WO2013050667A1 - Masse de captation a performances ameliorees et son utilisation dans la captation de metaux lourds - Google Patents
Masse de captation a performances ameliorees et son utilisation dans la captation de metaux lourds Download PDFInfo
- Publication number
- WO2013050667A1 WO2013050667A1 PCT/FR2012/000361 FR2012000361W WO2013050667A1 WO 2013050667 A1 WO2013050667 A1 WO 2013050667A1 FR 2012000361 W FR2012000361 W FR 2012000361W WO 2013050667 A1 WO2013050667 A1 WO 2013050667A1
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- WO
- WIPO (PCT)
- Prior art keywords
- capture mass
- capture
- alumina
- mercury
- mass
- Prior art date
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- B01D2257/00—Components to be removed
- B01D2257/60—Heavy metals or heavy metal compounds
- B01D2257/602—Mercury or mercury compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- 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
-
- 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
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
- Y10T428/00—Stock material or miscellaneous articles
- Y10T428/29—Coated or structually defined flake, particle, cell, strand, strand portion, rod, filament, macroscopic fiber or mass thereof
- Y10T428/2982—Particulate matter [e.g., sphere, flake, etc.]
Definitions
- the present invention relates to a mass of capture of heavy metals including mercury and possibly arsenic and lead present in a gaseous or liquid effluent. It also relates to the preparation of said capture mass and the process for the removal of heavy metals by means of this capture mass comprising a support essentially based on gel-obtained alumina and at least one element selected from the group consisting of copper, molybdenum, tungsten, iron, nickel and cobalt.
- the invention is advantageously applicable to the treatment of gases of industrial origin, synthesis gas, natural gas, condensates in the gas phase and liquid hydrocarbon feedstocks.
- Mercury is a metal contaminant found in gaseous or liquid hydrocarbons produced in many parts of the world, such as the Gulf of Niger, South America or North Africa.
- the performance of a capture mass in a purification process is characterized by the dynamic capacity, ie the ability of the latter to maintain a minimum level of performance during the greatest possible operating time.
- This level of performance is defined by the efficiency, E, according to the formula:
- E (%) [([M] 0 - [M] s) / [M] o] x 100 with [M] s the concentration of metal in the effluent at the outlet of the bed and [M] 0 the concentration of metal in the effluent at the entrance of the bed.
- the reaction (1) is spontaneous and has a free energy ⁇ (kJ / mol) negative over a wide temperature range, typically from 0 to 300 ° C. (data obtained via the bank thermochemical data from HSC Chemistry 7, Outotec, Outotec Oyj, Riihitontuntie 7D, PO Box 86, FI-02200 Espoo, Finland).
- cupric copper sulphide in the oxidation state (I), CU2S
- the reaction (2) has a positive characteristic free energy over a very wide temperature range, typically from 25 ° C to 300 ° C (data obtained via the thermochemical data bank of the HSC Chemistry 7 software, Outotec, Outotec Oyj, Riihitontuntie 7D, PO Box 86, FI-02200 Espoo, Finland).
- Porous aluminas are the medium of choice in the formulation of heavy metals capture masses, such as mercury.
- Aluminum supports can be synthesized mainly by two routes:
- boehmite gel can be obtained by precipitation of the basic and / or acidic solutions.
- aluminum salts induced by pH change or any other method known to those skilled in the art P. Euzen, P. Raybaud, X.
- the texture understood in the present invention as the characteristic of the distribution of pore diameters is generally very extensive for flash aluminas and generally comprises a significant fraction (> 20%) of the pore volume in the macroporous and / or microporous domains.
- the microporous volume is constituted by the cumulative volume of the pores of the alumina whose diameter is less than 0.002 ⁇ in the sense of IUPAC (International Union of Pure and Applied Chemistry) whereas the macroporous volume corresponds to the cumulative volume of the pores of alumina whose diameter is greater than 0.05 ⁇ within the meaning of IUPAC.
- Vx the porous volume characteristic of a porous support (ml / g) corresponding to the cumulative volume of its porosity, characterized in that the diameter of the pores, in all the pores of the support, is greater than x (in ⁇ )
- the flash aluminas are characterized by a ratio V 0 , oos / Vo, o3 ⁇ 2 (Zotin, JL & Faro Jr, AC, 1991, Effect of basicity and pore size distribution of transition aluminas on their performance in the hydrogen sulphide-sulphur dioxide reaction, Applied Catalysis, 75, 57-73, P. Euzen, P. Raybaud, X. Krokidis, H.
- gel aluminas generally have centrally located pore diameter distributions in the NUPAC sense of mesoporosity having a much narrower pore diameter dispersion than in the case of flash aluminas (Johnson, MF). & Mooi, J. (1968), which makes them totally different from flash aluminas from a textural point of view.
- the chemical composition of flash aluminas has more sodium than that of gel aluminas.
- the flash aluminas contain strictly more than 700 ppm (Na 2 O equivalent) of sodium and less than 0.5% of Na 2 O whereas this content is less than or equal to 700 ppm (Na 2 O equivalent) in the case of gel aluminas (P. Euzen, P. Raybaud, X. Krokidis, H. Toulhoat, JL Le Loarer, JP Jolivet, C. Froidefond, Alumina, Handbook of Porous Solids, Eds Schuth F., KSW Sing, J. Weitkamp, Wiley-VCH, Weinheim, Germany, 2002, pp. 1591-1677).
- US 6033556 (Didillon, Kasztelan, Harle, 2000), indicates that alumina gel type supports are not suitable for heavy metal removal applications, such as mercury.
- the technical limitations of this type of support cited in this patent concern the problems related to capillary condensation as well as the diffusional limitations related to the porosity profile of the support.
- gel aluminas have a pore diameter distribution centered on smaller values than in the case of flash aluminas. This characteristic promotes capillary condensation.
- the pore diameter distribution of the gel aluminas centered on smaller values than in the case of flash aluminas, leads to reduction of the accessibility of mercury at the heart of alumina gel-type supports due to diffusional limitations.
- US 6033556 thus explicitly discourages the use of alumina-type supports in the formulation of heavy metals capture masses such as mercury or arsenic.
- the Applicant has discovered that the use of the capture masses according to the invention, based on alumina gel, makes it possible to obtain improved adsorption performance of heavy metals, in particular mercury.
- the capture mass according to the invention has improved performance in that the amount of mercury captured by said mass is greater than the amount imposed by the stoichiometry of the reaction (1) described above.
- the Applicant has discovered that the implementation of a capture mass according to the invention, based on alumina gel, in a non-regenerable fixed bed type method makes it possible to obtain improved adsorption performance in terms of this means that the dynamic capacity is greater than that of the adsorbents using aluminas obtained by flash.
- the use of the capture mass according to the invention has an important advantage and advantage in all processes for the treatment of gaseous or liquid effluents for the removal of heavy metals, particularly mercury, present in these fillers. which also include arsenic and lead.
- the subject of the present invention is therefore a mass for capturing heavy metals, in particular mercury, possibly arsenic and lead present in a gaseous or liquid effluent. It also relates to the preparation of said capture mass and the process for removing heavy metals by means of this capture mass comprising a support essentially based on gel-derived alumina and at least one element selected from the group consisting of by copper, molybdenum, tungsten, iron, nickel and cobalt.
- the present invention relates to a mass of capture of heavy metals, in particular mercury, contained in a gaseous or liquid charge, said mass containing a porous support essentially based on gel-derived alumina, at least one metal M present at least partly in a sulfide form M x S y , said metal M being selected from the group consisting of copper, molybdenum, tungsten, iron, nickel and cobalt.
- said porous support comprises a quantity of sodium of between 1 and 700 ppm of sodium (Na 2 O equivalent) and has a pore diameter distribution such that:
- Vx is the porous volume of the porous support (ml / g) corresponding to the cumulative volume of its porosity, characterized in that the pore diameter, in all the pores of the support, is greater than x (in ⁇ m).
- the present invention has the advantage of eliminating heavy metals, such as mercury, arsenic and lead, from a gaseous or liquid effluent by the use of a specific capture mass whose adsorbent properties are very high. higher than those of reference capture masses used in particular in natural gas processing applications.
- the gel alumina support used in the present invention plays, by its characteristics, the role of dispersant of the active phase M x S y and has final textural properties compatible with the constraints related to capillary condensation, and capture heavy metals.
- the capture mass according to the invention has the advantage of adsorbing mercury quantities per gram of active phase M x Sy greater than that obtainable by any other capture mass implementing a step of chemisorption of mercury by reaction (1) for the same active phase content M x S y .
- the use of the capture mass according to the invention makes it possible to capture more heavy metals from a gaseous or liquid charge and thus to purify the charge to be treated more efficiently, and thus to reduce the investment cost by using a smaller volume of adsorbents for treating a gaseous or liquid charge containing heavy metals.
- the present invention relates to a mass-capture formulation for heavy metals, in particular mercury contained in a gaseous or liquid filler, said mass containing a porous support essentially based on gel-obtained alumina, at least a metal M present at least partly in a sulfide form M x S y , said metal M being selected from the group consisting of copper, molybdenum, tungsten, iron, nickel and cobalt.
- said element is selected from the group consisting of copper, molybdenum, iron and cobalt, more preferably in the group consisting of copper and iron.
- the metal M is copper.
- the porous support based on gel alumina can be obtained from aluminum oxy (hydroxide).
- Said support of the capture mass of the present invention advantageously comprises a quantity of sodium of between 1 and 700 ppm of sodium (Na 2 O equivalents) and has a pore diameter distribution such that:
- Vx is the porous volume of the porous support (ml / g) corresponding to the cumulative volume of its porosity, characterized in that the pore diameter, in all the pores of the support, is greater than x (in ⁇ m).
- the capture mass according to the invention preferably has at least 90% (mol / mol) of sulphidized M metal in the form of X S y, very preferably at least 95% (mol / mol) of sulphured M metal in the form M x S y .
- the capture mass according to the invention advantageously has a total pore volume of between 0.20 and 1 cm 3 .g -1 , preferably between 0.40 and 0.80 cm 3 .g -1 ; the surface area of the capture mass according to the invention, determined by the BET method, is advantageously between 20 and 400 m 2 .g "1, preferably between 50 and 390 m 2.
- g" 1, more preferably between 60 and 380 m 2 g -1 , even more preferably between 130 and 380 m 2 .g -1 and still more preferably between 150 and 320 m 2 .g -1 .
- the porous volume characteristic of a porous support (ml / g) corresponding to the cumulative volume of its porosity is defined by Vx, characterized in that the pore diameter, in all the pores of the support, is greater than x (in ⁇ m). ).
- the pore volume Vx is determined by mercury porosimetry according to the ASTM D4284-92 standard with a wetting angle of 140 °, for example by means of an Autopore III TM model apparatus of the Microméritics TM brand.
- the alumina supports gel of the capture mass according to the invention have a pore diameter distribution such that:
- the alumina supports gel of the capture mass according to the invention have a pore diameter distribution such that:
- the gel alumina supports of the capture mass according to the invention have a pore diameter distribution such that:
- the gel alumina support of the capture mass contains a quantity of sodium at least less than or equal to 700 ppm (Na 2 0 equivalents) by weight with respect to the alumina gel support, preferably an amount of sodium at least less than or equal to 200 ppm (Na 2 0 equivalents) by mass, preferably a quantity of sodium at least less than or equal to 100 ppm (Na 2 0 equivalents) by weight.
- the alumina gel support contains between 2 and 50 ppm of sodium (Na 2 O equivalents).
- the proportion by weight of metal in the sulphide state relative to the capture mass is between 1 and 60%, preferably between 5 and 40% and very preferably between 10 and 30%.
- the preferred active phase constituents belong to the group consisting of copper, molybdenum, iron, nickel, tungsten or cobalt.
- the metal M is selected from the group consisting of copper, molybdenum, iron and cobalt, more preferably in the group consisting of copper and iron. Even more preferably, the active phase consists at least completely of copper.
- the capture mass according to the invention may be in the form of a ball, cylinder, multilobe, cart wheel, hollow cylinder or any other geometric shape used by those skilled in the art. More preferably, the capture mass according to the invention is in the form of extrudates of cylindrical shape, trilobed or multilobed. Said extrudates are preferably of diameters generally between 0.4 and 100 mm, preferably between 0.5 and 100 mm, preferably between 0.5 and 50 mm and more preferably between 0.5 and 10 mm.
- the support consists of alumina gel, that is to say of an alumina having been obtained from an oxy (hydroxide) aluminum precursor, for example from gamma-oxy (hydroxide). aluminum or delta-oxy (hydroxide) aluminum.
- the carrier support of the capture mass according to the invention consists of at least 50% by weight of gamma-alumina and more preferably by at least 99% of gamma-alumina.
- the support of the capture mass is constituted by at least 50% by weight of delta alumina and preferably 80% of delta alumina.
- the support of the capture mass according to the invention consists of 100% gel alumina obtained from an oxy (hydroxide) aluminum precursor advantageously characterized by a specific surface area between 150 and 600 m 2 / g, preferably between 200 and 400 m 2 / g, even more preferably between 150 and 320 m 2 g -1 .
- the present invention also relates to the process for preparing the capture mass described above.
- the synthesis method of the capture mass according to the invention comprises the following steps:
- step b) shaping the alumina gel carrier from step a) by mixing the gel in an acidic or basic medium to transform the product into a paste followed by the passage of said paste through a die to obtain extruded,
- step b) drying the alumina support obtained at the end of step b) advantageously between 70 ° C and 150 ° C, followed by their calcination advantageously between 250 ° C and 1300X, d) the preparation of a solution aqueous composition containing at least one solubilized metal precursor selected from the group consisting of copper, molybdenum, tungsten, iron, nickel and cobalt,
- step e) the impregnation of the solution resulting from step d) on the alumina support resulting from step c), f) the maturation of the impregnated support resulting from step e) in a closed enclosure saturated with water at a temperature of temperature advantageously between 20 ° C and 60 ° C for a period advantageously between 0.5 h and 8 h,
- the preparation of the capture mass comprises, at the end of step g), an additional step h) comprising the calcination under air at high temperature, typically between 300 ° C. and 800 ° C. ° C in preferably dry atmosphere, preferably at a temperature between 350 ° C and 600 ° C.
- the solid is calcined in air containing a relative humidity at 25 ° C of between 10% and 80%, preferably between 15% and 50%.
- the capture mass to the state oxide from step g) or step h) is subjected to step i) of final sulfurization to be in active form M x S vis-à-vis the uptake of heavy metals there.
- This sulphurization step can be carried out according to any method leading to the formation of metal sulphide and preferably to the CuS phase in the case of the use of copper.
- Sulfur intake is generally carried out by hydrogen sulfide or any organo-sulfur precursor known to those skilled in the art.
- the sulfurization step is conducted in the ex situ gas phase or in situ, very preferably it is conducted in the ex-situ gas phase, that is to say outside the capture unit.
- the final sulphurization of step i) is carried out at atmospheric pressure.
- the capture mass in the oxide state is sulphurated by means of a gaseous mixture of nitrogen and hydrogen sulphide, the molar concentration of which is between 1000 ppm and 10% and preferably between 0.5 % and 6% at a temperature between 100 ° C and 400 ° C, preferably between 120 ° C and 250 ° C.
- the sulfuration rate of the capture mass defined as the ratio of the number of moles of sulfur contained in the capture mass to the number of moles of metal contained in the capture mass in the oxide state, is greater than or equal to preferably equal to 0.85 greater than or equal to 0.95 and very preferably greater than 0.98.
- the degree of sulfurization is equal to 1.
- the acidic salts used in step a) are chosen from the group consisting of aluminum sulphate, aluminum nitrate or aluminum chloride.
- said acid salt is aluminum sulphate.
- the alkaline solution of aluminum salts is selected from the group consisting of sodium aluminate and potassium aluminate.
- the gel of step a) is obtained by contacting a solution of sodium aluminate with nitric acid.
- the sodium aluminate solution advantageously has a concentration of between 10 -5 and 10 "1 mol.l “ 1 and preferably this concentration is between 10 "4 and 10 " 2 mol.l “1.
- Step a) is advantageously carried out at a temperature between 5 ° C and 80 ° And at a pH of between 6 and 10.
- the temperature of step a) is between 35 ° C and 70 ° C and the pH is between 6 and 10.
- step b) of the preparation process according to the invention the kneading preferably carried out in an acid medium (3 ⁇ pH ⁇ 7) is carried out in various tools known to those skilled in the art, such as Z-arm kneaders, wheel kneaders, continuous mono- or bi-screws allowing the transformation of the gel into a so-called dough product.
- extrudates of diameter advantageously between 0.4 and 100 mm, preferably between 0.5 and 100 mm, so that more preferably between 0.5 and 10 mm and even more preferably between 0.4 and 4 mm and of different shapes such as cylinder, preferably multilobed, more preferably trilobed.
- step c) of the alumina support obtained at the end of step b) is preferably carried out between 80 ° C. and 120 ° C.
- the subsequent calcination during step c) is carried out between 450 ° C. and 950 ° C., preferably between 450 ° C. and 700 ° C., even more preferably between 450 ° C. and 600 ° C.
- one or more thermal post-treatments are carried out on the extrudates obtained during the first drying and calcination phase of step c).
- the post-treatments are preferably carried out at a temperature of between 50 ° C. and 1300 ° C., preferably between 100 ° C. and 1200 ° C. or between 500 ° C. and 1000 ° C., for a duration of between 0 ° C. and 5 h and 8 h in the presence of water preferably between 3 h and 6 h, more preferably between 3 and 5 h.
- step d) is carried out by adjusting the amounts of precursors as a function of the amount of metal desired on the mass in the final state.
- the precursors are selected from the group consisting of copper carbonate, copper hydroxide, copper nitrate, copper hydroxy nitrate, copper chloride, copper copper acetate and copper citrate.
- the precursor of copper is copper nitrate. Even more preferably, the precursor of copper is copper citrate.
- the metal precursor solution is introduced by dry impregnation.
- the maturation of the impregnated support resulting from step e) in the closed water-saturated enclosure is preferably carried out during step f) at a temperature of between 25 ° C. and 50 ° C. for a period of between 1 h and 4 h. .
- Drying of the solid resulting from step f) is preferably between 70 ° C. and 130 ° C. and more preferably between 70 ° C. and 110 ° C.
- the capture mass according to the invention has the advantage of adsorbing quantities of mercury per gram of active phase M ⁇ S y greater than that obtainable by any other capture mass implementing a mercury chemisorption step. by the reaction (1) for the same active phase content M x S y .
- a [Hg] [([Hg] f - [Hg] th ) / [Hg] th ] x 100
- [Hg] f is the quantity of mercury adsorbed by the capture mass, expressed as a relative weight relative to the initial mass of the capture mass, ie the ratio of the amount of mercury by weight to the mass by weight of the capture mass
- [Hg] th is the quantity of mercury expressed as relative weight relative to the initial mass of the capture mass, which can theoretically be absorbed in the capture mass according to the stoichiometry defined by the reaction (1).
- the overcapacity AHg is between 1% and 100%. Preferably 1 ⁇ AHg ⁇ 50% and very preferably 1 ⁇ AHg ⁇ 30%.
- the subject of the present invention is also a process for the fixed bed removal of heavy metals, such as mercury, arsenic and lead, from a gaseous or liquid effluent, by contacting the capture mass described in FIG. beforehand with the effluent to be treated.
- heavy metals such as mercury, arsenic and lead
- gaseous or liquid effluent 1 is introduced via a line 2 into a bed comprising at least the capture mass 3 according to the invention described above.
- the bed of adsorption mass adsorbs the mercury contained in the effluent so as to obtain at the outlet of said bed a purified effluent of mercury 4, that is to say that the concentration of mercury in the effluent leaving the fixed bed is lower. the mercury concentration of the effluent at the inlet of the capture mass bed.
- the method of using the capture mass described above is carried out according to the different steps with reference to FIG. 2, namely that an effluent 1 is introduced via a line 2 into a dryer 5 allowing extract the water from the effluent.
- the effluent obtained at the outlet of the dryer is then introduced into a line 6 to a bed comprising at least the capture mass 3 according to the invention.
- the feedstock of the process according to the invention generally corresponds to gaseous or liquid effluents containing heavy metals.
- gaseous or liquid effluents containing heavy metals examples include combustion fumes, synthesis gas or even natural gas, liquid cuts of natural gas, petroleum, liquid or gaseous petroleum cuts, petrochemical intermediates.
- the combustion fumes are produced in particular by the combustion of hydrocarbons, biogas, coal in a boiler or by a combustion gas turbine, for example for the purpose of producing electricity.
- the synthesis gas contains carbon monoxide CO, hydrogen H 2 (generally in a ratio H 2 / CO close to 2), water vapor (generally at saturation at the temperature where the washing is carried out) and carbon dioxide CO 2 (of the order of ten percent).
- the pressure is generally between 2 and 3 MPa, but can reach up to 7 MPa. It contains, in addition, sulfur impurities (H 2 S, COS, etc.), nitrogen (NH 3 , HCN) and halogenated impurities.
- Natural gas consists mainly of gaseous hydrocarbons, but may contain several of the following acidic compounds: CO2, H 2 S, mercaptans, COS, CS2.
- the content of these acidic compounds is very variable and can be up to 40% for CO 2 and H 2 S.
- the temperature of the natural gas can be between 20 ° C and 100 ° C.
- the pressure of the natural gas to be treated may be between 1 and 12 MPa.
- the charge to be treated according to the invention contains heavy metals in different forms.
- mercury is found in a form called Hg °, corresponding to elemental or atomic mercury, in molecular form, or in ionic form, for example Hg 2+ and its complexes.
- the charge to be treated contains heavy metals in varying proportions.
- a natural gas effluent to be treated contains between 10 nanograms and 1 gram of mercury per Nm 3 of gas.
- the temperature of the charge to be treated during the implementation of the purification process of the invention is generally between -50 and + 200 ° C., preferably between 0 and 150 ° C. and very preferably between 20 and 100 ° C. ° C.
- the pressure of the charge to be treated is advantageously between 0 and 20 MPa, preferably between 1 and 15 MPa and very preferably between 1 and 12 MPa.
- the VVH (volume of the charge per volume of collection mass and per hour) used in the purification process according to the invention is between 500 and 50000 h "1.
- the VVH is preferably between 4000 and 20000 h -1 .
- the VVH is between 0.1 and 50 h -1 .
- the charge to be treated may contain water in varying proportions.
- the hygrometry rate in the off-gases varies preferably from 0 to 100%, preferably from 0 to 99% and very preferably from 0 to 90%. Examples Example A. Preparation of a capture mass according to the invention
- the preparation of the support of the capture mass M1 according to the invention is obtained via a series of steps: ⁇ Preparation of an alumina gel, shaping then drying and calcination.
- the alumina gel is synthesized via a mixture of sodium aluminate and aluminum sulphate.
- the precipitation reaction is carried out at a temperature of 60 ° C, a pH of 9, for 60 min and with stirring of 200 rpm.
- the gel thus obtained is kneaded on a Z-arm kneader to provide the dough.
- the extrusion is carried out by passing the dough through a die provided with a hole of diameter 1, 6 mm in the form of trilobe.
- the extrudates thus obtained are dried at 150 ° C. and then calcined at 500 ° C.
- the impregnation solution is prepared by mixing water and copper nitrate so as to have a final copper concentration on the final solid (CuO equivalent) of 15% by weight, in a stirred tank.
- the amount of solution is calculated to correspond to the water uptake volume of the support, that is to say the accessible pore volume.
- the solution is brought into contact with the support and the impregnation is carried out by slow spraying of the support.
- a maturation stage is then carried out in a closed vessel for 3 hours.
- the solid obtained then undergoes a drying step at a moderate temperature of 90 ° C and a calcination step at a higher temperature of 450 ° C in a humid atmosphere. ⁇ Sulfurization
- An ex-situ sulphurization step carried out at atmospheric pressure under a 5 mol% h 2 S flux (diluted in N 2) at a temperature of 150 ° C., is applied to the capture mass prepared previously.
- Impregnation and drying calcination The impregnation and drying protocol is identical to that described in Example A. The calcination step is carried out under a dry atmosphere.
- the support of the M3 capture mass according to the invention is obtained under the conditions described in Example A.
- a hydrothermal treatment is then carried out at 650 ° C. in the presence of 30% of water for 3 hours.
- the characteristics of the support thus obtained are BET surface: 130 mVg
- the impregnation and drying protocol is identical to that described in Example A.
- the calcination step is carried out under a dry atmosphere.
- Example D Preparation of an M 4 capture mass (comparative)
- the preparation of the support of the capture mass M 4 not according to the invention is obtained via a series of steps: ⁇ Preparation of a flash alumina, MEF then drying calcination.
- the first step consists of rapid dehydration of Gibbsite at high temperature (800 ° C) and low contact time (0.8 seconds), to obtain a Khi transition alumina powder.
- a washing allowing the reduction of the Na 2 0 content is carried out using water (3 kg / kg of A Oa), followed by a second rapid dehydration treatment similar to the preceding one, also making it possible to obtain a alumina powder.
- This powder is then shaped by dredger.
- Hydrothermal treatment is carried out at high partial pressure of water (100%) for 8 hours.
- the beads thus obtained are dried at 150 ° C. and then calcined at 500 ° C.
- the characteristics of the support thus obtained are:
- Example E Preparation of an MS-capture mass (comparative)
- the support of the capture mass Ms not according to the invention is obtained under the conditions described in Example D.
- the characteristics of the support thus obtained are: BET surface: 110 m 2 / g
- a liquid mercury ball of approximately 30 g is first poured into a glass cup which is then deposited in the bottom of the reactor Ri.
- the reactor R 2 Periodically, the reactor R 2 is taken out, weighed and then redeposited in the reactor Ri.
- the increase in the mass of the reactor R 2 corresponds to the mass of mercury captured by the capture mass according to the invention.
- the inertia of glass reactors with respect to mercury adsorption is previously verified.
- t f the capture mass does not see its mass by weight increase.
- the mass of mercury, rri f adsorbed at the end of this time t f is expressed as relative weight, [Hg] f, relative to the initial mass of the capture mass,
- the capture mass M 4 not in accordance with the invention is slightly below the stoichiometric limit set by the reaction (1).
- the M 5 capture mass not in accordance with the invention is very much below the stoichiometric limit fixed by the reaction (1).
- the capture masses Mi, IVfe and M3 according to the invention systematically show a mercury adsorption performance significantly improved not only with respect to the capture masses M 4 and Ms not according to the invention but also with respect to the stoichiometry imposed by the reaction (1).
- Example G Test of the dynamic mercury adsorption capacities of the Mi and IV caotation masses.
- the mercury adsorption performance of the capture masses thus prepared are tested in a fixed bed device.
- the tubular reactor containing the capture masses is introduced into a piercing device.
- a gaseous flow of methane containing a feed [Hg] e 5000 ⁇ g ⁇ Nm- 3 in mercury was passed through the adsorbent bed at a flow rate of 300 NIh -1 , a temperature of 50 ° C. and a pressure of 20 bars.
- the amount of mercury entering [Hg] e and leaving the reactor [Hg] s is measured by an on-line analyzer.
- the VVH volume of the charge per volume of capture mass per hour
- 17000 h "1 volume of the charge per volume of capture mass per hour
- the performance of the capture masses can also be expressed with respect to the same mercury absorption efficiency. We can then compare the maximum time of use of the process during which this efficiency is provided by the adsorbent bed.
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Abstract
Description
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Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
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GB1407446.2A GB2514916B (en) | 2011-10-04 | 2012-09-12 | Capture mass with improved performance, and its use in the capture of heavy metals |
US14/349,081 US9561487B2 (en) | 2011-10-04 | 2012-09-12 | Performance trapping mass and use thereof in heavy metal trapping |
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FR11/03.016 | 2011-10-04 | ||
FR1103016A FR2980722B1 (fr) | 2011-10-04 | 2011-10-04 | Masse de captation a performances ameliorees et son utilisation dans la captation de metaux lourds |
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WO2013050667A1 true WO2013050667A1 (fr) | 2013-04-11 |
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PCT/FR2012/000361 WO2013050667A1 (fr) | 2011-10-04 | 2012-09-12 | Masse de captation a performances ameliorees et son utilisation dans la captation de metaux lourds |
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US (1) | US9561487B2 (fr) |
FR (1) | FR2980722B1 (fr) |
GB (1) | GB2514916B (fr) |
WO (1) | WO2013050667A1 (fr) |
Cited By (1)
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WO2014143566A1 (fr) * | 2013-03-15 | 2014-09-18 | Clariant Corporation | Procédé et composition pour l'élimination d'arsenic et d'autres contaminants de gaz de synthèse |
Families Citing this family (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR3022155A1 (fr) * | 2014-06-13 | 2015-12-18 | IFP Energies Nouvelles | Masse de captation a porosite trimodale pour la captation des metaux lourds. |
FR3039161B1 (fr) | 2015-07-24 | 2019-01-25 | IFP Energies Nouvelles | Procede de traitement de coupes hydrocarbures comprenant du mercure |
FR3039164B1 (fr) | 2015-07-24 | 2019-01-25 | IFP Energies Nouvelles | Procede d'elimination de mercure d'une charge hydrocarbonee lourde en amont d'une unite de fractionnement |
FR3052686B1 (fr) * | 2016-06-21 | 2020-01-17 | IFP Energies Nouvelles | Masse de captation de metaux lourds a performances ameliorees |
FR3053260B1 (fr) * | 2016-06-30 | 2020-12-11 | Ifp Energies Now | Masse de captation constitue d'une phase active sous forme cristalline |
FR3130636A1 (fr) | 2021-12-20 | 2023-06-23 | IFP Energies Nouvelles | Procede de rejuvenation de masses de captation de metaux lourds |
FR3130635A1 (fr) | 2021-12-20 | 2023-06-23 | IFP Energies Nouvelles | Procede de captation de metaux lourds par co-alimentation d’un flux sulfurant |
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US7645306B2 (en) | 2007-12-13 | 2010-01-12 | Uop Llc | Removal of mercury from fluids by supported metal oxides |
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SU967546A1 (ru) * | 1980-01-24 | 1982-10-23 | Воронежский технологический институт | Способ получени неорганического сорбента |
WO2010061212A1 (fr) * | 2008-11-25 | 2010-06-03 | Johnson Matthey Plc | Sorbant de sulfure de cuivre réduit pour l'élimination de métaux lourds |
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Cited By (1)
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WO2014143566A1 (fr) * | 2013-03-15 | 2014-09-18 | Clariant Corporation | Procédé et composition pour l'élimination d'arsenic et d'autres contaminants de gaz de synthèse |
Also Published As
Publication number | Publication date |
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US20150034561A1 (en) | 2015-02-05 |
FR2980722A1 (fr) | 2013-04-05 |
GB2514916B (en) | 2018-02-07 |
GB2514916A (en) | 2014-12-10 |
FR2980722B1 (fr) | 2015-03-20 |
GB201407446D0 (en) | 2014-06-11 |
US9561487B2 (en) | 2017-02-07 |
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