EP3043133A1 - Method of removing nitrogen from a nitrogen containing stream - Google Patents
Method of removing nitrogen from a nitrogen containing stream Download PDFInfo
- Publication number
- EP3043133A1 EP3043133A1 EP15150823.1A EP15150823A EP3043133A1 EP 3043133 A1 EP3043133 A1 EP 3043133A1 EP 15150823 A EP15150823 A EP 15150823A EP 3043133 A1 EP3043133 A1 EP 3043133A1
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- Prior art keywords
- stream
- nitrogen
- split
- mol
- obtaining
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 156
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 78
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 title claims abstract description 63
- 238000000034 method Methods 0.000 title claims abstract description 35
- 238000011064 split stream procedure Methods 0.000 claims abstract description 54
- 239000007789 gas Substances 0.000 claims abstract description 43
- 239000007788 liquid Substances 0.000 claims abstract description 39
- 238000010438 heat treatment Methods 0.000 claims abstract description 6
- 238000001816 cooling Methods 0.000 claims abstract description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 14
- 239000000203 mixture Substances 0.000 description 4
- MWRWFPQBGSZWNV-UHFFFAOYSA-N Dinitrosopentamethylenetetramine Chemical compound C1N2CN(N=O)CN1CN(N=O)C2 MWRWFPQBGSZWNV-UHFFFAOYSA-N 0.000 description 1
- 229940112112 capex Drugs 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- FEBLZLNTKCEFIT-VSXGLTOVSA-N fluocinolone acetonide Chemical compound C1([C@@H](F)C2)=CC(=O)C=C[C@]1(C)[C@]1(F)[C@@H]2[C@@H]2C[C@H]3OC(C)(C)O[C@@]3(C(=O)CO)[C@@]2(C)C[C@@H]1O FEBLZLNTKCEFIT-VSXGLTOVSA-N 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Images
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
- F25J1/0025—Boil-off gases "BOG" from storages
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
- F25J1/0202—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
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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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
- F25J3/061—Natural gas or substitute natural 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/0635—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/066—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of nitrogen
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
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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
- F25J2230/30—Compression of the feed stream
Definitions
- the present invention relates to a method of removing nitrogen from a nitrogen-containing stream.
- NRU Nemrogen Rejection Unit
- One or more of the above or other objects are achieved according to the present invention by providing a method of removing nitrogen from a nitrogen-containing stream, the method comprising at least the steps of:
- An advantage of the method according to the present invention is that it has a surprisingly simple design and can be standardized to treat and liquefy a wide range of feed gas compositions. Further, there is relatively limited utility and chemicals requirement resulting in a significant OPEX and CAPEX reduction.
- a nitrogen-containing stream is provided.
- the nitrogen-containing stream is not particularly limited, it preferably is a methane-rich gas stream.
- the nitrogen-containing stream comprises at least 5 mol% nitrogen, preferably at least 10 mol%, more preferably at least 15 mol%.
- the nitrogen-containing stream contains less than 80 mol% nitrogen.
- the nitrogen-containing stream comprises at least 20 mol%, preferably at least 40 mol% methane, and typically below 85 mol%.
- the nitrogen-containing stream comprises at most 1.0 mol% C 2+ , preferably at most 0.5 mol%, more preferably at most 0.25 mol%, even more preferably at most 0.1 mol%.
- C 2+ refers to C 2+ -hydrocarbons, i.e. hydrocarbons containing 2 or more carbon atoms per molecule.
- the nitrogen-containing stream is a relatively cold stream having a temperature of at most (i.e. below) -90°C, preferably at most -140°C.
- the nitrogen-containing stream has a temperature of at most -150°C, preferably at most -160°C, more preferably at most -162°C.
- the nitrogen-containing stream typically has a pressure of below 10.0 bara, preferably below 5.0 bara, more preferably below 2.0 bara. In case the nitrogen-containing stream has an elevated pressure (i.e. above 6.0 bar such as from 6.0 to 25 bara), it preferably has a temperature of from -95°C to -140°C.
- step (b) the nitrogen-containing stream is heated in a first heat exchanger thereby obtaining a heated nitrogen-containing stream.
- the heated nitrogen-containing stream obtained in step (b) has a temperature of from -140°C to 20°C, preferably below 10°C, more preferably below -20°C and preferably above - 80°C, more preferably above -50°C.
- the heated nitrogen-containing stream has an elevated pressure (i.e. above 6.0 bara, such as from 6.0 to 25 bara), it typically has a temperature of from 20°C to -90°C, preferably below -55°C.
- step (c) the heated nitrogen-containing stream is compressed thereby obtaining a compressed nitrogen-containing stream.
- the compressed nitrogen-containing stream typically has a pressure of above 3.0 bara to 45.0 bara, preferably below 30 bara and more preferably from 3 to 10 bara.
- the compressed nitrogen-containing stream may be cooled before splitting in step (d), e.g. in an air cooler.
- step (d) the compressed nitrogen-containing stream is split into a first split stream and a second split stream, typically at a volume ratio [first split stream/second split stream] of 0.10 to 0.40.
- first split stream is reused.
- step (e) the second split stream is cooled in the first and a second heat exchanger thereby obtaining a cooled second split stream.
- the second split stream is cooled first in the second heat exchanger and then in the first heat exchanger to obtain the cooled second split stream.
- the cooled second split stream has a temperature of from -155°C to -160°C, preferably about - 158°C. Further, the cooled second split stream typically has a pressure of from 3 to 10 bara.
- the typical temperature of the cooled second split stream may depend on the pressure of the stream; in case the cooled second split stream has an elevated pressure (e.g. above 10 bara, such as in the range of from 17 to 45 bara) the temperature of said stream will typically be higher (i.e. warmer), preferably in the range of from -85°C to -145°C.
- step (f) the cooled second split stream is expanded thereby obtaining an expanded second split stream.
- the expander as used in step (f) according to the present invention is not particularly limited (and may include a JT valve an orifice, a common expander, etc.), it is preferred that in the expander enthalpy is withdrawn from the cooled second split stream.
- a suitable expander for withdrawing enthalpy whilst expanding is a turbo-expander.
- the expanded second split stream typically has a pressure of from 1.5 to 6.0 bara, preferably about 2.0 bara.
- the expanded second split stream obtained in step (f) has a temperature of at most -150°C, preferably at most -155°C, more preferably at most -160°C, even more preferably at most -165°C.
- the typical temperature of the expanded second split stream may depend on the pressure of the stream. In case the expanded second split stream has an elevated pressure (e.g. above 6.0 bara) the temperature of said stream will typically be higher (i.e. warmer); in the latter case, the pressure is preferably between 6.0 and 25 bara and the temperature between - 115°C and -145°C.
- the expanded second split stream is separated in a first gas/liquid separator thereby obtaining a gaseous nitrogen-enriched stream and a liquid nitrogen-depleted stream.
- the gaseous nitrogen-enriched stream obtained in step (g) comprises from 30 to 75 mol% nitrogen, preferably above 40 mol%, more preferably above 50 mol% and preferably less than 72 mol%.
- the liquid nitrogen-depleted stream obtained in step (g) comprises at least 90 mol% methane, preferably at least 92 mol% and typically less than 98 mol%, preferably less than 95 mol%.
- the liquid nitrogen-depleted stream obtained in step (g) comprises less than 10 mol% nitrogen.
- step (h) the gaseous nitrogen-enriched stream is heated in the first or second heat exchanger thereby obtaining a heated nitrogen-enriched stream.
- step (h) the gaseous nitrogen-enriched stream is heated in the second heat exchanger.
- the heated nitrogen-enriched stream has a temperature of from 10°C to 30°C, preferably about 15°C.
- the gaseous nitrogen-enriched stream typically has a pressure of from 1.5 to 6.0 bara.
- the method further comprises the steps of:
- the expanded nitrogen-depleted stream obtained in step (i) is a multiphase stream (in particular containing gas and liquid) and has a temperature of from -166°C to -173°C, preferably about - 171°C.
- the typical temperature of the expanded nitrogen-depleted stream may depend on the pressure of the stream; in case the expanded nitrogen-depleted stream has an elevated pressure the temperature of said stream will typically be higher.
- the second gaseous nitrogen-enriched stream is used as at least a part of the nitrogen-containing stream provided in step (a).
- all of the second gaseous nitrogen-enriched stream is used for the nitrogen-containing stream provided in step (a); of course, the nitrogen-containing stream provided in step (a) may be composed of more than only the second gaseous nitrogen-enriched stream.
- the second liquid nitrogen-depleted stream obtained in step (j) is stored in a storage tank, typically an LNG storage tank.
- a boil-off gas stream from said storage tank is fed into the second gas/liquid separator.
- Fig. 1 schematically shows a process scheme for performing a method of removing nitrogen from a nitrogen-containing stream.
- the process scheme is generally referred to with reference number 1.
- the process scheme 1 comprises a heat exchanger 2 ("the first heat exchanger") and a heat exchanger 3 ("the second heat exchanger"), a compressor 4, a first gas/liquid separator 5, a second gas/liquid separator 6, an LNG storage tank 7 and JT-valves 8 and 9.
- the process scheme may comprise further heat exchangers in addition to the first heat exchanger 2 and second heat exchanger 3.
- the first heat exchanger 2 and second heat exchanger 3 are separate heat exchangers.
- Fig. 1 shows the nitrogen rejection from a boil-off stream 140 coming from the LNG tank 7.
- a nitrogen-containing stream 10 is provided.
- the nitrogen-containing stream 10 is a cold stream.
- the nitrogen-containing stream 10 is heated in a first heat exchanger 2 thereby obtaining a heated nitrogen-containing stream 20 and subsequently compressed in the compressor 4 thereby obtaining a compressed nitrogen-containing stream 30.
- the compressed nitrogen-containing stream 30 is split into a first split stream 40 and a second split stream 50.
- the second split stream 50 is cooled in the first 2 and a second heat exchanger 3 thereby obtaining a cooled second split stream 70.
- the first and second heat exchangers 2 and 3 are indirect heat exchangers; hence no direct contact between the streams takes place, but only heat exchanging contact.
- the second split stream 50 is cooled first in the second heat exchanger 3 and then in the first heat exchanger 2 to obtain the cooled second split stream 70.
- the cooled second split stream 70 is expanded in JT-valve 8 thereby obtaining an expanded second split stream 80, which expanded second split stream 80 is separated in the first gas/liquid separator 5 to obtain a gaseous nitrogen-enriched stream 90 and a liquid nitrogen-depleted stream 110.
- the gaseous nitrogen-enriched stream 90 is heated (in the embodiment of Figure 1 ) in the second heat exchanger 3 thereby obtaining a heated nitrogen-enriched stream 100.
- the heated nitrogen-enriched stream 100 is sent to a duct (or auxiliary) burner of a gas turbine to be used as a fuel gas.
- the liquid nitrogen-depleted stream 110 is expanded thereby obtaining an expanded nitrogen-depleted stream 120. Subsequently, the expanded nitrogen-depleted stream 120 is separated in the second gas/liquid separator 6 thereby obtaining a second gaseous nitrogen-enriched stream and a second liquid nitrogen-depleted stream 130.
- the second gaseous nitrogen-enriched stream is used as (part of) the nitrogen-containing stream 10 heated in the first heat exchanger 2.
- the second liquid nitrogen-depleted stream 130 is stored in an LNG storage tank 7.
- a boil-off gas stream 140 from said storage tank 7 is fed into the second gas/liquid separator 6 and reused.
- the LNG storage tank 7 may contain further inlets than shown in Figure 1 .
- other streams may be fed into the second gas/liquid separator 6.
- FIG. 2 an alternative process scheme is shown that is in particular suitable for performing the removal nitrogen at an elevated pressure (i.e. stream 10 at above 6.0 bara).
- Fig. 2 differs from the embodiment shown in Fig. 1 that it does not comprise the separator 6 and JT-valve 9.
- stream 110 feeds directly feeding into the tank 7.
- nitrogen-containing stream 10 does not originate from the separator 6 (which is absent in Fig. 2 ), but may be drawn from elsewhere.
- Table 1 below shows an actual non-limiting example, providing information on conditions and composition of the various streams, whilst using the scheme of Figure 1 for removing nitrogen from a nitrogen-containing stream.
- nitrogen-containing stream 10 was at about atmospheric pressure and contained trace amounts (less than 0.1 mol%) of C 2+ .
- Table 1 Composition and properties of various streams Stream Pressure [bara] Temp.
- the present invention allows for an effective removal of nitrogen (via stream 100) from stream 10; stream 130 being returned to the LNG storage tank 7 contained 4 mol% N 2 .
- nitrogen-containing stream 10 had a higher pressure (17 bara) than in Example 1 and contained a small amount (0.2 mol%) of C 2+ .
- Table 2 Composition and properties of various streams Stream Pressure [bara] Temp.
- the present invention allows for an effective removal of nitrogen (via stream 100) from stream 10; stream 110 contained 5.4 mol% N 2 .
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Abstract
The present invention provides a method of removing nitrogen from a nitrogen-containing stream (10), the method comprising at least the steps of:
(a) providing a nitrogen-containing stream (10);
(b) heating the nitrogen-containing stream (10) in a first heat exchanger (2) thereby obtaining a heated nitrogen-containing stream (20);
(c) compressing the heated nitrogen-containing stream (20) thereby obtaining a compressed nitrogen-containing stream (30);
(d) splitting the compressed nitrogen-containing stream (30) into a first split stream (40) and a second split stream (50);
(e) cooling the second split stream (50) in the first (2) and a second heat exchanger (3) thereby obtaining a cooled second split stream (70);
(f) expanding the cooled second split stream (70) thereby obtaining an expanded second split stream (80);
(g) separating the expanded second split stream (80) in a first gas/liquid separator (5) thereby obtaining a gaseous nitrogen-enriched stream (90) and a liquid nitrogen-depleted stream (110);
(h) heating the gaseous nitrogen-enriched stream (90) in the first or second heat exchanger (2,3) thereby obtaining a heated nitrogen-enriched stream (100).
(a) providing a nitrogen-containing stream (10);
(b) heating the nitrogen-containing stream (10) in a first heat exchanger (2) thereby obtaining a heated nitrogen-containing stream (20);
(c) compressing the heated nitrogen-containing stream (20) thereby obtaining a compressed nitrogen-containing stream (30);
(d) splitting the compressed nitrogen-containing stream (30) into a first split stream (40) and a second split stream (50);
(e) cooling the second split stream (50) in the first (2) and a second heat exchanger (3) thereby obtaining a cooled second split stream (70);
(f) expanding the cooled second split stream (70) thereby obtaining an expanded second split stream (80);
(g) separating the expanded second split stream (80) in a first gas/liquid separator (5) thereby obtaining a gaseous nitrogen-enriched stream (90) and a liquid nitrogen-depleted stream (110);
(h) heating the gaseous nitrogen-enriched stream (90) in the first or second heat exchanger (2,3) thereby obtaining a heated nitrogen-enriched stream (100).
Description
- The present invention relates to a method of removing nitrogen from a nitrogen-containing stream.
- Methods of removing nitrogen from a nitrogen-containing stream are known in the art. As an example, it is known to remove nitrogen using an NRU (Nitrogen Rejection Unit). A problem of using an NRU for removing nitrogen is the high expenditure associated with it.
- It is an object of the present invention to solve or at least minimize the above problem.
- It is a further object of the present invention to provide a simpler and more cost-effective method of removing nitrogen from a nitrogen-containing stream, in particular a methane-rich stream such as obtained during the liquefaction of natural gas.
- One or more of the above or other objects are achieved according to the present invention by providing a method of removing nitrogen from a nitrogen-containing stream, the method comprising at least the steps of:
- (a) providing a nitrogen-containing stream;
- (b) heating the nitrogen-containing stream in a first heat exchanger thereby obtaining a heated nitrogen-containing stream;
- (c) compressing the heated nitrogen-containing stream thereby obtaining a compressed nitrogen-containing stream;
- (d) splitting the compressed nitrogen-containing stream into a first split stream and a second split stream;
- (e) cooling the second split stream in the first and a second heat exchanger thereby obtaining a cooled second split stream;
- (f) expanding the cooled second split stream thereby obtaining an expanded second split stream;
- (g) separating the expanded second split stream in a first gas/liquid separator thereby obtaining a gaseous nitrogen-enriched stream and a liquid nitrogen-depleted stream;
- (h) heating the gaseous nitrogen-enriched stream in the first or second heat exchanger thereby obtaining a heated nitrogen-enriched stream.
- An advantage of the method according to the present invention is that it has a surprisingly simple design and can be standardized to treat and liquefy a wide range of feed gas compositions. Further, there is relatively limited utility and chemicals requirement resulting in a significant OPEX and CAPEX reduction.
- In step (a), a nitrogen-containing stream is provided. Although the nitrogen-containing stream is not particularly limited, it preferably is a methane-rich gas stream. Preferably, the nitrogen-containing stream comprises at least 5 mol% nitrogen, preferably at least 10 mol%, more preferably at least 15 mol%. Typically, the nitrogen-containing stream contains less than 80 mol% nitrogen. According to a preferred embodiment, the nitrogen-containing stream comprises at least 20 mol%, preferably at least 40 mol% methane, and typically below 85 mol%. Preferably, the nitrogen-containing stream comprises at most 1.0 mol% C2+, preferably at most 0.5 mol%, more preferably at most 0.25 mol%, even more preferably at most 0.1 mol%. In the context of the present invention, "C2+" refers to C2+-hydrocarbons, i.e. hydrocarbons containing 2 or more carbon atoms per molecule.
- Typically, the nitrogen-containing stream is a relatively cold stream having a temperature of at most (i.e. below) -90°C, preferably at most -140°C. Preferably, the nitrogen-containing stream has a temperature of at most -150°C, preferably at most -160°C, more preferably at most -162°C. Further, the nitrogen-containing stream typically has a pressure of below 10.0 bara, preferably below 5.0 bara, more preferably below 2.0 bara. In case the nitrogen-containing stream has an elevated pressure (i.e. above 6.0 bar such as from 6.0 to 25 bara), it preferably has a temperature of from -95°C to -140°C.
- In step (b), the nitrogen-containing stream is heated in a first heat exchanger thereby obtaining a heated nitrogen-containing stream. Preferably, the heated nitrogen-containing stream obtained in step (b) has a temperature of from -140°C to 20°C, preferably below 10°C, more preferably below -20°C and preferably above - 80°C, more preferably above -50°C. In case the heated nitrogen-containing stream has an elevated pressure (i.e. above 6.0 bara, such as from 6.0 to 25 bara), it typically has a temperature of from 20°C to -90°C, preferably below -55°C.
- In step (c), the heated nitrogen-containing stream is compressed thereby obtaining a compressed nitrogen-containing stream. Typically, the compressed nitrogen-containing stream typically has a pressure of above 3.0 bara to 45.0 bara, preferably below 30 bara and more preferably from 3 to 10 bara. If desired, the compressed nitrogen-containing stream may be cooled before splitting in step (d), e.g. in an air cooler.
- In step (d), the compressed nitrogen-containing stream is split into a first split stream and a second split stream, typically at a volume ratio [first split stream/second split stream] of 0.10 to 0.40. Typically, the first split stream is reused.
- In step (e), the second split stream is cooled in the first and a second heat exchanger thereby obtaining a cooled second split stream. Preferably, in step (e) the second split stream is cooled first in the second heat exchanger and then in the first heat exchanger to obtain the cooled second split stream.
- Typically the cooled second split stream has a temperature of from -155°C to -160°C, preferably about - 158°C. Further, the cooled second split stream typically has a pressure of from 3 to 10 bara. The person skilled in the art will readily understand that the typical temperature of the cooled second split stream may depend on the pressure of the stream; in case the cooled second split stream has an elevated pressure (e.g. above 10 bara, such as in the range of from 17 to 45 bara) the temperature of said stream will typically be higher (i.e. warmer), preferably in the range of from -85°C to -145°C.
- In step (f), the cooled second split stream is expanded thereby obtaining an expanded second split stream. Although the expander as used in step (f) according to the present invention is not particularly limited (and may include a JT valve an orifice, a common expander, etc.), it is preferred that in the expander enthalpy is withdrawn from the cooled second split stream. A suitable expander for withdrawing enthalpy whilst expanding is a turbo-expander.
- Typically, the expanded second split stream typically has a pressure of from 1.5 to 6.0 bara, preferably about 2.0 bara. Preferably, the expanded second split stream obtained in step (f) has a temperature of at most -150°C, preferably at most -155°C, more preferably at most -160°C, even more preferably at most -165°C. Again, the person skilled in the art will readily understand that the typical temperature of the expanded second split stream may depend on the pressure of the stream. In case the expanded second split stream has an elevated pressure (e.g. above 6.0 bara) the temperature of said stream will typically be higher (i.e. warmer); in the latter case, the pressure is preferably between 6.0 and 25 bara and the temperature between - 115°C and -145°C.
- In step (g), the expanded second split stream is separated in a first gas/liquid separator thereby obtaining a gaseous nitrogen-enriched stream and a liquid nitrogen-depleted stream. Preferably, the gaseous nitrogen-enriched stream obtained in step (g) comprises from 30 to 75 mol% nitrogen, preferably above 40 mol%, more preferably above 50 mol% and preferably less than 72 mol%. Further it is preferred that the liquid nitrogen-depleted stream obtained in step (g) comprises at least 90 mol% methane, preferably at least 92 mol% and typically less than 98 mol%, preferably less than 95 mol%. Typically, the liquid nitrogen-depleted stream obtained in step (g) comprises less than 10 mol% nitrogen.
- In step (h) the gaseous nitrogen-enriched stream is heated in the first or second heat exchanger thereby obtaining a heated nitrogen-enriched stream. Preferably, in step (h) the gaseous nitrogen-enriched stream is heated in the second heat exchanger.
- Typically the heated nitrogen-enriched stream has a temperature of from 10°C to 30°C, preferably about 15°C. Further, the gaseous nitrogen-enriched stream typically has a pressure of from 1.5 to 6.0 bara.
- According to an especially preferred embodiment according to the present invention, the method further comprises the steps of:
- (i) expanding the liquid nitrogen-depleted stream obtained in step (g) thereby obtaining an expanded nitrogen-depleted stream; and
- (j) separating the expanded nitrogen-depleted stream in a second gas/liquid separator thereby obtaining a second gaseous nitrogen-enriched stream and a second liquid nitrogen-depleted stream.
- Typically, the expanded nitrogen-depleted stream obtained in step (i) is a multiphase stream (in particular containing gas and liquid) and has a temperature of from -166°C to -173°C, preferably about - 171°C. Again, the person skilled in the art will readily understand that the typical temperature of the expanded nitrogen-depleted stream may depend on the pressure of the stream; in case the expanded nitrogen-depleted stream has an elevated pressure the temperature of said stream will typically be higher.
- Preferably, the second gaseous nitrogen-enriched stream is used as at least a part of the nitrogen-containing stream provided in step (a). Preferably, all of the second gaseous nitrogen-enriched stream is used for the nitrogen-containing stream provided in step (a); of course, the nitrogen-containing stream provided in step (a) may be composed of more than only the second gaseous nitrogen-enriched stream.
- According to a preferred embodiment, the second liquid nitrogen-depleted stream obtained in step (j) is stored in a storage tank, typically an LNG storage tank. Preferably, a boil-off gas stream from said storage tank is fed into the second gas/liquid separator.
- Hereinafter the invention will be further illustrated by the following non-limiting drawings. Herein shows:
-
Fig. 1 schematically a process scheme for performing the method according to the present invention; and -
Fig. 2 schematically an alternative process scheme for performing the method according to the present invention, at an elevated pressure. - For the purpose of this description, same reference numbers refer to same or similar components.
-
Fig. 1 schematically shows a process scheme for performing a method of removing nitrogen from a nitrogen-containing stream. The process scheme is generally referred to withreference number 1. - The
process scheme 1 comprises a heat exchanger 2 ("the first heat exchanger") and a heat exchanger 3 ("the second heat exchanger"), acompressor 4, a first gas/liquid separator 5, a second gas/liquid separator 6, an LNG storage tank 7 and JT-valves 8 and 9. The process scheme may comprise further heat exchangers in addition to thefirst heat exchanger 2 and second heat exchanger 3. Preferably, thefirst heat exchanger 2 and second heat exchanger 3 are separate heat exchangers. - The particular embodiment as shown in
Fig. 1 shows the nitrogen rejection from a boil-off stream 140 coming from the LNG tank 7. - During use of the
process scheme 1 according to the present invention, a nitrogen-containingstream 10 is provided. Typically the nitrogen-containingstream 10 is a cold stream. The nitrogen-containingstream 10 is heated in afirst heat exchanger 2 thereby obtaining a heated nitrogen-containingstream 20 and subsequently compressed in thecompressor 4 thereby obtaining a compressed nitrogen-containingstream 30. The compressed nitrogen-containingstream 30 is split into afirst split stream 40 and asecond split stream 50. - The
second split stream 50 is cooled in the first 2 and a second heat exchanger 3 thereby obtaining a cooledsecond split stream 70. The first andsecond heat exchangers 2 and 3 are indirect heat exchangers; hence no direct contact between the streams takes place, but only heat exchanging contact. In the embodiment ofFigure 1 , thesecond split stream 50 is cooled first in the second heat exchanger 3 and then in thefirst heat exchanger 2 to obtain the cooledsecond split stream 70. - Then, the cooled
second split stream 70 is expanded in JT-valve 8 thereby obtaining an expandedsecond split stream 80, which expanded second splitstream 80 is separated in the first gas/liquid separator 5 to obtain a gaseous nitrogen-enrichedstream 90 and a liquid nitrogen-depletedstream 110. The gaseous nitrogen-enrichedstream 90 is heated (in the embodiment ofFigure 1 ) in the second heat exchanger 3 thereby obtaining a heated nitrogen-enrichedstream 100. The heated nitrogen-enrichedstream 100 is sent to a duct (or auxiliary) burner of a gas turbine to be used as a fuel gas. - In the embodiment of
Figure 1 , the liquid nitrogen-depletedstream 110 is expanded thereby obtaining an expanded nitrogen-depletedstream 120. Subsequently, the expanded nitrogen-depletedstream 120 is separated in the second gas/liquid separator 6 thereby obtaining a second gaseous nitrogen-enriched stream and a second liquid nitrogen-depletedstream 130. In the embodiment ofFigure 1 , the second gaseous nitrogen-enriched stream is used as (part of) the nitrogen-containingstream 10 heated in thefirst heat exchanger 2. - The second liquid nitrogen-depleted
stream 130 is stored in an LNG storage tank 7. A boil-offgas stream 140 from said storage tank 7 is fed into the second gas/liquid separator 6 and reused. Of course, the LNG storage tank 7 may contain further inlets than shown inFigure 1 . Also, other streams may be fed into the second gas/liquid separator 6. - In the embodiment of
Fig. 2 , an alternative process scheme is shown that is in particular suitable for performing the removal nitrogen at an elevated pressure (i.e.stream 10 at above 6.0 bara). Apart from different temperatures and pressures,Fig. 2 differs from the embodiment shown inFig. 1 that it does not comprise theseparator 6 and JT-valve 9. Also stream 110 feeds directly feeding into the tank 7. Further, nitrogen-containingstream 10 does not originate from the separator 6 (which is absent inFig. 2 ), but may be drawn from elsewhere. - Table 1 below shows an actual non-limiting example, providing information on conditions and composition of the various streams, whilst using the scheme of
Figure 1 for removing nitrogen from a nitrogen-containing stream. In the embodiment of Table 1, nitrogen-containingstream 10 was at about atmospheric pressure and contained trace amounts (less than 0.1 mol%) of C2+.Table 1. Composition and properties of various streams Stream Pressure [bara] Temp. [°C] State Amount of CH4 [mol%] Amount of N2 [mol%] 10 1.05 -162.7 Gas 82 18 20 0.85 -134.9 Gas 82 18 30 4.5 -38.5 Gas 82 18 40 4.5 -38.5 Gas 82 18 50 4.5 -38.5 Gas 82 18 60 4.5 -61.1 Gas 82 18 70 4.5 -158.5 Gas/liquid 82 18 80 2.0 -165.9 Gas/liquid 82 18 90 2.0 -165.9 Gas 30 70 100 1.8 -41.5 Gas 30 70 110 2.0 -165.9 Liquid 93 7 120 1.05 -171.1 Gas/liquid 93 7 130 1.05 -162.7 Liquid 96 4 140 1.05 -161.7 Gas 83 17 - As can be seen from Table 1, the present invention allows for an effective removal of nitrogen (via stream 100) from
stream 10;stream 130 being returned to the LNG storage tank 7 contained 4 mol% N2. - In a further non-limiting example, exemplified by Table 2 and whilst using the scheme of
Figure 2 , nitrogen-containingstream 10 had a higher pressure (17 bara) than in Example 1 and contained a small amount (0.2 mol%) of C2+.Table 2. Composition and properties of various streams Stream Pressure [bara] Temp. [°C] State Amount of CH4 [mol%] Amount of N2 [mol%] Amount of C2+ [mol%] 10 17.0 -111.3 Gas 92.1 7.7 0.2 20 16.65 -70.8 Gas 92.1 7.7 0.2 30 36.4 20.0 Gas 92.1 7.7 0.2 40 36.4 20.0 Gas 92.1 7.7 0.2 50 36.4 20.0 Gas 92.1 7.7 0.2 60 36.2 -108.8 Gas 92.1 7.7 0.2 70 36.0 -109.4 Gas 92.1 7.7 0.2 80 17.0 -118.7 Gas/ liquid 92.1 7.7 0.2 90 17.0 -118.7 Gas 76.4 23.6 0 100 16.8 -111.3 Gas 76.4 23.6 0 110 17.0 -118.7 Liquid 94.4 5.4 0.2 120 N.A. 130 N.A. 140 N.A. - As can be seen from Table 2, the present invention allows for an effective removal of nitrogen (via stream 100) from
stream 10;stream 110 contained 5.4 mol% N2. - The person skilled in the art will readily understand that many modifications may be made without departing from the scope of the invention.
Claims (13)
- A method of removing nitrogen from a nitrogen-containing stream (10), the method comprising at least the steps of:(a) providing a nitrogen-containing stream (10);(b) heating the nitrogen-containing stream (10) in a first heat exchanger (2) thereby obtaining a heated nitrogen-containing stream (20);(c) compressing the heated nitrogen-containing stream (20) thereby obtaining a compressed nitrogen-containing stream (30);(d) splitting the compressed nitrogen-containing stream (30) into a first split stream (40) and a second split stream (50);(e) cooling the second split stream (50) in the first (2) and a second heat exchanger (3) thereby obtaining a cooled second split stream (70);(f) expanding the cooled second split stream (70) thereby obtaining an expanded second split stream (80);(g) separating the expanded second split stream (80) in a first gas/liquid separator (5) thereby obtaining a gaseous nitrogen-enriched stream (90) and a liquid nitrogen-depleted stream (110);(h) heating the gaseous nitrogen-enriched stream (90) in the first or second heat exchanger (2,3) thereby obtaining a heated nitrogen-enriched stream (100).
- The method according to claim 1, wherein the nitrogen-containing stream (10) comprises at least 5 mol% nitrogen, preferably at least 10 mol%, more preferably at least 15 mol%.
- The method according to claim 1 or 2, wherein the nitrogen-containing stream (10) comprises at most 1.0 mol% C2+, preferably at most 0.5 mol%, more preferably at most 0.25 mol%, even more preferably at most 0.1 mol%.
- The method according to any one of claims 1-3, wherein the nitrogen-containing stream (10) has a temperature of at most -150°C, preferably at most -160°C, more preferably at most -162°C.
- The method according to any one of claims 1-4, wherein in step (e) the second split stream (50) is cooled first in the second heat exchanger (3) and then in the first heat exchanger (2) to obtain the cooled second split stream (70).
- The method according to any one of claims 1-5, wherein the expanded second split stream (80) obtained in step (f) has a temperature of at most -150°C, preferably at most -160°C, more preferably at most -165°C.
- The method according to any one of claims 1-6, wherein the gaseous nitrogen-enriched stream (90) obtained in step (g) comprises from 30 to 75 mol% nitrogen, preferably above 40 mol%, more preferably above 50 mol% and preferably less than 72 mol%.
- The method according to any one of claims 1-7, wherein the liquid nitrogen-depleted stream (110) obtained in step (g) comprises at least 90 mol% methane, preferably at least 92 mol%.
- The method according to any one of claims 1-8, wherein in step (h) the gaseous nitrogen-enriched stream (90) is heated in the second heat exchanger (3).
- The method according to any one of claims 1-9, further comprising the steps of:(i) expanding the liquid nitrogen-depleted stream (110) obtained in step (g) thereby obtaining an expanded nitrogen-depleted stream (120); and(j) separating the expanded nitrogen-depleted stream in a second gas/liquid separator (6) thereby obtaining a second gaseous nitrogen-enriched stream and a second liquid nitrogen-depleted stream (130).
- The method according to claim 10, wherein the second gaseous nitrogen-enriched stream is used as at least a part of the nitrogen-containing stream (10) provided in step (a).
- The method according to claim 10 or 11, wherein the second liquid nitrogen-depleted stream (130) obtained in step (j) is stored in a storage tank (7).
- The method according to claim 12, wherein a boil-off gas stream (140) from said storage tank (7) is fed into the second gas/liquid separator (6).
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IT201800010171A1 (en) * | 2018-11-08 | 2020-05-08 | Saipem Spa | PROCESS FOR THE RE-LIQUEFACTION AND CONTEMPORARY DECREASE OF THE NITROGEN CONTENT IN THE BOG FOR SELF-REFRIGERATED ABSORPTION |
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US6199403B1 (en) * | 1998-02-09 | 2001-03-13 | Exxonmobil Upstream Research Company | Process for separating a multi-component pressurizied feed stream using distillation |
US20040065113A1 (en) * | 2000-12-18 | 2004-04-08 | Henri Paradowski | Method for refrigerating liquefied gas and installation therefor |
US20080066493A1 (en) * | 2004-07-12 | 2008-03-20 | Cornelis Buijs | Treating Liquefied Natural Gas |
US20140083132A1 (en) * | 2011-06-15 | 2014-03-27 | Gasconsult Limited | Process for liquefaction of natural gas |
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2015
- 2015-01-12 EP EP15150823.1A patent/EP3043133A1/en not_active Withdrawn
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US6199403B1 (en) * | 1998-02-09 | 2001-03-13 | Exxonmobil Upstream Research Company | Process for separating a multi-component pressurizied feed stream using distillation |
US20040065113A1 (en) * | 2000-12-18 | 2004-04-08 | Henri Paradowski | Method for refrigerating liquefied gas and installation therefor |
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US20140083132A1 (en) * | 2011-06-15 | 2014-03-27 | Gasconsult Limited | Process for liquefaction of natural gas |
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IT201800010171A1 (en) * | 2018-11-08 | 2020-05-08 | Saipem Spa | PROCESS FOR THE RE-LIQUEFACTION AND CONTEMPORARY DECREASE OF THE NITROGEN CONTENT IN THE BOG FOR SELF-REFRIGERATED ABSORPTION |
WO2020095246A3 (en) * | 2018-11-08 | 2020-08-06 | Saipem S.P.A. | Process for the ri—liquefaction and simultaneous reduction of nitrogen content in the bog for self-frigerated absorption |
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