NL1001940C2 - Method and device for removing nitrogen from natural gas. - Google Patents
Method and device for removing nitrogen from natural gas. Download PDFInfo
- Publication number
- NL1001940C2 NL1001940C2 NL1001940A NL1001940A NL1001940C2 NL 1001940 C2 NL1001940 C2 NL 1001940C2 NL 1001940 A NL1001940 A NL 1001940A NL 1001940 A NL1001940 A NL 1001940A NL 1001940 C2 NL1001940 C2 NL 1001940C2
- Authority
- NL
- Netherlands
- Prior art keywords
- natural gas
- nitrogen
- heat exchanger
- liquid oxygen
- burner
- Prior art date
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Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
-
- 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
-
- 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
-
- 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
-
- 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
- F25J2210/50—Oxygen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Treating Waste Gases (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Gas Separation By Absorption (AREA)
Abstract
Description
Werkwijze en inrichting voor het verwijderen van stikstof uit aardgasMethod and device for removing nitrogen from natural gas
De onderhavige uitvinding heeft betrekking op een werkwijze en inrichting voor het verwijderen van stikstof uit aardgas.The present invention relates to a method and apparatus for removing nitrogen from natural gas.
Opgemerkt wordt, dat stikstof in aardgas ongewenst 5 is, omdat stikstof geen bijdrage levert tot hogere vlamtempe-raturen integendeel, stikstof vormt een ballast, redenen waarom stikstof uit aardgas verwijderd dient te worden.It is noted that nitrogen in natural gas is undesirable because nitrogen does not contribute to higher flame temperatures, on the contrary, nitrogen forms a ballast, reasons why nitrogen must be removed from natural gas.
Bovendien is het bekend dat stikstof bij hogere vlam-temperaturen verbindingen aangaat met zuurstof, waarbij toxi-10 sche ΝΟ,-verbindingen worden gevormd.In addition, it is known that nitrogen bonds with oxygen at higher flame temperatures to form toxic compounds.
Ook om die redenen is het duidelijk dat stikstof voor verbrandingsprocessen een uiterst ongewenst gas is.For these reasons, too, it is clear that nitrogen is an extremely undesirable gas for combustion processes.
Het is voorts algemeen bekend, dat oxyfuel een vaak toegepast proces is, waar tijdens een verbrandingsproces zui-15 ver zuurstof in plaats van lucht wordt gebruikt met als doel een rendementsverbetering bij ovens. Het spreekt voor zich dat ook hier de in de lucht aanwezige stikstof (ca. 79 vol.%) slechts ballast is en naast de zoeven vermelde nadelen tot warmteverlies leidt, omdat stikstof als opgewarmd gas weer de 20 atmosfeer wordt ingeblazen.It is furthermore well known that oxyfuel is a frequently used process where pure oxygen is used instead of air during a combustion process with the aim of improving furnace efficiency. It goes without saying that here too the nitrogen present in the air (approx. 79% by volume) is only ballast and, in addition to the disadvantages mentioned above, leads to heat loss, because nitrogen is blown back into the atmosphere as heated gas.
Doel van de uitvinding is het verwijderen van stikstof uit aardgas en het gebruik van zuiver zuurstof, gepaard gaande met rendementsverbeteringen.The object of the invention is the removal of nitrogen from natural gas and the use of pure oxygen, accompanied by efficiency improvements.
Hiertoe dient de in het aardas aanwezige stikstof, 25 voordat aardgas in het verbrandingsproces terechtkomt, te worden verwijderd.For this purpose, the nitrogen present in the natural ash must be removed before natural gas enters the combustion process.
Hiertoe verschaft de onderhavige uitvinding een werkwijze en inrichting.To this end, the present invention provides a method and apparatus.
De werkwijze voor het verwijderen van stikstof uit 30 aardgas door middel van cryocondensatie heeft volgens de uitvinding het kenmerk, dat als koude middel vloeibare zuurstof wordt gebruikt.According to the invention, the method for removing nitrogen from natural gas by means of cryocondensation is characterized in that liquid oxygen is used as the cold medium.
Volgens de stand der techniek wordt cryocondensatie van koolwaterstoffen uitgevoerd onder gebruikmaking van koude 35 stikstof als koudemiddel.In the prior art, cryocondensation of hydrocarbons is performed using cold nitrogen as the refrigerant.
1001940 21001940 2
Volgens de onderhavige uitvinding zijn de bovengenoemde nadelen op doeltreffende wijze opgeheven.According to the present invention, the above-mentioned drawbacks have been effectively eliminated.
Gebleken is, dat de werkwijze volgens de uitvinding bijzonder geschikt is stikstof uit aardgas, dat ca. 14 vol.% 5 stikstof bevat, te verwijderen.It has been found that the method according to the invention is particularly suitable for removing nitrogen from natural gas containing approximately 14% by volume of nitrogen.
In beginsel komt de uitvinding daarop neer, dat de vloeibare zuurstof wordt verdampt in een cryocondensatie-een-heid, waardoor de koolwaterstoffen condenseren. Na verwarming kunne de gecondenseerde koolwaterstoffen te zamen met de ont-10 stane gasvormige zuurstof benut worden in het verbrandingsproces .In principle, the invention boils down to the liquid oxygen being evaporated in a cryocondensation unit, whereby the hydrocarbons condensate. After heating, the condensed hydrocarbons, together with the resulting gaseous oxygen, can be used in the combustion process.
Volgens een gunstige uitvoeringsvorm van de onderhavige uitvinding wordt de vloeibare zuurstof geleid naar een warmtewisselaar alwaar het stikstof-rijke aardgas wordt gecon-15 denseerd en de achtergebleven gasvormige stikstof wordt afgevoerd terwijl de van stikstof ontdane gecondenseerde koolwaterstoffen, na te zijn verwarmd, als ook de gasvormige zuurstof worden geleid naar een brander.According to a favorable embodiment of the present invention, the liquid oxygen is passed to a heat exchanger where the nitrogen-rich natural gas is condensed and the residual gaseous nitrogen is discharged while the nitrogen-depleted condensed hydrocarbons, after being heated, as well as the gaseous oxygen are led to a burner.
Bij voorkeur wordt het te behandelen aardgas in een 20 warmtewisselaar voorgekoeld tot ca. -80°C voorafgaande aan de afkoeling met de vloeibare zuurstof tot ca. -165°C.Preferably, the natural gas to be treated is pre-cooled in a heat exchanger to about -80 ° C prior to cooling with the liquid oxygen to about -165 ° C.
De werkwijze volgens de uitvinding verschaft de volgende voordelen ten opzichte van de stand der techniek: 1) De toxische NOx-verbindingen worden tot een minimum 25 gereduceerd.The method of the invention provides the following advantages over the prior art: 1) The toxic NOx compounds are reduced to a minimum.
2) Er wordt een hoog calorisch aardgas verkregen uit een laag calorisch aardgas, zoals bijv. het geval is bij aardgas, dat afkomstig is uit de Noordzee.2) A high calorific natural gas is obtained from a low calorific natural gas, as is the case, for example, with natural gas originating from the North Sea.
3) Er wordt aardgas verkregen met een hogere verbran-30 dingswaarde, welk aardgas in het bijzonder geschikt is voor toepassing in smeltovens in de glasindustrie, keramische industrie, staalindustrie en non-ferro-industrie.3) Natural gas is obtained with a higher combustion value, which natural gas is particularly suitable for use in melting furnaces in the glass industry, ceramic industry, steel industry and non-ferrous industry.
Voorts heeft de onderhavige uitvinding betrekking op een inrichting voor het verwijderen van stikstof uit aardgas, 35 met het kenmerk, dat de inrichting (1) is voorzien van een opslagtank (2) voor vloeibare zuurstof, welke tank (2) door middel van een leiding (5) is verbonden met de warmtewisselaar (3) voor het condenseren van het aardgas, dat via leiding (7) en warmtewisselaar (3) in verbinding staat met warmtewisselaar 1001940 3 (4), waaruit het gecondenseerde en van stikstof bevrijde aardgas via leiding (6), na te zijn verwarmd in de warmtewisselaar (4) , via leiding (13) terechtkomt in de brander (12), terwijl vloeibare zuurstof uit warmtewisselaar (3), via leiding (9) 5 terechtkomt in warmtewisselaar (11) en daarvandaan via leiding (10) in de gasfase wordt geleid naar brander (12) en gasvormige stikstof uit warmtewisselaar (3) via leiding (8) wordt verwijderd.The present invention further relates to a device for removing nitrogen from natural gas, characterized in that the device (1) is provided with a storage tank (2) for liquid oxygen, which tank (2) by means of a pipe (5) is connected to the heat exchanger (3) for condensing the natural gas, which communicates via pipe (7) and heat exchanger (3) with heat exchanger 1001940 3 (4), from which the condensed and nitrogen-free natural gas is piped (6), after being heated in the heat exchanger (4), enters the burner (12) via line (13), while liquid oxygen from heat exchanger (3), enters heat exchanger (11) via line (9), and from there it is led via line (10) in the gas phase to burner (12) and gaseous nitrogen is removed from heat exchanger (3) via line (8).
De uitvinding zal thans nader worden toegelicht aan 10 de hand van de bijgaande tekening, die een voorkeursuitvoeringsvorm van de inrichting volgens de uitvinding weergeeft.The invention will now be further elucidated with reference to the accompanying drawing, which shows a preferred embodiment of the device according to the invention.
In de tekening wordt de inrichting volgens de uitvinding met verwijzingscijfer (1) weergegeven. De inrichting (1) volgens de uitvinding is voorzien van een opslagtank (2) voor 15 vloeibare zuurstof.In the drawing the device according to the invention is indicated with reference number (1). The device (1) according to the invention is provided with a storage tank (2) for liquid oxygen.
Voorts is de inrichting voorzien van warmtewisselaars (3,4 en 11) .The device is furthermore provided with heat exchangers (3,4 and 11).
Hierbij wordt bijv. aardgas uit Groningen met een stikstofgehalte van 14 vol.% uit het net toegevoerd aan de 20 warmtewisselaar (4), waarin het aardgas wordt afgekoeld tot -80°C. Het aldus afgekoelde aardgas wordt vervolgens via klep (15) geleid naar de warmtewisselaar (3) om verder te worden afgekoeld met behulp van vloeibare zuurstof tot -160 tot -165°C, welke vloeibare zuurstof via leiding (5) en kraan (14) 25 uit de opslagtank (2) in de warmtewisselaar wordt geleid. De in de warmtewisselaar (3) gecondenseerde koolwaterstoffen worden via leiding (6) gevoerd in warmtewisselaar (4), waar de vloeibare koolwaterstoffen in gasvormige toestand overgaan en als zodanig via leiding (13) worden getransporteerd naar bijv. 30 brander (12) van een smeltoven.For example, natural gas from Groningen with a nitrogen content of 14% by volume is supplied from the network to the heat exchanger (4), in which the natural gas is cooled to -80 ° C. The natural gas thus cooled is then passed via valve (15) to the heat exchanger (3) to be further cooled using liquid oxygen to -160 to -165 ° C, which liquid oxygen via line (5) and tap (14) 25 is led from the storage tank (2) into the heat exchanger. The hydrocarbons condensed in the heat exchanger (3) are fed via line (6) into heat exchanger (4), where the liquid hydrocarbons pass into gaseous form and are transported as such via line (13) to e.g. 30 burner (12) of a melting furnace.
Aan de brander (12) wordt voorts zuurstof, die afkomstig is van de warmtewisselaar (3) in vloeibare toestand via leiding (9) en kraan(16) in de warmtewisselaar (11) geleid. In de warmtewisselaar (11) wordt koude gasvormige zuurstof verder 35 opgewarmd tot omgevingstemperatuur. Via leiding (10) wordt de zuurstof in gasvormige toestand verenigd met de koolwaterstoffen in brander (12) van de smeltoven.Oxygen, which comes from the liquid heat exchanger (3), is also fed to the burner (12) via line (9) and tap (16) into the heat exchanger (11). In the heat exchanger (11), cold gaseous oxygen is further heated to ambient temperature. Gaseous oxygen is combined with the hydrocarbons in burner (12) of the melting furnace via line (10).
Het spreekt voor zich, dat andere uitvoeringsvormen van de werkwijze en inrichting volgens de uitvinding mogelijk 1001940 4 zijn zonder van de essentie ervan af te wijken. Dergelijke varianten worden vanzelfsprekend door de onderhavige uitvinding omvat.It goes without saying that other embodiments of the method and device according to the invention are possible 1001940 4 without deviating from its essence. Such variants are, of course, encompassed by the present invention.
10019401001940
Claims (5)
Priority Applications (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL1001940A NL1001940C2 (en) | 1995-12-20 | 1995-12-20 | Method and device for removing nitrogen from natural gas. |
| DE69613664T DE69613664T2 (en) | 1995-12-20 | 1996-12-16 | Process and plant for removing nitrogen from natural gas |
| AT96203555T ATE202840T1 (en) | 1995-12-20 | 1996-12-16 | METHOD AND SYSTEM FOR REMOVING NITROGEN FROM NATURAL GAS |
| EP96203555A EP0780649B1 (en) | 1995-12-20 | 1996-12-16 | A method and installation for the removal of nitrogen from natural gas |
| PL96317602A PL317602A1 (en) | 1995-12-20 | 1996-12-19 | Method of removing nitrogen from earth gas and system therefor |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL1001940A NL1001940C2 (en) | 1995-12-20 | 1995-12-20 | Method and device for removing nitrogen from natural gas. |
| NL1001940 | 1995-12-20 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| NL1001940C2 true NL1001940C2 (en) | 1997-06-24 |
Family
ID=19762059
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NL1001940A NL1001940C2 (en) | 1995-12-20 | 1995-12-20 | Method and device for removing nitrogen from natural gas. |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP0780649B1 (en) |
| AT (1) | ATE202840T1 (en) |
| DE (1) | DE69613664T2 (en) |
| NL (1) | NL1001940C2 (en) |
| PL (1) | PL317602A1 (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2763081C (en) | 2011-12-20 | 2019-08-13 | Jose Lourenco | Method to produce liquefied natural gas (lng) at midstream natural gas liquids (ngls) recovery plants. |
| CA2772479C (en) | 2012-03-21 | 2020-01-07 | Mackenzie Millar | Temperature controlled method to liquefy gas and a production plant using the method. |
| CA2790961C (en) | 2012-05-11 | 2019-09-03 | Jose Lourenco | A method to recover lpg and condensates from refineries fuel gas streams. |
| CA2787746C (en) | 2012-08-27 | 2019-08-13 | Mackenzie Millar | Method of producing and distributing liquid natural gas |
| CA2798057C (en) | 2012-12-04 | 2019-11-26 | Mackenzie Millar | A method to produce lng at gas pressure letdown stations in natural gas transmission pipeline systems |
| CA2813260C (en) | 2013-04-15 | 2021-07-06 | Mackenzie Millar | A method to produce lng |
| WO2016023098A1 (en) | 2014-08-15 | 2016-02-18 | 1304338 Alberta Ltd. | A method of removing carbon dioxide during liquid natural gas production from natural gas at gas pressure letdown stations |
| WO2017045055A1 (en) | 2015-09-16 | 2017-03-23 | 1304342 Alberta Ltd. | A method of preparing natural gas at a gas pressure reduction stations to produce liquid natural gas (lng) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5036671A (en) * | 1990-02-06 | 1991-08-06 | Liquid Air Engineering Company | Method of liquefying natural gas |
| US5390499A (en) * | 1993-10-27 | 1995-02-21 | Liquid Carbonic Corporation | Process to increase natural gas methane content |
-
1995
- 1995-12-20 NL NL1001940A patent/NL1001940C2/en not_active IP Right Cessation
-
1996
- 1996-12-16 AT AT96203555T patent/ATE202840T1/en not_active IP Right Cessation
- 1996-12-16 DE DE69613664T patent/DE69613664T2/en not_active Expired - Fee Related
- 1996-12-16 EP EP96203555A patent/EP0780649B1/en not_active Expired - Lifetime
- 1996-12-19 PL PL96317602A patent/PL317602A1/en unknown
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5036671A (en) * | 1990-02-06 | 1991-08-06 | Liquid Air Engineering Company | Method of liquefying natural gas |
| US5390499A (en) * | 1993-10-27 | 1995-02-21 | Liquid Carbonic Corporation | Process to increase natural gas methane content |
Also Published As
| Publication number | Publication date |
|---|---|
| EP0780649B1 (en) | 2001-07-04 |
| EP0780649A1 (en) | 1997-06-25 |
| ATE202840T1 (en) | 2001-07-15 |
| PL317602A1 (en) | 1997-06-23 |
| DE69613664D1 (en) | 2001-08-09 |
| DE69613664T2 (en) | 2002-05-29 |
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| VD1 | Lapsed due to non-payment of the annual fee |
Effective date: 20050701 |