[go: up one dir, main page]

EP2790810A1 - Procédé et installation pour séparer du dioxyde de carbone de gaz bruts contenant du méthane - Google Patents

Procédé et installation pour séparer du dioxyde de carbone de gaz bruts contenant du méthane

Info

Publication number
EP2790810A1
EP2790810A1 EP11831818.7A EP11831818A EP2790810A1 EP 2790810 A1 EP2790810 A1 EP 2790810A1 EP 11831818 A EP11831818 A EP 11831818A EP 2790810 A1 EP2790810 A1 EP 2790810A1
Authority
EP
European Patent Office
Prior art keywords
stripping
column
solution
scrubbing
methane
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Withdrawn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
EP11831818.7A
Other languages
German (de)
English (en)
Inventor
Lothar Günther
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.)
DGE Dr Ing Guenther Engineering GmbH
Original Assignee
DGE Dr Ing Guenther Engineering 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 DGE Dr Ing Guenther Engineering GmbH filed Critical DGE Dr Ing Guenther Engineering GmbH
Publication of EP2790810A1 publication Critical patent/EP2790810A1/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Withdrawn legal-status Critical Current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
    • B01D53/1456—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
    • B01D53/1406—Multiple stage absorption
    • 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
    • B01D53/1418—Recovery of products
    • 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, 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
    • C10L3/101—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, 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
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • C10L3/104—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, 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
    • C10L3/101—Removal of contaminants
    • C10L3/105—Removal of contaminants of nitrogen
    • 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
    • C10L3/101—Removal of contaminants
    • C10L3/106—Removal of contaminants of water
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C12M47/18—Gas cleaning, e.g. scrubbers; Separation of different gases
    • 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
    • B01D2252/10—Inorganic absorbents
    • B01D2252/103—Water
    • 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
    • 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
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B01D2256/245—Methane
    • 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
    • B01D2258/00—Sources of waste gases
    • B01D2258/05—Biogas
    • 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
    • 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, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • 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, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • 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
    • 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
    • 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
    • C10L2290/542—Adsorption of impurities during preparation or upgrading of 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, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • 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
    • C10L2290/545—Washing, scrubbing, stripping, scavenging for separating fractions, components or impurities during preparation or upgrading of a fuel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/20—Capture or disposal of greenhouse gases of methane
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/59—Biological synthesis; Biological purification

Definitions

  • the invention relates to a method for the separation of carbon dioxide from methane-containing raw gases, in particular biogas, by means of pressure washing, using a physically acting solvent, wherein the contaminated washing solution is recycled after regeneration. Furthermore, the invention relates to a suitable system for carrying out the method.
  • Pressure washing processes for the removal of carbon dioxide from methane-containing raw gases, in particular biogas, are based on the active principle of the solution of gases in liquids.
  • DE 10 2008 025 971 A1 and DE 10 2008 060 3 0 A1 disclose processes for purifying crude or biogas which use water as wash solution for the separation of CO 2 .
  • a significant advantage of this process compared to the pressurized water wash is a significantly better solubility of C0 2 in the scrubbing liquid (Selexol), whereby the consumption is significantly reduced.
  • a disadvantage of this washing liquid is its significantly higher solubility for organic and inorganic compounds compared to water.
  • the invention has for its object to provide a method for the separation of carbon dioxide from methane-containing raw gases, in particular biogas, by means of pressure washing with a physically acting detergent in which the Methanschlupf resulting methane loss is significantly reduced and the overall energy balance of the process can be improved.
  • the laden scrubbing solution obtained after pressure washing is treated at least in one expansion stage before the first stripping step.
  • the pressurized laden scrubbing solution is depressurized while reducing the system pressure to a value of 1.5 to 5 bar.
  • the temperature of the loaded wash solution can be increased in the expansion column by at least 5 ° C. This improves the separation of methane from the wash solution.
  • Essential for the process economy is the measure, in addition to integrate a washing stage in the overall system, in which withdrawn from the expansion stage nitrogen, oxygen, carbon dioxide and methane-containing gas mixture is removed by means of the second stripping withdrawn and supplied in countercurrent purified scrubbing solution.
  • the methane content of this expansion gas is 20 to 40% and corresponds to at least 7% of the total amount of methane.
  • the treatment of this flash gas with already purified scrubbing solution within the overall system produces a high-purity methane gas with a methane content of more than 90% by volume, which can be sent for further utilization.
  • the proposed measures in the expansion stage in the wash solution in dissolved form present gaseous components of nitrogen, oxygen, carbon dioxide and methane released as a gas mixture and washed out by circulating purified scrubber solution carbon dioxide from the gas mixture, so that high purity methane gas can be withdrawn at the top of the wash column , In the overall system, the methane slip can thus be reduced to below 0.2%.
  • the washing process only a smaller subset of purified washing solution is needed. The larger portion is used for pressure washing.
  • a further disadvantage of existing processes for the separation of carbon dioxide by means of washing solutions from biogas containing glycol ether is that despite the good washing Water uptake of the washing solution Dew points only up to 200 to 500 mg of water / Nm 3 biogas can be realized. At required water contents of 50 mg / Nm 3 in the biogas so a further Adsorptionstrocknung is necessary.
  • a subset is removed from purified scrubbing solution obtained in the second stripping step, subsequently heated to temperatures above 100 ° C. and fed to a vessel. In this residual water is expelled from the hot wash solution. After cooling, the nearly anhydrous wash solution is added back to the purified wash solution. The energy required to heat the wash solution is recovered within the system.
  • an oxygen-free or containing gas is used as stripping gas and precompressed air is used in the second stripping stage. This depends on the required oxygen demand for upstream desulfurization.
  • the supplied oxygen-containing stripping gas is used in an amount of from 0.1 to 2%, based on the amount of biogas to be purified fed to the pressure wash.
  • the stripping process can be carried out at temperatures of 20 to 120 D C and a pressure of 1, 5 to 5 bar. Thus, at least 90% of the methane dissolved in the scrubbing solution can be separated off.
  • the second stripping step is fed laden scrubbing solution from the first stripping, this relaxed to atmospheric pressure and separated from this by stripping air still contained in the scrubbing solution dissolved carbon dioxide at least to a residual content of less than 100 mg / l.
  • the washing solution thus obtained is completely regenerated and can be used again in the course of the circulation.
  • the purified scrubbing solution obtained at the bottom of the second stripping column is divided into two sub-streams, one sub-stream being fed to the scrubbing column and the other sub-stream being fed to the scrubber.
  • the raw gas for desulfurization is brought into contact with a suspension containing microorganisms, dissolved oxygen being present in the suspension which has come into contact with the suspension through contact with the oxygen-containing gas mixture withdrawn from the first stripping step.
  • Hydrogen sulphide which has been washed out is oxidised to SO 4 by means of microorganisms and converted to sulfuric acid.
  • the amount of oxygen required for biological desulfurization can be metered in via the oxygen concentration of the stripping gas supplied in the first stripping stage.
  • Btogas originating from the fermenter of a biogas plant has the following composition:
  • Biogas (250 NrrvVh) with a temperature of 38 ° C is fed directly from the fermenter via line 01 a biological desulfurization unit.
  • This consists of a wash column K0 as an absorber, a reaction vessel B0 and a circulation line 21, 22 in which a first pump PO is involved.
  • reaction vessel B0 is an aqueous suspension consisting of microorganisms, sulfuric acid formed and bound ammonium sulfate.
  • the pressurized gas mixture which is withdrawn at the top of the first stripping column S1 of the first stripping step, into the reaction vessel B0 initiated, being dissolved in the suspension contained in the reaction vessel BO of the oxygen contained in the gas mixture.
  • the consisting of methane and carbon dioxide gas mixture passes through a compensation line 20 in the supply line 01 for biogas.
  • hydrogen sulfide is washed out by means of the suspension (lines 21, 22) driven from the biogas (456 g H 2 S / h) and bound in the suspension.
  • H 2 S is converted via the intermediate sulfate (S0 4 2 " ), hydrogensulfate anion (HSGy) to sulfuric acid (H 2 S0 4 )
  • H 2 S0 4 hydrogensulfate anion
  • Additional oxygen can be metered if required via a higher oxygen concentration of the stripping gas fed to the first stripping column S1 or by direct introduction of oxygen into the reaction vessel B0.
  • the temperatures in the wash column K0 and in the reaction vessel B0 are kept constant at ca, 40 e C.
  • the proportion of H 2 S is reduced from 1,200 ppm to 15 ppm.
  • ammonia contained in the biogas is converted to ammonium sulfate and thereby reduces the ammonium content in biogas from 250 to 2 ppm.
  • the desulfurized biogas withdrawn at the top of the scrubbing column K0 via the line 02 is cooled and compressed to 7 bar by means of a compressor V1 connected to the line 02.
  • the temperature increase resulting from the compression (to about 180 ° C) of each stage must be reduced again by cooling (to 25 C C).
  • Resulting condensation products are separated and removed particles contained in biogas.
  • an activated carbon filter can be connected downstream as a fine filter for H 2 S.
  • the pretreated biogas is fed to an absorber, the scrubbing column K1, via line 03.
  • the wash column K1 has a column diameter of 450 mm and has a column height of 10 m. 7 m of the column height are designed as GearSchüt- device with two different packing.
  • the lower column bed has packing with a surface area of about 250 m 2 / m 3 and the upper column bed packing with a surface area of over 350 m 2 / m 3 .
  • the physically active washing solution used consists of tetraethylene glycol dimethyl ether (purity of more than 99%, molecular weight of more than 280 mol / g, boiling point above 250 ° C. at atmospheric pressure). The water content is less than 1%.
  • the wash column K1 12 m 3 / h of washing solution at a temperature of 18 ° C supplied. At the top of the scrubbing column K1 purified biogas (methane gas) with subsequent
  • the content of C0 2 in the biogas is reduced by the pressure washing of 44 vol .-% to 1.08 vol .-%. At the same time, water is removed from the biogas, from 2000 mg / Nm 3 to a value of less than 50 mg / Nm 3 .
  • the purified biogas of the aforementioned quality which is discharged via line 04 at a pressure of 7 bar, can be fed into the gas network after the odorization and the required calorific value adjustment as methane gas.
  • the regeneration of the laden at the bottom of the wash column K1 loaded washing solution takes place in a flash stage, a first stripping, a washing stage and a downstream second stripping.
  • the resulting gas mixture (12 Nm 3 / h CH 4 and 16 Nm 3 / h C0 2 ) is withdrawn at the top of the expansion column KE via line 23 and fed to a wash column K2.
  • the loaded washing solution is withdrawn via line 07 and fed to a first stripping column S1.
  • the temperature of the washing solution can be increased to improve the stripping performance via a heat exchanger W3 integrated in the line 07.
  • the first stripping column S1 is fed via the line 07 loaded scrubbing solution from the expansion column KE and via the line 25 loaded scrubbing solution from the second scrubbing column K2.
  • a slight pressure reduction takes place by about 0.5 bar to 2.5 bar.
  • the laden washing solutions from the expansion column KE and the second washing column K2 can be introduced without an additional pump at the top of the stripping column S1.
  • the stripping process is carried out with an oxygen-containing stripping gas with an oxygen quantity of 1 to 2 Nm 3 / h.
  • the stripping gas is supplied via the line 16. From the loaded washing solution, consisting of the two aforementioned partial flows (via lines 07 and 25) C0 2 and CH 4 are stripped off.
  • the scrubbing solution (15 m 3 / h) withdrawn from the bottom of the column still has a residual charge of 1.1 g / l of CO a and 0.01 g / l of CH 4 .
  • the gas mixture withdrawn at the top via line 17 (18 Nm 3 / h) has a composition of 49.8% by volume of CH 4 , 44.6% by volume of C0 2 and 5.6% by volume of O 2 and is, as already mentioned above, fed to the container B0.
  • the wash column K2 is supplied via the lines 08 and 08a, in which a pump P2 is integrated, a partial flow of purified washing solution from the second stripping column S2.
  • the withdrawn from the expansion column KE gas mixture (12 Nm 3 / h CH and 16 Nm 3 / h C0 2 ) is supplied at a pressure of 3 bar with 3 m 3 / h, which serves as a stripping gas.
  • CO 2 contained in the purified scrubbing solution is bound in the gas mixture.
  • the wash solution has a load of 10.3 g / l C0 2 and 0.26 g / l CH at the bottom. As already mentioned, this washing solution is fed via line 25 to the first stripping column S1.
  • the second stripping column S2 is fed via line 26 still laden wash solution from the first stripping column S1 and expanded to atmospheric pressure.
  • a second compressor V2 is supplied via the line 18 stripping.
  • an exhaust gas is discharged via the line 19.
  • the purified scrubbing solution leaving via line 08 has only a low residual charge of less than 0.1 g / l C0 2 and 0.001 g / l CH 4 .
  • only 0.2 Nm 3 / h of methane are released as a loss from the system in the environment via the line 19 of the second stripping S2.
  • the methane loss is only 0.15%.
  • a partial stream of the purified scrubbing solution is pumped via the line 08a into the scrubbing column K2 and the other sub-stream via the line 08b by means of the pump P1 through the first heat exchange W6 as heat transfer and after cooling in the second heat exchanger W1 to 18 ° C is again introduced via the line 05 into the scrubbing column K1 of the pressure washing.
  • a small proportion of partial flow (0.1 m 3 / h) can be removed via the line 09.
  • This partial stream is heated in the heat exchanger W4 and subsequently in a further heat exchanger W5 from 40 ° C to 160 ° C and fed to the container B2.
  • the transport of the washing solution via the lines 10 and 11.
  • the hot washing solution is withdrawn from the container B2 and flows through the heat exchanger W4 as a heat transfer medium.
  • a pump P3 is integrated.
  • the purified wash solution is cooled to normal temperature via the lines 14 and 15 as well as the heat exchanger W2 incorporated into it and mixed with the supplied wash solution in the top of the wash column K1.
  • the anhydrous partial stream can also be added to the wash solution of the second stripping column S2.
  • the water content of the biomethane produced can be further reduced to below 50 mg / Nm 3 .

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)
  • Analytical Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • Wood Science & Technology (AREA)
  • Biotechnology (AREA)
  • Zoology (AREA)
  • Health & Medical Sciences (AREA)
  • Microbiology (AREA)
  • Sustainable Development (AREA)
  • Biomedical Technology (AREA)
  • Biochemistry (AREA)
  • General Engineering & Computer Science (AREA)
  • General Health & Medical Sciences (AREA)
  • Genetics & Genomics (AREA)
  • Gas Separation By Absorption (AREA)
  • Physical Water Treatments (AREA)

Abstract

La présente invention concerne un procédé pour séparer du dioxyde de carbone de gaz bruts contenant du méthane, et plus particulièrement de biogaz, au moyen d'un lavage sous pression, en utilisant un solvant à action physique, la solution de lavage souillée étant recyclée après régénération. L'invention est également relative à une installation adaptée pour exécuter le procédé. Le but de l'invention est de réduire notablement la perte de méthane résultant de la fuite de méthane et d'améliorer le bilan énergétique global du procédé. À cet effet, l'invention propose comme solution de traiter la solution de lavage chargée résultant du lavage sous pression au moins dans un étage de détente avant le premier étage de stripping. Un mélange gazeux extrait de l'étage de détente et contenant de l'azote, de l'oxygène, du dioxyde de carbone et du méthane est en outre purifié dans un étage de lavage au moyen d'une solution de lavage purifiée, extraite du deuxième étage de stripping et amenée à contre-courant; un gaz méthane de haute pureté se forme.
EP11831818.7A 2011-12-16 2011-12-16 Procédé et installation pour séparer du dioxyde de carbone de gaz bruts contenant du méthane Withdrawn EP2790810A1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/DE2011/002152 WO2013087046A1 (fr) 2011-12-16 2011-12-16 Procédé et installation pour séparer du dioxyde de carbone de gaz bruts contenant du méthane

Publications (1)

Publication Number Publication Date
EP2790810A1 true EP2790810A1 (fr) 2014-10-22

Family

ID=45936581

Family Applications (1)

Application Number Title Priority Date Filing Date
EP11831818.7A Withdrawn EP2790810A1 (fr) 2011-12-16 2011-12-16 Procédé et installation pour séparer du dioxyde de carbone de gaz bruts contenant du méthane

Country Status (6)

Country Link
US (1) US20140329299A1 (fr)
EP (1) EP2790810A1 (fr)
CN (1) CN104023819A (fr)
DE (1) DE112011105958B4 (fr)
RU (1) RU2014128160A (fr)
WO (1) WO2013087046A1 (fr)

Families Citing this family (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108325340A (zh) * 2013-03-15 2018-07-27 Mecs公司 废气中污染物的再生回收
NL2013230B1 (en) * 2014-07-21 2016-08-16 Airpack Holding B V Method for upgrading biogas and production of ammonium sulphate.
NL2014997B1 (en) * 2015-06-19 2017-01-24 Koers Bonno Method and apparatus for removal of hydrogen sulphide from gas mixtures.
WO2017040268A1 (fr) * 2015-08-28 2017-03-09 Energy Tech Innovations, LLC Procédé et appareil pour traiter du biogaz
US11268063B2 (en) 2015-08-28 2022-03-08 Energy Tech Innovations, LLC Method and apparatus for treating biogas
NL2015921B1 (en) * 2015-12-08 2017-06-28 Frames Renewable Energy Solutions B V Process for the purification of a gas
FR3075659B1 (fr) * 2017-12-21 2019-11-15 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede de production d'un courant de gaz naturel a partir d'un courant de biogaz.
JP7175227B2 (ja) * 2019-03-19 2022-11-18 日立造船株式会社 メタン製造システム
CN113061475B (zh) * 2021-03-10 2024-05-31 广西大学 一种可调二氧化碳浓度的从临界沼气中分离二氧化碳的液化工艺方法及装置
WO2022220681A1 (fr) 2021-04-16 2022-10-20 Gashouders B.V. Compression d'un biogaz contenant du dioxyde de carbone, biogaz comprimé contenant du dioxyde de carbone, et son utilisation
EP4174160B1 (fr) * 2021-10-26 2025-03-12 Alpha Engineering Services GmbH Procédé et dispositif de séparation d'un mélange gazeux
CN115040990B (zh) * 2022-07-04 2023-05-23 云南水富云天化有限公司 一种低温甲醇洗甲醇洗涤塔段间推动力提升控制装置
WO2024008248A1 (fr) 2022-07-06 2024-01-11 DGE Dr. Ing. Günther Engineering GmbH Procédé pour séparer du méthane et du dioxyde de carbone de biogaz et installation de préparation
DE102022116799A1 (de) * 2022-07-06 2024-01-11 DGE Dr. Ing. Günther Engineering GmbH Verfahren zum Trennen von Methan und Kohlendioxid aus Biogas und Aufbereitungsanlage
CN117965216B (zh) * 2024-04-01 2024-07-12 上海联风气体有限公司 用于含氧煤层气的安全回收甲烷并提纯的方法

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
PL180622B1 (pl) * 1994-05-11 2001-03-30 Babcock Hitachi Kk Sposób mokry odsiarczania gazów spalinowych i instalacja do mokrego odsiarczania gazów spalinowych PL PL PL
ES2365474T3 (es) * 2002-12-12 2011-10-06 Fluor Corporation Procedimiento de eliminación de gases ácidos.
DE10313438A1 (de) * 2003-03-26 2004-11-04 Uhde Gmbh Verfahren zur selektiven Entfernung von Schwefelwasserstoff und CO2 aus Rohgas
DE10356276A1 (de) * 2003-11-28 2005-06-30 Tentscher, Wolfgang, Dr. Reinigung von Kohlendioxid aus Biogas von störenden Begleitstoffen während und nach der Aufbereitung mit der nassen Druckgaswäsche
CN2870960Y (zh) * 2006-01-18 2007-02-21 北京合百意生态能源科技开发有限公司 一种沼气生物脱硫设备
US20080081938A1 (en) * 2006-09-28 2008-04-03 Schultz Michael A Absorption recovery processing of light olefins free of carbon dioxide
WO2008097304A1 (fr) * 2006-12-11 2008-08-14 Jaf Enterprises, Llc. Procédé de conversion de biogaz en un gaz naturel renouvelable de pipeline
DE102008025971A1 (de) 2008-05-30 2009-12-03 Dge Dr.-Ing. Günther Engineering Gmbh Verfahren und Anlage zur Reinigung von Biogas zur Gewinnung von Methan
US8007567B2 (en) * 2008-08-13 2011-08-30 A & B Process Systems Corporation Apparatus and method for biogas purification
DE102008060310B4 (de) 2008-12-03 2013-01-31 Dge Dr.-Ing. Günther Engineering Gmbh Verfahren und Anlage zur Reinigung von Roh- oder Biogas zur Gewinnung von Methan
CN101780373A (zh) * 2010-03-23 2010-07-21 浙江大学 生物法脱除沼气中硫化氢的方法
NO333145B1 (no) * 2010-10-28 2013-03-18 Sargas As Varmeintegrering i et CO2-fangstanlegg

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2013087046A1 *

Also Published As

Publication number Publication date
CN104023819A (zh) 2014-09-03
US20140329299A1 (en) 2014-11-06
WO2013087046A1 (fr) 2013-06-20
DE112011105958A5 (de) 2014-08-28
RU2014128160A (ru) 2016-02-10
DE112011105958B4 (de) 2023-01-26

Similar Documents

Publication Publication Date Title
WO2013087046A1 (fr) Procédé et installation pour séparer du dioxyde de carbone de gaz bruts contenant du méthane
EP2361138B1 (fr) Procédé et dispositif pour épurer des gaz bruts, en particulier un biogaz pour obtenir du méthane
EP2066796B1 (fr) ProcÉdÉ et dispositif de séparation du méthane et du dioxyde dE carbone dU biogaz
EP1953130B1 (fr) Procédé et installation de gaz brut contenant du dioxyde de carbone et de méthane, en particulier du biogaz, pour un gain de méthane
EP2038045B1 (fr) Procédé de purification de biogaz produit par une installation de production de biogaz et système de purification de biogaz
CN101918104B (zh) 用于处理包含co2的工艺气流的方法
EP2288425B1 (fr) Procédé et installation de purification de biogaz pour la récupération de méthane
EP1289625B1 (fr) Procede de desacidification d'un courant fluidique d'hydrocarbure
WO2005044955A1 (fr) Procede d'extraction d'un flux de gaz acide sous haute pression par extraction des gaz acides contenus dans un flux fluidique
DE102014110190B4 (de) Verfahren zur Abtrennung von Kohlendioxid aus Biogas mittels einer aminhaltigen Waschlösung und Regeneration der beladenen Waschlösung sowie Anlagen zur Durchführung des Verfahrens
WO2008092603A1 (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
DE102005051952B3 (de) Verfahren zur Herstellung von Methan und flüssigem Kohlendioxid aus Raffinerie- und/oder Biogas
WO2019110443A1 (fr) Procédé pour la fourniture de co2 pour la synthèse de l'urée à partir de fumées et de gaz de synthèse
DE3222281C2 (de) Verfahren zum Entfernen von Kohlendioxid und, sofern vorhanden, Schwefelwasserstoff aus einem Gasgemisch
DE102009056660B4 (de) Verfahren und Anlage zur chemisorptiven Abtrennung von Kohlendioxid aus Bio- oder Klärgas mittels einer aminhaltigen Waschlösung und Regeneration der beladenen Waschlösung
WO2003013699A1 (fr) Procede et agent d'absorption destines a l'extraction de gaz acides dans des fluides
DE2433078C3 (de) Verfahren zur Reinigung von durch Vergasung fester fossiler Brennstoffe mittels Wasserdampf und Sauerstoff unter Druck erzeugter Gase
DE102009009753B4 (de) Verfahren zur chemisorptiven Reinigung von Bio- oder Klärgas
WO2013131517A1 (fr) Procédé et installation permettant de séparer du dioxyde de carbone de biogaz
DE102012023937A1 (de) Verfahren zur Entfernung von Sauergasen aus einem Restgas einer Alkoholsynthese
EP0341572A2 (fr) Procédé de régénération d'un absorbant chargé d'H2S et/ou de COS
DE102023117119A1 (de) Verfahren zum Aufbereiten von methan- und kohlendioxidhaltigen Rohgasen, insbesondere Biogas, zur Gewinnung von Methan und Aufbereitungsanlage
DE2226065C3 (de) Verfahren zur Erhöhung des Deuteriumgehaltes im Wasserstoff bei der Gewinnung eines Wasserstoff enthaltenden Gases durch Umsatz
WO2024008245A1 (fr) Procédé de préparation de biogaz et/ou de gaz naturel pour produire du méthane liquéfié et système de préparation
DE2928858A1 (de) Verfahren zur reinigung von gasgemischen

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: 20140702

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

DAX Request for extension of the european patent (deleted)
19U Interruption of proceedings before grant

Effective date: 20151016

19W Proceedings resumed before grant after interruption of proceedings

Effective date: 20160502

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

Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE

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: 20180703