EP2914366A1 - Procédé et dispositif permettant d'éliminer sans apport d'énergie de refroidissement des gaz absorbables présents dans des gaz industriels sous pression contaminés par des gaz absorbables - Google Patents

Procédé et dispositif permettant d'éliminer sans apport d'énergie de refroidissement des gaz absorbables présents dans des gaz industriels sous pression contaminés par des gaz absorbables

Info

Publication number
EP2914366A1
EP2914366A1 EP13794803.0A EP13794803A EP2914366A1 EP 2914366 A1 EP2914366 A1 EP 2914366A1 EP 13794803 A EP13794803 A EP 13794803A EP 2914366 A1 EP2914366 A1 EP 2914366A1
Authority
EP
European Patent Office
Prior art keywords
gases
gas
industrial
absorbable
contaminated
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.)
Withdrawn
Application number
EP13794803.0A
Other languages
German (de)
English (en)
Inventor
Johannes Menzel
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.)
ThyssenKrupp Industrial Solutions AG
Original Assignee
ThyssenKrupp Industrial Solutions AG
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 ThyssenKrupp Industrial Solutions AG filed Critical ThyssenKrupp Industrial Solutions AG
Publication of EP2914366A1 publication Critical patent/EP2914366A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1468—Removing hydrogen sulfide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • 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
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • C10L3/103—Sulfur containing contaminants
    • 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
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • C10L3/104—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/202—Alcohols or their derivatives
    • B01D2252/2021—Methanol
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/202—Alcohols or their derivatives
    • B01D2252/2023—Glycols, diols or their derivatives
    • B01D2252/2026—Polyethylene glycol, ethers or esters thereof, e.g. Selexol
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B01D2252/20478—Alkanolamines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/304—Hydrogen sulfide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/65—Employing advanced heat integration, e.g. Pinch technology
    • 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
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/06—Heat exchange, direct or indirect
    • 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
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/12—Regeneration of a solvent, catalyst, adsorbent or any other component used to treat or prepare a fuel
    • 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
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/24—Mixing, stirring of fuel components
    • 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
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/46—Compressors or pumps
    • 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
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/48—Expanders, e.g. throttles or flash tanks
    • 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
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/541—Absorption of impurities during preparation or upgrading of a fuel

Definitions

  • the invention relates to a process for the removal of absorbable gases from pressurized industrial gas contaminated with absorbable gases without supplying cooling energy, whereby an industrial gas to be purified is purified by an absorbing solvent from the gases absorbable by the solvent, and adding the loaded solvent to a flash stage in which the absorbed gas is desorbed again, and the desorbed gas is compressed so that it is heated by the compression, whereupon it is cooled to normal temperature by means of cooling water or cooling air, then expanded is, so that it cools, and this cooled desorption gas is recycled back into the industrial gas, so that this is cooled by the admixture and a supply of cooling energy, for example by a refrigerator, is no longer necessary to the erforderl for absorption I adjust low temperature level.
  • the invention also relates to a device with which this method can be carried out.
  • the absorption of the added unwanted acid gases is typically carried out with an absorbing solvent.
  • Physically or chemically acting solvents are used. Typical physical solvents are methanol, alkylated polyethylene glycol ethers, or morpholine derivatives. Typical chemical solvents are alkanolamines or alkali salt solutions. Physically acting solvents are typically used at low temperatures because the desired uptake of this type of solvent for components to be absorbed increases at lower temperatures. To provide the appropriately cooled
  • CONFIRMATION COPY Solvents require chillers that require an amount of energy that is proportional to the amount of gas to be cooled. Since many industrial gases are treated with large amounts of cooled solvents for the absorption of acid gases, this is associated with a considerable cost factor. A typical process for the absorption of associated gases in industrial gases teaches WO 2004105919 A1.
  • This document teaches a process for sour gas removal from pressurized sulfur-contaminated natural gas, wherein the natural gas to be desulphurised is first passed into an acid gas absorption stage where the sulfur compounds and optionally other components are absorbed with a physico-acting solution which heats the absorbate and the sorbate is placed in a high pressure flash stage where the mixture of acid lean absorbent and desorbed sour gas separates, and the desorbed sour gas is cooled and the vaporized absorbent is condensed out of the sour gas stream is removed, and the sauergasarme absorber from the "high pressure flash stage" is freed in a further stage by means of stripping of Sauerergasresten and the resulting laden stripping gas is cooled and passed into the acid gas absorption stage, and the resulting absorbent cooled and recycled in the cycle in the acid gas absorption stage.
  • the regenerated absorption solution is returned to the absorption process after the heat exchange in a heat exchanger and the cooling in a cooler which
  • the invention solves this problem by a method which compresses the recirculated gas stream from a gas scrubbing with a physically acting solvent after spewing in a downstream spouting stage to a pressure which is significantly higher than the pressure of the industrial gas, which by the compression heated and compressed gas is cooled down again to ambient temperature by means of cooling water or cooling air and then expanded to the industrial gas pressure, so that the gas cools strongly by the "Joule-Thomson" effect, and this cooled gas admixes the industrial gas, so that the mixture of the two gases adjusts to a temperature suitable for absorption, thus eliminating the otherwise required refrigerating machine and eliminating the heat exchangers required to transfer the low temperature level of the refrigerant to the recirculated gas, which reduces the investment costs ng the process of the invention further reduced.
  • the use of the method according to the invention leads to systems with a correspondingly smaller space requirement.
  • the compressed recycle gas can also be cooled down so far that it can be liquefied at a sufficiently high recycle compressor end pressure, and this liquefied recycle gas is admixed or added to the industrial gas in liquid form, which is the quenching fluid - significantly increased.
  • An industrial gas to be purified which is contaminated by an acid gas, is first led to an absorption stage, in which the gases to be absorbed are absorbed under pressure by means of an absorbing solvent, and
  • the absorbent is placed in a high pressure flash tank in which the absorbate separates into a solvent depleted in absorbed gases and a desorbed gas,
  • the desorbed gas is compressed by a compressor to a pressure at which a portion of the sour gas contained therein liquefies, and the compressed and desorbed gas is cooled by means of cooling water or cooling air via an indirect heat exchanger, and
  • the cooled compressed gas is expanded by a relaxing device so that it cools further, and this gas is added to the industrial gas to be purified, and
  • the remaining laden solvent from the high-pressure flash tank contains the remaining sour gases and is generally fed to a further purification.
  • This can be, for example, a desorption column or a further Austriebs capableer.
  • the remaining sour gases which are obtained during the purification of the industrial gas and can be discharged from the process are also obtained.
  • the cooling of a raw gas with a cooled condensate from a cooling stage belongs to the prior art.
  • DE 2853989 B1 describes a process for treating hydrous condensate from the cooling of a raw gas from the gasification of solid fuels with oxygen, water vapor, and / or carbon dioxide. the gasification agents, wherein the raw gas is cooled in at least one cooling stage, wherein a condensate is obtained, which is expanded, the expansion steam dissipates, the relaxed condensate feeds a separator, and deducted from the separator substantially consisting of water condensate phase and as a cooling medium for the Raw gas reused.
  • the invention does not disclose any additional compression of the vapor, which by suitable means enables the cooling down of the raw gas to a temperature suitable for absorption of gases from gas mixtures with absorbing solvents. Also, the technical conditions under which a hot raw gas from a fuel gasification is cooled with water are different as compared to an absorption process with an absorbing solvent at low temperatures.
  • the compression of desorbed gases from a high-pressure flash stage is also found in the prior art.
  • the US 3266219 A discloses a process for removing acid gases from mixtures with gaseous C ⁇ C 3 - alkanes, through which the said gas mixture containing a carbon dioxide and hydrogen sulphide-containing sour gas is brought into contact with a sauergasabsorb Schlourden solvent and the absorbing solvent consists essentially of dimethoxyacetate, wherein the absorption conditions are adjusted so that the sour gas is completely absorbed by the absorbing solvent and the unabsorbed gases from the gas mixture are completely separated from the solvent.
  • the carbon dioxide content of the acidic gas with the non-acidic gases contained therein is withdrawn from the solvent in a high pressure flash stage, compressed, and returned to the starting gas mixture.
  • a relaxation of this carbon dioxide content with the non-acidic gases contained therein for the purpose of cooling the industrial gas to make the absorption process more efficient, is not listed.
  • the desorbed gas is expanded in the process of cooling and relaxation to the absorption pressure or a slightly higher pressure. As a result, no recompression of the desorbed industrial gas is required in the absorption process.
  • the desorbed gas is compressed to a pressure at least 10% higher than the pressure of the industrial gas.
  • the desorbed gas condenses in the process of cooling and relaxation at least partially or completely.
  • the admixture of the returned th gas to the industrial gas is advantageously carried out by a mixer, but can also, depending on the state of aggregation, via a gas valve or via a gas tank.
  • the liquid desorbed gas is added via a nebulizer, a carburetor or similar type of mixer in the starting gas.
  • the desorbed gas is added in liquid or partially in liquid form to the industrial gas.
  • the industrial gas to be purified is first cooled prior to introduction into the absorption stage, before the cooled and expanded desorption gas is added. Finally, the desorbed gas may be further cooled after expansion and prior to introduction into the absorption stage before being added to the industrial gas to be purified.
  • the cooling of the industrial gas before the addition of the cooled and expanded desorption gas can be done by any type of device. It is also possible, instead of the industrial gas to be purified, to cool the cooled and expanded desorption gas still further. This can also be done by any type of device. These may be, for example, heat exchangers, air or water coolers. It is also possible to use an additional chiller, although this is not usually required to practice the invention.
  • the compression and expansion of the desorbed gas can be done arbitrarily.
  • the compression can be done by way of example via a compressor.
  • This can be, for example, a turbocompressor or a reciprocating compressor.
  • the relaxation can also be done in any way. This can be done by way of example via a throttle valve as expansion valve. However, this can also take place via an expansion turbine, which generates rotational energy from the pressure energy. This in turn can be used as an example for generating electricity.
  • the Austriebs skilleder in turn may be of any kind. These are widely known in the art.
  • US Pat. No. 4997630 A teaches an example of a method in which flash tanks are used.
  • easily desorbable gases are released by a sudden expansion from a pressure of 5 to 110 bar to a pressure of 0.3 to 1.0 bar relaxed. This relaxation takes place at temperatures of 35 to 100 ° C.
  • the relaxed solvent is freed of easily desorbable gases.
  • Typical temperatures at which absorption of the gas to be absorbed takes place in an absorption column are -40 ° C to 20 ° C and preferably -20 ° C to 0 ° C.
  • the pressures during absorption are typically 20 to 200 bar.
  • Typical pressures at which desorption of the absorbed gas takes place in a high pressure flash tank are 10 to 100 bar.
  • the temperatures here are typically -10 ° C to 80 ° C and preferably 0 to 60 ° C.
  • the Austriebs discloseder may be provided in an exemplary embodiment also with packing.
  • the Austriebs realizeer can also be supplied to a Austriebsgas.
  • Suitable flue gases are inert gases such as hydrocarbons or nitrogen. In one embodiment of the invention, the flue gas can also be wholly or partly recycled to the industrial gas to be purified.
  • the industrial gas to be purified may be of any kind insofar as it is to be cleaned by an absorbing solvent.
  • This can be, for example, natural gas or a synthesis gas.
  • the absorbable gas can also be of any kind. These may be, for example, sour gas components or the absorbable gas may contain them.
  • the absorbable gas may be exemplified by carbon dioxide (CO 2 ) or contain carbon dioxide.
  • the absorbable gas may also be hydrogen sulfide (H 2 S) or contain hydrogen sulfide.
  • the absorbable gas may also contain both gases in any proportion.
  • the absorbable gases may also be non-acidic gases, such as heavier hydrocarbons. But it may also contain other admixtures, insofar as they do not interfere with the absorption process by the absorbing solvent.
  • the present invention purified industrial gas can be used freely after cleaning and providing. Also, the desorbed and discharged from the plant sour gas can be used arbitrarily. This can also be reinjected by way of example after recompression into a deposit.
  • a device with which this method is executable is also claimed.
  • a device is claimed for removing absorbable gases from pressurized industrial gases polluted with absorbable gases without supplying cooling energy
  • An absorption column equipped with a feed pipe for an industrial gas to be cleaned and a discharge pipe for the purified industrial gas,
  • a high pressure flash tank equipped with a desorbed sour gas bleed port and a sour gas absorbent bleed port connected by a conduit to the absorption tower;
  • a cooler that cools a pressurized heated gas by indirect heat exchange with cooling air or cooling water
  • a mixer which is suitable for returning the cooled and expanded desorbed gas to the industrial gas
  • the outlet port for the desorbed sour gas of the high pressure flash tank in the gas flow is sequentially piped to the compressor, the cooler, the relaxing device and the mixer into the industrial gas to be purified prior to the absorption step, so that the cooled and expanded desorbed sour gas enters the industrial gas to be purified is traceable.
  • the device contains as a relaxing device on or immediately behind the Austriebs employer at least one expansion valve.
  • the device includes as a relaxing device on or immediately behind the Austriebs employer instead of the expansion valve or throttle valve, an expansion turbine.
  • the expansion turbine can be used by way of example for generating electricity or for operating a compressor.
  • the high-pressure Austriebs employer may be associated with various auxiliary equipment and other system components. These are, for example, compressors, pumps, heat exchangers, heaters or coolers. This may also be a desorption column in which the absorbing solvent is heated or distilled under reduced pressure.
  • the invention has the advantage of an energy-saving method for absorbing absorbable gases from an industrial gas.
  • the method comes in a favorable embodiment without chiller and thereby saves a considerable amount of energy compared to the methods of the prior art. Also is a considerable reduction in the size of the equipment required due to the saving of chillers.
  • FIG. 1 shows an exemplary process with absorption column, high-pressure discharge container, compressor, cooling device and expansion valve.
  • FIG. FIG. 2 shows the same apparatus that supplies flash gas into the high pressure flash tank, uses an expansion turbine to generate electricity, and is equipped with two high pressure flare tanks instead of a desorption column.
  • FIG. 1 shows an apparatus which transfers an industrial gas (1) to be purified, which is contaminated with an absorbable gas, via a mixer (2) into an absorption column (3).
  • the mixer (2) mixes a cool and relaxed desorption gas (4), so that a cooled industrial gas (1a) is introduced into the absorption column (3).
  • the gas to be absorbed which is an example of sour gas
  • the loaded solvent (5) is transferred to a high pressure Austriebs hereer (6).
  • the loaded solvent is released.
  • Easily desorbable gases (7) are released.
  • the desorbed gas (7) which in addition to the gas components to be absorbed also contains absorbed useful gas components, is compressed by a compressor (8).
  • the compressed stream of the desorption gas (9) is cooled down to normal temperature by a cooler (10) which cools with air or water. In this case, a part of the desorption gas liquefies.
  • the compressed and cooled to normal temperature desorption gas (10a) is released via a throttle valve (11). This is cooled by the "Joule-Thomson" effect whereby a portion of the acid gas liquefies,
  • the cooled and expanded desorption gas (4) is returned via the mixer (2) in the industrial gas (1).
  • FIG. Fig. 2 shows a comparable apparatus which transfers an industrial gas (1) to be purified, which is contaminated with an absorbable gas, via a mixer (2) into an absorption column (3).
  • the mixer (2) mixes a cool and relaxed sour gas (4), so that a cooled industrial gas (1a) is introduced into the absorption column (3).
  • the gas to be absorbed which is an example of sour gas
  • the loaded solvent (5) is transferred to a high pressure Austriebs actuallyer (6). There, the loaded solvent is released.
  • a Austriebsgas (6a) is supplied to support the desorption process.
  • the easily desorbable gases (7) are released.
  • the desorbed gas (7) is compressed by a compressor (8) to a pressure which is significantly higher than the pressure of the industrial gas (1). In this case, a part of the desorption gas liquefies.
  • the compressed stream of the sour gas (9) is cooled down to normal temperature by a cooler (10) which cools with air or water.
  • the compressed and cooled to normal temperature oxygen gas (10a) is expanded by an expansion turbine (18). This is cooled by the "Joule-Thomson" effect and the work done in the expansion turbine The work done in the expansion turbine (18a) is used to assist the drive of the compressor (8) .
  • the cooled and relaxed Sour gas (4) is returned to the industrial gas (1) via the mixer (2), and the purified industrial gas (12) is obtained from the absorption column (3).
  • the expanded solvent obtained from the first high-pressure flash tank (6) (FIG. 13), which still contains sour gas, is transferred to a second flash tank (19), in which further absorbed sour gas (7a) is obtained by depressurization from the solvent, from the second flash stage (19) a regenerated solvent (20) is obtained. which is returned by a pump (20a) via a cooler (20b) in the absorption column (3).

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Organic Chemistry (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

L'invention concerne un procédé permettant d'éliminer sans apport d'énergie de refroidissement des gaz absorbables présents dans des gaz industriels sous pression contaminés par des gaz absorbables. Selon le procédé, un gaz industriel à épurer est épuré par un solvant d'absorption des gaz qu'il contient et qui sont absorbables par le solvant, et le solvant chargé est livré à un étage d'extraction dans lequel le gaz absorbé est à nouveau désorbé et le gaz désorbé est comprimé, de sorte qu'il est chauffé par la compression, après quoi il est refroidi à une température normale au moyen d'eau ou d'air de refroidissement puis décompressé, de sorte qu'il refroidit. Ce gaz de désorption refroidi est retourné dans le gaz industriel, de sorte que ce dernier refroidit également sous l'effet du mélange et qu'un apport d'énergie de refroidissement, par exemple par une machine de froid, n'est plus nécessaire pour établir le bas niveau de température exigé pour l'absorption. L'invention concerne également un dispositif permettant la mise en œuvre de ce procédé.
EP13794803.0A 2012-11-05 2013-10-29 Procédé et dispositif permettant d'éliminer sans apport d'énergie de refroidissement des gaz absorbables présents dans des gaz industriels sous pression contaminés par des gaz absorbables Withdrawn EP2914366A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102012021478.2A DE102012021478A1 (de) 2012-11-05 2012-11-05 Verfahren und Vorrichtung zur Entfernung von absorbierbaren Gasen aus unter Druck befindlichen, mit absorbierbaren Gasen verunreinigten Industriegasen ohne Zuführung von Kühlenergie
PCT/EP2013/003250 WO2014067649A1 (fr) 2012-11-05 2013-10-29 Procédé et dispositif permettant d'éliminer sans apport d'énergie de refroidissement des gaz absorbables présents dans des gaz industriels sous pression contaminés par des gaz absorbables

Publications (1)

Publication Number Publication Date
EP2914366A1 true EP2914366A1 (fr) 2015-09-09

Family

ID=49626886

Family Applications (1)

Application Number Title Priority Date Filing Date
EP13794803.0A Withdrawn EP2914366A1 (fr) 2012-11-05 2013-10-29 Procédé et dispositif permettant d'éliminer sans apport d'énergie de refroidissement des gaz absorbables présents dans des gaz industriels sous pression contaminés par des gaz absorbables

Country Status (6)

Country Link
US (1) US9844751B2 (fr)
EP (1) EP2914366A1 (fr)
CN (1) CN104918680B (fr)
CA (1) CA2890037A1 (fr)
DE (1) DE102012021478A1 (fr)
WO (1) WO2014067649A1 (fr)

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9562201B2 (en) * 2014-06-28 2017-02-07 Saudi Arabian Oil Company Energy efficient apparatus employing energy efficient process schemes providing enhanced integration of gasification-based multi-generation and hydrocarbon refining facilities and related methods
DE102015013796A1 (de) * 2015-10-22 2017-04-27 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von Gasprodukten
CN107754558B (zh) * 2016-08-19 2020-10-20 中国石油化工股份有限公司 一种聚乙二醇二甲醚脱硫提浓方法
CN106110841B (zh) * 2016-08-30 2019-02-22 贺少君 一种沼气提纯用的水洗吸收塔
US10688435B2 (en) * 2017-02-27 2020-06-23 Honeywell International Inc. Dual stripper with water sweep gas
EP3608010A1 (fr) * 2018-08-07 2020-02-12 L'air Liquide, Société Anonyme Pour L'Étude Et L'exploitation Des Procédés Georges Claude Procédé et dispositif de séparation des composants gazeux acides d'un mélange gazeux
EP4041436A1 (fr) * 2019-10-11 2022-08-17 thyssenkrupp Industrial Solutions AG Épurateur de gaz d'échappement à intégration d'énergie
US11484825B1 (en) * 2021-12-20 2022-11-01 Next Carbon Solutions, Llc Devices, systems, facilities and processes for carbon capture optimization in industrial facilities
CN114984727B (zh) * 2022-07-28 2022-10-28 北京百利时能源技术股份有限公司 一种低温深冷co2捕集装置及捕集方法

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3266219A (en) 1962-12-27 1966-08-16 Union Oil Co Removal of acid constituents from gas mixtures
DE2853989C2 (de) 1978-12-14 1980-07-31 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zum Behandeln von wasserhaltigem Kondensat aus der Kühlung des Rohgases der Druckvergasung
US4421535A (en) * 1982-05-03 1983-12-20 El Paso Hydrocarbons Company Process for recovery of natural gas liquids from a sweetened natural gas stream
DE3408851A1 (de) * 1984-03-10 1985-09-12 Basf Ag, 6700 Ludwigshafen Verfahren zum entfernen von co(pfeil abwaerts)2(pfeil abwaerts) und/oder h(pfeil abwaerts)2(pfeil abwaerts)s aus gasen
IT1190357B (it) * 1985-05-24 1988-02-16 Snam Progetti Procedimento criogenito di rimozione di gas acidi da miscele di gas mediante solventi
AU2002307364C1 (en) * 2002-04-15 2008-07-10 Fluor Technologies Corporation Configurations and methods for improved acid gas removal
WO2004026441A1 (fr) 2002-09-17 2004-04-01 Fluor Corporation Configurations et procedes d'extraction de gaz acide
EA009089B1 (ru) * 2002-12-12 2007-10-26 Флуор Корпорейшн Установка и способ удаления кислых газов
DE10313438A1 (de) * 2003-03-26 2004-11-04 Uhde Gmbh Verfahren zur selektiven Entfernung von Schwefelwasserstoff und CO2 aus Rohgas
DE10324694A1 (de) * 2003-05-28 2004-12-23 Uhde Gmbh Verfahren zur Entfernung von Sauergasen aus unter Druck befindlichem, mit Sauergasverbindungen verunreinigtem Erdgas und Gewinnung der entfernten Sauergase auf erhöhtem Druckniveau
MX2012003246A (es) * 2009-09-18 2012-04-10 Fluor Tech Corp Configuraciones de alta remocion de co2 de alta presion y metodos.
CA2825266C (fr) 2011-03-10 2016-01-26 Uop Llc Procedes et systemes d'elimination de gaz acides de gaz de synthese

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
None *
See also references of WO2014067649A1 *

Also Published As

Publication number Publication date
DE102012021478A1 (de) 2014-05-08
CN104918680A (zh) 2015-09-16
US20150273386A1 (en) 2015-10-01
CN104918680B (zh) 2018-05-11
WO2014067649A1 (fr) 2014-05-08
US9844751B2 (en) 2017-12-19
CA2890037A1 (fr) 2014-05-08

Similar Documents

Publication Publication Date Title
EP2914366A1 (fr) Procédé et dispositif permettant d'éliminer sans apport d'énergie de refroidissement des gaz absorbables présents dans des gaz industriels sous pression contaminés par des gaz absorbables
DE19753903C2 (de) Verfahren zur Entfernung von CO¶2¶ und Schwefelverbindungen aus technischen Gasen, insbesondere aus Erdgas und Roh-Synthesegas
DE60004795T2 (de) Verfahren zur entfernung und wiedergewinnung von c02 aus abgasen
DE102005051952B3 (de) Verfahren zur Herstellung von Methan und flüssigem Kohlendioxid aus Raffinerie- und/oder Biogas
DE102014110190B4 (de) Verfahren zur Abtrennung von Kohlendioxid aus Biogas mittels einer aminhaltigen Waschlösung und Regeneration der beladenen Waschlösung sowie Anlagen zur Durchführung des Verfahrens
EP1289625B1 (fr) Procede de desacidification d'un courant fluidique d'hydrocarbure
EP2300128A1 (fr) Agent absorbant et procédé pour éliminer des gaz acides contenus dans des flux de fluide, en particulier des gaz de fumée
DE19947845A1 (de) Verfahren zum Entfernen von COS aus einem Kohlenwasserstoff-Fluidstrom und Waschflüssikgkeit zur Verwendung in derartigen Verfahren
EP2503271A2 (fr) Procédé et dispositif destinés au traitement d'un flux de gaz contenant du dioxyde de carbone
DE19933301A1 (de) Verfahren zum Entfernen von Mercaptanen aus Fluidströmen
EP2736625A1 (fr) Récupération de chaleur au cours de processus d'absorption et de désorption
EP2117677A1 (fr) Procédé et installation de récupération de méthane liquide à partir de gaz bruts, en particulier de biogaz contenant du méthane et du dioxyde de carbone
EP1628741B1 (fr) Procede pour extraire des gaz acides d'un gaz naturel sous pression contamine par des composes de gaz acides et recuperation des gaz acides extraits a un niveau de pression superieur
WO2003013699A1 (fr) Procede et agent d'absorption destines a l'extraction de gaz acides dans des fluides
EP2480314A1 (fr) Procédé et dispositif permettant d'éliminer l'eau contenue dans un gaz naturel ou des gaz industriels au moyen de solvants physiques
DE60301399T2 (de) Methode und system zur desorption und rückgewinnung von desorbierten verbindungen
EP3132840B1 (fr) Procédé et dispositif de séparation de substances toxiques gazeuses d'un flux gazeux
DE2325422A1 (de) Verfahren und vorrichtung zur zerlegung von rohargon
DE19538614C2 (de) Verfahren und Anlage zum Aufbereiten von stickstoffhaltigem Erdgas
DE102022116799A1 (de) Verfahren zum Trennen von Methan und Kohlendioxid aus Biogas und Aufbereitungsanlage
CN114870570A (zh) 一种用于二氧化碳分离的液固分相吸收剂
WO2024008245A1 (fr) Procédé de préparation de biogaz et/ou de gaz naturel pour produire du méthane liquéfié et système de préparation
WO2024008248A1 (fr) Procédé pour séparer du méthane et du dioxyde de carbone de biogaz et installation de préparation
EP3608010A1 (fr) Procédé et dispositif de séparation des composants gazeux acides d'un mélange gazeux
DE102023208672A1 (de) Anlage und Verfahren zur Abtrennung von in einem Fluidstrom befindlichem Kohlenstoffdioxid

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20150413

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

AX Request for extension of the european patent

Extension state: BA ME

DAX Request for extension of the european patent (deleted)
RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: THYSSENKRUPP INDUSTRIAL SOLUTIONS AG

17Q First examination report despatched

Effective date: 20190711

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: GRANT OF PATENT IS INTENDED

INTG Intention to grant announced

Effective date: 20200617

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20201028