EP0476449A2 - Procédé et dispositif pour le séchage du gaz naturel et pour le recyclage du solvant de l'eau utilisé en cela - Google Patents

Procédé et dispositif pour le séchage du gaz naturel et pour le recyclage du solvant de l'eau utilisé en cela Download PDF

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Publication number
EP0476449A2
EP0476449A2 EP91115048A EP91115048A EP0476449A2 EP 0476449 A2 EP0476449 A2 EP 0476449A2 EP 91115048 A EP91115048 A EP 91115048A EP 91115048 A EP91115048 A EP 91115048A EP 0476449 A2 EP0476449 A2 EP 0476449A2
Authority
EP
European Patent Office
Prior art keywords
water solvent
natural gas
boiling chamber
boiler
heat
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP91115048A
Other languages
German (de)
English (en)
Other versions
EP0476449A3 (en
EP0476449B1 (fr
Inventor
Paul-Rene Duerloo
Rolf Dipl.-Ing. Remer
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Remer Rolf En Duerloo Paul
Original Assignee
BEB Erdgas und Erdol GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by BEB Erdgas und Erdol GmbH filed Critical BEB Erdgas und Erdol GmbH
Publication of EP0476449A2 publication Critical patent/EP0476449A2/fr
Publication of EP0476449A3 publication Critical patent/EP0476449A3/de
Application granted granted Critical
Publication of EP0476449B1 publication Critical patent/EP0476449B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • 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

Definitions

  • the invention relates to a method for drying natural gas and for reprocessing the water solvent used therefor, in which the natural gas is heated as required and passed through a contact device and in which the water solvent is reprocessed in a distillation device, and a device for drying natural gas and for the reprocessing of the water solvent used for this purpose, consisting of a plant part in which natural gas is brought into contact with water solvent as an absorbent in an absorber or as a hydrate inhibitor in a refrigeration drying system and a distillation device comprising heating devices, heat exchangers and pipelines provided with a boiling chamber and distillation column.
  • the regeneration of the water solvent on natural gas drying systems is carried out by relaxing the solvent and subsequent distillation at a slight excess pressure or at atmospheric pressure or even under vacuum.
  • the method of distillation is based on different dynamic equilibria between the vapor and liquid of a multi-component system, equilibria that result from the height of the distillation column as a function of temperature and temperature gradients.
  • the necessary energy is usually introduced partly by adding external heat, often in the lower area of the column or the distillation system.
  • the regeneration often has a solvent stripping system with low-water gas as the stripping medium.
  • a gas heater is usually part of the gas drying system. If necessary, this heater heats the natural gas to a temperature at the borehole head flow pressure which, when the wet gas subsequently expands to the pressure level of the drying process, precludes hydrate formation conditions.
  • the hydrate suppression can also be achieved in whole or in part by dosing suitable substances into the gas stream.
  • the reprocessing of these substances may be possible during regeneration.
  • the natural gas heater using the standard process uses electrical resistance heaters or firing systems with flame and smoke pipes as an external heat source under conditions of singular operation. According to the construction of these devices, the heat energy is transferred from the heat source via a heat transfer medium to the heat consumer.
  • a pressurized liquid which is only exposed to free convection and which surrounds the heat exchanger coils through which natural gas flows, serves as the heat carrier.
  • the regeneration is carried out in a separate plant.
  • the systems using the standard process also use electrical resistance heaters or firing systems with flame and smoke pipes as external heat sources to generate the necessary process heat, in individual cases there is also heating via heat exchangers with an intermediate heat transfer medium, but in all cases the heat is transferred to the regenerated one Water solvent via a heat exchanger, which is a structurally integrated part of the distillation vessel or is directly assigned to the distillation column as part of a boiling chamber according to the thermosiphon principle. This heat transfer takes place on the side of the water solvent according to the laws of "free convection".
  • the water solvent After regeneration by distillation and possibly also stripping, the water solvent enters a collector, which also serves as a template for the circulation pump.
  • the cooling of the water solvent required in terms of process technology is brought about by heat exchange in apparatuses which are either designed as part of the collector without forced circulation on the side of the medium to be cooled or in apparatuses with forced circulation on the side of the cooling medium using an additional back pressure pump for the regenerated water solvent .
  • the collector / cooler concept mentioned requires additional heating of the loaded water solvent - usually additional exchanger coil in the boiling chamber - so that the solvent can be introduced into the distillation column without adverse effects on the process.
  • the invention avoids the disadvantages of the prior art. It is the object of the invention to be a simple one Possibility to find un drying the natural gas with less equipment and using less energy under better defined and manageable process parameters and with largely improved environmental technology.
  • the invention consists in that the process for temperature control of the natural gas necessary for the drying process is coupled with the process for the reprocessing of the water solvent, the water solvent being used as the heat carrier for the heating of the natural gas.
  • the new method is able to record both the regeneration function and the natural gas heating function in a simple and uniform manner.
  • the heat required for regeneration is covered by a heat transfer medium that is also used to heat the natural gas.
  • the water solvent serves as the heat transfer medium, which is pumped around in two interlocking circuits to fulfill the different tasks.
  • this concept leads to a system with a central heat generator and several consumers.
  • the water solvent is conducted in two interlocking circuits, one from the boiler into the boiling chamber of the distillation device and from this via a natural gas / water solvent heat exchanger back to the boiler and a second circuit leading from the boiling chamber over the drying section of the plant into the distillation apparatus, in which heat of the water solvent coming from the boiling chamber is transferred into the water solvent entering the distillation column.
  • the heat supply in the boiling chamber of the regeneration if one disregards the heat supply through the boiler, does not take place via heat exchangers, but through direct injection of the heat transfer medium.
  • the energy state of the injected water solvent is to be selected so that the boiling temperature assigned in the process is generated and maintained in the boiling chamber.
  • An optimal process flow is guaranteed if the injection of the heat transfer medium ensures the constant boiling temperature in the boiling chamber. Since the process engineering conditions only allow a limited temperature difference between the boiling chamber and the circulating heat transfer medium, a possible delay in boiling, which could result from the mixture, is undesirable.
  • hydrocarbons drawn off from the drying plant part are drawn off at an intermediate pressure stage, utilizing the stripping gas which occurs, before entering the distillation column.
  • the device according to the invention is characterized in that two interlocking pipe circuits are provided for the water solvent, namely a pipe circuit which leads from a boiler into the boiling chamber and from there via a water solvent / raw gas heat exchanger back to the boiler and in which a circulation pump is arranged , and another pipeline circuit, which leads from the boiling chamber via the natural gas drying section to a condenser in the distillation column, then into a heat exchanger and then into the distillation column via the boiling chamber and in which a circulation pump is also arranged, the pipeline branch being arranged in front of the through the heat exchanger Route the natural gas drying section and the pipe branch behind the natural gas drying section.
  • the natural gas drying part essentially consists of either an absorber or a refrigeration section with one or different separators, gas / gas heat exchangers, control valves and possibly also a third-party refrigeration section, in addition to a pre-treatment system with e.g. Pressure reduction, cooling and separation of the liquids carried with the gas or from auxiliary systems such as the measuring section, control air system, safety system etc.
  • a pre-treatment system e.g. Pressure reduction, cooling and separation of the liquids carried with the gas or from auxiliary systems such as the measuring section, control air system, safety system etc.
  • an expansion valve is arranged in front of the boiling chamber so that the water solvent is heated under pressure in the boiler and only begins to boil in the boiling chamber.
  • a stripper for the water solvent is arranged behind the boiling chamber, in which the water solvent is freed from residues of the water.
  • a hydrocarbon separator is arranged between the condenser and the heat exchanger, in which the water solvent entering the distillation column is freed from liquid hydrocarbons and in which the released final solution gas is collected in order to be able to use it as fuel gas.
  • a bypass line provided with a valve is provided parallel to the gas / water solvent heat exchanger.
  • this heat cycle is achieved in sequence with a separate heat generator, pressure reduction at the boiling chamber level, a distillation column as the heat consumer, a pump for circulating the heat transfer medium including pressure increase and possibly another consumer as a heater for the natural gas.
  • the water solvent / natural gas heat exchanger is connected downstream of the pump. Due to the forced circulation of the heat transfer medium and the much larger temperature differences between the two media compared to the standard natural gas heater, a jacket and tube heat exchanger construction with a relatively small area is possible. A bypass line with a three-way valve for the heat transfer medium ensures temperature control of the outgoing natural gas that is independent of the rest of the process.
  • the proportion of the water solvent that is not removed from the distillation column for heat transfer purposes is - as in the standard concept - after it has been subjected to further stripping, if necessary, in order to achieve the final purity required by the drying process is collected in a template.
  • the amount of stripping gas can be reduced compared to the known systems.
  • Other measures that are part of the new concept, with the aim of reducing the amount of residual gas in the regeneration system and thus possible emissions, are an automatic quantity control of the water solvent used for drying as a function of all relevant parameters, the automatic regulation of the strip gas quantity accordingly the water solvent circulation rate and a recycling of the dissolving gases which escape from the water solvent when it relaxes in the loaded state during the reprocessing.
  • the recycling of the flash gases is realized with a 3-phase separator that works at an operating pressure that enables the flash gases to be fed into the fuel gas rail.
  • the separation of possible liquid hydrocarbons, which are also removed from the drying process, is also promoted by the installation of appropriate fabric candles.
  • the water solvent e.g. a glycol
  • the water solvent is heated in the boiler 1 under pressure, fed to the boiling chamber 4 via a magnetic separator 2 and a heat exchanger 3 after it has been released in the throttle valve 5.
  • the water solvent takes two different routes: one route leads from the boiling chamber 4 via the pipeline 6, the circulation pump 7 into the gas / glycol heat exchanger 8 into which the material to be dried Natural gas enters via line 9 and exits via line 10, and from there back into the boiler 1.
  • a bypass line 11 and a valve 12 are provided for switching off and regulating this gas / glycol 8 heat exchanger from the circuit.
  • the other way for the water solvent leads from the boiling chamber 4 via the glycol stripper 13, to which the stripping gas is fed via line 14, into the collector 15, from there via line 16, the heat exchanger glycol / glycol 17 and the circulation pump 18 into the Natural gas drying section 19, where the water solvent or hydrate inhibitor glycol 19 is brought into connection with the natural gas emerging from the line 10, which may be subjected to further pretreatment such as pressure reduction, cooling and separation of liquids carried along.
  • the glycol in the circuit emerges from the natural gas drying section via line 20 and is fed via filter 21 to top condenser 22 in distillation column 23 and then continues via the glycol / hydrocarbon separator with glycol level control 24 through line 25 into the glycol / glycol Heat exchanger 17 and from there via line 26 to the nozzle 27 in the distillation column 23, where the glycol heated in the top condenser 22 and heated in the heat exchanger 17 enters heat into the distillation column 23.
  • Strip gas is fed to the heat exchanger 3 through the line 30, which then enters the glycol stripper 13 via the line 14.
  • the 31 is a temperature-controlled actuating device for the valve 12, which controls the valve 12 depending on the temperature of the escaping natural gas.
  • the actuating device 32 controls the valve 5 as a function of pressure or temperature in the line leading to the valve 5.
  • the method of the invention has considerable advantages: Instead of two fired boilers, one can now make do with one, which can also be a boiler, how it is manufactured industrially in large numbers and how, due to these large numbers, it also uses the best energy was developed.
  • This boiler can be located away from the natural gas heating system and away from the boiling chamber of the distillation column. You can work with this method much cheaper both in terms of equipment and energy.
  • both the water solvent for heating the natural gas and the water solvent for supplying heat to the boiling chamber of the distillation column are heated in one and the same boiler, preferably heating the heat transfer medium in one of the Boiling chamber and boiler located away from the natural gas heater.

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)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)
  • Drying Of Solid Materials (AREA)
EP91115048A 1990-09-19 1991-09-06 Procédé et dispositif pour le séchage du gaz naturel et pour le recyclage du solvant de l'eau utilisé en cela Expired - Lifetime EP0476449B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE4029660 1990-09-19
DE4029660A DE4029660C2 (de) 1990-09-19 1990-09-19 Verfahren und Vorrichtung für die Trocknung von Erdgas und für die Wiederaufbereitung des hierfür benutzten Wasserlösemittels

Publications (3)

Publication Number Publication Date
EP0476449A2 true EP0476449A2 (fr) 1992-03-25
EP0476449A3 EP0476449A3 (en) 1993-03-10
EP0476449B1 EP0476449B1 (fr) 1996-07-24

Family

ID=6414536

Family Applications (1)

Application Number Title Priority Date Filing Date
EP91115048A Expired - Lifetime EP0476449B1 (fr) 1990-09-19 1991-09-06 Procédé et dispositif pour le séchage du gaz naturel et pour le recyclage du solvant de l'eau utilisé en cela

Country Status (4)

Country Link
EP (1) EP0476449B1 (fr)
AT (1) ATE140633T1 (fr)
DE (2) DE4029660C2 (fr)
DK (1) DK0476449T3 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2129041C1 (ru) * 1994-10-24 1999-04-20 Текни Способ сушки газа
CN103239943A (zh) * 2013-05-14 2013-08-14 陈朝阳 一种含固体汽态物分离装置
CN104610032A (zh) * 2014-12-26 2015-05-13 浙江大学 一种丁辛醇尾气回收装置及其方法
CN105622319A (zh) * 2014-11-05 2016-06-01 杭州双安科技有限公司 一种丁辛醇尾气回收装置及方法

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19621908A1 (de) * 1996-05-31 1997-12-04 Filtan Gmbh Verfahren und Vorrichtung zur Trocknung von Gas, insbesondere Erdgas
DE19808291C2 (de) * 1998-02-27 2000-04-13 Dsd Gas Und Tankanlagenbau Gmb Verfahren und Anlage zum Beheizen von Regeneratoren bei der Trocknung von Erdgas
DE19830458C1 (de) * 1998-07-08 2000-03-16 Dsd Gas Und Tankanlagenbau Gmb Verfahren und Vorrichtung zum Trocknen von bei der Erdölförderung anfallenden Erdgasen
DE19963305A1 (de) * 1999-12-16 2001-07-05 Vng Verbundnetz Gas Ag Verfahren und Anlage zur Regenerierung von Trocknungsmitteln
RU2176053C1 (ru) * 2000-04-05 2001-11-20 Общество с ограниченной ответственностью "Кубаньгазпром" Способ подготовки магистрального газа на компрессорной станции
DE102010006892B4 (de) 2010-02-05 2013-07-11 Sven Kneifel Vorrichtung zur Erhitzung von Erdgas

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4635446A (en) * 1981-05-15 1987-01-13 Camp Dresser & Mckee Dehumidification apparatus
US4674446A (en) * 1986-04-18 1987-06-23 Padilla Sr Isaac F Gas dehydrator with gas recovery system

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2129041C1 (ru) * 1994-10-24 1999-04-20 Текни Способ сушки газа
CN103239943A (zh) * 2013-05-14 2013-08-14 陈朝阳 一种含固体汽态物分离装置
CN103239943B (zh) * 2013-05-14 2015-09-23 陈朝阳 一种含固体汽态物分离装置
CN105622319A (zh) * 2014-11-05 2016-06-01 杭州双安科技有限公司 一种丁辛醇尾气回收装置及方法
CN105622319B (zh) * 2014-11-05 2018-02-09 杭州双安科技有限公司 一种丁辛醇尾气回收装置及方法
CN104610032A (zh) * 2014-12-26 2015-05-13 浙江大学 一种丁辛醇尾气回收装置及其方法
CN104610032B (zh) * 2014-12-26 2016-09-14 浙江大学 一种丁辛醇尾气回收装置及其方法

Also Published As

Publication number Publication date
EP0476449A3 (en) 1993-03-10
EP0476449B1 (fr) 1996-07-24
DK0476449T3 (da) 1996-08-26
DE59108016D1 (de) 1996-08-29
ATE140633T1 (de) 1996-08-15
DE4029660C2 (de) 1994-08-11
DE4029660A1 (de) 1992-03-26

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