NO172080B - PROCEDURE FOR THE PREPARATION OF GAS HYDRATES AND APPLIANCES FOR PERFORMING THE SAME - Google Patents
PROCEDURE FOR THE PREPARATION OF GAS HYDRATES AND APPLIANCES FOR PERFORMING THE SAME Download PDFInfo
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- NO172080B NO172080B NO90900395A NO900395A NO172080B NO 172080 B NO172080 B NO 172080B NO 90900395 A NO90900395 A NO 90900395A NO 900395 A NO900395 A NO 900395A NO 172080 B NO172080 B NO 172080B
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- Prior art keywords
- gas
- hydrate
- water
- particles
- reactor
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims description 22
- 150000004677 hydrates Chemical class 0.000 title claims description 8
- 239000007789 gas Substances 0.000 claims description 75
- 239000002245 particle Substances 0.000 claims description 62
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 49
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 36
- 239000003345 natural gas Substances 0.000 claims description 18
- 238000001816 cooling Methods 0.000 claims description 16
- 238000003860 storage Methods 0.000 claims description 13
- 229930195733 hydrocarbon Natural products 0.000 claims description 11
- 150000002430 hydrocarbons Chemical class 0.000 claims description 11
- 238000000280 densification Methods 0.000 claims description 9
- 238000004519 manufacturing process Methods 0.000 claims description 9
- NMJORVOYSJLJGU-UHFFFAOYSA-N methane clathrate Chemical compound C.C.C.C.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O NMJORVOYSJLJGU-UHFFFAOYSA-N 0.000 claims description 8
- 239000000654 additive Substances 0.000 claims description 6
- 239000004215 Carbon black (E152) Substances 0.000 claims description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 4
- 238000005054 agglomeration Methods 0.000 claims description 4
- 230000002776 aggregation Effects 0.000 claims description 4
- 239000003381 stabilizer Substances 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 claims description 2
- 238000003825 pressing Methods 0.000 claims description 2
- 239000000377 silicon dioxide Substances 0.000 claims description 2
- 239000010410 layer Substances 0.000 claims 2
- 239000004615 ingredient Substances 0.000 claims 1
- 239000011241 protective layer Substances 0.000 claims 1
- 239000012779 reinforcing material Substances 0.000 claims 1
- 238000005507 spraying Methods 0.000 claims 1
- 239000007788 liquid Substances 0.000 description 11
- 239000013535 sea water Substances 0.000 description 5
- 230000015572 biosynthetic process Effects 0.000 description 4
- 238000007710 freezing Methods 0.000 description 4
- 230000008014 freezing Effects 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 239000002657 fibrous material Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000011248 coating agent Substances 0.000 description 2
- 238000000576 coating method Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000155 melt Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 241000251468 Actinopterygii Species 0.000 description 1
- 240000001546 Byrsonima crassifolia Species 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000003949 liquefied natural gas Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000009372 pisciculture Methods 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000002787 reinforcement Effects 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/108—Production of gas hydrates
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C11/00—Use of gas-solvents or gas-sorbents in vessels
- F17C11/007—Use of gas-solvents or gas-sorbents in vessels for hydrocarbon gases, such as methane or natural gas, propane, butane or mixtures thereof [LPG]
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
Oppfinnelsen gjelder en framgangsmåte som angitt i innledningen til patentkrav 1, for lagring av gassformete stoffer, særlig naturgass, samt apparat til utførelse av samme. The invention relates to a method as stated in the introduction to patent claim 1, for the storage of gaseous substances, in particular natural gas, as well as an apparatus for performing the same.
Bakgrunn Background
I tilfeller hvor det mangler rørledning for transport av gass, enten naturgass eller gass blandet med andre hydrokarboner, er det vanskelig å gjennomføre en rasjonell utnyttelse. Gassen kan ikke forbrennes kontinuerlig, den kan heller ikke utnyttes på stedet, f.eks. på en offshore plattform og kan heller ikke føres til brukeren gjennom en rørledning. In cases where there is no pipeline for the transport of gas, either natural gas or gas mixed with other hydrocarbons, it is difficult to carry out a rational utilization. The gas cannot be burned continuously, nor can it be utilized on site, e.g. on an offshore platform and cannot be brought to the user through a pipeline either.
En mulighet i slike tilfeller er å reinjisere gassen i reservoaret, i håp om å fremme oljeutvinningen. Utviklingen av enkelte isolerte gassfelt, f.eks. offshore, er økonomisk umulig, uten at det kan skje en utnyttelse på stedet eller en transport gjennom rørledning. One option in such cases is to re-inject the gas into the reservoir, in the hope of promoting oil recovery. The development of some isolated gas fields, e.g. offshore, is economically impossible, without an on-site utilization or transport via pipeline.
Det er også mulig å foreta en behandling på stedet, ved produksjon av flytende naturgass, metanol og ammoniakk. Disse tre muligheten krever imidlertid omfattende behandling av naturgassen og/eller et annet gassprodukt og krever utstyr som er omfattende og dessuten i en skala som ikke er egnet for offshore drift. It is also possible to carry out an on-site treatment, when producing liquefied natural gas, methanol and ammonia. However, these three options require extensive treatment of the natural gas and/or another gas product and require equipment that is extensive and, moreover, on a scale that is not suitable for offshore operation.
I noen tilfeller står en overfor gassutvikling, for eksempel som et forurensende biprodukt av industrielle prosesser, hvor en ønsker å fjerne gassen, men ikke kan foreta rensing eller destruksjon på stedet. In some cases, you are faced with gas development, for example as a polluting by-product of industrial processes, where you want to remove the gas, but cannot carry out purification or destruction on site.
Slike oppgaver har tidligere blitt forsøkt løst ved framstilling av gasshydrater. US patentskrift 3.888.434 beskriver transport av hydrater i vogner inne i et rørsystem. Rørsystemet kjøles og trykksettes for å holde hydratet over dets likevektslinje. Rørtrykket vil typisk ligge i området fra 40 til 60 bar og temperaturen fra -40°C eller høyere. Fra dette skriftet framgår det at hydratframstillingen finner sted ved at naturgass ved et trykk på 60-40 bar og en temperatur på 20-30 minusgrader inndeles i to strømmer, der den første strømmen blandes med finfordelt vann som tidligere har blitt avkjølt til +1 til 2°C, for på denne måten å danne hydrater. Hydratene underkjøles deretter av den andre naturgasstrømmen som i mellomtiden har blitt avkjølt til -45°C. Den andre gasstrømmen brukes dessuten som drivkraft for å transportere de hydratfylte vognene. Ved f.eks. -10°C kreves det ifølge dette US-skriftet et trykk på omlag 20 bar for å holde hydratet stabilt. Such tasks have previously been attempted to be solved by the production of gas hydrates. US patent 3,888,434 describes the transport of hydrates in wagons inside a pipe system. The piping system is cooled and pressurized to keep the hydrate above its equilibrium line. The pipe pressure will typically be in the range from 40 to 60 bar and the temperature from -40°C or higher. From this document it appears that the hydrate production takes place by dividing natural gas at a pressure of 60-40 bar and a temperature of 20-30 minus degrees into two streams, where the first stream is mixed with finely divided water that has previously been cooled to +1 to 2°C, to form hydrates in this way. The hydrates are then subcooled by the second natural gas stream which has meanwhile been cooled to -45°C. The second gas stream is also used as motive power to transport the hydrate-filled wagons. By e.g. -10°C, according to this US document, a pressure of around 20 bar is required to keep the hydrate stable.
NO patentskrift 149976 beskriver en framgangsmåte for transport av naturgass i et undervannsfartøy, hvorved naturgass føres sammen med avkjølt vann for dannelse av gasshydrater ved bestemt temperatur/trykk. Temperatur- og trykkbetingelsene i forbindelse med hydratdannelsen bestemmes av undervannsfartøyets dybdeposisjon og sjøvannets temperatur. Framstillingen skjer satsvis ved at gass finfordeles i en kontinuerlig vannfase nede i undervannsfartøyet. For å oppnå tilfredsstillende hydratdannelse må vann være tilstede i overskudd. Reaksjonsvarmen blir dessuten fjernet ved direkte vanninnsprøytning i sonen der hydratet dannes. Dette vil imidlertid resultere i mye dødvekt i form av vann, og gasstransport i henhold til dette skriftet er naturligvis begrenset til havområdene med de ulemper som en slik transportmåte medfører, slik som spesialbygde fartøyer og krav til dybdeforhold ved laste/lossested. NO patent 149976 describes a procedure for transporting natural gas in an underwater vessel, whereby natural gas is fed together with cooled water to form gas hydrates at a specific temperature/pressure. The temperature and pressure conditions in connection with hydrate formation are determined by the underwater vessel's depth position and the temperature of the seawater. The production takes place in batches by finely distributing gas in a continuous water phase down in the underwater vessel. To achieve satisfactory hydrate formation, water must be present in excess. The heat of reaction is also removed by direct water injection into the zone where the hydrate is formed. However, this will result in a lot of dead weight in the form of water, and gas transport according to this document is naturally limited to the sea areas with the disadvantages that such a method of transport entails, such as specially built vessels and requirements for depth conditions at the loading/unloading point.
Formål Purpose
Oppfinnelsens hovedformål er å komme fram til en framgangsmåte for behandling av gassformete stoffer, slik som naturgass eller naturgass blandet med eller innesluttet i andre hydrokarboner eller vann, eller forurensningsgass eller gass som skal tilføres en industriell eller bioteknisk prosess, som gjør det mulig å foreta en økonomisk tilfredsstillende lagring, transport og utnyttelse av gassen uten bruk av rørledning eller umiddelbar transport med tankfartøy eller tankkjøretøy. Framgangsmåten må dessuten være miljømessig tilfredsstillende og kunne gjennomføres med en akseptabel risiko sikkerhetsmessig og økonomisk. The main purpose of the invention is to come up with a method for treating gaseous substances, such as natural gas or natural gas mixed with or contained in other hydrocarbons or water, or pollution gas or gas to be supplied to an industrial or biotechnical process, which makes it possible to carry out a economically satisfactory storage, transport and utilization of the gas without the use of a pipeline or immediate transport by tanker or tank vehicle. The procedure must also be environmentally satisfactory and can be carried out with an acceptable risk in terms of safety and economics.
Prinsipp Principle
Disse formål oppnås med en framgangsmåte og et apparat som angitt i den karakteriserende del av henholdsvis patentkrav 1 og 7. Ytterligere fordelaktige trekk framgår av de uselvstendige kravene. These objects are achieved with a method and an apparatus as stated in the characterizing part of patent claims 1 and 7, respectively. Further advantageous features appear from the independent claims.
Nærmere omtale av oppfinnelsen og eksempler. Detailed description of the invention and examples.
Naturgass og naturgass i blanding med andre hydrokarboner blir på utvinningsstedet fraskilt olje og vann. Den rensete gassen føres gjennom en kompressor og kjøles i en varmeveksler som kan være kjølt med luft eller sjøvann. Den kondenserte gassen som dannes ved denne kompresjonen og kjølingen blir fraskilt i en separator, temperaturen og trykket blir innstilt slik at bestemte hydrokarboner utvinnes. Disse utskilte bestanddelene i væskeform kan brukes for forbrenningsprosesser og drift av plattformer. Den fraskilte, nedkjølte gassen komprimeres og føres gjennom en varmeveksler og kjøles, f.eks. med luft eller sjøvann. Kjølingen med sjøvann kan f.eks. skje i ei sløyfe, for å utnytte siffong-virkningen. Natural gas and natural gas mixed with other hydrocarbons are separated from oil and water at the extraction site. The purified gas is passed through a compressor and cooled in a heat exchanger which can be cooled with air or seawater. The condensed gas formed by this compression and cooling is separated in a separator, the temperature and pressure are adjusted so that specific hydrocarbons are extracted. These separated components in liquid form can be used for combustion processes and operation of platforms. The separated, cooled gas is compressed and passed through a heat exchanger and cooled, e.g. with air or seawater. The cooling with seawater can e.g. spoon in a loop, to take advantage of the siphon effect.
Den komprimerte og avkjølte gassen føres i henhold til oppfinnelsen til en reaktorbeholder hvor den føres sammen med trykksatt vann, f.eks. til 100-200 bar, for dannelse av hydratpartikler med innesluttet gass. Dette trykksatte vannet tilføres reaktorbeholderen gjennom dyser eller liknende og ekspanderes til et lavere trykk og til en temperatur som resulterer i frysing av vannet med hydratdannelse. For eksempel vil vannets frysepunkt avta med økende trykk med omtrent 0.0074 °K/bar. Utformingen og driftsvilkårene, særlig trykket, velges slik at kjølingen på de inngående strømmene blir størst mulig. Trykket i gassen som slippes inn i reaktorbeholderen innstilles slik at det oppnås kjøling ved ekspansjon. De resulterende hydratpartiklene bestående av is med innesluttet gass blir deretter ført ut av reaktorbeholderen, f.eks. ved hjelp av en mekanisk transportanordning eller ved hjelp av reaktorbeholderens overtrykk, til en hensiktsmessig anordning for agglomerering av partiklene, f.eks. ei presse. According to the invention, the compressed and cooled gas is fed to a reactor container where it is fed together with pressurized water, e.g. to 100-200 bar, for the formation of hydrate particles with trapped gas. This pressurized water is supplied to the reactor vessel through nozzles or the like and is expanded to a lower pressure and to a temperature which results in freezing of the water with hydrate formation. For example, the freezing point of water will decrease with increasing pressure by approximately 0.0074 °K/bar. The design and operating conditions, especially the pressure, are chosen so that the cooling of the incoming streams is as great as possible. The pressure in the gas that is admitted into the reactor vessel is set so that cooling is achieved by expansion. The resulting hydrate particles consisting of ice with trapped gas are then passed out of the reactor vessel, e.g. by means of a mechanical transport device or by means of the overpressure of the reactor vessel, to a suitable device for agglomeration of the particles, e.g. a press.
Forut for dette kan vannet som brukes avluftes for å fjerne oksygen og andre gasser. Vannet kan behandles med tilsetningsstoffer og/eller stabiliseringsmidler. Tilsetnings-og stabiliseringsmidlene bidrar til å øke lagrings- og transportevnen til hydratpartiklene med innesluttet gass. Disse midlene kan eventuelt tilvirkes på stedet av hydrokarbon-fraksjoner som skilles ut av utgangsmaterialet, enten dette er naturgass eller naturgass sammen med andre hydrokarboner. Det kan også brukes andre tilsetningsstoffer, så som silica. Prior to this, the water used can be deaerated to remove oxygen and other gases. The water can be treated with additives and/or stabilizers. The additives and stabilizers help to increase the storage and transport capacity of the hydrate particles with trapped gas. These agents can optionally be produced on site from hydrocarbon fractions that are separated from the starting material, whether this is natural gas or natural gas together with other hydrocarbons. Other additives, such as silica, can also be used.
Reaktorbeholderen kan utformes slik at den blir kjølt med fremmede væsker. Den kan være forsynt med kjølesløyfer. Massen og energibalansen til strømmen som slippes inn i reaktorbeholderen innstilles slik at storparten av vannet omdannes til hydratpartikler, slik at prosessen drives med overskudd av gass. Reaktorbeholderen kan også drives med overskudd av vann, slik at flytende vann må skilles fra. Prosessen kan også ha overskudd av både gass og flytende vann. Partiklene av hydrat med innesluttet gass transporteres ut av reaktorbeholderen og eventuell ureagert gass og flytende vann tømmes. Gassen og det flytende vannet skilles altså fra ispartiklene med innesluttet gass. The reactor vessel can be designed so that it is cooled with foreign liquids. It can be equipped with cooling loops. The mass and energy balance of the flow that is admitted into the reactor vessel is adjusted so that the majority of the water is converted into hydrate particles, so that the process is run with an excess of gas. The reactor vessel can also be operated with an excess of water, so that liquid water must be separated. The process can also have an excess of both gas and liquid water. The particles of hydrate with trapped gas are transported out of the reactor vessel and any unreacted gas and liquid water are emptied. The gas and liquid water are thus separated from the ice particles with trapped gas.
Mindre mengder gass og eventuelt flytende vann kan følge med hydratpartiklene. De ureagerte bestanddelene av gass og flytende vann kan resirkuleres, idet vannet blir trykksatt og gassen komprimert på ny. De resirkulerte strømmene kan kjøles og også behandles med tilsetningsstoffer og behandles videre med tanke på tilvirkning av hydratpartikler. Ureagert gass fra reaktoren kan eventuelt komprimeres og tilføres et annet tilsvarende system som drives med høyere trykk. Smaller amounts of gas and possibly liquid water may accompany the hydrate particles. The unreacted components of gas and liquid water can be recycled, the water being pressurized and the gas compressed again. The recycled streams can be cooled and also treated with additives and further processed with a view to the production of hydrate particles. Unreacted gas from the reactor can possibly be compressed and supplied to another similar system which is operated at higher pressure.
Hydratpartiklene med innesluttet gass transporteres så til utstyr som agglomererer eller samler de små partiklene til større partikler. De første hydratpartiklene nedkjøles og/eller nedfryses før de føres inn i dette fortetningstrinnet. Kjøling og frysing kan gjennomføres ved trykkforandring, direkte tilsetning av kjølt/frossen gass og/eller indirekte varmeveksling. Formålet med fortetningen er å agglomerere materialet slik at dets volum blir redusert og samtidig gi plass for gasslagring i partiklenes porevolum. Fortetningen eller "agglomerasjonen" kan finne sted ved trykk- og The hydrate particles with trapped gas are then transported to equipment that agglomerates or collects the small particles into larger particles. The first hydrate particles are cooled and/or frozen before being fed into this densification step. Cooling and freezing can be carried out by pressure change, direct addition of chilled/frozen gas and/or indirect heat exchange. The purpose of densification is to agglomerate the material so that its volume is reduced and at the same time provide space for gas storage in the pore volume of the particles. The densification or "agglomeration" can take place by pressure and
temperaturbetingelser som velges slik at det oppnås optimalt temperature conditions that are chosen so that it is optimally achieved
gassinnhold og partikkelstabilitet. Tilsetningsstoffer kan blandes inn i hydratpartiklene for å forbedre deres egenskaper. Avhengig av de prosessvilkår som velges, vil den totale masseprosenten av gass generelt ligge i området 10-40% av partikkelvekten. Etter fortetningen kan hydratpartiklene kjøles og/eller fryses. Dette tjener til å holde fast den totale gassen i hver partikkel. gas content and particle stability. Additives can be mixed into the hydrate particles to improve their properties. Depending on the process conditions chosen, the total mass percentage of gas will generally be in the range of 10-40% of the particle weight. After densification, the hydrate particles can be cooled and/or frozen. This serves to retain the total gas in each particle.
Dersom det ønskes kan de fortettete hydratpartiklene transporteres til utstyr som dekker de gassimpregnerte partiklene med et rent issjikt. Isbelegget på partiklene bidrar ytterligere til å inneslutte gassen i partiklene, slik at de kan tåle høyere indre og ytre trykk. Fibermaterialer, naturlige eller syntetiske, kan innesluttes i isbelegget, for å gjøre det sterkere. Styrken på isen øker med senkning av temperaturen og med bruken av fiberforsterkning. Fibermaterialet kan også innføres ved den første partikkelproduksjonen, ved tilsetning til det trykksatte og avkjølte vannet eller på annen måte. Fibermaterialet kan også tilsettes i fortetningstrinnet når det tilvirkes større ispartikler fra de minste gassfylte ispartiklene. If desired, the condensed hydrate particles can be transported to equipment that covers the gas-impregnated particles with a clean layer of ice. The ice coating on the particles further helps to contain the gas in the particles, so that they can withstand higher internal and external pressures. Fiber materials, natural or synthetic, can be embedded in the ice coating to make it stronger. The strength of the ice increases with lowering the temperature and with the use of fiber reinforcement. The fiber material can also be introduced during the first particle production, by addition to the pressurized and cooled water or in another way. The fiber material can also be added in the densification step when larger ice particles are produced from the smallest gas-filled ice particles.
Slike gassholdige hydratpartikler kan tilvirkes på offshore plattformer eller på land. Plattformene kan være midlertidige eller permanente. På land kan de gassholdige hydratpartiklene tilvirkes nær hydrokarbon-kilder eller andre plasser. Gassen som tilføres på denne måten kan være naturgass eller naturgass sammen med andre bestanddeler. Det kan også være en forurensningsgass som skal transporteres bort for videre behandling eller gass for bruk ved fiskeoppdrett. I det siste tilfellet kan hydratpartikelne tilføres til vannet hvor oppdrettsfisken befinner seg. Such gaseous hydrate particles can be produced on offshore platforms or on land. The platforms can be temporary or permanent. On land, the gaseous hydrate particles can be produced near hydrocarbon sources or other locations. The gas supplied in this way can be natural gas or natural gas together with other components. It can also be a pollutant gas that must be transported away for further treatment or gas for use in fish farming. In the latter case, the hydrate particles can be added to the water where the farmed fish are located.
De gassholdige hydratpartiklene kan brukes for lagring og transport av gasser. De kan også brukes for drift av transportmidler på land og sjø. Andre gasser kan også brukes for å tilvirke gassholdige hydratpartikler. Disse andre gassene kan være kommersielle produkter eller forurensninger eller andre type gasser som oppstår ved naturlige eller industrielle prosesser. Gassholdige hydratpartikler kan brukes i kraftverk og i prosesser som er beregnet for å redusere forurensning. Gassholdige hydratpartikler kan brukes der hvor gasser må tilsettes i styrte mengder, i akvatiske omgivelser, både naturlige og konstruerte. The gaseous hydrate particles can be used for the storage and transport of gases. They can also be used for the operation of means of transport on land and sea. Other gases can also be used to produce gaseous hydrate particles. These other gases can be commercial products or pollutants or other types of gases that arise from natural or industrial processes. Gas hydrate particles can be used in power plants and in processes designed to reduce pollution. Gas-containing hydrate particles can be used where gases must be added in controlled quantities, in aquatic environments, both natural and engineered.
På offshore plattformer kan gasspartiklene lagres i undersjøiske tanker under trykk. Disse tankene kan plasseres på havbunnen under eller nær plattformen. De kan trykksettes hydrostatisk med ei vannsøyle gjennom et ventilarrangement med manometer, slik at ei væskesøyle skiller tanken fra sjøvann. De gassholdige partiklene kan lagres i form av faste stoffer i gass eller omgis med avkjølt vann eller en hydrokarbon-basert væske. I tillegg til undersjøiske tanker, kan det brukes tankskip, lektere o.l., eller nedsenkete beholdere tilvirket av stivt eller fleksibelt materiale. On offshore platforms, the gas particles can be stored in pressurized underwater tanks. These tanks can be placed on the seabed below or near the platform. They can be pressurized hydrostatically with a column of water through a valve arrangement with manometers, so that a liquid column separates the tank from seawater. The gaseous particles can be stored as solids in gas or surrounded by cooled water or a hydrocarbon-based liquid. In addition to submarine tanks, tankers, barges etc., or submerged containers made of rigid or flexible material can be used.
Hydratpartikler med innesluttet gass kan transporteres fra offshore-lagertanker med båter, tankskip, lektere eller flytende containere som taues med slepebåter til lands. Mest aktuelt er det å pumpe hydratpartiklene fra lagertankene offshore gjennom en rørledning til en tankbåt. Tankbåten kan, men trenger ikke nødvendigvis være i stand til å lagre partiklene under overtrykk. Partiklene kan transporteres som fast gods eller i vann eller i en hydrokarbon-basert væske til lands. Gass som unnslipper fra partiklene under transporten kan trykksettes og/eller brukes for å drive tankbåten og kjøleutstyret. Hydrate particles with trapped gas can be transported from offshore storage tanks by boats, tankers, barges or floating containers that are towed ashore by tugboats. The most relevant is to pump the hydrate particles from the storage tanks offshore through a pipeline to a tanker. The tanker may, but does not necessarily have to be able to store the particles under overpressure. The particles can be transported as solid goods or in water or in a hydrocarbon-based liquid on land. Gas that escapes from the particles during transport can be pressurized and/or used to power the tanker and the refrigeration equipment.
Hydratpartiklene med innesluttet gass blir etter transporten pumpet eller overført på annen måte fra tankbåten til en eller flere lagertanker på land. Partiklene får da smelte og gassen kan unnslippe. Smeltingen kan gjennomføres med mange typer oppvarming, f.eks. med utslipp fra et gassdrevet kraftverk. Kaldt smeltevann kan brukes som kjølemedium for ethvert kraftverk, slik at de vanlige kjøletårnene ikke trenges. After transport, the hydrate particles with trapped gas are pumped or transferred in another way from the tanker to one or more storage tanks on land. The particles are then allowed to melt and the gas can escape. The melting can be carried out with many types of heating, e.g. with emissions from a gas-fired power plant. Cold meltwater can be used as a cooling medium for any power plant, so that the usual cooling towers are not needed.
Når tankbåten tømmes for partiklene, kan den ta inn smeltevann og prosessvann. Vannet kan komme fra en tidligere last. Smeltevannet vil være ballast for tankeren fra land til en offshore plattform. Når tankeren laster partiklene ved plattformen, losser den smeltevannet. Tankene på plattformen tar imot smeltevannet for bruk ved hydratproduksjonen. Smeltevannet og prosessvannet kan, men trenger nødvendigvis utluftes og forbehandles. Utluftingen kan finne sted både på land og/eller offshore. I tillegg kan vannet brukes for innsprøyting i et reservoar. When the tanker is emptied of the particles, it can take in melt water and process water. The water may come from a previous load. The melt water will be ballast for the tanker from land to an offshore platform. When the tanker loads the particles at the platform, it discharges the meltwater. The tanks on the platform receive the meltwater for use in hydrate production. The melt water and process water can, but must necessarily be vented and pre-treated. The venting can take place both on land and/or offshore. In addition, the water can be used for injection into a reservoir.
I figuren er oppfinnelsen illustrert, idet denne viser et forenklet flytskjema som illustrerer et eksempel på en framgangsmåte i samsvar med oppfinnelsen. In the figure, the invention is illustrated, as this shows a simplified flow chart illustrating an example of a procedure in accordance with the invention.
Naturgass, som på forhånd er fraskilt olje og vann og komprimert, blir i et første trinn fraseparert kondenserte gasser (3) i en separator (2). Den resterende gassen komprimeres deretter i en kompressor (4), kjøles i en varmeveksler (5) og ekspanderes inn i en reaktor (6) gjennom dyser (10) eller tilsvarende, hvor den føres sammen med trykksatt vann (7) tilført reaktoren gjennom dyser (9) eller tilsvarende, for dannelse av gasshydrat (8A). Reaktoren (6) kan være forsynt med kjølesløyfer (6A) eller tilsvarende. Det resulterende gasshydratet (8A) føres deretter ut av reaktoren (6) og frasepareres eventuell ureagert gass (1C), som komprimeres, kjøles og resirkuleres tilbake til reaktoren (6). Eventuelt ureagert vann (7A) kan også skilles fra de dannete gasshydratene (8A) og ledes tilbake til reaktoren (6) sammen med det friske vannet (7). Natural gas, which has previously been separated from oil and water and compressed, is separated from condensed gases (3) in a separator (2) in a first step. The remaining gas is then compressed in a compressor (4), cooled in a heat exchanger (5) and expanded into a reactor (6) through nozzles (10) or equivalent, where it is fed together with pressurized water (7) supplied to the reactor through nozzles (9) or equivalent, to form gas hydrate (8A). The reactor (6) can be provided with cooling loops (6A) or equivalent. The resulting gas hydrate (8A) is then led out of the reactor (6) and any unreacted gas (1C) is separated, which is compressed, cooled and recycled back to the reactor (6). Any unreacted water (7A) can also be separated from the formed gas hydrates (8A) and led back to the reactor (6) together with the fresh water (7).
Hydratet (8A) kan deretter eventuelt kjøles i et kjøletrinn (11) og agglomereres i et fortetningstrinn (12) ved pressing med etterfølgende kjøling i et avsluttende kjøletrinn (17). Om ønskelig kan de fortettete hydratpartiklene (8B) transporteres til utstyr (13) som dekker disse med et rent issjikt, eventuelt armert med fibre eller tilsvarende, og deretter kjøles i det avsluttende kjøletrinnet (17). Hydratpartiklene (8D) ledes deretter til den aktuelle lager- eller transportanordning. The hydrate (8A) can then optionally be cooled in a cooling step (11) and agglomerated in a densification step (12) by pressing with subsequent cooling in a final cooling step (17). If desired, the condensed hydrate particles (8B) can be transported to equipment (13) which covers them with a clean layer of ice, optionally reinforced with fibers or similar, and then cooled in the final cooling step (17). The hydrate particles (8D) are then directed to the relevant storage or transport device.
De kjølte og frossete hydratpartiklene føres videre til lagertanker f.eks. ved hjelp av komprimert og avkjølt gass. Partiklene blir (som for vanlig is) lagret ved nær adiabatiske betingelser for å sikre deres stabilitet ved nær atmosfæriske trykk og frysetemperaturer. Hydratpartiklene kan deretter transporteres med f.eks. tankbiler eller tankbåter, helst med kjøleanlegg, eller lagres på annen måte. Når gassen etter lagring eller transport igjen skal håndteres i gassform, blir hydratpartiklene smeltet på passende måte, avhengig av hvordan gassen og smeltevannet skal anvendes. The cooled and frozen hydrate particles are carried on to storage tanks, e.g. using compressed and cooled gas. The particles are (as for regular ice) stored under near-adiabatic conditions to ensure their stability at near-atmospheric pressures and freezing temperatures. The hydrate particles can then be transported with e.g. tankers or tankers, preferably with refrigeration, or stored in another way. When, after storage or transport, the gas is to be handled again in gaseous form, the hydrate particles are melted in a suitable way, depending on how the gas and melt water are to be used.
Claims (7)
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
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NO90900395A NO172080C (en) | 1990-01-29 | 1990-01-29 | PROCEDURE FOR THE PREPARATION OF GAS HYDRATES AND APPLIANCES FOR PERFORMING THE SAME |
PCT/NO1991/000101 WO1993001153A1 (en) | 1990-01-29 | 1991-07-08 | Method for production of gas hydrates for transportation and storage |
CA002113071A CA2113071C (en) | 1990-01-29 | 1991-07-08 | Method for production of gas hydrates for transportation and storage |
EP91911763A EP0594616B1 (en) | 1990-01-29 | 1991-07-08 | Method for production of gas hydrates for transportation and storage |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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NO90900395A NO172080C (en) | 1990-01-29 | 1990-01-29 | PROCEDURE FOR THE PREPARATION OF GAS HYDRATES AND APPLIANCES FOR PERFORMING THE SAME |
CA002113071A CA2113071C (en) | 1990-01-29 | 1991-07-08 | Method for production of gas hydrates for transportation and storage |
Publications (4)
Publication Number | Publication Date |
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NO900395D0 NO900395D0 (en) | 1990-01-29 |
NO900395L NO900395L (en) | 1991-07-30 |
NO172080B true NO172080B (en) | 1993-02-22 |
NO172080C NO172080C (en) | 1993-06-02 |
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NO90900395A NO172080C (en) | 1990-01-29 | 1990-01-29 | PROCEDURE FOR THE PREPARATION OF GAS HYDRATES AND APPLIANCES FOR PERFORMING THE SAME |
Country Status (4)
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EP (1) | EP0594616B1 (en) |
CA (1) | CA2113071C (en) |
NO (1) | NO172080C (en) |
WO (1) | WO1993001153A1 (en) |
Cited By (1)
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WO1994000713A1 (en) * | 1992-06-29 | 1994-01-06 | Den Norske Stats Oljeselskap A.S | Method and plant for converting gas into hydrate |
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NO300936B1 (en) * | 1995-04-28 | 1997-08-18 | Norske Stats Oljeselskap | Process and plant for the manufacture of a hydrocarbon saturated product, as well as a product |
NO952241D0 (en) * | 1995-06-07 | 1995-06-07 | Jon Steinar Gudmundsson | Procedure for transport and storage of oil and gas |
GB9601030D0 (en) * | 1996-01-18 | 1996-03-20 | British Gas Plc | a method of producing gas hydrate |
NO304483B1 (en) * | 1996-04-25 | 1998-12-28 | Norske Stats Oljeselskap | Process for Capturing Low Molecular Volatile Compounds from Hydrocarbon Containing Liquids |
NO304564B1 (en) * | 1996-10-22 | 1999-01-11 | Norske Stats Oljeselskap | Procedure for treating a non-stabilized crude oil |
NO311381B1 (en) * | 1996-10-25 | 2001-11-19 | Norske Stats Oljeselskap | Process and apparatus for the manufacture, storage and regassification of a hydrocarbon product, the product manufactured and its use |
US6028234A (en) * | 1996-12-17 | 2000-02-22 | Mobil Oil Corporation | Process for making gas hydrates |
US6028235A (en) * | 1997-10-14 | 2000-02-22 | Mobil Oil Corporation | Gas hydrate regassification method and apparatus using steam or other heated gas or liquid |
US6180843B1 (en) | 1997-10-14 | 2001-01-30 | Mobil Oil Corporation | Method for producing gas hydrates utilizing a fluidized bed |
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US6082118A (en) * | 1998-07-07 | 2000-07-04 | Mobil Oil Corporation | Storage and transport of gas hydrates as a slurry suspenion under metastable conditions |
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GB9906731D0 (en) * | 1999-03-24 | 1999-05-19 | British Gas Plc | Formation,processing,transportation and storage of hydrates |
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AUPQ118899A0 (en) * | 1999-06-24 | 1999-07-22 | Woodside Energy Limited | Natural gas hydrate and method for producing same |
AUPQ228399A0 (en) * | 1999-08-17 | 1999-09-09 | Woodside Energy Limited | Production plant |
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RU2457010C1 (en) * | 2010-11-17 | 2012-07-27 | Учреждение Российской Академии наук Институт теплофизики Уральского отделения РАН | Method of obtaining gas hydrates |
RU2714468C1 (en) * | 2019-05-13 | 2020-02-17 | Федеральное государственное бюджетное учреждение науки Федеральный исследовательский центр "Якутский научный центр Сибирского отделения Российской академии наук" | Method of producing hydrates from natural gas and ice |
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-
1991
- 1991-07-08 WO PCT/NO1991/000101 patent/WO1993001153A1/en active IP Right Grant
- 1991-07-08 CA CA002113071A patent/CA2113071C/en not_active Expired - Fee Related
- 1991-07-08 EP EP91911763A patent/EP0594616B1/en not_active Expired - Lifetime
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Publication number | Priority date | Publication date | Assignee | Title |
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WO1994000713A1 (en) * | 1992-06-29 | 1994-01-06 | Den Norske Stats Oljeselskap A.S | Method and plant for converting gas into hydrate |
Also Published As
Publication number | Publication date |
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NO172080C (en) | 1993-06-02 |
CA2113071C (en) | 2001-09-11 |
CA2113071A1 (en) | 1993-01-09 |
NO900395D0 (en) | 1990-01-29 |
EP0594616A1 (en) | 1994-05-04 |
EP0594616B1 (en) | 1999-06-02 |
NO900395L (en) | 1991-07-30 |
WO1993001153A1 (en) | 1993-01-21 |
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