containing the liquid phase of nitrogen and methane.At least Part I of low temperature hydrocarbon composition is fed to nitrogen stripping tower as the first nitrogen stripping device incoming flow.Nitrogen stripping tower operates under stripping pressure.Stripping steam is passed in nitrogen stripping tower, described stripping steam comprises at least Stripping section of the compression process steam produced by the liquid through nitrogen stripping, from nitrogen stripping tower extract described after the liquid of nitrogen stripping by the described liquid pressure-reducing through nitrogen stripping.By heat being passed to auxiliary refrigerant stream from overhead vapor with certain cooling power, thus produce backflow, described backflow relates to the overhead vapor of partial condensation nitrogen stripping tower.Discharge by the waste gas of the non-condensable vapor fractional composition from overhead vapor.Regulate cooling power to control the calorific value of the vapor fraction of discharging.
The cooling power of auxiliary refrigerant stream is passed to from overhead vapor, the relative quantity of methane in adjustable waste gas by adjustment heat.As a result, adjustable discharge vapor fraction calorific value with heating power specifically need mate.This makes waste gas be suitable as fuel gas stream, even if when the needs of calorific value are variable.
When vapor fraction as delivery of fuel to burner, and when being consumed by burner, adjustable calorific value, mates with the actual needs of the heating power with burner.
Preferably, waste gas consumes under not higher than the fuel gas pressure of stripping pressure.But, the needs of special fuel air compressor can be avoided.In addition, by selecting the stripping pressure under the pressure exceeding fuel gas pressure, the compression of any applying has extra associated benefits, such as, increase the enthalpy of process steam, and this allows process steam to be used as stripped vapor.
In the context of the present specification, cooling power reflects the speed that heat exchanges within the condenser, and it can represent with power unit (such as watt or megawatt).Cooling power is relevant to the flow stood with the auxiliary refrigerant of the heat exchange of overhead vapor.
Regulated calorific value can be selected as the suitable situation of the desired use of fuel gas according to waste gas.Can according to DIN51857 standard determination calorific value.For many application, the calorific value regulated can with low heat value (LHV; Be sometimes referred to as net heating value) proportional, described low heat value may be defined as by burning specified amount (at first at 25 DEG C) and makes the temperature of combustion product be back to the heat of 150 DEG C and release.This supposes the evaporation of water latent heat do not reclaimed in product.
But, in order to regulate the object of calorific value in context of the present disclosure, without the need to the actual calorific value of vapor fraction determining to be discharged on absolute value basis.Usually, in order to make any shortage of sent heating power or excessively reach minimum, relative to heating power actual needs and regulate calorific value namely enough.
Preferably, respond therefore relevant to regulated calorific value signal and automatically regulate cooling power.
It is suggested, when thick liquiefied product or low temperature hydrocarbon composition contain 1.5mol% (preferred 1.8mol%) until the nitrogen of 5mol% time, method and apparatus in this paper is the most favourable.When nitrogen content is lower than about 1.8mol% and/or lower than about 1.5mol%, existing selectable method is also enough to work.
The method and apparatus proposed allows the stream by any this steam being contained methane to be added into (compression) process vapor stream, thus form the steam methane of the part of thick liquiefied product again before condensation, until exceed the degree of the aim parameter of the methane in discharge vapor fraction.Once form the part of (compression) process steam, steam methane can be managed and auxiliary refrigerant heat exchange, thus, steam methane optionally condenses from the overhead vapor from nitrogen stripping tower, and allows the major part of nitrogen to discharge together with waste gas simultaneously.Therefore, likely from low temperature hydrocarbon composition, remove enough nitrogen, to produce the liquid hydrocarbon product stream in Maximum Index needed for nitrogen content, and do not produce in the offgas than required more thermal capacity simultaneously.
Due to many reasons, can be formed in LNG liquefies factory at the steam methane of the part forming thick liquiefied product before.In the course of normal operation of natural gas liquefaction facility, the steam containing methane is formed by (slightly) liquiefied product with following form:
-flashed vapour, it obtains the flash distillation of thick liquiefied product in comfortable decompression process; And
-Volatile Gas, it must be freed from the heat being added into liquiefied product and the thermal evaporation caused, described heat such as entering storage tank, the ducted heat leak of LNG, and from the form that the heat of factory's LNG pump inputs.In described operator scheme (being called that Holdover mode operates) process, storage tank is filled by Liquefied Hydrocarbon series products when Liquefied Hydrocarbon series products leaves equipment, and does not carry out any conveyor load operation simultaneously.When in Holdover mode, the steam containing methane produces at the equipment side of storage tank.
The operator scheme of the LNG plant when there is conveyor load operation (usual ship loading operation) continued is called that loading pattern operates.In loading pattern operating process, such as, due to the initial cooling of boats and ships tank, by connecting storage tank and the pipeline of boats and ships and the heat leak of container, and to input from the heat of LNG loading pump, Volatile Gas produces in addition in the boats and ships side of storage tank.
The solution proposed can process these steams in Holdover mode and loading pattern operating process.It is combined with the condensation again of removing nitrogen and excessive steam methane from low temperature hydrocarbon composition.When needing a small amount of factory's fuel (as used the situation from the electric drive factory of the electric power of external electrical network), this results in excellent solution.The method and apparatus proposed is suitable in conjunction with hydro carbons liquefaction system (as natural gas liquefaction system) application especially, to remove nitrogen from thick liquiefied product.Find, even if when thick liquiefied product or low temperature hydrocarbon composition contain 1mol% (or about 1mol%) until the nitrogen of quite high amount of 5mol% (or until about 5mol%) time, gained liquid hydrocarbon product can meet the nitrogen content in the index of the nitrogen between 0.5 to 1mol%.The remainder of nitrogen discharges together with the methane of controlled quatity as the part of the vapor fraction in waste gas.
Fig. 1 shows a kind of device comprising one embodiment of the invention.Low temperature feeding line 8 is communicated with nitrogen stripping tower 20 fluid via the first entrance system 21.First feeding line 10 optionally connects the first entrance system 21 of low temperature feeding line 8 and nitrogen stripping tower 20 via initial flow current divider 9, described initial flow current divider 9 is arranged between low temperature feeding line 8 and the first feeding line 10.
Liquefaction system 100 can be arranged at the upstream of low temperature feeding line 8.Liquefaction system 100 is used as the source of low temperature hydrocarbon composition.Liquefaction system 100 is communicated with low temperature feeding line 8 fluid via main depressurized system 5, and described main depressurized system 5 is communicated with liquefaction system 100 via thick liquiefied product pipeline 1.In the illustrated embodiment, main depressurized system 5 is made up of dynamic cell (as decompressor turbine 6) and static cell (as Joule Thompson valve 6), but other variants are possible.Preferably, but not necessarily, form any compressor of the part of the hydro carbons liquefaction process in liquefaction system, particularly any coolant compressor is driven by one or more motor, and can't help any steam turbine and/or gas turbine mechanical and drive.This compressor can only be driven by one or more motor.
Nitrogen stripping tower 20 comprises inner rectifying portion section 22 and inner stripping portion section 24.Inner rectifying portion section 24 is arranged in the nitrogen stripping tower 20 below rectifying portion section 22 gravity.First entrance system 21 gravity is arranged between inner rectifying portion section 22 and inner stripping portion section 24.
Overhead vapor discharge pipe line 30 is communicated with nitrogen stripping tower 20 via top section 26, and described top section 26 is formed by the space in the nitrogen stripping tower 20 above the gravity of rectifying portion section 22.Discharge pipe line 40 through the liquid of nitrogen stripping is communicated with nitrogen stripping tower 20 via the liquid storage space 28 in nitrogen stripping tower 20, and described liquid storage space 28 is below the gravity of stripping portion section 24.
Inner rectifying portion section 22 contacts intensifier to improve Component seperation and denitrogenation with each the comprised vapor/liquid in inner stripping portion section 24.This contact intensifier with the form of tower tray and/or filler, can provide with the form of structuring or destructuring filler.Depend on the nitrogen amount in the Tolerance of the nitrogen in nitrogen stripping liquid and low temperature feeding line 8, usually altogether can need the theoretical stage between 2 to 8.In one particular embodiment, 4 theoretical stages are needed.
Intermediate relief device 45 is arranged in the discharge pipe line 40 of the liquid of nitrogen stripping, and fluid is connected to nitrogen stripping tower 20 thus.Intermediate relief device 45 is functionally attached to liquid-level controller LC, and described liquid-level controller LC cooperates with the liquid storage space 28 of nitrogen stripping tower 20.
Intermediate relief device 45 is arranged on the interface that comprises between the stripping pressure side of nitrogen stripping tower 20 and flashing pressure side.Flashing pressure side comprises liquid hydrocarbon product pipeline 90 and process steam pipeline 60, described liquid hydrocarbon product pipeline 90 arranges in order to discharge the liquid hydrocarbon product stream produced by the liquid 40 through nitrogen stripping, and described process steam pipeline 60 is arranged in order to receive the process steam produced by the liquid 40 through nitrogen stripping.In the embodiment illustrated, flashing pressure side also comprises the low-temperature storage tank 210 being connected to liquid hydrocarbon product pipeline 90 for storing liquid hydrocarbon product stream, optional Volatile Gas supply line 230 and optional end flash gas separator 50.
If provide this end flash gas separator 50 (situation as in the implementation of figure 1), it can be configured to be communicated with nitrogen stripping tower 20 fluid with the discharge pipe line 40 of the liquid through nitrogen stripping via intermediate relief device 45.End flash gas separator 50 can be connected to low-temperature storage tank 210 via liquid hydrocarbon product pipeline 90 subsequently.Cryogenic pump 95 can be present in liquid hydrocarbon product pipeline 90, to assist liquid hydrocarbon product to be delivered to low-temperature storage tank 210.
As shown in the embodiment of figure 1, process steam pipeline 60 can be connected to optional end flash gas separator 50 via flashed vapour pipeline 64 and flash vapor stream brake control valve 65, and is connected to low-temperature storage tank 210 via optional Volatile Gas supply line 230.Rear one advantage connected is, it to allow by evaporator overhead condenser 35 at least part of from the Volatile Gas of low-temperature storage tank 210 of condensation again, and this discusses hereinafter further.
In typical LNG factory, the generation of Volatile Gas can exceed the flow several times of flashed vapour, particularly operating in the process of engineering with so-called loading pattern, therefore, if the scene to heating power of Shortcomings needs to use the whole methane be contained in Volatile Gas, then important advantageously not only condensation flashed vapour, also condensation Volatile Gas more again.
Also process compresses machine 260 is configured on the interface between stripping pressure side and flashing pressure side.Preferably, process compresses machine 260 is driven by motor.Process compresses machine 260 is arranged in process steam pipeline 60, with receiving course steam and compression process steam.Compressed vapour discharge pipe line 70 is connected with process compresses machine exhaust outlet 261 fluid of process compresses machine 260.Suitably, process compresses machine 260 is provided with Anti-surge Control and recycle cooler, (does not show in the drawings) and use described recycle cooler when process compressor is in recirculation and in start-up course.
Stripping steam pipeline 71 is communicated with nitrogen stripping tower 20 fluid via the second entrance system 23, and described second entrance system 23 is configured in the level place below the gravity of stripping portion section 24, and preferably above liquid storage space 28.Stripping steam pipeline 71 is connected to compressed vapour discharge pipe line 70 via optional bypass diverter 79.Stripping steam valve 75 is arranged in stripping steam pipeline 71.
Optionally, outside stripping steam supply line 74 is set to be communicated with the second entrance system 23 fluid of nitrogen stripping tower 20.In one embodiment, as shown in Figure 1, optional outside stripping steam supply line 74 is connected to compressed vapour discharge pipe line 70.Outside stripping steam flow control valve 73 is arranged in optional outside stripping steam supply line 74.In one embodiment, optional outside stripping steam supply line 74 is suitably connected in liquefaction system 100 or the hydrocarbon steam pipeline of liquefaction system 100 upstream.
Evaporator overhead condenser 35 is arranged in overhead vapor discharge pipe line 30.Inner at evaporator overhead condenser 35, overhead vapor can with auxiliary refrigerant stream 132 indirect heat exchange contact and process, heat is passed to auxiliary refrigerant stream with certain cooling power from overhead vapor thus.Auxiliary refrigerant stream flow control valve 135 is arranged in auxiliary refrigerant pipeline 132.
Cooling power controller 34 responds indicator relative to the Volatile Gas calorific value of the needs to heating power and controlled cooling model power, and described cooling power is that heat is passed to the speed of auxiliary refrigerant stream from overhead vapor.In the embodiment illustrated, cooling power controller 34 presents with the form of pressure controller PC and auxiliary refrigerant stream flow control valve 135, and described pressure controller PC and auxiliary refrigerant stream flow control valve 135 are functionally coupled to each other.
Still with reference to Fig. 1, top separator 33 is arranged on the downstream of overhead vapor discharge pipe line 30.Overhead vapor discharge pipe line 30 is disposed in top separator 33.Top separator 33 is arranged in order to be separated any NC vapor fraction from any condensate fraction of overhead vapor.Vapor fraction discharge pipe line 80 arranges to discharge vapor fraction.
Return-flow system is set and enters nitrogen stripping tower 20 to allow the level place of at least refluxing portion 36 of condensate fraction above rectifying portion section 22.In the implementation of figure 1, return-flow system comprises condensate fraction discharge pipe line 37, optional reflux pump 38 and optional condensate fraction current divider 39, described condensate fraction discharge pipe line 37 fluid is connected to the bottom of top separator 33, and described optional reflux pump 38 is arranged in condensate fraction discharge pipe line 37.Via refluxing portion pipeline 36 and reflux inlet system 25, fluid is connected condensate fraction discharge pipe line 37 and nitrogen stripping tower 20 to optional condensate fraction current divider 39, and fluid connects condensate fraction discharge pipe line 37 and optional liquid recycle pipeline 13.Liquid recycle pipeline 13 is communicated with liquid hydrocarbon product pipeline 90 fluid.Fluid connection means liquid recycle pipeline 13 and is connected to any suitable position, liquid recycle part can flow to liquid hydrocarbon product pipeline 90 from described position at least partially, and to keep in the liquid phase simultaneously.Therefore, liquid recycle pipeline 13 such as can be connected directly to following one or more: nitrogen stripping tower 20, low temperature feeding line 8, first feeding line 10, the second optional feeding line 11 (will be described below), the discharge pipe line 40 through the liquid of nitrogen stripping, optional end flash gas separator 50 and liquid hydrocarbon product pipeline 90.Recycle valve 14 is configured in optional liquid recycle pipeline 13.The optional Modelling of Flow with Recirculation valve 32 controlled by Modelling of Flow with Recirculation controller (not shown) function can preferably be arranged in refluxing portion pipeline 36.
Liquid recycle pipeline 13 is preferably via recirculation path and liquid hydrocarbon product pipeline 90 fluid connection, and described recirculation path is without rectifying portion section 22.In this way, liquid recycle pipeline 13 assists to avoid too much liquid to be fed to rectifying portion section 22, and avoids recycled liquid through rectifying portion section 22.This is conducive to being avoided the balance in disturbance nitrogen stripping tower 20.
Optional bypass diverter 79 is communicated with overhead vapor discharge pipe line 30 fluid, and described overhead vapor discharge pipe line 30 is at the upstream side of evaporator overhead condenser 35.Optional vapor bypass pipeline 76 can be arranged between optional bypass diverter 79 and overhead vapor discharge pipe line 30.Vapor bypass control valve 77 is preferably disposed in vapor bypass pipeline 76.A benefit of this vapor bypass pipeline 76 is, when sometimes there is excessive process steam, it can process together with waste gas in vapor fraction discharge pipe line 80, and can not upset the Material Balance in nitrogen stripping tower 20.Vapor bypass pipeline 76 suitably extends along bypass diverter 79 and the bypass path between the overhead vapor discharge pipe line 30 of the upstream side of evaporator overhead condenser 35.Bypass path extends between bypass diverter 79 and overhead vapor discharge pipe line 30 and/or vapor fraction discharge pipe line 80.Bypass path is without stripping portion, the inside section 24 in nitrogen stripping tower 20.By this mode, non-Stripping section can be avoided through inner stripping portion section 24, and this helps avoid the balance in disturbance nitrogen stripping tower 20.
If provide initial flow current divider 9, then low temperature feeding line 8 be also connected to following at least one: through the discharge pipe line 40 of the liquid of nitrogen stripping, liquid hydrocarbon product pipeline 90 and process steam pipeline 60.For this purpose, the second feeding line 11 is connected to optional initial current divider 9 in side at its upstream.Described second feeding line 11 walks around nitrogen stripping tower 20.Bypass stream flow control valve 15 is arranged in the second feeding line 11.Bypass stream flow control valve function is connected to the flow governor FC be arranged in the first feeding line 10.Suitably, the second feeding line 11 is fed to optional end flash gas separator 50.
The second optional feeding line 11 and a benefit of optional initial current divider 9 are, less in the comparable following situation of size of nitrogen stripping tower 20: low temperature feeding line 8 is directly connected and diverterless with the first feeding line 10, make all low temperature hydrocarbon compositions enter nitrogen stripping tower 20 via the first entrance system 21.
Burner 220 is arranged in the downstream of vapor fraction discharge pipe line 80, to receive at least fuel meat of the vapor fraction in vapor fraction discharge pipe line 80.Burner can comprise multiple fuel element, and/or it can comprise one or more as follows: such as stove, boiler, incinerator, dual-fuel diesel engine or their combination.Boiler and dual-fuel diesel engine can be attached to generator.
Cold recovery heat exchanger 85 can be arranged in vapor fraction discharge pipe line 80, with cold by what keep vapor fraction 80 to have with the heat exchange of cold recovery stream 86 before vapor fraction 80 is fed to any burner.
In one embodiment, cold recovery stream 86 can comprise the effluent of the hydrocarbon feed stream be derived from the hydrocarbon feed pipeline 110 of liquefaction system 100, or can be made up of described effluent.Gained through cooling effluent can such as with the low temperature hydrocarbon combination of compositions in low temperature feeding line 8.Therefore, the cold recovery heat exchange in cold recovery heat exchanger 85 supplements the productivity ratio of low temperature hydrocarbon composition.In another embodiment, cold recovery stream 86 can to comprise in overhead vapor discharge pipe line 30 (preferably in the part of overhead vapor discharge pipe line 30, overhead vapor is passed to evaporator overhead condenser 35 from nitrogen stripping tower 20 by described part) overhead vapor, or can be made up of described overhead vapor.Thus reduce the required power from the auxiliary refrigerant stream 132 in evaporator overhead condenser 35.
Optional vapor fraction current divider 89 can be arranged in vapor fraction pipeline 80, thus provides the controlled fluid between vapor fraction pipeline 80 with vapor recirculation pipeline 87 to be communicated with.Nitrogen stripping tower 20 walked around by vapor recirculation pipeline 87, and at least one is as follows got back in charging: liquid hydrocarbon product pipeline 90 and process steam pipeline 60.Vapor recirculation flow control valve 88 is preferably disposed in vapor recirculation pipeline 87.A benefit of the vapor recirculation pipeline 87 proposed is, it allows optionally to increase the nitrogen content in liquid hydrocarbon product stream 90.
Any one or both in second feeding line 11 and vapor recirculation pipeline 87 can suitably be fed in optional end flash gas separator 50.
Liquefaction system 100 in this description is up to the present to the utmost schematically to be described.It can represent any suitable hydro carbons liquefaction system and/or process, particularly prepares any gas deliquescence process of liquefied natural gas, and the present invention is not limited to the concrete selection of liquefaction system.The example of suitable liquefaction system uses single refrigerant circulating process (to be generally the cold-producing medium-SMR process of single mixing, as being described in the PRICO in Gastech (Dubai) article " LNGProductiononfloatingplatforms " of KRJohnsen and PChristiansen that proposes in 1998, but be also likely one-component cold-producing medium, such as, be also described in the BHP-cLNG process in the aforementioned document of Johnsen and Christiansen); Two refrigerant circulating process (such as conventional propane-mixing-refrigerant process being usually abbreviated as C3MR, as being such as described in United States Patent (USP) 4,404, in 008, or such as (an one example is described in United States Patent (USP) 6 to double-mixed refrigerant-DMR – process, 658, in 891), or such as wherein each refrigerant circulation contain the Two-way Cycle process of one-component cold-producing medium); With the process based on three or more the compressor bank for three or more kind of refrigeration cycle (an one example is described in United States Patent (USP) 7,114, in 351).
Other examples of suitable liquefaction system are described in: United States Patent (USP) 5,832,745 (ShellSMR), United States Patent (USP) 6,295,833, United States Patent (USP) 5,657,643 (both are the variant of BlackandVeatchSMR), United States Patent (USP) 6,370,910 (ShellDMR).The people such as another suitable example of DMR is so-called AxensLIQUEFIN process, the P-YMartin that the 22nd WorldGasConference (2003) as being such as described in Tokyo proposes are entitled as in the article of " LIQUEFIN:ANINNOVATIVEPROCESSTOREDUCELNGCOSTS ".Other three suitable cyclic processes comprise such as United States Patent (USP) 6, 962, 060, WO2008/020044, United States Patent (USP) 7, 127, 914, DE3521060A1, United States Patent (USP) 5, 669, 234 (commercial being called, optimizes cascade process), United States Patent (USP) 6, 253, 574 (commercial be called fluid-mixing cascade process), United States Patent (USP) 6, 308, 531, U.S. Application Publication 2008/0141711, the people such as MarkJ.Roberts " LargecapacitysingletrainAP-X (TM) HybridLNGProcess ", Doha, QAT, Gastech, 2002 (13-16 days in October, 2002).There is provided these suggestions so that applicability widely of the present invention to be described, and be not intended to the exclusive list for exclusive and/or possibility.All examples not as listed above use motor as coolant compressor driver.Be apparent that and any driver except motor can be used to replace motor with greatest benefit in the present invention.
An example (wherein liquefaction system 100 is based on such as C3MR or ShellDMR) is briefly shown in Figure 2.It uses low temperature heat exchanger 180, it is the form of Wound-rotor type heat exchanger in this case, and described Wound-rotor type heat exchanger comprises bottom and top hydrocarbon products tube bank (being respectively 181 and 182), bottom and top LMR restrain (being respectively 183 and 184) and HMR tube bank 185.
Bottom is connected thick liquiefied product pipeline 1 and hydrocarbon feed pipeline 110 with top hydrocarbon products tube bank 181 with 182 fluids.The pre-cooled heat exchanger 115 of at least one freezing hydro carbons can be arranged in the hydrocarbon feed pipeline 110 of the upstream of low temperature heat exchanger 180.
The main refrigerant of mix refrigerant form provides in main refrigerant circuit 101.Main refrigerant circuit 101 comprises and is consumed refrigerant lines 150 and compressed refrigerant lines 120, the described main aspiration end being consumed refrigerant lines 150 and connecting low temperature heat exchanger 180 (being the shell-side 186 of low temperature heat exchanger 180 in this case) and main refrigerant compressor 160, described compressed refrigerant lines 120 connects main refrigerant compressor 160 exhaust outlet and MR separator 128.One or more heat exchanger is arranged in compressed refrigerant lines 120, comprises at least one ambient heat exchanger 124 and the pre-cooled heat exchanger 125 of at least one freezing main refrigerant in the present embodiment.MR separator 128 is restrained 183 fluids via light refrigerant fraction pipeline 121 with bottom LMR and is connected, and to restrain with HMR via heavy refrigerant fraction line 122 and be connected.
The pre-cooled heat exchanger of at least one freezing hydro carbons described 115 and the pre-cooled heat exchanger of at least one freezing main refrigerant described 125 are by pre-cooled cold-producing medium freezing (respectively via pipeline 127 and 126).Identical pre-cooled cold-producing medium can be shared by identical pre-cooled refrigerant circulation.In addition, the pre-cooled heat exchanger of at least one freezing hydro carbons described 115 may be combined with into a pre-cooled heat exchanger unit (not shown) with the pre-cooled heat exchanger of at least one freezing main refrigerant described 125.With reference to United States Patent (USP) 6,370,910 as nonrestrictive example.
Optional outside stripping steam supply line 74 (if providing) can point suitably in the upstream of the pre-cooled heat exchanger of at least one freezing hydro carbons described 115, the pre-cooled heat exchanger 115 of at least one freezing hydro carbons described the point in downstream, or (such as possibly, if provide two or more freezing hydro carbons pre-cooled heat exchanger) some place between two pre-cooled heat exchangers of the freezing hydro carbons of continuous print is connected to hydrocarbon feed pipeline 110, to obtain a part for the hydrocarbon feed stream from hydrocarbon feed pipeline 110.
Transition point place between top (182,184) and bottom (181,183) tube bank, HMR tube bank 185 is connected with HMR pipeline 141 fluid, in described HMR pipeline 141, configure HMR control valve 144.HMR pipeline 141 is communicated with shell-side 186 fluid of low temperature heat exchanger 180, and via shell-side 186 and with bottom hydrocarbon products restrain 181 with bottom LMR restrain 183 to arrange with the heat exchange of each that HMR restrains in 185 and be consumed refrigerant lines 150 fluid and be communicated with.
Above upper bundle 182 and 184, close to the top of low temperature heat exchanger 180, LMR tube bank 184 is connected with LMR pipeline 131 fluid.One LMR return line 133 is set up fluid and is communicated with between LMR pipeline 131 and the shell-side 186 of low temperature heat exchanger 180.LMR control valve 134 is configured in a LMR return line 133.One LMR return line 133 via described shell-side 186 and with upper and lower hydrocarbon products restrain each in 182 and 181 to restrain with LMR heat exchange that each in 183 and 184 to restrain 185 with HMR arrange and be consumed refrigerant lines 150 fluid and be communicated with.
Fig. 2 shows the possible source of of auxiliary refrigerant.LMR pipeline 131 is divided into auxiliary refrigerant pipeline 132 and a LMR return line 133.2nd LMR return line 138 is connected with supplement heat rejecter agent pipeline 132 fluid via evaporator overhead condenser (its can the form of integral inner evaporator overhead condenser 235 implement) at its upstream end, and described in downstream the 2nd LMR return line 138 suitably via a HMR pipeline 141 final be consumed refrigerant lines 150 and be connected.
Similar around the pipeline shown in the pipeline of nitrogen stripping tower 20 and Fig. 1 in fig. 2, and state no longer in detail.Optional pipeline (comprising optional liquid recycle pipeline 13, optional outside stripping steam supply line 74, optional vapor bypass pipeline 76 and optional vapor recirculation pipeline 87) can be provided, but in order to clear and do not reproduce in fig. 2.
The embodiment of comparison diagram 2 and the embodiment of Fig. 1, it should be noted that evaporator overhead condenser 35, top separator 33 and return-flow system are implemented with the form of integral inner evaporator overhead condenser 235 known in the art, described integral inner evaporator overhead condenser 235 is configured at the inside of the top section 26 in nitrogen stripping tower 20.If needed, optional liquid recycle pipeline 13 also can provide when Fig. 2, such as, pass through the optional condensate fraction current divider 39 of setting unit liquid drain tower tray (not shown) form between integral inner evaporator overhead condenser 235 and rectifying portion section 22 on gravity.
Apparatus and method for removing nitrogen from the low temperature hydrocarbon composition comprised containing the liquid phase of nitrogen and methane can operate as follows:
Providing package is containing the low temperature hydrocarbon composition 8 of the liquid phase containing nitrogen and methane, and described low temperature hydrocarbon composition 8 is preferably under the initial pressure of 2 to 15 bars absolute (bara) and preferably lower than at the temperature of-130 DEG C.
Low temperature hydrocarbon composition 8 can available from natural gas or oil reservoir or coal bed.Select as one, low temperature hydrocarbon composition 8 also can be originated available from another, comprises and such as synthesizes source, as Fischer-Tropsch process.Preferably, low temperature hydrocarbon composition 8 comprises the methane of at least 50mol%, more preferably the methane of at least 80mol%.
In a typical implementation, the temperature by making hydrocarbon feed stream 110 realize lower than-130 DEG C through liquefaction system 100.In this liquefaction system 100, comprise the feed stream of hydrocarbon-containifirst hydrocarbon feed stream 110 can such as in low temperature heat exchanger 180 with the heat exchange of main refrigerant stream, the feed stream of liquefaction feed stream is to provide the thick fluidized flow in thick liquiefied product pipeline 1 thus.Required low temperature hydrocarbon composition 8 can subsequently available from thick fluidized flow 1.
Main refrigerant stream produces by the main refrigerant in circulation main refrigerant circuit 101, and the cold-producing medium 150 be consumed thus is compressed in main refrigerant compressor 160, thus forms compressed cold-producing medium 120 by the cold-producing medium 150 be consumed.Via the one or more heat exchangers be arranged in compressed refrigerant lines 120, heat extraction from the compressed cold-producing medium of discharge from main refrigerant compressor 160.The compressed cold-producing medium of this generating portion condensation, it is separated into light refrigerant fraction 121 and heavy refrigerant cut 122 in MR separator 128, described light refrigerant fraction 121 is made up of the vapor composition of the compressed cold-producing medium of partial condensation, and described heavy refrigerant cut 122 is made up of the liquid component of the compressed cold-producing medium of partial condensation.
Light refrigerant fraction 121 continuously via bottom LMR restraint 183 and top LMR restraint 184 and through low temperature heat exchanger 180, and heavy refrigerant cut 122 via HMR bundle 185 through low temperature heat exchanger 180 until transition point.When through other tube bank of these points, point other light and heavy refrigerant cut, by again evaporating the light of (thus producing the cold-producing medium 150 be consumed) and the cooling of heavy refrigerant cut in shell-side 186, this accomplishes circulation.Meanwhile, hydrocarbon feed stream 110 continuously via bottom hydro carbons bundle 181 and top hydro carbons bundle 182 through low temperature heat exchanger 180, and by the light of identical evaporation and the liquefaction of heavy refrigerant cut and excessively cold.
Depend on source, hydrocarbon feed stream 110 can component containing difference amount except methane and nitrogen, comprises one or more non-hydrocarbons components in addition to water (as CO
2, Hg, H
2s and other sulphur compounds); With one or more hydro carbons heavier than methane (such as ethane, propane and butane especially, and the pentane of possible less amount and aromatic hydrocarbons).The hydro carbons that molecular weight is at least the molecular weight of propane can be described as C herein
3+ hydro carbons, the hydro carbons that molecular weight is at least the molecular weight of ethane can be described as C herein
2+ hydro carbons.
If need, hydrocarbon feed stream 110 can pretreatment with reduce and/or remove one or more undesirable components, as CO
2and H
2s, or experienced other steps, as precharge etc.This step well known to a person skilled in the art, and their mechanism is not discussed further herein.Therefore, the composition of hydrocarbon feed stream 110 depends on the type of gas and position and one or more pretreatment of applying and changes.
Nitrogen between 1mol% to 5mol% under liquefaction pressure under thick fluidized flow 1 can be included in the original temperature between-165 DEG C to-120 DEG C and between 15bara to 120bara.In many cases, original temperature can be between-155 DEG C to-140 DEG C.In described narrower range, cooling power required in liquefaction system 100 lower than cooling power required at lower temperatures, and higher than under the pressure of 15bara to cross cold enough high to avoid the excessive generation being decompressed to the flashed vapour between 1 to 2bara.
By thick fluidized flow 1 is mainly decompressed to initial pressure by liquefaction pressure, and obtain low temperature hydrocarbon composition 8 by thick fluidized flow 1.First nitrogen stripping device incoming flow 10 derived from low temperature hydrocarbon composition 8, and via the nitrogen stripping tower 20 that the first entrance system 21 is fed under stripping pressure.
Stripping pressure is generally equal to or lower than initial pressure.In preferred embodiments, stripping pressure is chosen as between 2 to 15 bars absolute.Preferably, stripping pressure is at least 4bara, be more preferably at least 5bara, because use slightly higher stripping pressure, then the stripping steam in stripping steam pipeline 71 can benefit from some the other enthalpys (form of the heat of compression) being added into process streams 60 in process compresses machine 260.Preferably, stripping pressure is 8bara at the most, is more preferably 7bara at the most, to be conducive to the separative efficiency in nitrogen stripping tower 20.In addition, if in the scope of stripping pressure between 4 to 8bara, then the waste gas in vapor fraction pipeline 80 can be easy to as so-called low-pressure fuel gas stream without the need to further compression.
In one embodiment, the original temperature of thick fluidized flow 1 is-161 DEG C, and liquefaction pressure is 55bara.Main decompression can complete in two stages: the movement segment first using expansion turbine 6, so that pressure is reduced to about 10bara from 55bara, then uses JouleThomson valve 7 in process segment, be decompressed to the pressure of 7bara further.In this case, stripping pressure is assumed to be 6bara.
First nitrogen stripping device incoming flow 10 comprises the Part I of low temperature hydrocarbon composition 8.It can contain whole low temperature hydrocarbon composition 8, but in practice, preferably low temperature hydrocarbon composition 8 is divided into Part I 10 and the Part II 11 with the composition identical with Part I 10 and phase, and makes described Part II be diverted to such as optional end flash gas separator 50 with the form of bypass incoming flow.Low temperature hydrocarbon combined stream is split into the first and second parts, makes Part II 11 have the composition identical with Part I 10 and phase.
Bypass stream flow control valve 15 can be used to control split ratio, and described split ratio is defined as the flow of the Part II of the flow relative to the low temperature hydrocarbon composition in low temperature hydrocarbon composition pipeline 8.Described bypass stream flow control valve 15 controls by flow governor FC, enters predeterminated target flow in nitrogen stripping tower 20 to keep the first nitrogen stripping device incoming flow 10.Exceed the flow of the surplus of target flow if existed, then flow governor FC opens part by what increase bypass stream flow control valve 15, if there is underfed compared to target flow, then reduction is opened part by flow governor FC.
As general principle, split ratio can advantageously be chosen as between 50% to 95%.For nitrogen content higher in low temperature hydrocarbon composition, usually recommend lower value, and for lower nitrogen content, preferably higher value.In one embodiment, the nitrogen content in low temperature hydrocarbon composition 8 is 3.0mol%, and split ratio selected is thus 75%.
Overhead vapor stream 30 is available from the top section 26 of the nitrogen stripping tower 20 above rectifying portion section 22.
The liquid 40 through nitrogen stripping is extracted from the liquid storage space 28 of nitrogen stripping tower 20.Through the temperature of the liquid 40 of nitrogen stripping usually above the temperature of the first nitrogen stripping device incoming flow 10.Usually, expect that temperature through the liquid 40 of nitrogen stripping is higher than the temperature of the first nitrogen stripping device incoming flow 10, and be between-140 DEG C to-80 DEG C, between being preferably-140 DEG C to-120 DEG C.
Then preferably use intermediate relief device 45 that the liquid 40 through nitrogen stripping is decompressed to flashing pressure, described flashing pressure lower than stripping pressure, and in scope suitably between 1 to 2 bars absolute.Preferably, in the scope of flashing pressure between 1.0 to 1.4bara.Under difference between slightly higher flashing pressure and stripping pressure, the stripping steam in stripping steam pipeline 71 can benefit from some the other heats of compression being added into process streams 60 in process compresses machine 260.
Intermediate relief device 45 can be controlled by liquid-level controller LC, described liquid-level controller LC is set as: if the fluid level of accumulation is increased to more than target level in the liquid storage space 28 of nitrogen stripping tower 20, then described liquid-level controller LC increases the flow by intermediate relief device.As the result of decompression, temperature is reduced to less than-160 DEG C usually.Liquid hydrocarbon product stream 90 obtained thus can keep under atmospheric pressure usually in the low-temperature storage tank of open insulation.
Also production process steam 60.Process steam 60 can comprise the flashed vapour 64 usually by producing through the liquid 40 of nitrogen stripping and/or the decompression of Volatile Gas 230, described Volatile Gas 230 can due to following and produce: heat is added into liquid hydrocarbon product stream 90, makes a part for liquid hydrocarbon product stream 90 evaporate and form Volatile Gas.
Subsequently the optional Part II being derived from optional initial flow current divider 9 is being fed at least one in the discharge pipe line 40 of the liquid of nitrogen stripping, liquid hydrocarbon product pipeline 90 and process steam pipeline 60, and before walking around nitrogen stripping tower 20, also described Part II is decompressed to described flashing pressure simultaneously.Suitably, optional Part II is passed in optional end flash gas separator 50.
In order to promote that Volatile Gas is passed to process steam stream 60, preferably, optional Volatile Gas supply line 230 connect low temperature storage pipe 210 in vapor space and process steam pipeline 60.In order to promote that flashed vapour 64 is passed to process vapor stream 60, and further liquid hydrocarbon product stream 90 is denitrogenated, preferably, after the liquid pressure-reducing through nitrogen stripping, liquid through nitrogen stripping is fed in optional end flash gas separator, in described optional end flash gas separator, the liquid through nitrogen stripping is separated into liquid hydrocarbon product stream 90 and flashed vapour 64 under flash separation pressure.Flash separation pressure is equal to or less than flashing pressure, and is suitably in the scope between 1 to 2 bars absolute, is separated into liquid hydrocarbon product stream 90 and flashed vapour 64.In one embodiment, flash separation pressure is contemplated to 1.05bara.
Process steam 60 is compressed at least stripping pressure, obtains compressed steam stream 70 thus.Stripping steam stream 71 available from compressed steam stream 70, and is passed to nitrogen stripping tower 20 via the second entrance system 23.Described stripping steam can with downward diafiltration by the liquid comes into contact adverse current of stripping portion section 23 upwards diafiltration by stripping portion section 23.
Arrange if outside stripping steam supply line 74 is communicated with the second entrance system 23 fluid, then outside stripping steam is optionally fed to nitrogen stripping tower 20 via the second entrance system 23.The chief destructive of nitrogen stripping tower 20 can be avoided thus, such as, when process compresses machine 260 does not play the effect of the compressed steam stream 70 providing q.s.
Obtain stripping steam stream 71 by compressed steam stream 70 can relate to compressed steam stream 70 is divided into stripping steam stream 71 and vapor bypass part, described vapor bypass part does not comprise Stripping section, and optionally injects overhead vapor pipeline 30 to walk around nitrogen stripping tower 20 thus.Vapor bypass control valve 77 can be used to control Selective implantation.Suitably, vapor bypass control valve 77 is controlled by the pressure controller on compressed vapour pipeline 70, and what described pressure controller was set to respond the pressure that increases in compressed steam pipeline 70 and increased vapor bypass control valve 77 opens part.Expection allows to flow through vapor bypass pipeline 76 and to enter the flow of the vapor bypass part in overhead vapor stream 30 high especially in so-called loading pattern process, and the amount of the Volatile Gas when described loading pattern is usually than much higher in so-called Holdover mode process.Preferably, vapor bypass control valve 77 is closed in course of normal operation in the hold mode completely.
The intermediate flow of partial condensation is formed by overhead vapor 30, and described overhead vapor is available from the top section of the nitrogen stripping tower 20 above rectifying portion section 22.This relates to makes overhead vapor 30 and auxiliary refrigerant stream 132 indirect heat exchange, and heat is passed to auxiliary refrigerant stream 132 with selected cooling power from overhead vapor 30 thus.The intermediate flow of gained partial condensation comprises condensate fraction and vapor fraction.
Condensate fraction is separated with vapor fraction under separating pressure in top separator 33, and described separating pressure can lower than stripping pressure, and in scope preferably between 2 to 15 bars absolute.Vapor fraction is discharged via vapor fraction discharge pipe line 80.Condensate fraction is such as disposed to return-flow system from top separator 33 via condensate fraction discharge pipe line 37.
Suitably, at least fuel meat of vapor fraction 80 is passed to not higher than the burner 220 under the fuel gas pressure of stripping pressure.In embodiments, such as, when burner 220 is made up of one or more stove, fuel gas pressure can in the scope of 3 to 5bara.Stripping pressure can such as in the scope of 5 to 7bara.In this way, there is no need for the compressor of fuel gas, and fuel gas flows to burner 220 by Stress control.
Automatic adjustment cooling power is with the calorific value of the vapor fraction regulating and controlling to discharge.Vapor fraction is passed in the embodiment of selectivity consume person (burner 220 such as shown in Fig. 1) of one or more methane wherein, required heating power can be responded and complete control, the calorific value that the partial discharge controlling methane thus needs to obtain coupling.Suitably, auxiliary refrigerant stream flow control valve 135 controls by pressure controller PC, to keep auxiliary refrigerant stream 132 by the predeterminated target flow of evaporator overhead condenser 35.The calorific value of actual pressure in vapor fraction discharge pipe line 80 therefore to regulated is relevant.When pressure drop is below horizontal to predeterminated target (it represents that the depletion rate of methane is higher than the delivery rate of vapor fraction 80), what pressure controller PC was set as reducing auxiliary refrigerant stream flow control valve 135 opens part.On the contrary, when pressure exceedes predeterminated target level, what pressure controller PC was set as increasing auxiliary refrigerant stream flow control valve 135 opens part.
Expection vapor fraction 80 is containing the nitrogen between 50mol% to 95mol%, nitrogen between preferred 70mol% to 95mol% or the nitrogen between 50mol% to 90mol%, more preferably the nitrogen between 70mol% to 90mol%, nitrogen also more preferably between 75mol% to 95mol%, the nitrogen most preferably between 75mol% to 90mol%.Expection condensate fraction 37 is containing the nitrogen being less than 35mol%.
Originate in the level place above rectifying portion section 22, make at least refluxing portion 36 of condensate fraction enter nitrogen stripping tower 20.When the embodiment of Fig. 1, condensate fraction can be passed through optional reflux pump 38 (and/or it can flow under the influence of gravity).Refluxing portion subsequently available from condensate fraction, and loads nitrogen stripping tower 20 via reflux inlet system 25 and refluxing portion pipeline 36.When the embodiment of Fig. 2, condensate fraction is separated in the inside of the top section of nitrogen stripping tower 20, and therefore obtains above rectifying portion section, and to contact with the steam upwards rising through rectifying portion section 22, downward diafiltration is by rectifying portion section.
Refluxing portion can contain whole condensate fraction, but optionally, condensate fraction is divided into liquid recycle part and refluxing portion in the optional condensate fraction current divider 39 arranged, described liquid recycle part is disposed in such as the first incoming flow 10 via liquid recycle pipeline 13, and described refluxing portion is disposed in nitrogen stripping tower 20 via reflux inlet system 25 and refluxing portion pipeline 36.Ability condensate fraction being divided into refluxing portion 36 and liquid recycle part 13 is conducive to any excessive condensate fraction is turned to around rectifying portion section 22, such as, not disturb the operation of rectifying portion section 22.The flow governor that is arranged in condensate fraction discharge pipe line 37 and/or the liquid-level controller be arranged in top separator 33 can be used suitably to control recycle valve 14.
Partial condensation also can relate to and other the direct and/or indirect heat exchange flowed in the top heat exchanger arranged continuously at other.Such as, cold recovery heat exchanger 85 can be a kind of top heat exchanger, and by described top heat exchanger, the partial condensation of overhead stream also comprises and vapor fraction 80 indirect heat exchange.
Auxiliary refrigerant 132 flows at the temperature of the bubbling point lower than overhead vapor stream 30, preferably has bubbling point (ISO13443 standard: under 1.0 atmospheric pressure 15 DEG C) at the standard conditions at the standard conditions.This is conducive to the methane be present in overhead vapor stream 30 of the relatively more a large amount of condensation again, thus and then promotes the controllability of the methane content in vapor fraction 80.Such as, auxiliary refrigerant can containing the nitrogen between 5mol% to 75mol%.In a preferred embodiment, auxiliary refrigerant stream is formed by the slip-stream of main refrigerant stream, is more preferably formed by the slip-stream of light refrigerant fraction.A rear situation is shown in Figure 2, but is also applicable to the embodiment of Fig. 1.This slip-stream can be transmitted back in main refrigerant circuit expediently via the shell-side 186 of low temperature heat exchanger 180, and wherein said slip-stream can still assist to extract heat from the stream top and/or lower bundle.
In one embodiment, a contemplated composition of auxiliary refrigerant contains the C2 (ethane and/or ethene) of methane between nitrogen between 25mol% to 40mol%, 30mol% to 60mol% and 30mol% at the most, thus, auxiliary refrigerant contain at least 95% these compositions and/or nitrogen and methane be total up at least 65mol%.If use excessively cold for the hydrocarbon stream that liquefies of mix refrigerant, then the composition within the scope of these can be easy to derive from main refrigerant circuit.
Also kind of refrigeration cycle separately may be used with the object in order to partial condensation overhead vapor stream 30.But, use the slip-stream tool from main refrigerant stream to have the following advantages: the amount of the other equipment of installation is minimum.Such as, other auxiliary refrigerant compressor and auxiliary refrigerant condenser is not needed.
Can suitably by optionally opening steam recycle control valve 88 and optionally use optional vapor recirculation pipeline 87, increasing the nitrogen amount be held in liquid hydrocarbon product stream 90.This is by completing as follows: from vapor fraction, extract vapor recirculation part, by vapor recirculation part reduced pressure to flashing pressure, and subsequently vapor recirculation part is injected the liquid 40 through nitrogen stripping.The remainder not being passed to the vapor fraction 80 in vapor recirculation pipeline 87 can form fuel meat, and described fuel meat can be sent to burner 220.
In some embodiments, the aim parameter being dissolved in the nitrogen in liquid hydrocarbon product stream 90 is between 0.5 to 1mol%, preferably close to 1.0mol%, but is no more than 1.1mol% as far as possible.Vapor recirculation flow control valve 88 regulates charging to be back in such as end flash gas separator 50 and walks around the amount of the vapor fraction stream 80 of nitrogen stripping tower 20 simultaneously.Therefore, the nitrogen amount in liquid hydrocarbon product stream 90 can be affected.In order to contribute to meeting target nitrogen content further, the signal from the mass measurer QMI be optionally arranged in liquid hydrocarbon product pipeline 90 can be responded and control vapor recirculation flow control valve 88.
For both Holdover mode (table 1) and loading pattern (table 2), the embodiment shown in Fig. 1 carries out static simulation.Suppose that low temperature hydrocarbon composition 8 comprises the mixture (98.204mol%) of nitrogen more than 90mol% and methane.In an embodiment, the amount of nitrogen (1.654mol%) and methane (98.204mol%) is made up of carbon dioxide (0.005mol%) more than the surplus of 99.8mol%, 0.142mol%.Carbon dioxide leaves described process via through the liquid 40 of nitrogen stripping and liquid hydrocarbon product stream 90.
Can find out, in Holdover mode and loading pattern, although the measurer of process steam has large difference, but in the scope under the amount of methane in discharge vapor fraction 80 can be maintained at about 80mol% and suitably between 10mol% to 25mol%, and the nitrogen content simultaneously in liquid hydrocarbon product stream 90 remains on close to 1.0mol% and is no more than in the target of 1.1mol%.
In Holdover mode, the Volatile Gas be made up of of about 2.0kg/s is added into process via Volatile Gas supply line 230, and Volatile Gas is about 4.4kg/s described in loading pattern the nitrogen of about 17mol% and the methane of 83mol%.
In both cases, the split ratio of initial steam current divider 9 is about 75%.In Holdover mode, steam is not guided through vapor bypass pipeline 76, and in loading pattern, 30% in compressed vapour 70 is guided through vapor bypass pipeline 76, to hold the other steam brought by the inflow of other Volatile Gas.In loading pattern, liquid recycle 13 is also increased to about 41% of described condensate fraction by about 8% of the condensate fraction in condensate fraction discharge pipe line 37.The flowing of other condensate fraction caused by the other methane of condensation again.
Liquefaction system 100 in calculating uses setting as shown in Figure 2, and the mix refrigerant in compressed refrigerant pipeline 120 has as composition listed in the row being labeled as " 120 " in table 3.
Table 3: mix refrigerant composition (in mol%)
In Holdover mode, the pressure in compressed refrigerant pipeline 120 is 58bara, and described in loading pattern, pressure is higher, is 61bara.In both cases, the total pressure drop restrained in (being respectively 183 and 184) in the bottom of low temperature heat exchanger and top LMR is 13bar.The pressure drop applied by auxiliary refrigerant stream flow control valve 135 is 39bar in Holdover mode situation, is 42bar in loading pattern, thus for Holdover mode and loading pattern, the shell pressure in the shell-side 186 of low temperature heat exchanger 180 is identical.
The relative discharge of auxiliary refrigerant stream 132 is 11% of the total LMR flow in LMR pipeline 131.In loading pattern, the relative discharge of auxiliary refrigerant stream 132 is 18% of the total LMR flow in LMR pipeline 131.And actual flow is 1.6 times in Holdover mode situation, but compared in Holdover mode operation, in loading pattern operation, make the separation slightly more preference HMR in MR separator 128 between HMR and LMR.
In as above embodiment, suppose low temperature hydrocarbon composition not containing the hydro carbons (C heavier than methane
2+ hydro carbons), such as following situation: low temperature hydrocarbon composition, derived from non-conventional gas body source, synthesizes as coalbed methane, shale gas or possible some and originates.But the method and apparatus proposed also can be applicable to wherein low temperature hydrocarbon composition and contains the C of about 15mol% at the most
2the situation of+hydro carbons (comprise be selected from ethane, propane, iso-butane, normal butane and pentane one or more).In fact, these other C are not expected
2+ hydro carbons changes the running of the method and apparatus proposed, because it is expected that this C
2+ hydro carbons is all present in the waste gas of overhead vapor 30 or vapor fraction discharge pipe line 80 unlike the carbon dioxide of embodiment.
It will be apparent to those skilled in the art that when not departing from the scope of appended claims, the present invention can be carried out in a number of different ways.
Claims (16)
1. from low temperature hydrocarbon composition, remove the method for nitrogen, described low temperature hydrocarbon composition comprises the liquid phase containing nitrogen and methane, and described method comprises:
-providing package is containing the low temperature hydrocarbon composition of the liquid phase containing nitrogen and methane;
-the first nitrogen stripping device incoming flow under stripping pressure is fed to nitrogen stripping tower, described nitrogen stripping tower comprises at least one inner rectifying portion section and is arranged at least one the inner stripping portion section in the nitrogen stripping tower below described rectifying portion section gravity, and described first nitrogen stripping device incoming flow comprises the Part I of described low temperature hydrocarbon composition;
-from liquid through nitrogen stripping of the liquid storage spatial extraction of the nitrogen stripping tower below described stripping portion section;
-prepare at least liquid hydrocarbon product stream and process steam by the described liquid through nitrogen stripping, at least comprise the described liquid pressure-reducing through nitrogen stripping to the step of flashing pressure;
-described process steam is compressed at least stripping pressure, obtain compressed vapour thus;
-stripping steam is spread in the nitrogen stripping tower of the At The Height be handed to below described stripping portion section gravity, described stripping steam flow to the Stripping section comprising described compressed vapour less;
-by the intermediate flow of the overhead vapor forming section condensation of the top section available from the nitrogen stripping tower above described rectifying portion section, the intermediate flow of described partial condensation comprises condensate fraction and vapor fraction, described formation comprises by making described overhead vapor and the heat exchange of auxiliary refrigerant stream and thus heat being passed to auxiliary refrigerant stream with certain cooling power from described overhead vapor, thus overhead vapor described in partial condensation;
-under separating pressure, described condensate fraction is separated with described vapor fraction;
-discharge vapor fraction as waste gas, described vapor fraction has calorific value;
-at least refluxing portion of described condensate fraction is entered originate in the nitrogen stripping tower of the height above described rectifying portion section;
-regulate described cooling power to regulate the calorific value of the vapor fraction of discharging.
2. method according to claim 1, in the scope of wherein said stripping pressure between 2 to 15 bars absolute and/or wherein said flashing pressure be between 1 to 2 bars absolute.
3., according to method according to claim 1 or claim 2, it also comprises and to be passed to by least fuel meat of described vapor fraction not higher than the burner under the fuel gas pressure of stripping pressure.
4., according to method according to claim 1 or claim 2, it also comprises the steps:
-described low temperature hydrocarbon combined stream is split into described Part I and there is the composition identical with described Part I and the Part II of phase;
-described Part II is decompressed to described flashing pressure; And
-subsequently described Part II is fed in following at least one: through the liquid of nitrogen stripping, liquid hydrocarbon product stream and process steam;
Wherein from described diverting flow to described charging Part II, described Part II walks around described nitrogen stripping tower.
5. method according to claim 4, it is further comprising the steps of:
-control the split ratio that described low temperature hydrocarbon composition is split into described Part I and described Part II, under thus the flow of described Part I being remained on predeterminated target flow, described split ratio is defined as the flow of the described Part I relative to described first and second parts total flow together.
6. according to method according to claim 1 or claim 2, wherein said process steam comprises the Volatile Gas obtained by heat being added into described liquid hydrocarbon product stream, and a part for liquid hydrocarbon product stream is evaporated and forms described Volatile Gas thus.
7., according to method according to claim 1 or claim 2, wherein described, the described liquid pressure-reducing through nitrogen stripping is produced flashed vapour to the process of described flashing pressure, and wherein said process steam comprises described flashed vapour.
8. method according to claim 7, wherein said described in prepared by the described liquid through nitrogen stripping at least liquid hydrocarbon product stream and process steam also comprise the steps: under flash separation pressure in end flash gas separator, the described liquid through nitrogen stripping is separated into liquid hydrocarbon product stream and flashed vapour.
9., according to method according to claim 1 or claim 2, the wherein said described low temperature hydrocarbon composition that provides comprises:
-make the incoming flow of the feed stream comprising hydrocarbon-containifirst in low temperature heat exchanger with the heat exchange of main refrigerant stream, the feed stream of described incoming flow of liquefying thus is to provide thick fluidized flow; And
-obtain described low temperature hydrocarbon composition by described thick fluidized flow.
10. method according to claim 9, wherein said auxiliary refrigerant stream is formed by the slip-stream of described main refrigerant stream.
11. according to method according to claim 1 or claim 2, it also comprises the by-passing part of described compressed vapour is optionally injected described overhead vapor, walk around at least stripping portion section of described nitrogen stripping tower thus, described by-passing part does not comprise Stripping section.
12. according to method according to claim 1 or claim 2, and it also comprises:
-extract vapor recirculation part from described vapor fraction;
-by described vapor recirculation part reduced pressure to flashing pressure;
-described vapor recirculation part is injected following at least one: through the liquid of nitrogen stripping, liquid hydrocarbon product stream and process steam.
13. according to method according to claim 1 or claim 2, and wherein said auxiliary refrigerant stream contains the nitrogen between 5mol% to 75mol%.
14. according to method according to claim 1 or claim 2, and wherein said vapor fraction comprises the nitrogen between 50mol% to 95mol%.
15. according to method according to claim 1 or claim 2, and wherein said condensate fraction comprises the nitrogen being less than 35mol%.
16. 1 kinds for removing the device of nitrogen from low temperature hydrocarbon composition, described low temperature hydrocarbon composition comprises the liquid phase containing nitrogen and methane, and described device comprises:
-for providing the low temperature feeding line of low temperature hydrocarbon composition, described low temperature hydrocarbon composition comprises the liquid phase containing nitrogen and methane;
-nitrogen stripping the tower that is communicated with described low temperature feeding line fluid, described nitrogen stripping tower comprises at least one inner rectifying portion section and is arranged at least one the inner stripping portion section in the nitrogen stripping tower below described rectifying portion section gravity;
-intermediate relief device, described intermediate relief device fluid is connected to described nitrogen stripping tower, and the liquid through nitrogen stripping in the liquid storage space in order to receive the nitrogen stripping tower below comfortable described stripping portion section gravity is set, and by the described liquid pressure-reducing through nitrogen stripping, on the interface of described intermediate relief device between the stripping pressure side comprising described nitrogen stripping tower and flashing pressure side;
-be arranged at liquid hydrocarbon product pipeline on described flashing pressure side, to discharge the liquid hydrocarbon product stream produced by the described liquid through nitrogen stripping;
-be arranged at process steam pipeline on described flashing pressure side, to receive the process steam produced by the described liquid through nitrogen stripping;
-be arranged at process compresses machine in described process steam pipeline, it is arranged in order to receive described process steam and to compress described process steam, compressed vapour is provided, on the described interface of described process compresses machine between stripping pressure side and flashing pressure side with the process compresses machine floss hole place at described process compresses machine;
-stripping steam pipeline, the At The Height of described stripping steam pipeline below the gravity of described stripping portion section is communicated with described nitrogen stripping tower fluid, and arranges at least Stripping section in order to receive from the described compressed vapour of described process compresses machine;
-evaporator overhead condenser, described evaporator overhead condenser arranges overhead vapor and the auxiliary refrigerant stream indirect heat exchange contact of the top section in order to make the nitrogen stripping tower above available from described rectifying portion section, obtain the intermediate flow comprising the partial condensation of condensate fraction and vapor fraction thus, wherein in operation, heat is passed to described auxiliary refrigerant stream with certain cooling power from described overhead vapor;
-discharge pipe line, described discharge pipe line arranges the vapor fraction in order to discharge with calorific value;
-return-flow system, described return-flow system is arranged in order to allow the At The Height of at least refluxing portion of described condensate fraction above described rectifying portion section to enter described nitrogen stripping tower;
-cooling power controller, described cooling power controller is arranged in order to regulate cooling power, to regulate and control the calorific value of the vapor fraction of discharge.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP11192920 | 2011-12-12 | ||
| EP11192920.4 | 2011-12-12 | ||
| PCT/EP2012/074959 WO2013087571A2 (en) | 2011-12-12 | 2012-12-10 | Method and apparatus for removing nitrogen from a cryogenic hydrocarbon composition |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104011489A CN104011489A (en) | 2014-08-27 |
| CN104011489B true CN104011489B (en) | 2016-03-23 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201280061162.5A Active CN104011489B (en) | 2011-12-12 | 2012-12-10 | For removing the method and apparatus of nitrogen from low temperature hydrocarbon composition |
Country Status (7)
| Country | Link |
|---|---|
| US (1) | US20140345319A1 (en) |
| CN (1) | CN104011489B (en) |
| AU (1) | AU2012354774B2 (en) |
| CA (1) | CA2858155C (en) |
| MY (1) | MY185531A (en) |
| RU (1) | RU2607708C2 (en) |
| WO (1) | WO2013087571A2 (en) |
Families Citing this family (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9441877B2 (en) | 2010-03-17 | 2016-09-13 | Chart Inc. | Integrated pre-cooled mixed refrigerant system and method |
| PE20160913A1 (en) | 2013-03-15 | 2016-09-01 | Chart Energy And Chemicals Inc | MIXED REFRIGERANT SYSTEM AND METHOD |
| US11428463B2 (en) | 2013-03-15 | 2022-08-30 | Chart Energy & Chemicals, Inc. | Mixed refrigerant system and method |
| US11408673B2 (en) | 2013-03-15 | 2022-08-09 | Chart Energy & Chemicals, Inc. | Mixed refrigerant system and method |
| EP2857782A1 (en) * | 2013-10-04 | 2015-04-08 | Shell International Research Maatschappij B.V. | Coil wound heat exchanger and method of cooling a process stream |
| US10563913B2 (en) * | 2013-11-15 | 2020-02-18 | Black & Veatch Holding Company | Systems and methods for hydrocarbon refrigeration with a mixed refrigerant cycle |
| US20150276307A1 (en) * | 2014-03-26 | 2015-10-01 | Dresser-Rand Company | System and method for the production of liquefied natural gas |
| US20150308737A1 (en) | 2014-04-24 | 2015-10-29 | Air Products And Chemicals, Inc. | Integrated Nitrogen Removal in the Production of Liquefied Natural Gas Using Intermediate Feed Gas Separation |
| US9945604B2 (en) * | 2014-04-24 | 2018-04-17 | Air Products And Chemicals, Inc. | Integrated nitrogen removal in the production of liquefied natural gas using refrigerated heat pump |
| EP2977430A1 (en) * | 2014-07-24 | 2016-01-27 | Shell Internationale Research Maatschappij B.V. | A hydrocarbon condensate stabilizer and a method for producing a stabilized hydrocarbon condenstate stream |
| AR105277A1 (en) | 2015-07-08 | 2017-09-20 | Chart Energy & Chemicals Inc | MIXED REFRIGERATION SYSTEM AND METHOD |
| US10330382B2 (en) | 2016-05-18 | 2019-06-25 | Fluor Technologies Corporation | Systems and methods for LNG production with propane and ethane recovery |
| CA3033088A1 (en) * | 2016-09-09 | 2018-03-15 | Fluor Technologies Corporation | Methods and configuration for retrofitting ngl plant for high ethane recovery |
| CN106885713B (en) * | 2017-03-20 | 2019-06-11 | 上海锐宇流体系统有限公司 | High pressure easily flashes mixing liquid sampler |
| AU2019234226B2 (en) * | 2018-03-14 | 2022-04-14 | Exxonmobil Upstream Research Company | Method and system for liquefaction of natural gas using liquid nitrogen |
| US12098882B2 (en) | 2018-12-13 | 2024-09-24 | Fluor Technologies Corporation | Heavy hydrocarbon and BTEX removal from pipeline gas to LNG liquefaction |
| US20230076428A1 (en) * | 2021-09-02 | 2023-03-09 | Air Products And Chemicals, Inc. | Integrated nitrogen rejection for liquefaction of natural gas |
Family Cites Families (30)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3165454A (en) * | 1962-03-01 | 1965-01-12 | Phillips Petroleum Co | Fractionation control |
| US4096574A (en) * | 1977-07-28 | 1978-06-20 | Phillips Petroleum Company | Fractionation control |
| US4357153A (en) * | 1981-03-30 | 1982-11-02 | Erickson Donald C | Internally heat pumped single pressure distillative separations |
| US4404008A (en) | 1982-02-18 | 1983-09-13 | Air Products And Chemicals, Inc. | Combined cascade and multicomponent refrigeration method with refrigerant intercooling |
| IT1176290B (en) | 1984-06-12 | 1987-08-18 | Snam Progetti | LOW-BOILING GAS COOLING AND LIQUEFATION PROCESS |
| US4604117A (en) * | 1984-11-15 | 1986-08-05 | Union Carbide Corporation | Hybrid nitrogen generator with auxiliary column drive |
| US5137559A (en) * | 1990-08-06 | 1992-08-11 | Air Products And Chemicals, Inc. | Production of nitrogen free of light impurities |
| MY118329A (en) | 1995-04-18 | 2004-10-30 | Shell Int Research | Cooling a fluid stream |
| US5657643A (en) | 1996-02-28 | 1997-08-19 | The Pritchard Corporation | Closed loop single mixed refrigerant process |
| US5669234A (en) | 1996-07-16 | 1997-09-23 | Phillips Petroleum Company | Efficiency improvement of open-cycle cascaded refrigeration process |
| DE19716415C1 (en) | 1997-04-18 | 1998-10-22 | Linde Ag | Process for liquefying a hydrocarbon-rich stream |
| TW477890B (en) | 1998-05-21 | 2002-03-01 | Shell Int Research | Method of liquefying a stream enriched in methane |
| US6308531B1 (en) | 1999-10-12 | 2001-10-30 | Air Products And Chemicals, Inc. | Hybrid cycle for the production of liquefied natural gas |
| TW480325B (en) | 1999-12-01 | 2002-03-21 | Shell Int Research | Plant for liquefying natural gas |
| US6295833B1 (en) | 2000-06-09 | 2001-10-02 | Shawn D. Hoffart | Closed loop single mixed refrigerant process |
| US6640161B1 (en) * | 2001-02-02 | 2003-10-28 | Uop Llc | Method for operating a steam stripped fractionation column |
| GB0111961D0 (en) * | 2001-05-16 | 2001-07-04 | Boc Group Plc | Nitrogen rejection method |
| EG24658A (en) | 2002-09-30 | 2010-04-07 | Bpcorporation North America In | All electric lng system and process |
| US7127914B2 (en) | 2003-09-17 | 2006-10-31 | Air Products And Chemicals, Inc. | Hybrid gas liquefaction cycle with multiple expanders |
| US6962060B2 (en) | 2003-12-10 | 2005-11-08 | Air Products And Chemicals, Inc. | Refrigeration compression system with multiple inlet streams |
| US7213413B2 (en) * | 2004-06-16 | 2007-05-08 | Conocophillips Company | Noninvasive measurement and control system for use in hydrocarbon processing |
| PE20060221A1 (en) * | 2004-07-12 | 2006-05-03 | Shell Int Research | LIQUEFIED NATURAL GAS TREATMENT |
| US20080006649A1 (en) * | 2006-01-30 | 2008-01-10 | Fawn Engineering Corp. | Apparatus, method, and system for promoting charitable contributions in association with an automated merchandising machine |
| US20110185767A1 (en) | 2006-08-17 | 2011-08-04 | Marco Dick Jager | Method and apparatus for liquefying a hydrocarbon-containing feed stream |
| US7798161B2 (en) * | 2006-09-05 | 2010-09-21 | Oliver Joen-An Ma | Shade structures such as umbrellas |
| US20080141711A1 (en) | 2006-12-18 | 2008-06-19 | Mark Julian Roberts | Hybrid cycle liquefaction of natural gas with propane pre-cooling |
| DE102007010032A1 (en) * | 2007-03-01 | 2008-09-04 | Linde Ag | Procedure for separating a nitrogen-rich fraction from a liquefied natural gas, comprises supplying the natural gas after its liquefaction and super cooling, to a stripping column that serves the separation of the nitrogen-rich fraction |
| JP2012514050A (en) * | 2008-11-03 | 2012-06-21 | シエル・インターナシヨナル・リサーチ・マートスハツペイ・ベー・ヴエー | Method and apparatus for providing a fuel gas stream by eliminating nitrogen from a hydrocarbon stream |
| RU2554736C2 (en) * | 2009-07-21 | 2015-06-27 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | Method of purifying multi-phase hydrocarbon flow and installation intended therefore |
| DE102009038458A1 (en) * | 2009-08-21 | 2011-02-24 | Linde Ag | Process for separating nitrogen from natural gas |
-
2012
- 2012-12-10 CN CN201280061162.5A patent/CN104011489B/en active Active
- 2012-12-10 AU AU2012354774A patent/AU2012354774B2/en active Active
- 2012-12-10 RU RU2014128666A patent/RU2607708C2/en active
- 2012-12-10 CA CA2858155A patent/CA2858155C/en active Active
- 2012-12-10 WO PCT/EP2012/074959 patent/WO2013087571A2/en active Application Filing
- 2012-12-10 MY MYPI2014701217A patent/MY185531A/en unknown
- 2012-12-10 US US14/364,262 patent/US20140345319A1/en not_active Abandoned
Also Published As
| Publication number | Publication date |
|---|---|
| CN104011489A (en) | 2014-08-27 |
| CA2858155A1 (en) | 2013-06-20 |
| RU2607708C2 (en) | 2017-01-10 |
| CA2858155C (en) | 2020-04-28 |
| RU2014128666A (en) | 2016-02-10 |
| US20140345319A1 (en) | 2014-11-27 |
| MY185531A (en) | 2021-05-19 |
| WO2013087571A3 (en) | 2014-05-01 |
| WO2013087571A2 (en) | 2013-06-20 |
| AU2012354774A1 (en) | 2013-07-18 |
| AU2012354774B2 (en) | 2015-09-10 |
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